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Appendix J

Modified ISR System Design

Imagine the result

Raytheon Company

REMEDIAL ACTION PLAN ADDENDUM

FDEP Site # 65215/FDEP Project #66061

St. Petersburg, Florida

Appendix J – Modified ISR System Design

February 25, 2010

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Table of Contents

1. Introduction 1

2. Modified ISR System 1

2.1 Modified ISR System Design Requirements 2

2.1.1 Modified ISR System Design Basis 2

2.1.1.1 Expected Flow Rate 2

2.1.1.2 Influent Calculations 3

2.1.1.3 Discharge Requirements 3

2.1.1.4 Process Flow Diagram and Mass Balance 4

2.1.1.5 Piping and Instrumentation Diagram 4

2.2 AOP Pre-Treatment System Design 4

2.2.1 Design Basis 4

2.2.1.1 Heat Exchanger Feed Tank (T-100) 5

2.2.1.2 Heat Exchanger Feed Pumps (P-100A/B) 6

2.2.1.3 Heat Exchangers (HX-100A/B) 7

2.2.1.4 Influent Equalization Tanks (T-200A/B/C) 8

2.2.1.5 Aeration Tank Feed Pumps (P-200A/B) 9

2.2.1.6 Recirculation Pump (P-200C) 10

2.2.1.7 Aeration Tank (T-300) 11

2.2.1.8 Aeration Blower (B-100) 12

2.2.1.9 Coarse Bubble Diffusers 13

2.2.1.10 Sodium Hydroxide Injection System (T-1000 and P-700) 14

2.2.1.11 Filter Feed Tank (T-400) 15

2.2.1.12 Filter Feed Pumps (P-300A/B) 16

2.2.1.13 Backwash Pump (P-300C) 17

2.2.1.14 Multi-Media Filters (T-500A/B/C) 17

2.2.1.15 Backwash Tank (T-800) 19

2.2.1.16 Decant Pump (P-600) 20

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2.2.1.17 Polymer Injection System (T-900, P-500 and SM-200) 20

2.2.1.18 Air Stripper System (T-600A/B) 21

2.2.1.19 Air Stripper Discharge Tank (T-700) 23

2.2.1.20 Air Stripper Discharge Pumps (P-400A/B) 24

2.2.1.21 Tank Vent Blower (B-300) 24

2.2.1.22 Scrubber Blow-Down Water Treatment 25

2.2.1.23 AOP Pre-Treatment System Discharge Line 28

2.3 AOP Treatment System Design 28

2.3.1 Design Basis 28

2.3.1.1 Potential Sodium Sulfite Addition during ISCO Implementation 29

2.3.1.2 Influent Equalization Tank (T-1300) 31

2.3.1.3 Vapor-Phase Granular Activated Carbon (T-2300) 31

2.3.1.4 Advanced Oxidation Process – HiPOxTM System (AOP-100) 32

2.3.1.5 Existing Advanced Oxidation Process – HiPOxTM System (AOP-200) 33

2.3.1.6 Filter Feed Tanks (T-1400 and T-1600) 34

2.3.1.7 Filter Feed Pumps (P-1100A/B) 34

2.3.1.8 Backwash Pump (P-1200) 35

2.3.1.9 Catalytic Media Filters - LayneOxTM (T-1700A/B/C) 36

2.3.1.10 Multi-Media Filters (T-1800A/B) 37

2.3.1.11 Backwash Tank (T-2000) 38

2.3.1.12 Decant Pump (P-1300) 39

2.3.1.13 Polymer Injection System (T-2100, P-1400 and SM-300) 40

2.3.1.14 Liquid-Phase Granular Activated Carbon Adsorption (T-1900A/B/C) 41

2.3.2 Discharge of Treated Water 42

2.4 Modified ISR System General Arrangement 43

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2.4.1 Containment Curb 43

2.4.2 Floor Sumps and Pumps 43

2.5 Modified ISR System Support Equipment 43

2.5.1 Air Compressors (A-100 and A-200) 44

2.5.2 Safety Showers 45

2.5.3 Treatment System Control and Interconnections 45

2.5.3.1 Process Piping Interconnections 45

2.5.3.2 Programmable Logic Controllers and Control Interconnections 46

2.5.4 Modified ISR System Piping and Instrumentation 47

2.5.4.1 Treatment System Piping 47

2.5.4.2 Process and Instrumentation 48

2.5.4.3 Modified ISR System Sampling Ports 49

2.5.5 Chemical Handling and Storage 49

2.5.6 Air Emissions 50

2.5.7 Utility Requirements 50

2.5.7.1 Electricity 50

2.5.7.2 Water 50

2.6 Operation and Maintenance Plan 50

2.6.1 Pre-Start-Up Inspection 51

2.6.2 System Start-Up 51

2.6.2.1 Start-Up Operation 51

2.6.2.2 Level of Monitoring 52

2.6.3 System Proof of Performance Testing 53

2.6.3.1 Performance Testing 53


2.6.4 System Continuous Operation 53


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2.6.4.2 Operational Optimization 54

2.6.5 Maintenance Activities 54

2.6.5.1 Routine Operation and Maintenance 55

2.6.5.2 Monthly Operation and Maintenance 57

2.6.5.3 Scheduled Operation and Maintenance 57

2.7 Best Management Practice Plan 58

2.8 Monitoring Plan 58

2.8.1 Treatment System Process Monitoring 59

2.8.2 Treated Water Discharge Monitoring 60

2.8.3 Air Monitoring 61

2.9 Reporting 61

2.10 Cessation Criteria 63

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Tab

#1 Modified ISR System – Design Basis

• Figure J-1: Schematic of the Modified ISR System

• Table J-1: AOP Pre-Treatment System Design Basis Summary

• Table J-2: Modified ISR System Design Basis Summary

• Figure J-2: AOP Pre-Treatment System Process Flow Diagram

• Figure J-3: AOP Treatment System Process Flow Diagram

• Table J-3: AOP Pre-Treatment System Mass Balance

• Table J-4: AOP Treatment System Mass Balance

#2 Modified ISR System – Piping & Instrumentation

• Figures J-4 – J-7: AOP Pre-Treatment System Piping and Instrumentation Diagrams (Sheets #1 through #4)

• Figures J-8 – J-10: AOP Treatment System Piping and Instrumentation Diagrams (Sheets #1 through #3)

• Figure J-11: Piping and Instrumentation Diagram Legend Sheet

#3 Modified ISR System – AOP Pre-Treatment System Heat Exchanger

• Heat Exchanger Feed Tank (T-100) Tank Sizing Calculations

• Gould’s Pump Model 3196 STi Product Bulletin

• Heat Exchanger Feed Pumps (P-100A/B) TDH Calculations and Performance Curve

• Heat Exchanger (HX-100A/B) Sizing Calculations and Specification Sheets

#4 Modified ISR System – AOP Pre-Treatment System Influent Equalization and Iron Oxidation

• Influent Equalization Tanks (T-200A/B/C) Specification Sheets and Tank Sizing Calculations

• Aeration Tank Feed Pumps (P-200A/B) TDH Calculations and Performance Curve

• Recirculation Pump (P-200C) TDH Calculations and Performance Curve

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• Aeration Tank (T-300) Specification Sheets and Tank Sizing Calculations

• Air Flow Requirements for Iron Oxidation Calculation Sheet

• Aeration Blower (B-100) Sizing Calculations, Specification Sheets and Performance Curve

• Coarse Bubble Diffuser Specification Sheets and Performance Curves

• Sodium Hydroxide Tank (T-1000) Specification Sheet

• Sodium Hydroxide Metering Pump (P-700) Specification Sheets and Performance Curve

• Static Mixer (SM-100) Specification Sheet

#5 Modified ISR System – AOP Pre-Treatment System Filtration and Solids Settling

• Filter Feed Tank (T-400) Specification Sheets and Tank Sizing Calculations

• Filter Feed Pumps (P-300A/B) TDH Calculations and Performance Curve

• Backwash Pump (P-300C) TDH Calculations and Performance Curve

• Multi-Media Filters (T-500A/B/C) Specification Sheets and Sizing Calculation

• Backwash Tank (T-800) Specification Sheets and Tank Sizing Calculations

• Decant Pump (P-600) TDH Calculations, Specification Sheets and Performance Curve

• Polymer Usage Rate Calculation Sheet and MSDS

• Polymer Metering Pump (P-500) Specification Sheets and Performance Data

• Static Mixer (SM-200) Specification Sheets

#6 Modified ISR System – AOP Pre-Treatment System Air Stripping

• Air Stripper VOC Removal Efficiency Model

• Air Stripper (T-600A/B) Specification Sheets

• Air Stripper Blower (B-200A/B) Sizing Calculations, Specification Sheets and Performance Curve

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• Air Stripper Discharge Tank (T-700) Specification Sheets and Tank Sizing Calculations

• Air Stripper Discharge Pumps (P-400A/B) TDH Calculations and Performance Curve

#7 Modified ISR System – AOP Pre-Treatment System Tank Venting

• Tank Vent Blower (B-300) Sizing Calculations, Specification Sheets and Performance Curve

#8 Modified ISR System – AOP Pre-Treatment System Scrubber Blow-Down System

• Scrubber Blow-Down Tank (T-1100) Tank Sizing Calculations

• Transfer Pump (P-900) TDH Calculations, Specification Sheets and Performance Curve

• LPGAC Unit Specification Sheet and Vendor Model

#9 Modified ISR System – AOP Treatment System Sodium Sulfite Contactor System

• Sodium Sulfite Contactor Specification Sheets

• Sodium Sulfite Materials Safety Data Sheet (MSDS)

• ARCADIS Permanganate – Sulfite Bench Test Report

#10 Modified ISR System – AOP Treatment System Influent Equalization and Advanced Oxidation Process

• Influent Equalization Tank (T-1300) Specification Sheets and Tank Sizing Calculations

• VPGAC Unit Specification Sheet and Usage Calculations

• AOP-100 HiPOxTM System Specification Sheets

#11 Modified ISR System – AOP Treatment System Filtration and Solids Settling

• Filter Feed Pumps (P-1100A/B) TDH Calculations and Performance Curve

• Backwash Pump (P-1200) TDH Calculations and Performance Curve

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• Catalytic Media Filters (T-1700A/B/C) Specification Sheets and Sizing Calculation

• LayneOxTM Media MSDS

• Multi-Media Filters (T-1800A/B) Specification Sheets and Sizing Calculation

• Backwash Tank (T-2000) Specification Sheets and Tank Sizing Calculations

• Decant Pump (P-1300) TDH Calculations, Specification Sheets and Performance Curve

• Polymer Usage Rate Calculation Sheet and MSDS

• Polymer Metering Pump (P-1400) Specification Sheets and Performance Curve

• Static Mixer (SM-300) Specification Sheet

#12 Modified ISR System – AOP Treatment System Granular Activated Carbon

• LPGAC Unit Specification Sheet and Usage Calculations

#13 Modified ISR System – General Arrangement Plans

• Figure J-12: AOP Pre-Treatment System Layout

• Figure J-13: AOP Treatment System Layout

#14 Modified ISR System – Building Containment Curb

• AOP Pre-Treatment System Required Containment Volume Calculations

• AOP Treatment System Required Containment Volume Calculations

#15 Modified ISR System – Support Equipment

• Air Compressor (A-100 and A-200) Specification Sheets and Performance Curve

#16 Modified ISR System – Process and Instrumentation

• Table J-5: AOP Pre-Treatment System Control Logic

• Table J-6: AOP Treatment System Control Logic

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#17 Modified ISR System – Sampling Port locations

• Table J-7: Modified ISR System Sample Port Locations

#18 Modified ISR System – Air Emission Calculations

• AOP Pre-Treatment System – Air Stripper Off-Gas Emissions

• AOP Pre-Treatment System – Aeration Tank Off-Gas Emissions

#19 Modified ISR System – Electrical Load Calculation

• Electrical Load Calculation

#20 Modified ISR System – Operation and Maintenance Plan

• Table J-8: Modified ISR System Start-up and Proof of Performance Monitoring Plan

• Table J-9: Modified ISR System Process Monitoring Plan and Reporting Schedule

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Acronym List

AOP Advanced Oxidation Process

APT Applied Process Technology, Inc.

BMPP Best Management Practices Plan

MEK 2-Butanone

City City of St. Petersburg

CO2 Carbon Dioxide

COC Constituent of Concern

CVOCs Chlorinated Volatile Organic Compounds

DNAPL Dense Non-Aqueous Phase Liquids F Degrees Fahrenheit

EQ tank Equalization Tank

Fe+2 Ferrous Iron

Fe+3 Ferric Iron

F.A.C. Florida Administrative Code

ft Feet

ft/sec Feet per Second

ft3 Cubic Feet

GCTLs Groundwater Cleanup Target Levels

gpd Gallons per Day

gpm Gallons per Minute

H2O2 Hydrogen Peroxide

HAP Hazardous Air Pollutant

HX Heat Exchanger

HDPE High Density Polyethylene

ISCO In-Situ Chemical Oxidation

ISR Interim Source Removal

IWD Industrial Wastewater Discharge

KVA Kilovolt-ampere

LPGAC Liquid -Phase Granular Activated Carbon

MIBK 4-Methyl-2-pentanone

mg/L Milligrams per Liter

mL/min Milliliters per Minute

MSDS Material Safety Data Sheet

O3 Ozone

O&M Operation and Maintenance

PCRs Periodic Compliance Reports

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Acronym List

PFD Process Flow Diagram

PID Piping and Instrumentation Diagram

PLC Programmable Logic Controller

POTW Publicly Owned Treatment Works

ppm Parts per Million

psi Pounds per Square Inch

PVC Polyvinyl Chloride

SCFM Standard Cubic Feet per Minute

Site Raytheon Site

SU Standard Units

ton/yr Tons per Year

TDH Total Dynamic Head

VFD Variable Frequency Drive

VPGAC Vapor Phase Granular Activated Carbon

VOCs Volatile Organic Compounds

VSA Vacuum Swing Absorption

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Raytheon Remedial Action Plan Addendum

1. Introduction

This document provides design information for the modified interim source removal

(ISR) system and treatment units which includes water treatment for the ISR system

and Building M source area treatment by in-situ thermal remediation technology. It has

been prepared to support the Remedial Action Plan Addendum (RAPA) for the

Raytheon Site located at 1501 72nd Street, St. Petersburg, Pinellas County, Florida

(Site). The in-situ thermal system and modified ISR systems are projected to operate

for 7 to 8 months. After operation of the in-situ thermal system is discontinued, the

modified ISR system operation will be discontinued and some of the process

equipment will be re-used and incorporated into the groundwater recovery and

treatment system. The design objectives of the modified ISR treatment system are to

remove Site-related constituents of concern (COCs) in groundwater near the source

areas within an accelerated time frame and reduce concentrations of COCs in

recovered groundwater to acceptable discharge limits specified by the City of St.

Petersburg (City).

2. Modified ISR System

The modified ISR system will include two separate treatment systems, the advanced

oxidation process (AOP) pre-treatment system and the AOP treatment system, which

are further discussed in Sections 2.2 and 2.3, respectively. The treatment systems will

be installed to treat groundwater from different areas of the Site. In addition, an in-situ

thermal system will be installed for source reduction beneath Building M. This system

has been designed and will be operated by TerraTherm Inc. (refer to Appendix I).

Groundwater recovered from the in-situ thermal system will be treated in both the AOP

pre-treatment and AOP treatment systems, prior to discharge to the City’s publicly

owned treatment works (POTW). The AOP pre-treatment system will be installed

inside of Building M near the in-situ thermal system. Effluent from the AOP pre-

treatment system will be routed to the AOP treatment system, which will be located on

the south side of Building E.

Some of the existing treatment components of the ISR system will be incorporated into

the treatment components of the modified ISR system and some additional

components will be added. In addition to treating water from the AOP pre-treatment

system, the AOP treatment system will continue to treat groundwater from the four

existing recovery wells (RW-2 through RW-5). Figure J-1, Tab #1 illustrates a

schematic of the modified ISR system process flow.




Treated process water from the AOP treatment system will be discharged to the City’s

POTW in accordance with an Industrial Wastewater Discharge Permit (IWDP). The

discharge permit will identify maximum allowable flow rates and establish chemical

discharge limitations.

2.1 Modified ISR System Design Requirements

The following sections include discussions of the modified ISR system design basis,

the treatment process and associated details related to each process unit, and

disposition of treated effluent. In addition, the process flow diagram (PFD), plant

layout, and treatment system piping and instrumentation diagram (PID) are presented.

2.1.1 Modified ISR System Design Basis

The design of the AOP pre-treatment system needs to be flexible to accommodate the

changing flow rates and water quality conditions that are anticipated during the in-situ

thermal system operation. High concentrations of COCs are expected in recovered

groundwater (discussed further in subsequent sections) at temperatures ranging from

70 degrees Fahrenheit (oF) to 180oF. To address these variable conditions, the

modified ISR system will be highly automated to:

• Reduce the need for 24-hour manned operation;

• Reduce the level of operator attention required; and

• Minimize the potential for untreated water to be released to the environment.

The following sections present the evaluation of expected flow rates and influent

concentrations that the design must take into account.

2.1.1.1 Expected Flow Rate

The process flow rate for the modified ISR system was established through

groundwater modeling. The design of the system is based on the following criteria:

• Expected term of operation – 7 to 8 months;

• Flow rates – ranging from 32 to 92 gallons per minute (gpm);




– 40 gpm average flow from the in-situ thermal system with design maximum flows of 60 gpm

Treated by the AOP pre-treatment system

AOP pre-treatment system effluent will be routed to the AOP treatment system for further treatment

– 32 gpm from existing ISR recovery wells

On-Site recovery wells – 4 wells @ 8 gpm = 32 gpm

Treated by the AOP treatment system

– 92 gpm total process flow

Combination of AOP pre-treatment system effluent and recovered groundwater from the existing ISR recovery wells

2.1.1.2 Influent Calculations

Influent calculations were prepared to estimate the concentrations of volatile organic compounds (VOCs) and other compounds of interest that would need to be treated by either the AOP pre-treatment system or the AOP treatment system. The estimated concentrations for the AOP pre-treatment system influent were estimated by averaging the groundwater concentrations detected during the vertical profile investigation performed at Building M in November 2009, then applying peaking and safety factors based on professional judgment. This calculation is summarized in the AOP pre-treatment system design basis summary table (Table J-1, Tab #1).

The AOP treatment system has been designed to accept water from two influent streams as discussed above. An estimate of influent concentrations to the AOP treatment system was prepared by evaluating influent concentrations to the existing ISR system and estimated effluent concentrations from the AOP pre-treatment system. Concentrations in the effluent of the AOP pre-treatment system were estimated based on assumed removal efficiencies during the pre-treatment process. This calculation is summarized in the modified ISR system design basis summary table (Table J-2, Tab #1).

2.1.1.3 Discharge Requirements

The required effluent concentrations for each compound of interest are summarized in the design basis summary table (Table J-2, Tab #1), in accordance with the discharge requirements for the City’s POTW. Following treatment by the modified ISR system, the final water quality will meet the applicable POTW discharge permit limits for all COCs. Currently, the treated water from the existing ISR system is discharged to the




City’s POTW through an on-Site connection under IWDP # SPFL-562910-SIU-08-112. A modification to this permit has been requested for discharging the processed water through the modified ISR system. The City has tentatively approved this modification which is discussed in a letter included in Appendix A.

2.1.1.4 Process Flow Diagram and Mass Balance

The PFD for the AOP pre-treatment and AOP treatment systems are presented in

Figures J-2 and J-3, Tab #1, respectively. The PFD identifies the treatment process

units and illustrates general orientation of flow through the system. A mass balance is

presented for the operating conditions of each system and is summarized in Tables J-

3 and J-4, Tab #1. The mass balances present the influent flow rate and

concentrations that are discussed above, and illustrates where compounds of interest

are removed within each treatment process.

2.1.1.5 Piping and Instrumentation Diagram

The design for the modified ISR system is fully detailed in the PID (Figures J-4

through J-11, Tab #2). The PIDs identify pipe material, pipe size, instrumentation,

process units, process unit interconnection, and some control features for both the

AOP pre-treatment and AOP treatment systems.

2.2 AOP Pre-Treatment System Design

The AOP pre-treatment system will only receive water from the in-situ thermal system.

The system is designed to treat an average flow rate of 40 gpm; however, the total

design flow rate for the AOP pre-treatment system is 60 gpm. The selected influent

concentrations for each COC were generally the highest of the evaluated data sets,

and are summarized in Tables J-1 and J-3, Tab #1.

The following sections include discussions of the AOP pre-treatment system design

basis, the treatment process and associated details related to each process unit.

2.2.1 Design Basis

In general, the in-situ thermal system will address the area with the highest

concentrations of VOCs and 1,4-dioxane; and the area with highest likelihood of dense

non-aqueous phase liquids (DNAPL). Any DNAPL recovered will be stored in the AOP

pre-treatment system influent equalization tanks and disposed off-site at an approved

facility.




Heated groundwater recovered by the in-situ thermal system will be cooled to

approximately 120oF using a multi-pass shell and tube heat exchanger system. The

heat exchanger is a non-contact system where heated process water and cooling

water do not come into contact. The cooling water will be provided by a chilled water

system, utilizing potable water provided by the City, which is operated within the in-situ

thermal system.

The VOCs in the AOP pre-treatment system process water will be primarily removed

(volatilized) by the air stripper. Additional treatment (oxidation and adsorption) for

organic compounds will be by the HiPOxTM system developed by Applied Process

Technology, Inc. (APT), and liquid-phase granular activated carbon (LPGAC) units in

the downstream AOP treatment system. Based on performance of the existing ISR

system and bench-scale testing results, it was determined that the HiPOxTM system

was able to achieve the objectives of the project and treat recovered groundwater to

the established criteria.

Dissolved iron will be removed by oxidation (through pH adjustment and aeration) and

multi-media filtration. Iron and other suspended solids that are removed by the filters

will be settled in the backwash tank. Settled solids will be removed from the backwash

tank via vacuum truck and will be taken off-site for disposal as needed. The air stripper

vapor effluent and vapors extracted from tank vents will be routed to the in-situ thermal

system prior to discharge, which is discussed further in Appendix I. Each process unit

in the AOP pre-treatment system is further discussed in subsequent sections.

2.2.1.1 Heat Exchanger Feed Tank (T-100)

The heat exchanger (HX) feed tank (T-100) will provide storage capacity for

equalization of groundwater from the in-situ thermal system recovery wells prior to

processing through the heat exchanger. The HX feed tank will provide a minimum of

20 minutes residence time at the design flow rate of 60 gpm. The HX feed tank will

have a design operation capacity of 1,150 gallons. Process water from the HX feed

tank will be transferred to the heat exchangers (HX-100A/B) by heat exchanger feed

pumps (P-100A/B).

The HX feed tank will be equipped with a pressure transducer to sense water level in

the tank. Data will be transferred to the plant programmable logic controller (PLC).

Water level set points will be programmed into the control logic for the system so the

PLC will automatically control the speed of the heat exchanger feed pumps (P-100A/B)

to maintain water level in the heat exchanger feed tank. In addition, a redundant




high/high float switch will shut down the AOP pre-treatment system when activated and

disable the transfer of groundwater and condensate from the in-situ thermal system. It

may be possible that solids accumulate in the tank; if solids need to be removed from

the tank, the system will be shutdown and solids will be removed and taken off-site for

disposal.

Venting of this tank will occur as the tank is filled and drained. The vapor venting from

the HX feed tank will be routed to the in-situ thermal system using a blower (B-300).

The blower will be used to convey vapors into a pressurized line in the in-situ thermal

system.

The HX feed tank will be a custom built carbon steel tank with an epoxy liner that can

withstand temperatures to 180oF. Tank sizing calculations are presented in Tab #3.

The specifications for the HX feed tank are summarized below.

Item: Heat Exchanger Feed Tank T-100

Quantity: 1

Manufacturer: Custom, to be determined

Type: Vertical bulk storage tank, closed top

Material: Carbon steel with interior epoxy coating rated for 180o F

Volume: 2,000 gallons

2.2.1.2 Heat Exchanger Feed Pumps (P-100A/B)

The water from the HX feed tank will be pumped by the HX feed pumps (P-100 A/B)

through the heat exchanger system. Two pumps will be provided with one pump

operating continuously and the other pump in standby. The pumps have been

designed to each operate at the design rate of 60 gpm and provide sufficient pressure

to pump process water through the heat exchangers to the influent equalization tank

(T-200A). The pump motors will be operated using a variable frequency drive (VFD)

controlled by the plant PLC that will receive water level data from the HX feed tank (T-

100). The speed of the pump will be controlled to maintain a constant water level in

the heat exchanger feed tank (T-100).




The pump head loss calculations, vendor cut sheets, and performance curves are

presented in Tab #3. The specifications for the HX feed pumps are provided below.

Item: Heat Exchanger Feed Pumps P-100A/B

Manufacturer: Gould’s, or equal Quantity: 2 Model: 3196 STi Type: End Suction Centrifugal Size: 2x3-8; 7.125-inch impeller Seal: Single mechanical seal Horsepower and Power Requirement:

3 HP, 1750 RPM, 230/460/3/60 TEFC

Design Flow Rate and TDH:

60 gpm @ 53 feet (ft) total dynamic head (TDH)

2.2.1.3 Heat Exchangers (HX-100A/B)

The heat exchangers (HX-100A/B) will cool the process water from the in-situ thermal

system recovery wells. Two heat exchangers will be provided with one exchanger

operating continuously and the other operating in standby. The heat exchanger will

cool the process water temperature from approximately 180oF to 120oF using a multi-

pass shell and tube heat exchanger system. The HX will operate at the design flow

rate of 60 gpm and will require approximately 80 gpm of 40oF cooling water to achieve

the desired cooling. The process water will be processed in four passes through the

system, while the cooling water will be processed in a single pass. The cooling water

will be provided by a chilled water system operated within the in-situ thermal system,

as discussed in detail in Appendix I.

The sizing of the heat exchanger is presented in a calculation included in Tab #3. The

heat exchanger specifications are presented below.

Item Heat Exchanger HX-100A/B

Quantity: 2

Manufacturer: API Basco, or equal

Type: Basco Type 500, Series 08114

No. Process Water Passes:

4




Item Heat Exchanger HX-100A/B

Materials: 316L stainless steel shell and tubes

Hot Water Capacity: 60 gpm @ 180oF

Cooling Water Capacity:

80 gpm @ 40oF

2.2.1.4 Influent Equalization Tanks (T-200A/B/C)

The influent equalization tanks (EQ tanks) T-200A/B/C will provide storage capacity for

equalization of process water flows from the heat exchanger system. EQ tank (T-

200A) will provide approximately 18,000 gallons of useable volume and will use a

normal operating level of 50 percent (9,000 gallons). Therefore, approximately 150

minutes of residence time will be provided at the maximum design flow rate of 60 gpm.

Process water from EQ tank (T-200A) will be transferred to the aeration tank (T-300)

by aeration tank feed pumps (P-200A/B).

Equalization tanks (T-200B/C) will be used for additional storage capacity in the event

the AOP pre-treatment system is shut down for maintenance or unscheduled shut-

down events, and the in-situ thermal system is still operating. EQ tanks (T-200B/C) will

provide 18,000 gallons of usable storage capacity each, for a total additional storage

capacity of 36,000 gallons. This additional capacity will allow the in-situ thermal

system to continue to operate for an additional 10 hours (at 60 gpm) to 16 hours (at 40

gpm) without the downstream treatment systems operating. The stored water will be

processed once the treatment system is placed back on-line. Recirculation pump (P-

200C) will transfer the process water to EQ tank (T-200A) to be processed through the

system.

The EQ tanks will be equipped with a pressure transducer to sense water level in the

tank and data will be transferred to the plant PLC. Water level set points will be

programmed into the control logic for the system so the PLC will automatically control

the speed of the aeration tank feed pumps. In addition, a redundant high/high float

switch will be installed in each equalization tank that will shut down the AOP pre-

treatment system and disable the transfer of groundwater and condensate from the in-

situ thermal system when activated. It may be possible that solids and DNAPL

accumulate in the tank; if solids and/or DNAPL need to be removed from the tank, the

system will be shutdown and the solids/DNAPL will be removed and taken off-site for

disposal.




The EQ tanks will be steel tanks with two sealed top access hatches and smooth

interior walls for easy cleaning. The sizing of the EQ tanks is presented in a calculation

included in Tab #4. The specifications are summarized below.

Item: Influent Equalization Tanks T-200A/B/C

Quantity: 3

Manufacturer: Baker Corp., or equal

Type: EZ Clean Fixed Axle Safety Vapor Frac Tank

Material: Carbon Steel with no interior coating

Working Volume: 18,000 gallons

Dimensions: 37-ft, 6-inches long by 8-ft, 6-inches wide by 11-ft, 2-inches high

2.2.1.5 Aeration Tank Feed Pumps (P-200A/B)

The water from the influent equalization tank (T-200A) will be pumped by aeration tank

feed pumps (P-200A/B) to the aeration tank (T-300). Two pumps will be provided with

one pump operating continuously and the other pump in standby. The pumps have

been designed to each operate at the design rate of 60 gpm and provide sufficient

pressure to pump process water to the aeration tank. The pump motors will be

operated using a VFD controlled by the plant PLC that will receive water level data

from the EQ tank (T-200A). The pump speed will be controlled to maintain a constant

water level in the influent equalization tank (T-200A).

The pump head loss calculations and performance curves are presented in Tab #4.

The pump specification sheets are presented in Tab #3. The specifications for the

aeration tank feed pumps are provided below.

Item: Aeration Tank Feed Pumps P-200A/B

Manufacturer: Gould’s, or equal

Quantity: 2

Model: 3196 STi




Item: Aeration Tank Feed Pumps P-200A/B

Type: End Suction Centrifugal

Size: 2x3-8; 5.875-inch impeller

Seal: Single mechanical seal

Horsepower and Power Requirement:

1.5 HP, 1750 RPM, 230/460/3/60 TEFC


60 gpm @ 35 ft TDH

2.2.1.6 Recirculation Pump (P-200C)

The overflow water from the influent EQ tanks (T-200B/C) will be pumped by the

recirculation pump (P-200C) back to the influent EQ tank (T-200A) to be processed

through the AOP pre-treatment system. One pump will be provided and will operate on

as-needed basis. The pump has been designed to operate at a design rate of 40 gpm

and will provide sufficient pressure to pump process water to the influent EQ tank. The

pump motor will be operated using a VFD controlled by the plant PLC that will receive

water level from the influent EQ tanks (T-200A/B/C).


The pump specification sheets are presented in Tab #3. The specifications for the

recirculation pump are provided below.

Item: Recirculation Pump P-200C


Quantity: 1

Model: 3196 STi





2 HP, 1750 RPM, 230/460/3/60 TEFC


40 gpm @ 46 ft TDH




2.2.1.7 Aeration Tank (T-300)

The aeration tank (T-300) will provide aeration of water and sufficient residence time to

allow for oxidation of iron and complete mixing of the tank. Sodium hydroxide will be

added to the process stream to increase the pH of the water from approximately 6.0

standard units (SU) to 7.4 SU to enhance the oxidation of iron. Sodium hydroxide will

be metered into an injection port in an in-line static mixer (SM-100) that will provide

rapid mixing of the injected sodium hydroxide. The static mixer will be a 3-inch

diameter, schedule 40 carbon steel unit containing six mixing elements.

In addition, the aeration tank influent line will include an approximately 5-ft section of

12-inch diameter piping to provide additional residence time for the pH control loop to

respond. A pH analyzer will be installed downstream of this pipe section and will

provide data to the PLC to control operation of the sodium hydroxide metering pump.

Air flow requirement calculations have been performed to determine the air flow rate

required to oxidize iron. Based on influent concentrations and flow rate, 8 standard

cubic feet per minute (scfm) of air is required to complete the iron oxidation process as

shown in the design calculation in Tab #4. Oxygen transfer requirements to achieve

complete mixing are approximately 30 scfm per 1,000 cubic ft (ft3) of tank volume. The

aeration tank is approximately 870 ft3 (6,500 gallons); therefore, 26 scfm is required to

achieve complete mixing. The aeration tank blower was sized to operate at a design

flow rate of 30 scfm to provide sufficient air flow for both mixing and iron oxidation.

The aeration tank will be equipped with a coarse bubble diffuser system to promote

distribution of air within the tank. The air will provide mixing that will prevent the

settling of iron particulates and suspended solids. The aeration tank will provide a

minimum 90 minutes of residence time at the design flow rate of 60 gpm. The

operating capacity will be 5,400 gallons, with 6,500 gallons of total storage capacity.

Process water from aeration tank (T-300) will be transferred to the filter feed tank (T-

400) by gravity.

The aeration tank will be equipped with a pressure transducer to sense water level in

the tank and data will be transferred to the plant PLC. In addition, a redundant

high/high float switch will shut down the AOP pre-treatment system components

downstream of the influent EQ tanks when activated.




The aeration tank will be a vertical high density polyethylene tank with one sealed top

access hatch. The sizing of the aeration tank and air flow requirement calculations are

presented in Tab #4. The specifications are summarized below.

Item: Aeration Tank T-300

Quantity: 1


Type: 6,500 Gallon Poly Tank (vertical, cylindrical, closed-top tank)

Material: High density polyethylene


Dimensions: 10-ft diameter by 12-ft, 4-inch total height (10-ft, 6-inch sidewall)

Item: Static Mixer SM-100

Manufacturer: Koflo, or equal

Model: Series 275

Type: Low pressure loss, flange mounted mixer with FNPT injection port

Size: 3-inch

2.2.1.8 Aeration Blower (B-100)

The aeration blower (B-100) will provide air to the coarse bubble diffusers installed

inside of aeration tank (T-300) to provide complete mixing of the tank. Oxygen transfer

requirements to achieve complete mixing of the aeration tank are approximately 26

scfm, as discussed above. Blower (B-100) was sized to operate at a design flow rate

of 30 scfm to provide sufficient air flow to the aeration tank.

The blower has been designed to operate at the design air flow rate and provide

sufficient pressure to push air through the coarse bubble diffusers and the water

column within the aeration tank. The blower discharge line will be equipped with a

pressure indicator to sense pressure in the piping and data will be transferred to the

plant PLC. Pressure set points will be programmed into the control logic for the system




so the PLC will automatically operate the aeration blower (B-100), as part of blower

cycle operations.

The blower sizing calculations, vendor cut sheets, and performance curves are

presented in Tab #4. The specifications for the aeration blower are provided below.

Item: Aeration Blower B-100

Manufacturer: Becker Pumps Corp., or equal

Quantity: 1

Model: KDT 3.60

Type: Oil-less, rotary vane, low pressure compressor


3 HP, 1740 RPM, 230/460/3/60

Max Flow Rate and Pressure:

39 scfm @ 22 psig

Design Flow Rate and Pressure:

36 scfm @ 5 psig

2.2.1.9 Coarse Bubble Diffusers

The coarse bubble diffusers will be provided to aid in complete mixing of the aeration

tank. Cap diffusers will be installed in the main air feed line in the tank using a pipe tap

and threaded grommet connection. The cap diffusers have been designed to operate

at the design air flow rate.

The coarse bubble diffuser vendor cut sheets and performance curves are presented

in Tab #4. The specifications for the coarse bubble diffusers are provided below.

Item: Coarse Bubble Diffusers

Manufacturer: Stamford Scientific International, or equal

Quantity: 6

Model: CAP AFC75

Type: Cap Diffuser with (10) 5 millimeter diameter holes

Design Flow Rate: 4 – 6 scfm per diffuser




2.2.1.10 Sodium Hydroxide Injection System (T-1000 and P-700)

Given the expected pH of the recovered groundwater (approximately 6.0 SU), the

treatment system will include a sodium hydroxide injection system to increase the pH

required for efficient treatment. Sodium hydroxide (50 percent) will be added to the

influent line of the aeration tank, as discussed above, to increase pH to 7.4 SU. The

total amount of sodium hydroxide required for the 60 gpm design flow rate is estimated

to be approximately 8.3 gallons per day (gpd). This estimated volume was based on

sodium hydroxide usage observed during operation of the existing ISR system.

The sodium hydroxide injection system will include a sodium hydroxide tank (T-1000)

and one chemical metering pump (P-700). The sodium hydroxide tank has been sized

to contain a 30-day supply of sodium hydroxide (275 gallons) and will be equipped with

individual secondary containment. The metering pump will be controlled by the plant

PLC that will receive pH data from a pH probe installed in the aeration tank influent

line. Anticipated flow rate for sodium hydroxide injection is approximately 8.3 gpd, and

the pump has the capability of pumping 0.1 to 18 gpd.

The vendor cut sheets for the sodium hydroxide tank and metering pump are provided

in Tab #4. The specifications are summarized below.

Item: Sodium Hydroxide Tank T-1000

Quantity: 1

Manufacturer: Snyder Tank, or equal

Type: Double Wall Containment Tank (vertical, cylindrical, closed top tank)


Volume: 250 gallons

Dimensions: 47-inch diameter by 64-inch total height




Item Sodium Hydroxide Metering Pump, P-700

Quantity: 1

Manufacturer: LMI, or equal

Model: AA-962-362HI

Max Pumping Rate and Pressure:

18 gpd @ 80 pounds per square inch (psi)

Design Flow Rate: 8.3 gpd

2.2.1.11 Filter Feed Tank (T-400)

The filter feed tank (T-400) will receive discharge water from the aeration tank (T-300)

and decant water generated from the backwash tank (T-800). The filter feed tank will

be the source of main process water and clean backwash water to the multi-media

filters. Total backwash volume is 2,545 gallons per cycle which will be decanted to the

filter feed tank once per day, just prior to the beginning of the backwash cycle.

The filter feed tank will provide a minimum of 30 minutes of residence time, with an

average operating capacity of 3,250 gallons. The total storage capacity of the tank is

6,500 gallons. This tank will operate at 50 percent capacity to leave sufficient capacity

to accept the backwash decant water. Process water from filter feed tank (T-400) will

be pumped through the multi-media filters (T-500A/B/C) by filter feed pumps (P-

300A/B).

The filter feed tank will be equipped with a pressure transducer to sense water level in

the tank and data will be transferred to the plant PLC. Water level set points will be

programmed into the control logic for the system so the PLC will control the speed of

filter feed pumps (P-300A/B) to maintain a constant water level in the filter feed tank.

In addition, a redundant high/high float switch will shut down the AOP pre-treatment

system components downstream of the influent EQ tanks when activated.

The filter feed tank will be a vertical high density polyethylene tank with one sealed top

access hatch. The sizing of the filter feed tank is presented in a calculation included in

Tab #5. The specifications are summarized below.




Item: Filter Feed Tank T-400

Quantity: 1


Type: 6,500 Gallon Poly Tank (vertical, cylindrical, closed top tank)




2.2.1.12 Filter Feed Pumps (P-300A/B)

The water from the filter feed tank will be pumped by filter feed pumps (P-300 A/B)

through the multi-media filters to the air strippers (T-600A/B). Two pumps will be

provided with one pump operating continuously and the other pump in standby. Each

pump has been designed to operate at the design rate of 60 gpm and provide sufficient

pressure to pump process water through the multi-media filters to the air strippers. The

pump motors will be operated using a VFD controlled by the plant PLC that will receive

water level data from the filter feed tank (T-400).


The pump specification sheets are presented in Tab #3. The specifications for the filter

feed pumps are provided below.

Item: Filter Feed Pumps P-300A/B


Quantity: 2

Model: 3196 STi


Size: 1.5x3-6; 5.125-inch impeller


Horsepower and Power Requirement

7.5 HP, 3520 RPM, 230/460/3/60 TEFC


60 gpm @ 112 ft TDH




2.2.1.13 Backwash Pump (P-300C)

Backwash pump (P-300C) will pump water from the filter feed tank through the multi-

media filters to the backwash tank (T-800). The filter feed tank (T-400) will be the

source of backwash water for the multi-media filter backwash cycle. Filter feed pumps

(P-300A/B) will be shut-down during the backwash cycle. The backwash cycle will be

106 gpm for 8 minutes (for three multi-media filter vessels), resulting in a total

backwash volume of 2,545 gallons.

The backwash pump has been designed to operate at the design backwash rate of

106 gpm and provide sufficient pressure to pump process water through the multi-

media filters to the backwash tank. The pump motor will be operated using a VFD

controlled by the plant PLC that will receive water level data from the filter feed tank (T-

400). The VFD will allow for maximum flow and pressure control, and will allow

adjustments to be made during each application.


The pump specification sheets are presented in Tab #3. The backwash pump

specifications are provided below.

Item: Backwash Pump P-300C


Quantity: 1

Model: 3196 STi


Size: 1.5x3-6; 5.125-inch impeller



7.5 HP, 3520 RPM, 230/460/3/60 TEFC


110 gpm @ 103 ft TDH

2.2.1.14 Multi-Media Filters (T-500A/B/C)

A multi-media filtration system (T-500A/B/C) will be installed for primary filtration of iron

particulates and suspended solids produced in the upstream aeration process. The




multi-media filters are designed to protect the air strippers from significant iron fouling.

Multi-media filters were selected for their good filtration performance (consistent

removal of particles 5 microns in size or greater) and ability to handle the design flow

rate 60 gpm. Filtration performance will not be affected by lower flow rates in the event

of reduced flow rates from the in-situ thermal system.

The multi-media filter package will include three 3-foot diameter vessels in a pre-

packaged skid with an internal control system. During normal operation, all three

vessels will operate continuously in parallel. During a backwash cycle, water will be

processed through two vessels while the third is backwashed. The filtered water from

the two operating vessels will be used as clean backwash water for the third vessel.

Each vessel contains four layers of filtration media including gravel, coarse garnet, fine

garnet, and anthracite. To prevent clogging, the filters will be backwashed when the

differential pressure across the filters is approximately 15 to 20 psi. Backwash

frequency is anticipated to be once per day, and process water from the filter feed tank

will be used as the source of water for backwashing.

Calculations for multi-media filter sizing, backwash requirements, and vendor cut

sheets are presented in Tab #5. Specifications are provided below.

Item: Multi-Media Filters T-500A/B/C

Manufacturer: Yardney, or equal

Model: MM-3660-3AS

Type: 3-vessel filtration system with manifolded influent, effluent and backwash piping; and automated valves

Service Flow Rate: Nominal flow range 105-320 gpm; max flow rate 426 gpm

Backwash Flow Rate: 106 gpm

Max Pressure: 80 psi

Material: Epoxy-coated steel

Vessel Dimensions: 36-inch diameter by 60-inch side shell height




2.2.1.15 Backwash Tank (T-800)

The backwash tank (T-800) will receive backwash water from the multi-media filters (T-

500A/B/C). The backwash tank will provide a total storage capacity of 6,500 gallons.

The tank was designed for sufficient volume to handle a single backwash event plus

21-days of solids storage capacity. Backwash solids from the multi-media filters will be

allowed to settle between backwash cycles, which are estimated to be approximately

once per day. Prior to the backwash sequence, the supernatant within the tank will be

decanted to the filter feed tank (T-400). One backwash cycle storage volume (2,545

gallons) will be decanted to provide room to accept water from the new backwash

cycle. This cycle of backwashing, settling and decanting will continue until solids build

up in the bottom of the tank. At this time, the system will be shutdown and the solids

will be removed via vacuum truck and taken off-site for disposal.

The backwash tank will be equipped with a pressure transducer to sense water level in



the decant pump (P-600) to maintain a set water level in the tank. In addition, a

redundant high/high float switch will shut down the AOP pre-treatment system

components downstream of the influent EQ tanks when activated.

The backwash tank will be a vertical high density polyethylene tank with one sealed top

access hatch. The sizing of the backwash tank is presented in a calculation included in

Tab #5. Specifications are summarized below.

Item: Backwash Tank T-800

Quantity: 1


Type: 6,500 Gallon Poly Tank (vertical, cylindrical, closed top tank)


Volume: 6,500 gallons nominal





2.2.1.16 Decant Pump (P-600)

The decant pump (P-600) will pump water from the backwash tank to the filter feed

tank (T-400). One backwash cycle storage volume (2,545 gallons) will be decanted

prior to each new backwash cycle. The decant pump has been designed to decant the

required volume of supernatant in approximately 2 hours. The pump motor will be

operated using a VFD controlled by the plant PLC that will receive water level data

from the filter feed tank (T-400) and the backwash tank (T-800). The VFD will allow for

maximum flow and pressure control, and will allow adjustments to be made during

each application.

The pump head loss calculations, vendor cut sheet, and performance curves are

presented in Tab #5. The decant pump specifications are provided below.

Item: Decant Pump P-600


Quantity: 1

Model: 1SC51C-F

Type: Submersible

Size: 1.25-inch discharge; 3 stage


1/2 HP, 3450 RPM, 115/1/60 TEFC


30 gpm @ 41 ft TDH

2.2.1.17 Polymer Injection System (T-900, P-500 and SM-200)

During the multi-media filter backwash sequence polymer will be added to the water

stream to promote the formation of larger and heavier particles that will aid in settling

the suspended solids. The polymer injection system will include a storage tank (T-

900), chemical metering pump (P-500) and an in-line static mixer (SM-200). Based on

jar testing completed during operation of the existing ISR system, the selected polymer

is PolyFloc AS1002 which will be metered at a dosage rate of 15 parts per million

(ppm). The Material Safety Data Sheet (MSDS) and fact sheet for the PolyFloc are

included in Tab #5.




A summary of polymer usage rates and volumes, and vendor cut sheets are presented

in Tab #5. The polymer will be supplied from the vendor in a 5-gallon bucket that is

expected to last approximately 6 months based on the estimated polymer usage rate of

0.27 gallons per week. The polymer metering pump (P-500) will inject polymer into an

injection port in the in-line static mixer (SM-200) which will provide rapid mixing of the

injected polymer. The static mixer will be a 3-inch diameter, schedule 40 carbon steel

unit containing six mixing elements.

Polymer metering pump and static mixer specifications are provided below.

Item: Polymer Metering Pump P-500


Model: AA-971-352HI


10 gpd @ 140 psi

(27 mL/min)

Design Flow Rate: 2.3 gpd (6 milliliters per minute [mL/min])



Model: Series 275


Size: 3-inch

2.2.1.18 Air Stripper System (T-600A/B)

The air strippers (T-600A/B) will be used to remove the majority of VOCs from the

water stream. The air strippers were designed for greater than 99.9 percent removal

rates of all COCs except 1,4-dioxane, acetone, 2-butanone [i.e., methyl ethyl ketone

(MEK)], and 4-methyl 2-pentanone [i.e., methyl isobutyl ketone (MIBK)]. 1,4-Dioxane

will be treated in downstream AOP unit. Two air strippers will be provided with one air

stripper operating continuously and the other in standby. The air stripper is a tray type

stripper equipped with 4 trays, a plexiglass front hatch, polypropylene de-mister, liquid




level sight gauge, sump pressure gauge and other appurtenances. Process water will

drain via gravity from the air stripper sump to the air stripper discharge tank (T-700).

Each air stripper will be equipped with a high-pressure blower that will be positioned to

allow an induced draft configuration. The air stripper blowers (B-200A/B) have been

designed to operate at the design air flow rate of 900 scfm and provide sufficient

pressure to pull air through the air stripper to the in-situ thermal system (Appendix I).

The blower inlet line will be equipped with a pressure indicator to sense pressure in the

piping and data will be transferred to the plant PLC. Pressure set points will be

programmed into the control logic for system monitoring.

The air stripper COC removal model, blower sizing calculations, vendor cut sheets,

and performance curves are presented in a calculation included in Tab #6. The air

stripper and air stripper blower specifications are presented below.

Item: Air Stripper T-600A/B

Quantity: 2

Manufacturer: QED, or equal

Type: E-Z Tray Model 16.6 SS

No. Trays: 4

Max Flow Range: 1 – 150 gpm

Design Flow Rate: 60 gpm

Shell Dimensions: 49-inch by 52-inch by 104-inch height

Materials: 304 SS

Item: Air Stripper Blowers B-200A/B

Manufacturer: New York Blower Co., or equal

Quantity: 2

Model: 28506, Arrangement 4

Type: HP Pressure Blower


7.5 HP, 3500 RPM, 230/460/3/60




Item: Air Stripper Blowers B-200A/B


900 scfm @ 60 inches water

2.2.1.19 Air Stripper Discharge Tank (T-700)

Process water from the air stripper sump will drain via gravity to the air stripper

discharge tank (T-700). The tank was designed to supplement the volume of the air

stripper sump capacity. The tank was sized for approximately 10 minutes of residence

time at the design flow rate of 60 gpm, providing 1,100 gallons of total storage

capacity. Process water from the air stripper discharge tank (T-700) will be transferred

to the influent EQ Tank (T-1300) in the AOP treatment system via air stripper discharge

pumps (P-400A/B).

The air stripper tank will be equipped with a pressure transducer to sense water level in



the air stripper discharge pumps (P-400A/B) to maintain a constant water level in the

air stripper discharge tank (T-700). In addition, a redundant high/high float switch will

shut down the AOP pre-treatment system components downstream of the influent EQ

tanks when activated.

The air stripper discharge tank will be a vertical high density polyethylene tank with one

sealed top access hatch. The sizing of the air stripper discharge tank is presented in a

calculation included in Tab #6. The specifications are summarized below.

Item: Air Stripper Discharge Tank T-700

Quantity: 1

Manufacturer: Snyder Industries Inc., or equal

Type: 1,100 Gallon Dome Bottom Tank



Dimensions: 86-inch diameter by 55-inch total height (36-inch sidewall)




2.2.1.20 Air Stripper Discharge Pumps (P-400A/B)

The water from the air stripper discharge tank will be pumped by air stripper discharge

pumps (P-400A/B) to influent EQ tank (T-1300) in the downstream AOP treatment

system. Two pumps will be provided with one pump operating continuously and the

other pump in standby. The pumps have been designed to operate at the design rate

of 60 gpm and provide sufficient pressure to pump process water the approximate

1,400 ft distance to influent EQ tank (T-1300). The pump motors will be operated

using a VFD controlled by the plant PLC that will receive water level data from the air

stripper discharge tank (T-700).


The pump specification sheets are presented in Tab #3. The specifications for the air

stripper discharge pumps are provided below.

Item: Air Stripper Discharge Pumps P-400A/B


Quantity: 2

Model: 3196 STi





3 HP, 1750 RPM, 230/460/3/60 TEFC


60 gpm @ 64 ft TDH

2.2.1.21 Tank Vent Blower (B-300)

The tank vent blower (B-300) will be used to convey vapors from tanks upstream of the

air strippers (T-600A/B) to the in-situ thermal system. The blower was sized to provide

sufficient air flow and pressure to convey tank vapors into a pressurized line.

The blower suction line will be equipped with a pressure indicator to sense pressure in

the piping. This data will be transferred to the plant PLC to verify continuous operation

of the vent blower.




The blower sizing calculations, vendor cut sheets, and performance curves are

presented in Tab #7. The specifications for the tank vent blower are provided below.

Item: Tank Vent Blower B-300

Manufacturer: Rotron, or equal

Quantity: 1

Model: DR303AE72M

Type: Regenerative Blower


0.5 HP, 230/460/3/60

Max Flow Rate and Pressure:

55 scfm @ 45 inches of water


30 scfm @ 24 inches of water

2.2.1.22 Scrubber Blow-Down Water Treatment

Several sources of water generated within the in-situ thermal system will be

segregated and not processed by the AOP pre-treatment system. This water stream

includes the scrubber sump discharge water, the boiler water softener discharge, and

various blow-down ports throughout the in-situ thermal system. Most of this water is

non-contact water, meaning that the water does not contact any COCs. However, the

scrubber discharge water has the potential to include low concentrations of COCs

since the water comes into contact with scrubber gases that may potentially contain

COCs. Any COCs in the scrubber blow-down water would likely be VOCs; 1,4-dioxane

is not expected to be in this water stream. The majority of this segregated stream will

be scrubber blow-down water at an expected flow rate ranging from 3 to 8 gpm.

The scrubber blow-down water will contain sodium chloride (NaCl) that is generated in

the scrubber unit. The concentrations of NaCl will vary during operations and will

depend on the amount of chlorinated VOCs (CVOCs) being oxidized in the thermal

oxidizer. The estimated NaCl concentrations within the scrubber discharge may range

from 1,700 – 12,000 milligrams per liter (mg/L). Chlorides can have a detrimental

effect on AOP treatment reactions, in addition to being corrosive to plant components.

Therefore, to prevent damage to downstream operations, the blow-down water will be

segregated and handled separately.




The blow-down water will be treated by LPGAC to remove potential VOCs. Following

treatment, the water will be pumped to the AOP treatment system and combined with

AOP treatment system effluent prior to discharging to the City’s POTW. The AOP

treatment system effluent is expected to have low NaCl concentrations; therefore, the

NaCl concentration of the combined flow stream will be reduced. The maximum

chloride concentrations of the combined effluent flow streams discharged to the City

are expected to be less than 1,150 mg/L, with typical chloride concentrations in the

range of 100 to 500 mg/L; well below the discharge limit of 1,350 mg/L. Components

of the scrubber blow-down system include a blow-down collection tank, process

pumps, and two LPGAC vessels; which are further described below.

2.2.1.22.1 Scrubber Blow-Down Tank (T-1100)

The scrubber blow-down tank (T-1100) will collect water from several sources including

the scrubber sump discharge water, the boiler water softener, and various blow-down

ports throughout the in-situ thermal system. The average flow rate is expected to vary

and will range from 3 to 8 gpm. The system will be designed for a maximum flow rate

of 15 gpm. The scrubber blow-down tank will provide a minimum of 60 minute

residence time at the maximum design flow rate of 15 gpm, and will have a minimum

storage capacity of 1,200 gallons. The tank will be a vertical, domed top custom

reinforced fiberglass epoxy tank with approximate dimensions of 6-ft diameter and 6-ft

sidewall height. Tank sizing calculations are included in Tab #8.

The scrubber blow-down tank will be equipped with a pressure transducer to sense

water level in the tank and data will be transferred to the plant PLC. Water level set

points will be programmed into the control logic for the system so the PLC will

automatically control the speed of the transfer pump (P-900). In addition, a redundant

high/high level float switch will shut down the AOP pre-treatment system and disable

transfer of scrubber blow-down water from the in-situ thermal system when activated.

2.2.1.22.2 Transfer Pump (P-900)

The water from the scrubber blow-down tank will be pumped by transfer pump (P-900).

The pump has been designed to operate at the design flow rate of 15 gpm and provide

sufficient pressure to pump water through the LPGAC vessels to the modified ISR

system discharge point to the City’s POTW. The pump motor will be operated using a

VFD controlled by the plant PLC that will receive water level data from the scrubber

blow-down tank (T-1100).

The pump head loss calculations, vendor cut sheets and performance curves are

presented in Tab #8. The specifications for transfer pump (P-900) are provided below.




Item: Transfer Pump P-900


Quantity: 1

Model: 1SVD1FSD1H

Type: Vertical Multi-Stage Pump (SSV Series)

No. Stages: 6


0.75 HP, 3500 RPM, 230/460/1/60 TEFC


15 gpm @ 126 ft TDH

2.2.1.22.3 Liquid-Phase Granular Activated Carbon (T-1200A/B)

Water from the scrubber blow-down tank will be pumped through two LPGAC vessels

that will be operated in series for VOC removal. The potential of having VOCs in the

scrubber blow-down is low, but LPGAC is provided to remove any VOCs that may be

present in the water stream. Each vessel will contain 250 pounds of acid-washed

coconut carbon. The vessels will be constructed of fiberglass in order to prevent

corrosion due to the high salt content. The LPGAC COC removal model and vendor

cut sheets are provided in Tab #8. Specifications are provided below.

Item: LPGAC Vessels T-1200A/B

Manufacturer: Carbonair, or equal

Model: PC3, complete skid mounted


Material: Reinforced fiberglass

The estimated time for breakthrough through the first vessel is 30 days and the second

vessel is 120 days (Tab #8); however, other factors besides VOC loading that may

contribute to the carbon life include bio-fouling and solids build-up. These factors will

result in pressure increases across the LPGAC vessel. Water from between the

LPGAC vessels will be sampled and analyzed monthly to determine if VOCs are

breaking through the first LPGAC vessel. If break-through above City discharge limits

is occurring after the first vessel or the vessels become clogged with solids, the first




vessel will be taken off-line and the second vessel will be moved to the first position. A

new LPGAC unit will be placed as the second vessel. The spent LPGAC will be taken

off-site for proper disposal.

2.2.1.23 AOP Pre-Treatment System Discharge Line

The effluent from the AOP pre-treatment system will be routed approximately 1,400 ft

to the AOP treatment system influent EQ tank (T-1300) to be processed through the

AOP treatment system. The pre-treated process water pipeline will be 3-inch high

density polyethylene (HDPE) piping. The HDPE piping will transition to 3-inch carbon

steel at the influent EQ tank (T-1300) to connect to the influent nozzle on the tank.

2.3 AOP Treatment System Design

The AOP treatment system is designed to treat groundwater extracted from the

existing ISR recovery wells and process water from the AOP pre-treatment system. It

is anticipated that the AOP treatment system will operate for approximately 7 to 8

months, which is the expected time of operation of the in-situ thermal system. Based

on data obtained during operation of the existing ISR system, the AOP treatment

system is expected to be effective in containing affected on-Site groundwater and

removing COCs from the groundwater prior to discharge to the City’s POTW.

The total design flow rate for the AOP treatment system is 92 gpm and includes 32

gpm from the existing ISR wells and 60 gpm from the AOP pre-treatment system. The

selected influent concentration for each COC was generally the highest of the

evaluated data sets, as shown in Tables J-2 and J-4, Tab #1.

The following sections include discussions of the AOP treatment system design basis,

the treatment process and associated details related to each process unit, and

disposition of treated effluent. Since the groundwater recovery system of the modified

ISR system remains the same as the existing ISR system, the details provided below

focus on the treatment system components.

2.3.1 Design Basis

In general, the organic compounds in the AOP treatment system will be primarily

destroyed (oxidized) by the HiPOxTM AOP treatment system developed by APT.

Additional polishing treatment for organic compounds will be provided by LPGAC units.

The recovered groundwater and AOP pre-treatment system effluent will be treated to




meet the required effluent concentrations for each compound of interest, and will be

discharged to the City’s POTW in accordance with the discharge limits requirements.

Dissolved iron in the process water and in the AOP pre-treatment system effluent will

be removed by oxidation through AOP treatment and by catalytic media (LayneOxTM)

and multi-media filtration units. Iron and other suspended solids that are removed by

the filters will be settled in the backwash tank (T-2000). Settled solids will be removed

from the backwash tank via vacuum truck and will be taken off-site for disposal as

needed.

Some of the process units in the existing ISR system will continue to be used in the

AOP treatment system and include the groundwater recovery wells (RW-2 through

RW-5), EQ tank (T-1500), AOP feed pump (P-1000), HiPOxTM system (AOP-200), filter

feed tanks (T-1400 and T-1600), vapor-phase granular activated carbon (VPGAC)

vessel (T-2200) and associated piping, valves and instrumentation. In addition, the

media filter vessels that are currently being used with LayneOxTM catalytic media, will

be used, but the media will be replaced with a multi-media consisting of gravel, coarse

garnet, fine garnet, and anthracite. This equipment has been discussed in previously

submitted reports; therefore, will only be briefly discussed in the following sections.

2.3.1.1 Potential Sodium Sulfite Addition during ISCO Implementation

It is anticipated that during the in-situ chemical oxidation (ISCO) injections performed in

the area south of Building E, sodium permanganate may be recovered by recovery well

RW-4. Sodium permanganate may adversely affect the oxidation process within the

HiPOxTM system by causing an increase in the hydrogen peroxide (H2O2) and ozone

(O3) demand. Also, additional manganese (from permanganate reactions) may cause

fouling within the treatment system.

Two contingency mechanisms will be used to evaluate and control the permanganate

in RW-4 so that the treatment system is not adversely affected. First, groundwater in

the vicinity of RW-4 and recovered by RW-4, will be monitored to evaluate the

permanganate concentrations. Second, if permanganate does get recovered from

RW-4, a sodium sulfite contactor will be installed on the RW-4 recovery piping to react

the permanganate.

Monitoring for permanganate will include periodic groundwater sampling at RW-4 and

an upgradient monitoring well during and following the permanganate injections.

Permanganate concentrations at the upgradient well will provide an early indication of




approaching permanganate levels to RW-4. If permanganate concentrations in

groundwater recovered at RW-4 exceeds 1 mg/L, then the sodium sulfite contactor will

be placed on the RW-4 recovery piping. Detailed information on groundwater

monitoring during ISCO injections can be found in the Groundwater Monitoring Plan

included in Appendix L.

Sodium sulfite is commonly used to neutralize chlorine in water treatment processes.

Chlorine is an oxidizer, like permanganate, and reacts in a similar manner. Sodium

sulfite will neutralize the permanganate according to the following theoretical chemical

reaction:

2MnO4- + 3SO3

-2 2MnO2 + 3SO4-2 + 2OH-

ARCADIS performed bench testing to verify the reaction and to confirm theoretical

molar and mass reaction ratios. This study was needed to evaluate the dosages of

sodium sulfite required at varying concentrations of permanganate. The bench test

results are provided in Tab #9. The results of the bench test confirmed that the sodium

sulfite neutralized the permanganate and reaction ratios were similar to the theoretical

values. As shown by this reaction, the molar relationship between permanganate and

sulfite is 2:3 and the mass ratio is 1.33 mg of sulfite per 1.0 mg of permanganate.

The sodium sulfite contactor installed on the RW-4 recovery piping will be filled with

sodium sulfite tablets. A slip stream from the groundwater recovery piping will direct

water into the contactor which will dissolve the sodium sulfite tablets. Sodium sulfite

solution will then be routed into the process flow stream. The concentration of sodium

sulfite will be controlled by adjusting the flow rate of process water through the

contactor. As the sodium sulfite tablets are dissolved, new tablets will be added.

Sodium sulfite usage will be based on the concentration of permanganate in the

recovered groundwater and the mass relationship noted above. Vendor specifications

and the sodium sulfite MSDS are included in Tab #9.

Based on the bench test results and professional judgment, the sodium sulfite

neutralization will be effective from 1 to greater than 1,000 mg/L of permanganate.

However, it is not desirable to exceed permanganate concentrations of 100 mg/L due

of the significant amounts of manganese that will be produced. Therefore, from

concentrations of 1 to 100 mg/L, the sodium sulfite contactors will be used to react the

permanganate. For permanganate concentrations exceeding 100 mg/L, extraction

from RW-4 will be discontinued until permanganate concentrations within the

groundwater surrounding RW-4 are naturally reduced.




2.3.1.2 Influent Equalization Tank (T-1300)

The influent EQ tank (T-1300) will provide 18,000 gallons of useable storage capacity

for pre-treated process water flows from the AOP pre-treatment system. EQ tank (T-

1300) will provide approximately 150 minutes of residence time at the design flow rate

of 60 gpm (from the AOP pre-treatment system) and will have a minimum operating

capacity of 9,000 gallons. Process water from influent EQ tank (T-1300) will be treated

by AOP-100. A pump within the AOP-100 unit will transfer process water from the EQ

tank through the AOP process to the existing filter feed tank (T-1400).

EQ tank (T-1300) will be equipped with a pressure transducer to sense water level in



the air stripper discharge pumps (P-400A/B) in the AOP pre-treatment system to

maintain a constant water level in the EQ tank. In addition, a redundant high/high float

switch will shut down the AOP treatment system and will disable transfer of pre-treated

process water from the AOP pre-treatment system when activated.

EQ tank (T-1300) will be a steel tank with two sealed top access hatches and smooth

interior walls for easy cleaning. The sizing of the EQ tank (T-1300) is presented in a


Item: Equalization Tank T-1300

Quantity: 1




Working Volume: 18,000 gallons


2.3.1.3 Vapor-Phase Granular Activated Carbon (T-2300)

A passive vapor treatment system including VPGAC vessels will be used to absorb

constituents that may volatilize inside influent EQ tank (T-1300). Passive venting of




this tank will occur as the tank is filled and drained. A calculation was prepared to

estimate the amount of vapors and associated COC concentrations in the vapor

stream from the EQ tank (Tab #10). These will be the only air emissions associated

with the AOP treatment system. Based on the calculations, the air emissions from the

EQ tank is not anticipated to exceed vapor-phase treatment requirements. However,

VPGAC units (T-2300) will be used to prevent potential VOCs in the influent EQ tank

vapor stream from being released to the environment.

The vapor venting from the EQ tank will be treated using a single G-1S Carbtrol®

VPGAC vessel, or equal, containing 200 pounds of carbon and rated for a maximum

flow of 100 cubic feet per minute. The spent VPGAC will be replaced as required

according to air monitoring results; the estimated time for breakthrough is 285 days for

T-1300. A summary of calculations, vendor cut sheets and performance curves for the

VPGAC treatment unit are included in Tab #10.

2.3.1.4 Advanced Oxidation Process – HiPOxTM System (AOP-100)

Pre-treated process water accumulated in influent EQ tank (T-1300) will be transferred

to proposed HiPOxTM unit (AOP-100) by a transfer pump included in the HiPOxTM

system. The HiPOxTM system uses O3 and H2O2 chemistry within an oxidation reactor.

The reactants are injected directly into the water stream in precisely controlled ratios

and locations, generating hydroxyl radicals that attack the bonds in the organic

molecules, progressively oxidizing these compounds and any resulting intermediate

by-products until the basic atoms ultimately recombine into benign end-products of

carbon dioxide (CO2), water, and salts.

The HiPOxTM system is a proprietary system developed by APT, with fully constructed

modules. The process components include feed pumps, an H2O2 storage and delivery

system, oxygen generation and delivery system, an O3 generation and delivery

system, and a process cooling system for the O3 generators. Oxygen will be

generated on-site using vacuum swing absorption (VSA) process and fed into the O3

generator, which is subsequently injected into the reactor along with H2O2. The

treatment module will include plug-flow reactors, O3 and H2O2 injectors, and gas/liquid

separation system. The treatment system will include a caustic solution addition

system to improve the buffering capacity required for efficient treatment. Sodium

hydroxide (50 percent) will be added on the influent and effluent sides of the HiPOxTM

unit to provide pH control capabilities, if needed.




The unit is configured with an integral PLC system which includes controls and sensors

to monitor performance. The control system will operate independently, but there will

be communication links between the HiPOxTM PLC and the main plant PLC to provide

a seamless control system for the AOP treatment system.

The vendor design basis summary, laboratory bench testing results and specifications

for the HiPOxTM unit are included in Tab #10, and are summarized below.

Item: Advanced Oxidation Process Unit AOP-100

Quantity: 1

Manufacturer: Applied Process Technology, Inc.

Type: HiPOxTM SRS Remediation System

Model: SRS-4.0-SS-100

No. Reactors: 4

Reactor Size and Materials:

Nominal 4-inch diameter, stainless steel

Max Flow Range: 1 – 150 gpm


Ozone Generation Capacity:

100 pounds per day

2.3.1.5 Existing Advanced Oxidation Process – HiPOxTM System (AOP-200)

The AOP-200 HiPOxTM system supplied by APT is currently in operation at the ISR

system treating a process flow rate of 32 gpm. This HiPOxTM unit (AOP-100) has been

treating recovered groundwater at the Site for more than 12 months, and has

consistently met discharge requirements. The operational experience with the ISR unit

has provided information for the development of destruction curves and models for

influent concentrations reported at the Site. These models have been taken into

consideration for the design of the HiPOxTM unit (AOP-200) discussed above.

The oxidation process components of the AOP-200 unit include an H2O2 storage and

delivery system, liquid oxygen storage and delivery system, O3 generation and delivery

system, integrated control system, and process cooling system for the ozone

generators. As the water enters the process, pH and alkalinity are adjusted to the




desired range prior to entering the oxidation reactor. Liquid oxygen is vaporized and

fed into the O3 generator, which is subsequently injected into the reactor along with

H2O2 in precisely controlled ratios and locations in the reactor. The system is

configured with controls and sensors to monitor system performance.

2.3.1.6 Filter Feed Tanks (T-1400 and T-1600)

The existing filter feed tanks (T-1400 and T-1600) receive discharge water from the

AOP-200 HiPOxTM unit. During AOP treatment system operation, system piping will be

reconfigured so that filter feed tank (T-1600) will receive flow from the AOP-200

HiPOxTM unit and filter feed tank (T-1400) will receive flow from the AOP-100 HiPOxTM

unit. Process water from the filter feed tanks will be pumped through the catalytic

media filters, multi-media filters and LPGAC vessels by filter feed pumps (P-1100A/B).

The filter feed tanks will be equipped with pressure transducers to sense water level in

the tanks and data is transferred to the plant PLC. Water level set points were


the filter feed pumps (P-200A/B) to maintain a constant water level in the filter feed

tanks. In addition, a redundant high/high float switch will shut down the AOP treatment

system when activated.

2.3.1.7 Filter Feed Pumps (P-1100A/B)

The water from the existing filter feed tanks (T-1400 and T-1600) will be pumped by

filter feed pumps (P-1100A/B) through the catalytic media filters, multi-media filters,

LPGAC vessels and the approximately 2,400 ft distance to the City’s POTW

connection. Two pumps will be provided with one pump operating continuously and the

other pump in standby. The filter feed pumps will be used in the full-scale treatment

system, following discontinuation of modified ISR system operation; therefore, they

have been designed to operate at the maximum full-scale system design flow rate of

146 gpm, but will be operated using VFDs to provide sufficient turn-down capacity to

operate at 92 gpm when used in the modified ISR system. The pump motors and

VFDs will be controlled by the plant PLC that will receive water level data from the filter

feed tanks (T-1400 and T-1600).


The pump specification sheets are presented in Tab #3. The specifications for the filter

feed pumps are provided below.




Item: Filter Feed Pumps P-1100A/B


Quantity: 2

Model: 3196 STi





15 HP, 3560 RPM, 230/460/3/60 TEFC


92 gpm @ 180 ft TDH

2.3.1.8 Backwash Pump (P-1200)

Backwash pump (P-1200) will pump water from the filter feed tanks (T-1400 and T-

1600) through the catalytic media filters (T-1700A/B/C) or the multi-media filters (T-

1800A/B) to the backwash tank (T-2000). Only one set of filters will be backwashed at

a time. The filter feed tanks will be the source of backwash water for the both filter

backwash cycles. The filter feed pumps (P-1100A/B) will be shut-down during the

backwash cycle. The backwash sequence for the catalytic media filters will include a

phase of combined air at 38 SCFM and water at 63 gpm, followed by a water only

backwash at 188 gpm. The required backwash flow rate for the multi-media filter is

106 gpm. Total backwash volume will be 4,710 gallons for the catalytic media filter

backwash cycle and 1,480 gallons for the multi-media filter backwash cycle. Each

backwash will be completed using treated process water; therefore, the solids removed

by filters should generally be free of VOCs.

The backwash pump will be used in the full-scale system following discontinuation of

AOP treatment system operation; therefore, has been designed to operate at the

design backwash rate of 188 gpm. The pump motor will be operated using a VFD

controlled by the plant PLC that will receive water level data from the filter feed tanks

(T-1400 and T-1600). The VFD will allow for maximum flow and pressure control, and

will allow adjustments to be made during each application.


The pump specification sheets are presented in Tab #3. The backwash pump

specifications are provided below.




Item: Backwash Pump P-1200


Quantity: 1

Model: 3196 STi





15 HP, 3000 RPM, 230/460/3/60 TEFC


190 gpm @ 160 ft TDH

2.3.1.9 Catalytic Media Filters - LayneOxTM (T-1700A/B/C)

Following AOP treatment through the HiPOxTM systems, water will be pumped through

a catalytic media filter package that will include three vessels filled with LayneOxTM

granular filter media. LayneOxTM operates both as a classic filter and as a catalytic

media, converting ferrous iron (Fe+2) to ferric iron (Fe+3), and accelerating the

precipitation and adsorption of the particles. Although the retention time in the

HiPOxTM reactor will be sufficient to complete oxidation of iron through AOP treatment,

iron that is not oxidized will become catalytically precipitated and then adsorbed

directly onto the LayneOxTM media. The H2O2 residual from the HiPOxTM unit will work

as the oxidant needed to continuously regenerate and replenish the media. The

specifications and MSDS for the LayneOxTM media are included in Tab #11.

The filters are designed for the full-scale treatment design flow of 146 gpm and the

filtration performance will not be affected by lower flow rates that will occur during

operation of the AOP treatment system. The catalytic media filter unit will include three

4-foot diameter carbon steel vessels (T-1700A/B/C) in a pre-packaged skid with an

internal control system. The selected vessels will provide a minimum bed depth of 36

inches, and a media contact time of approximately 5.8 minutes. The removed particles

and adsorbed iron will be expelled during backwash. The backwash frequency of the

LayneOxTM media is anticipated to be once per day when the differential pressure

across the filters is approximately 10 psi. The backwash procedures will include a

combined air scour and water phase, followed by a water only phase. Backwashing

with combined air and water will allow the use of lower backwash rates, reducing the

generated backwash volumes. Treated process water will be used as the source of




water for backwashing. The calculation for the catalytic media filter sizing, backwash

requirements, and vendor cut sheets are presented in Tab #11. Specifications are

provided below.

Item: Catalytic Media Filters T-400A/B/C


Model: MM-4860-3AS, complete skid mounted


Service Flow Rates: Nominal flow range 189-567 gpm; max flow rate 756 gpm


Backwash Flow Rate: 63 gpm and 188 gpm water;

38 scfm air scour




2.3.1.10 Multi-Media Filters (T-1800A/B)

A multi-media filtration system (T-1800A/B) is currently being used in the existing ISR

system operation. The vessels currently contain LayneOxTM media, which will be

switched out for a multi-media consisting of gravel, coarse garnet, fine garnet, and

anthracite. The filters will be used for back-up filtration of iron particulates and

suspended solids that may break-through the upstream catalytic media filters. The

multi-media filters are going to be used to protect the LPGAC vessels from fouling.

Multi-media filters were selected for their good filtration performance (consistent

removal of particles 5 microns in size or greater) and ability to handle the design flow

rate 92 gpm.

The multi-media filter package includes two 30-inch diameter vessels in a pre-

packaged skid with an internal control system supplied by Yardney. During normal

AOP treatment system operation, both vessels will operate continuously in parallel. To




prevent clogging, the filters will be backwashed when the differential pressure across

the filters is approximately 15 to 20 psi. Backwash frequency is anticipated to be once

every three days, and treated process water will be used as the source of water for

backwashing. Calculations for multi-media filter sizing, backwash requirements, and

vendor cut sheets are presented in Tab #11. Specifications are provided below.

Item: Multi-Media Filters T-1800A/B


Model: MM-3060-2AS


Service Flow Rate: Nominal flow range 50-147 gpm; max flow rate 196 gpm

Backwash Flow Rate: 74 gpm




2.3.1.11 Backwash Tank (T-2000)

The backwash tank (T-2000) will receive backwash water from the catalytic media

filters (T-1700A/B/C) and multi-media filters (T-1800A/B/C). The backwash tank will

provide 18,000 gallons of usable storage capacity. This will be a sufficient volume to

handle daily backwash events plus 21-days of solids storage capacity. Backwash

solids from the catalytic media and multi-media filters will be allowed to settle between

backwash cycles. The catalytic media filters will be backwashed daily, while the multi-

media filter backwash cycle is estimated to be approximately once every 3 days. Prior

to the backwash sequence, the supernatant within the tank will be decanted to the

influent EQ tank (T-1300). Sufficient volume will be decanted to provide room to

accept water from the new backwash cycle. Each backwash cycle for the catalytic

media and multi-media filters results in 4,170 and 1,480 gallons of backwash solids to

the backwash tank, respectively. This cycle of backwashing, settling and decanting will

continue until solids build up in the bottom of the tank. At this time, the system will be

shutdown and the solids will be removed and taken off-site for disposal.




The backwash tank will be equipped with a pressure transducer to sense water level in

the tank and data will be transferred to the plant PLC. In addition, a redundant

high/high float switch will shut down the AOP treatment system when activated.

The backwash tank will be a steel tank with two sealed top access hatches and smooth

interior walls for easy cleaning. The sizing of the backwash tank is presented in a


Item: Backwash tank T-2000

Quantity: 1






2.3.1.12 Decant Pump (P-1300)

The decant pump (P-1300) will pump water from the backwash tank (T-2000) to the

influent EQ tank (T-1300). One backwash cycle storage volume (4,170 gallons or

1,480 gallons for catalytic media and multi-media filter backwash cycles, respectively)

will be decanted prior to each new backwash cycle. The decant pump has been

designed to decant the required volume of supernatant in approximately 4 hours. The

pump motor will be operated using a VFD controlled by the plant PLC that will receive

water level data from the existing filter feed tanks (T-1400 and T-1600) and the

backwash tank (T-2000). The VFD will allow for maximum flow and pressure control,

and will allow adjustments to be made during each application.

The pump head loss calculations, vendor cut sheet, and performance curves are

presented in Tab #11. The decant pump specifications are provided below.




Item: Decant Pump P-1300


Quantity: 1

Model: 1SC51C-F

Type: Submersible

Size: 1.25-inch discharge; 3 stage


1/2 HP, 3450 RPM, 115/1/60 TEFC


30 gpm @ 43 ft TDH

2.3.1.13 Polymer Injection System (T-2100, P-1400 and SM-300)

During the catalytic media and multi-media filter backwash sequences polymer will be

added to the water stream to promote the formation of larger and heavier particles that

will aid in settling. The polymer injection system will include a storage tank (T-2100),

chemical metering pump (P-1400) and an in-line static mixer (SM-300). Based on jar

testing completed during operation of the existing ISR system, the selected polymer is

PolyFloc AS1002 which will be metered at a dosage rate of 15 ppm. The MSDS and

fact sheet for the PolyFloc are included in Tab #11.

The polymer will be supplied by the vendor in a 5-gallon bucket that is expected to last

approximately 6 months based on the calculated usage rate of 0.56 gallons per week.

The polymer metering pump (P-1400) will inject polymer into an injection port in the in-

line static mixer (SM-300) which will provide rapid mixing of the injected polymer. The

static mixer will be a 4-inch diameter, schedule 40 carbon steel unit containing six

mixing elements.

A summary of polymer usage rates and volumes, and vendor cut sheets are presented

in Tab #11. Polymer metering pump and static mixer specifications are provided

below.




Item: Polymer Metering Pump P-400


Model: AA-971-352HI


10 gpd (27 mL/min) @ 140 psi

Design Flow Range: 3.6 – 10.7 mL/min



Model: Series 275


Size: 4-inch

2.3.1.14 Liquid-Phase Granular Activated Carbon Adsorption (T-1900A/B/C)

Following catalytic media and multi-media filtration, water will be pumped through a

series of two LPGAC vessels for polishing treatment. The HiPOxTM systems (AOP-100

and AOP-200) are designed to reduce COC concentrations to meet the required

effluent concentrations in accordance with discharge limit requirements. Therefore, the

contaminant loading on the LPGAC vessels will be minimal. The LPGAC vessels will

provide an additional polishing treatment step to provide a factor of safety against

unintended discharges of VOCs.

The LPGAC module will include three 72-inch diameter vessels, containing 2,500

pounds of acid-washed coconut carbon each. During normal operation, two vessels

will be on-line (lead and lag configuration) with one vessel on stand-by. The selected

LPGAC module is a skid-mounted, fully piped unit that allows the flow to be switched

between the vessels.

As the useful life of the carbon is reached, it will be scheduled for change-out. In the

event that process monitoring results indicate that compounds are breaking through

the lead vessel, the vessel will be taken out of service and replaced with a new unit

(stand-by vessel). The estimated time for breakthrough is 85 days (Tab #12);




however, other factors besides VOC loading may contribute to the carbon adsorber life

including bio-fouling and scaling. These factors will result in pressure build up across

the LPGAC vessel. When the flow rate through the LPGAC vessel drops below the

required level due to pressure build up, the vessel will be changed out with a new unit.

The spent LPGAC will be taken off-site for proper regeneration or disposal.

The calculation for the sizing of the LPGAC module and vendor cut sheets are

provided in Tab #12. Specifications are provided below.

Item: LPGAC Vessels T-1900A/B/C


Model: LPGAC 7272-3MS, complete skid mounted

Type: 3-vessel system with manifolded influent, effluent and backwash piping; and manual valves



2.3.2 Discharge of Treated Water

Recovered groundwater from the existing ISR recovery wells and the AOP pre-

treatment system will be treated via air stripping, AOP technology, subsequent catalytic

and multi-media filtration, and final carbon polishing. Following treatment through the

LPGAC system, the water will be discharged to the City’s POTW under an IWDP.

Currently, the treated process water from the existing ISR system is discharged to the

City’s POTW through an on-Site connection under IWDP # SPFL-562910-SIU-08-112.

The existing sewer discharge location does not have sufficient hydraulic capacity for

the modified ISR system; therefore, a new discharge location will be established. A

new 6-inch diameter underground pipeline will be routed north along 72nd Street from

the AOP treatment system and will tie-in to an existing gravity pipeline located on 22nd

Avenue. In addition, the permit is expected to be increased to 100 gpm to

accommodate the increased flow rate from the modified ISR system. The City has

tentatively approved this modification which is discussed in a letter included in

Appendix A.




2.4 Modified ISR System General Arrangement

The general arrangement layout for both the AOP pre-treatment and AOP treatment

systems will be located as shown on Figures J-12 and J-13, Tab #13. Each layout

illustrates the general arrangement of process equipment and control panels for the

treatment systems. The AOP pre-treatment system will be housed inside Building M

and will be situated near the in-situ thermal system. The AOP treatment system will be

placed outdoors, on the parking lot on the south end of Building E. Equipment for the

AOP treatment system will be specified consistent with outdoor use and will be

properly grounded.

2.4.1 Containment Curb

A 9-inch high containment curb will be provided around the perimeter of the AOP pre-

treatment system. The containment berm walls and bottom of containment area will be

sealed with a concrete floor sealer. A 9-inch high containment curb will be provided

around the perimeter of the AOP treatment system. The containment berm walls and

bottom of containment area will be sealed with an asphalt sealant. The purpose of the

containment curbs is to contain any water that leaks from process piping or tank

rupture. A calculation is provided in Tab #14 that determines the required and actual

containment volume for each system.

2.4.2 Floor Sumps and Pumps

One floor sump equipped with a sump pump will be provided for each treatment

system and will be installed within the containment area. The sumps will be

approximately 2.5 ft wide by 2.5 ft long by 2 ft deep. Each floor sump will be sealed to

prevent infiltration of spills through the asphalt or concrete slab. Water collected in the

AOP pre-treatment system floor sump will be pumped using sump pump (P-800) to

influent EQ tank (P-200A) to be processed through the system. In addition, water

collected in the AOP treatment system floor sump will be pumped using sump pump

(P-1500) to the influent EQ tank (T-1500) for processing.

2.5 Modified ISR System Support Equipment

The support equipment needed for operation of the treatment system includes air

compressors and eyewash/safety showers. The following sections present the details

for these treatment components.




2.5.1 Air Compressors (A-100 and A-200)

Air compressor (A-100) will be installed in the AOP pre-treatment system to provide

compressed air for instrument air and pneumatic valve operation. The air compressor

has been designed to operate to provide sufficient pressure to operate the

instrumentation and valves as necessary.

Air compressor (A-200) will be installed in the AOP treatment system to provide

compressed air to the catalytic media filters as part of the backwash sequence. The air

compressor was sized to provide 38 scfm of air flow to the catalytic media filters to

promote scouring of the media and optimize the backwash cycle. The air compressor

has been designed to operate at the design air flow rate and provide sufficient pressure

to push air through the catalytic media.

The air compressor inlet and discharge lines will be equipped with pressure indicators

to sense pressure in the piping and data will be transferred to the plant PLC. Pressure

set points will be programmed into the control logic for the system so the PLC will

automatically operate the air compressors (A-100 and A-200), as part of compressor

cycle operations.

The air compressor vendor cut sheets and performance curves are presented in Tab

#15. The specifications for the compressor are provided below.

Item: Air Compressor A-100

Manufacturer: Atlas-Copco, or equal

Quantity: 1

Model: SF 1

Type: Oil free, scroll compressor


2 HP, 230/460/3/60


5.7 scfm @ 116 psi




Item: Air Compressor A-200

Manufacturer: Atlas-Copco, or equal

Quantity: 1

Model: SF 11

Type: Oil free, scroll compressor


15 HP, 230/460/3/60


42.8 scfm @ 116 psi

2.5.2 Safety Showers

Two eyewash/safety shower units will be installed in the modified ISR system; one

within the AOP pre-treatment system area and the other in the AOP treatment system

area. Potable water will be provided to each safety shower.

2.5.3 Treatment System Control and Interconnections

Operation of the modified ISR system includes the operation and process control of

three interconnected treatment systems including the in-situ thermal system, the AOP

pre-treatment system, and the AOP treatment system. These three systems are

interconnected by water and vapor piping, in addition to process control

communications. The treatment system piping and process control interconnections

are discussed below.

2.5.3.1 Process Piping Interconnections

The process piping interconnections between the in-situ thermal, AOP pre-treatment,

and AOP treatment systems are described below.

1. Piping routed from the in-situ thermal system to the AOP pre-treatment system

includes:

Process water (maximum flow of 60 gpm from multi-phase extraction wells

and condensate);

Chilled water feed to the heat exchangers (80 gpm at 40 oF); and




Blow-down water (a total of 3-8 gpm from the air scrubber, water softener, and other miscellaneous blow-down ports in the in-situ thermal system).

2. Piping routed from the AOP pre-treatment system to the in-situ thermal system:

Air strippers vapors (approximately 900 SCFM);

Tank vent vapors (approximately 70 SCFM); and

Chilled water return from heat exchangers (80 gpm at 85oF).

3. Piping routed from the AOP pre-treatment system to the AOP treatment system:

Process water (maximum flow of 60 gpm from multi-phase extraction wells

and condensate pre-treated through AOP pre-treatment system); and

Blow-down water (a total of 3-8 gpm from the air scrubber, water softener, and other miscellaneous blow-down ports in the in-situ thermal system treated through LPGAC).

2.5.3.2 Programmable Logic Controllers and Control Interconnections

The in-situ thermal, AOP pre-treatment, and AOP treatment systems are operated

using independent control systems. Each system is controlled using individual PLCs.

The PLC includes a program or set of detailed instructions for operation of the

treatment system. The function of the PLC is to automate the operation and

monitoring of the treatment process. Some examples of the PLC functions include:

• Receiving and recording process data including

– Tank water levels;

– Motor speeds;

– Alarm conditions;

– System operating time; and

– Temperature and pressure within the various process units and piping.

• Controlling the speed of pumps or blowers in the system

• Shut down portions or all of the treatment system during alarm conditions




• Phone (or text message) the plant operators for maintenance reminders and/or

notification of an alarm indication or plant shutdown

• Provide the ability to remotely monitor the plant and/or trouble shoot problems

when they arise

Each PLC will control and monitor the operation of the treatment system. Since the

three treatment systems are interconnected, it is necessary for the three individual

PLCs to be able to communicate. For example, if one system is automatically shut

down by the PLC, notifications to the other treatment system PLCs and/or operators

are necessary so that the other systems adjust operations for changing conditions.

Each system will have the ability to send and receive status signals (status – plant is

on, plant is off) between the other system PLCs. Specific details on the type of signals

and the response to the signals are discussed in the control logic table presented in

Tables J-5 and J-6, Tab #16.

The PLC for each treatment system will be located within the control panels associated

with each system. Control wiring between the three PLCs will be installed to allow

these communications mechanisms.

2.5.4 Modified ISR System Piping and Instrumentation

As discussed in previous sections, the PID for the modified ISR system is provided on

Figures J-4 through J-11, Tab #2. Piping details are presented in the PID, which

includes the general orientation of piping, pipe sizes, pipe materials, and pipe fittings.

Further discussions on treatment system piping and process and instrumentation

details are presented below.

2.5.4.1 Treatment System Piping

Most process and vent piping used in the modified ISR will be painted schedule 40

carbon steel, appropriately sized for specific design flow rates of individual process

lines. In general, pipes will be sized to maintain flow velocities in the range of 2 – 5 feet

per second (ft/sec). Velocities within this range will prevent solids deposition in the

pipe lines and avoid water hammer that may be caused at higher velocities. The

piping within the plant will be well supported and fastened according to manufacturer

recommendations. Other pipe materials may be used (including polyvinyl chloride

[PVC], chlorinated PVC, tubing, stainless steel, and/or hose) for secondary process

streams and chemical metering. In areas that are prone to vibration and/or heat, such




as at the inlet and outlet connections of pumps, braided steel flexible connections will

be used to reduce wear on pumps and prevent damage to piping joints. The piping

materials will be compatible with the conditions present in the modified ISR system.

2.5.4.2 Process and Instrumentation

The modified ISR system has been designed to run continuously. The instrumentation

and control logic for the treatment system is summarized in Tables J-5 and J-6, Tab

#16. The location of various instrumentation components is shown on the PIDs

included in Tab #2. The PLC system will monitor key treatment system parameters

that will include pressure of the influent groundwater recovery piping (for pipeline

break); influent and post-process tank water levels; containment levels; multiple system

alarms for treatment equipment including the air strippers, AOP treatment systems,

catalytic media filters, multi-media filters and LPGAC; pump operation; effluent flow

rates and pH levels. The control scheme for the modified ISR system includes

redundant control devices in critical control features such as tank water level alarms to

prevent tank overflows.

The system parameters and alarms will be able to be remotely monitored via

computer-to-computer software such as PCAnywhere. This will allow treatment

system operation to be monitored off-site, remote diagnosis of alarm conditions, and

remote system shut down, as necessary. When operating parameters are out of the

operation range, the modified ISR system will automatically shut down and the

monitoring system will notify on-call personnel by text message and email. The system

will not be re-started from a remote location; plant startup will only be conducted by an

operator located at the facility.

Flow meters and/or totalizers will be placed throughout the AOP pre-treatment and

AOP treatment systems to monitor and record process flow rates. Flow meters in the

AOP pre-treatment system will be placed on the scrubber blow-down LPGAC effluent

line, multi-media filter influent line, multi-media filter backwash line and system effluent

line. Flow meters in the AOP treatment system will be placed on each recovery well,

the catalytic media filter influent line, filter backwash line, and at the discharge line to

the POTW. This will enable quantification of water processed through the AOP unit,

and treated water discharged to the POTW.




2.5.4.3 Modified ISR System Sampling Ports

Sampling ports will be located in the system process lines so that the performance of

the AOP pre-treatment and AOP treatment systems can be monitored. Sample port

locations within the modified ISR system are detailed in Table J-7, Tab #17. The

Operation and Maintenance Plan (O&M), which is discussed in subsequent sections,

will provide additional details regarding AOP pre-treatment and AOP treatment system

sampling and analysis.

2.5.5 Chemical Handling and Storage

The chemicals used throughout the modified ISR system include 50 percent sodium

hydroxide, 25 percent H2O2, ozone gas (generated on-Site), liquid/gaseous oxygen

and PolyFloc flocculent polymer. The 50 percent sodium hydroxide will be utilized for

pH adjustment will be stored in a 275-gallon tank (T-1000) in the AOP pre-treatment

system. An 800-gallon tank will be used for storage of 25 percent H2O2, which will be

included with the HiPOxTM system equipment in the AOP treatment system. These

chemical storage tanks will have individual secondary containment to prevent the

spread of potentially leaked chemicals. The secondary containment vessels will be

inspected daily for signs of damage, weakening, or leakage. Appropriate physical

separation will be provided to prevent reactivity between chemicals or their containers

should a leak in any container occur.

The HiPOxTM system uses oxygen to generate ozone. Oxygen will be generated on-

Site using VSA process for the AOP-100 unit, and liquid oxygen will continue to be

used for the AOP-200 unit as discussed in previous sections. Secondary containment

for this equipment is not required for gases. Similarly, the PolyFloc AS1002 does not

require secondary containment; however, spilled polymer may be slippery resulting in a

health and safety concern. Small amounts of spilled polymer will be wiped up and

washed down with copious amounts of water. A large spill will be contained and

absorbed on inert material, then disposed as solid waste, prior to flushing with water.

Chemicals will be delivered to the Site as needed. As chemicals are delivered, they

will be transferred to the on-line process tanks. A Best Management Practices Plan

(BMPP) has been developed for the RAPA and is included in Appendix M. The

document provides further information on handling and storage of the chemicals

needed for the treatment process.




2.5.6 Air Emissions

In the AOP pre-treatment system, air emissions are associated with the influent EQ

tanks (T-200A/B/C), the aeration tank (T-300), the filter feed tank (T-400), the

backwash tank (T-800) and the air strippers (T-600A/B). These emissions will be

treated by the in-situ thermal system to destroy any COCs in the vapor prior to

discharge to the atmosphere. An estimate of air emissions from the AOP pre-

treatment system is summarized in Tab #18.

Air emissions from the AOP treatment system are primarily associated with the EQ

tanks (T-1300 and T-1500). These emissions will be treated by VPGAC to capture any

COCs in the vapor prior to discharge to the atmosphere. An estimate of air emissions

from the AOP treatment system is summarized in the VPGAC calculations provided in

Tab #10.

2.5.7 Utility Requirements

Utility requirements for the modified ISR system will be potable water, electricity,

telephone and POTW discharge.

2.5.7.1 Electricity

Electric power for the modified ISR system will be used to operate all motors, controls,

lighting and other electrical devices required at the treatment facility. Power

requirements will be three-phase 460 volt power is anticipated to be used. An

electrical load calculation is presented in Tab #19; the anticipated electrical load for the

AOP pre-treatment and AOP treatment systems is approximately 65 kilovolt-ampere

(KVA) and 95 KVA, respectively.

2.5.7.2 Water

Water will be required for general system maintenance, initial treatment plant filling and

hydraulic testing, and some process make-up water. Adequate potable water service

to the Site exists.

2.6 Operation and Maintenance Plan

The proposed PFDs for the Modified ISR system are shown on Figures J-2 and J-3,

Tab #1. The PID is presented on Figures J-4 through J-11, Tab #2. The AOP pre-




treatment and AOP treatment systems have been designed to run on a continuous

basis; however, prior to continuous operation the modified ISR system will be started-

up and tested for performance optimization. To promote proper operation of the

system, O&M activities described in this section will be conducted.

2.6.1 Pre-Start-Up Inspection

Pre-start-up activities will be conducted to test mechanical and electrical functionality of

unit processes, system controls, and fail-safe mechanisms. These activities will

include inspection of the system installation when it is mechanically and electrically

complete to verify that it meets installation specifications. A clean water test will be

completed to verify that the tanks and piping system are leak-free.

The modified ISR system equipment, control panels, level switches, fail-safe

mechanisms, and alarms will be tested and verified to confirm appropriate operation

and correct response of the PLC. The sensors will be manually triggered to confirm

the correct response and activities will be recorded in pre-start-up inspection and alarm

checklists developed prior to start-up.

2.6.2 System Start-Up

Following the installation inspection and equipment check, the start-up procedure will

be initiated. System start-up activities will be conducted to test and optimize system

performance. Start-up procedures are described in the subsequent sections.

2.6.2.1 Start-Up Operation

Based on the performance of the existing ISR system, it has been determined that the

current operating settings for the HiPOxTM unit are consistently effective in treating

groundwater extracted from the existing ISR recovery wells (RW-2 through RW-5) to

the discharge standards established by the City, and to levels below the applicable

groundwater cleanup target levels (GCTLs) specified in Chapter 62-777 Florida

Administrative Code (F.A.C.). Therefore, start-up operation of the current AOP unit

(AOP-200) is not warranted. The ISR recovery wells and associated HiPOxTM unit will

be operated in continuous mode while the remaining modified ISR system equipment

is under-going start-up testing.

Start-up procedures will be implemented for the AOP pre-treatment system and the

HiPOxTM unit (AOP-100). During the start-up operation, the influent for the AOP pre-




treatment system will consist of groundwater recovered during the start-up period of

the in-situ thermal system (refer to Appendix I). The recovered groundwater will be

discharged into the heat exchanger feed tank (T-100) and treated through the AOP

pre-treatment process prior to being routed to the AOP treatment system. An initial

range of O3 and H2O2 dosage conditions for the AOP-100 unit will be pre-determined

based on ISR operational experience and bench testing results. The chemical

dosages within the pre-determined range will be evaluated to optimize AOP-100

operating parameters, with analytical samples collected for each condition.

The treated effluent of the AOP-100 unit will be containerized in the filter feed tank (T-

1400) pending laboratory analysis. Effluent COC concentrations will be verified to be

below permitted discharge levels prior to combining the treated effluent of both AOP

units for POTW discharge. In the event that laboratory analytical results indicate that

IWDP requirements are not met for the AOP-100 treated effluent; the water will be

pumped back to the influent equalization tank (T-1300) for re-processing. Adjustments

will be made to the AOP-100 settings as necessary. This procedure will be repeated

until effluent analytical results are below discharge permit criteria.

The start-up period is expected to last approximately two weeks; however, the

schedule may be adjusted based on field experience and system performance. The

start-up period will provide information to define the AOP pre-treatment system and

AOP-100 unit operating settings for continuous operation.

2.6.2.2 Level of Monitoring

The start-up monitoring program for the AOP pre-treatment system and AOP-100 unit

is summarized in Table J-8, Tab #20. Samples will be collected throughout the

treatment process to obtain data required to evaluate system performance. The

samples will be placed in iced coolers and delivered to a certified laboratory to be

analyzed on an expedited turnaround-time (24 to 48 hours).

Laboratory analytical results for the different operating settings will be evaluated to

optimize system performance. When laboratory analytical results for the effluent

samples indicate that concentrations of target constituents are in compliance, the

treated water will be discharged to the POTW and samples will be collected during

discharge in accordance with the IWDP.




2.6.3 System Proof of Performance Testing

The results of the start-up operation will provide information to define the operating

parameters for continuous operation of the AOP pre-treatment system and the

operating settings for the AOP-100 unit. During the system proof of performance

testing, the capability of the treatment process to consistently treat recovered

groundwater from the in-situ thermal system will be verified. Based on the results of

the performance testing, reaction rates will be estimated for the AOP process. System

proof of performance procedures are described in the following sections.

2.6.3.1 Performance Testing

Based on start-up results, operating parameters will be selected and tested in batch

mode to confirm output conditions. Three consecutive batches will be completed using

the selected operating settings to confirm compliance with the discharge permit

requirements. During the confirmatory batches, AOP pre-treatment system operation

will be consistent with the start-up period.

In compliance with discharge protocols, treated water will be discharged after

laboratory analysis confirms that the water has been successfully treated to the

discharge standards established by the IWDP. This testing period is expected to last

approximately two weeks, although the schedule may be adjusted based on field

experience and system performance.


The same level of monitoring and effluent disposal protocol associated with the start-up

operation will be maintained during the proof of performance period.

2.6.4 System Continuous Operation

At the completion of the proof of performance testing, the modified ISR system will be

considered ready for continuous operation and discharge to the POTW. When

compliance is verified, the AOP pre-treatment system and AOP-100 unit will be

operated in continuous mode using the confirmed operating parameters, in conjunction

with the previously established continuous operation of the AOP-200 unit and ISR

recovery well network.





The modified ISR system treated water discharge samples will be collected in

accordance with Rule 62-780.700(3)(g), F.A.C. and the IWDP requirements. In

addition, operational samples will also be collected to evaluate the performance of the

AOP pre-treatment system and the AOP units. Sampling location, analysis, and

frequencies are further discussed in Section 2.8.1 – Treatment System Process

Monitoring.

The alarms and system operation will be accessible by remote telemetry using the

treatment system computer and PCAnywhere software. System shutdown will result in

activation of the system auto dialer, which will be used to alert pre-designated

personnel by text message and/or email. The PLC, treatment system computer, and

PCAnywhere software will be used to remotely investigate, identify necessary action,

and document alarm conditions that occur.

2.6.4.2 Operational Optimization

The modified ISR system has been designed to handle variations in influent

concentrations and flow rates. Based on data obtained during operation of the existing

ISR system, the modified ISR system is expected to be effective in containing affected

groundwater and removing COCs from the water prior to discharge to the City POTW.

The process monitoring program discussed in Section 2.8.1. includes collection of

samples from the influent to AOP-100 to monitor the incoming conditions for the

treatment unit. Adjustments to the operating conditions will be performed based on the

monitoring results and the established reaction rates for the HiPOxTM unit.

2.6.5 Maintenance Activities

Two full-time operators and support staff, as needed, will operate the modified ISR

treatment system. The operators will be responsible for maintaining records

throughout the operation of the treatment systems to verify performance and document

proper O&M. The O&M activities performed on the AOP pre-treatment and AOP

treatment system components will be documented on appropriate O&M Field Logs.

The operator will be responsible for performing and documenting preventative

maintenance tasks on treatment system components and safety controls. A managing

engineer will oversee operation of the system. Copies of the O&M Manuals provided

by the equipment manufacturers will be stored at the treatment system, and a separate




treatment system O&M Manual will be developed as part of the design documents. A

supply of expendables and tools will be maintained on-Site for O&M purposes.

2.6.5.1 Routine Operation and Maintenance

Operating personnel will perform routine O&M activities on a daily basis during the

start-up operation and proof of performance period. During continuous operation, the

routine O&M activities will be conducted daily for the first five days and then reduced to

at least two times a week. The following practices will be considered routine O&M

activities:

AOP Pre-Treatment System

• Visually inspect tanks and piping for leaks and integrity.

• Inspect heat exchangers and record operating temperatures.

• Observe treatment system blowers and process pumps during normal operation

and check for unusual noises or general indications of poor performance.

• Record treatment system blower and process pump operating data (flow rates and

pressures).

• Record tank operating water levels.

• Record sodium hydroxide levels and usage rates.

• Record pH levels through treatment units.

• Observe chemical metering pump during normal operation and check for leaks and

general indications of poor performance.

• Record multi-media filter pressures and backwash data.

• Inspect backwash tank.




• Observe operation of polymer injection system (storage tank, metering pump, and

tank water levels) during operation and check for general indications of poor

performance.

• Record instantaneous and totalized system flow rates.

• Inspect and test air compressor.

AOP Treatment System

• Observe recovery well vaults for indications of flooding or damage.

• Observe recovery well pumps during normal operation and check for leaks or

general indications of poor performance.

• Observe piping and tanks for leaks and spills.

• Observe treatment system process pumps during normal operation and check for

leaks, unusual noises or general indications of poor performance.

• Record instantaneous and totalized system flow rates.

• Record tank operating water levels.

• Record HiPOxTM unit operating data.

• Record chemical tank levels.

• Record catalytic media filter pressures and backwash data.

• Record multi-media filter pressures and backwash data.

• Inspect backwash tank.

• Observe operation of polymer injection system (storage tank, metering pump, and

tank water levels) during operation and check for general indications of poor

performance.




• Record pH levels through treatment units and effluent discharge.

• Record LPGAC vessel pressures.

• Inspect and test air compressor.

2.6.5.2 Monthly Operation and Maintenance

In addition to the specific routine O&M activities, operating personnel will perform the

following O&M activities at least once per month in both the AOP pre-treatment and

AOP treatment systems:

• Visually inspect tanks, equipment, associated piping, and containment areas for

leaks, cracks, chips, exterior corrosion, or other damage;

• Check tanks for sediment buildup;

• As is practical, visually verify proper operation of instrumentation (operational and

free of obstruction). Compare local transmitter/gauge displays to the data

displayed at the PLC units;

• Calibrate pH meters;

• Inspect and test the eye wash/safety shower unit; and

• Test high-level tank and spill containment berm alarms.

2.6.5.3 Scheduled Operation and Maintenance

Specific maintenance tasks associated with the treatment units will be scheduled as

required by the equipment manufacturer specifications. For detailed instruction on

performing preventative maintenance on system components, Site personnel will refer

to the manufacturer’s O&M Manual and vendor literature, and the treatment system

O&M Manual that will be stored at the treatment system. The frequency of the

following specific maintenance tasks will be further optimized by operational

experience:




• Clean air stripper trays;

• Clean recovery wells;

• Clean recovery well pumps;

• Clean treatment system tanks;

• Change out VPGAC units;

• Grease motor bearings in treatment system pumps;

• Clean HiPOxTM reactors;

• Replenish treatment chemicals (H2O2, sodium hydroxide, and polymer);

• Backwash for catalytic media filter;

• Backwash for multi-media filter; and

• Change out LPGAC units.

2.7 Best Management Practice Plan

A BMPP has been developed for the RAPA and is included in Appendix M. The

objective of the BMPP is to identify those features and actions that will prevent or

minimize the potential for a release or spill at the recovery and transmission system,

and at the treatment facility. The document provides information on handling and

proper disposal of wastes generated, in addition to the handling and storage of

chemicals needed for the operation of the modified ISR treatment system.

2.8 Monitoring Plan

Three types of performance monitoring are discussed in this section: (1) treatment

system process monitoring, (2) treated water discharge monitoring, and (3) air

monitoring. The performance monitoring activities associated with groundwater

recovery, capture zones, and groundwater quality are discussed in further detail in the

Groundwater Monitoring Plan included in Appendix L.




2.8.1 Treatment System Process Monitoring

Treatment system process sampling and analysis are summarized in Table J-9, Tab

#20. To evaluate the operational performance of the modified ISR treatment system,

the following operational samples will be collected:


• Aeration tank influent – sample will be used to estimate source recovery rates from

the in-situ thermal system and monitor iron concentration/state in the process

water.

• Filter feed – sample will be used to evaluate performance of the iron oxidation

system and determine the solids loading to the multi-media filter.

• Multi-media filter effluent – sample will be used to determine filter efficiency to

remove oxidized iron particles and optimize backwash frequency. Results will be

used to monitor influent concentrations to the air stripper.

• Air stripper discharge – sample will be used to verify treatment efficiency. Results

will be used to determine influent concentrations to the AOP-100 unit.

• Backwash solids – sample will be used to develop waste profile for proper

disposal.


• Recovery wells – sample will be used to monitor source recovery for individual

recovery wells.

• Equalization tank (T-1300) effluent – sample will be used to monitor influent

conditions for the AOP-100 unit.

• AOP-100 unit discharge – sample will be used to verify treatment efficiency to

remove COCs and update destruction curve/model generated for the HiPOxTM unit.




• AOP-200 feed pump (P-1000) – sample will be used to estimate source recovery

rates for the recovery well network and monitor influent conditions for the AOP-200

unit.

• AOP-200 unit discharge – sample will be used to verify treatment efficiency to

remove COCs and update destruction curve/model generated for the HiPOxTM unit.

• Filter feed – Results will be used to determine the influent solids loading to the

catalytic media filter.

• Catalytic media filter effluent – sample will be used to determine filter efficiency to

remove oxidized iron and other particles. Results will be used to optimize

backwash frequency, and determine the influent solids loading to the multi-media

filter.

• Multi-media filter effluent – sample will be used to determine filter efficiency to

remove particles that may break through the catalytic media filter, and optimize

backwash frequency.

• Intermediate LPGAC – sample will be used to determine the time and volume of

water required for COC break through, and optimize the LPGAC change out

frequency.

Additional samples may be collected from supplemental locations as necessary to

monitor system performance and evaluate operational protocols.

2.8.2 Treated Water Discharge Monitoring

Treatment system effluent sampling and analysis are summarized in Table J-9, Tab

#20. The treated water discharge sample will be collected from the secondary (lag)

LPGAC vessel effluent. In accordance with requirements specified in the IWDP and

Rule 62-780-700(3)(g), F.A.C., treated water discharge samples will be collected on

the following frequency:

• Daily – for the first five days of operation;

• Weekly – for the next three weeks; and




• Monthly – for the duration of the remedial action and/or IWDP.

2.8.3 Air Monitoring

Air emissions from the modified ISR system are associated with aeration tank venting,

air stripper discharge and passive venting of process tanks. Vapors from the aeration

tank, process tank venting and air stripper discharge in the AOP pre-treatment system

will be treated by the in-situ thermal system. Passive venting from the influent EQ

tanks in the AOP treatment system will be treated by VPGAC units (T-2200 and T-

2300). Pursuant to Rules 62-780.700(3)(f)(3) and 62-210.300 F.A.C., total air

emissions from the modified ISR system will be maintained below the thresholds for

any single hazardous air pollutant (HAP) or total HAPs; thus no air permits will be

required. As a precautionary measure, the exhaust side of the VPGAC unit will be

monitored using a PID.

Air monitoring activities will be conducted weekly during the first month of operation

and monthly thereafter. The PID monitoring results will be used as an indication of

VPGAC status. In the event that PID results are above 10 ppm, the VPGAC will be

replaced with a new unit. The spent VPGAC will be taken off-site for proper

regeneration or disposal.

2.9 Reporting

Within 120 days of completion of the start-up of the modified ISR treatment system,

Raytheon will provide the FDEP with two signed and sealed sets of As-Built

engineering drawings (Record Drawings). The engineering drawing will include

construction and equipment design specifications of the installed modified ISR system,

and any operational parameters different from those in the approved RAPA. A

summary of the system start-up activities will be included in the engineering drawings.

In accordance with Rule 62-780.700(13), two copies of a Remedial Action Status

Report will be submitted to the FDEP on a quarterly basis during operation of the

modified ISR treatment system (Table J-9, Tab #20). The Remedial Action Status

Reports will document the recovery progress and will summarize recovery activities for

the specified period. The Reports will be submitted within 60 days of the end of the

reporting period and will include the following information:




• Operational summary

– O&M data and activities; and

– BMPP compliance.

• Summary of flow data including

– Flow totalizer readings for the AOP pre-treatment system effluent;

– Summation of recovery well totalizer readings to indicate total recovered groundwater;

– HiPOxTM unit process flow data; and

– Totalizer data for treated water discharged to the sewer.

• Summary of groundwater data

– Groundwater level data;

– Groundwater elevation contour maps;

– Capture zones of the groundwater recovery system based upon groundwater elevation data;

– Groundwater quality summary tables included data from monitoring wells and recovery wells;

– Maps posting groundwater Site COC analytical results in the groundwater stratigraphic units; and

– Analytical reports.

• Summary of treatment efficiency

– Process water analytical data summary;

– Graphs of groundwater COC concentrations versus time for select monitoring locations;

– Site COC source removal rates; and

– Analytical reports.

• Conclusions and recommendations based on the effectiveness of the active

remediation effort

Periodic Compliance Reports (PCRs) will be submitted to the City in accordance with

the requirements specified in the IWDP.




2.10 Cessation Criteria

After in-situ thermal remediation is discontinued, components of the modified ISR

system will be incorporated into the groundwater recovery and treatment system

described in Appendix K. It is expected that active thermal remediation will be

conducted at the Site for up to one year during which time COC source removal will be

optimized. After six to eight months of in-situ thermal system operation, the benefits of

continued remediation will be evaluated in the context of the expected diminished

concentrations of COCs in the extraction system effluent stream.

The cessation criterion for the modified ISR system is contingent upon completion of

the in-situ thermal system operations. Once in-situ thermal system operation is

complete, the modified ISR system operation will also be completed. The cessation

criterion for the in-situ thermal system is discussed in Section 8.6 of the RAPA text.

After shutdown of the modified ISR system, select process equipment will be relocated

and used for the groundwater RTS system described in Appendix K.

Tab 1

Modified ISR System – Design Basis

Table J-1AOP Pre-Treatment System Design Basis Summary

Raytheon CompanySt. Petersburg, Florida

Page 1 of 1

Estimated Flow Estimated Flow Calculated Applied Factor for Calculated Additional DesignUpper Sand Interbedded Upper sand Interbedded Contribution From Contribution From Average Concentration Increased Solubility Maximum Concentration Design Safety Maximum Concentration

Concentration Concentration Concentration Concentration Upper Sand Zone (4) Interbedded Unit (4) From Heating System (5) Due to Heating (6) From Heating System (7) Factor From Heating System (8)

Chemicals of Concern1,1,1-Trichloroethane 111 5,644 50 2,565 60% 40% 1,056 3.4 3,592 20% 4,3101,1-Dichloroethene 871 17,282 396 7,855 60% 40% 3,380 3.4 11,491 20% 13,789cis-1,2-Dichloroethene 701 15,359 319 6,981 60% 40% 2,984 3.4 10,145 20% 12,174Vinyl chloride 729 5,643 331 2,565 60% 40% 1,225 3.4 4,164 20% 4,997Trichloroethene 1,305 57,596 593 26,180 60% 40% 10,828 3.4 36,815 20% 44,1781,1-Dichloroethane 242 8,154 110 3,706 60% 40% 1,549 3.4 5,265 20% 6,3181,4-Dioxane 1,135 19,552 516 8,887 60% 40% 3,864 3.4 13,139 20% 15,767

Other Compounds1,1,2-Trichloroethane 130 470 59 214 60% 40% 121 3.4 411 20% 4931,2,4-Trimethylbenzene 31 775 (1) 14 352 60% 40% 149 3.4 508 20% 6091,2-Dichloroethane 50 (1) 1,261 (1) 23 573 60% 40% 243 3.4 826 20% 9921,3,5-Trimethylbenzene 56 1,400 (1) 25 636 60% 40% 270 3.4 917 20% 1,1012-Butanone (MEK) 475 (1) 11,878 216 5,399 60% 40% 2,289 3.4 7,783 20% 9,3404-Methyl-2-pentanone (MIBK) 58 8,145 26 3,702 60% 40% 1,497 3.4 5,089 20% 6,107Acetone 890 19,121 405 8,691 60% 40% 3,719 3.4 12,646 20% 15,175Benzene 29 (1) 723 13 329 60% 40% 139 3.4 474 20% 569Carbon Disulfide 127 755 58 343 60% 40% 172 3.4 584 20% 701Chloroethane 3 664 1 302 60% 40% 122 3.4 413 20% 496Chloroform 49 17,414 22 7,915 60% 40% 3,180 3.4 10,810 20% 12,973Ethylbenzene 150 180 68 82 60% 40% 74 3.4 250 20% 300Isopropylbenzene 24 600 (1) 11 273 60% 40% 116 3.4 393 20% 472m,p-Xylene 269 171 122 78 60% 40% 104 3.4 355 20% 426Methylene chloride 22 17,550 10 7,977 60% 40% 3,197 3.4 10,869 20% 13,043Naphthalene 8 195 (1) 4 89 60% 40% 38 3.4 128 20% 153o-Xylene 115 170 52 77 60% 40% 62 3.4 212 20% 254Tetrachloroethene 77 1,925 (1) 35 875 60% 40% 371 3.4 1,261 20% 1,514Toluene 1,180 5,789 536 2,631 60% 40% 1,374 3.4 4,673 20% 5,607trans-1,2-Dichloroethene 6 140 3 64 60% 40% 27 3.4 92 20% 111Trichlorofluoromethane 30 750 (1) 14 341 60% 40% 145 3.4 491 20% 590

Bromide -- -- -- -- -- -- 2.0 -- -- -- 2.0Bromate -- -- -- -- -- -- 0 -- -- -- 0Iron (total) -- -- -- -- -- -- 20 -- -- -- 20

Footnotes:

Concentrations in micrograms per liter (g/L). (1) Data was not available. Estimated values were based on a typical ratio of concentrations detected in interbedded unit and upper sand zone. Concentrations are typically 25 times higher in the intebedded unit.(2) Represents the average groundwater concentration detected during the vertical profile investigation performed at Building M in November 2009(3) A factor of 2.2 was estimated to adjust the vertical profile data to reflect expected data from a monitoring well. This factor is based on an analysis of two monitoring wells within the thermal treatment zone using the compounds Trichloroethene and 1,4-Dioxane. VAP results were generally 2.2 times higher than monitoring well data.(4) Based on professional judgment.(5) Flow weighted average calculation (Upper sand zone concentration x flow contribution %) + (Interbedded unit concentration x flow contribution %).(6) The peaking factor of 3.4 was based on other application thermal treatment system data that compares baseline data versus concentrations throughout the thermal treatment operation. (7) Peaking factor x calculated average concentration.(8) Maximum concentration x safety factor.VAP Vertical Aquifer Profilinggpm Gallons per minute-- Not applicable

VAP Analysis (2) Estimated Well Analysis (3)

Compounds

G:\ENV\TF\901-1000\TF922\Reports\2010\RAPA 2010\Final FDEP RAPA\Appendix J\Tab #1\(2) Table J-1 (Tab 1)_PreAOP Design Summary.xls ARCADIS

Table J-2Modified ISR System Design Basis Summary


Page 1 of 1

60 gpm32 gpm

CompoundsDesign Influent

Concentration to AOP Pre-

Treatment System (1)

Estimated Effluent Concentration from AOP

Pre-Treatment System (2)

Detected Concentration from Existing ISR System

Influent (3)

Estimated Effluent Concentration from Modified

ISR System (Standard

Operation) (4)

Estimated Effluent Concentration from Modified ISR System

(Contingency Operation) (5)

St. Petersburg POTW Discharge

Limits

Chemicals of Concern1,1,1-Trichloroethane 4,310 0 0 <200 <200 2001,1-Dichloroethene 13,789 1 61 <7 <7 7cis-1,2-Dichloroethene 12,174 1 480 <70 <70 70Vinyl chloride 4,997 0 0 <1 <1 1Trichloroethene 44,178 4 2,300 <3 <3 31,1-Dichloroethane 6,318 1 38 <70 <70 701,4-Dioxane 15,767 15,767 425 <3.2 <3.2 3.2

Other Compounds1,1,2-Trichloroethane 493 2 0 <5 <5 51,2,4-Trimethylbenzene 609 0 0 <10 <10 101,2-Dichloroethane 992 2 0 <3 <3 31,3,5-Trimethylbenzene 1,101 0 0 <10 <10 102-Butanone (MEK) 9,340 7,076 0 4,615 7,021 7,750 (6)

4-Methyl-2-pentanone (MIBK) 6,107 555 0 362 550 1,640 (6)

Acetone 15,175 12,540 0 8,178 12,442 13,700 (6)

Benzene 569 0 0 <1 <1 1Carbon Disulfide 701 0 0 <700 <700 700Chloroethane 496 0 0 <12 <12 12Chloroform 12,973 1 0 <70 <70 70Ethylbenzene 300 0 0 <30 <30 30Isopropylbenzene 472 0 0 <0.8 <0.8 0.8m,p-Xylene 426 0 0 <20 <20 20Methylene chloride 13,043 4 0 <5 <5 5Naphthalene 153 6 0 <14 <14 14o-Xylene 254 0 0 <20 <20 20Tetrachloroethene 1,514 0 0 <3 <3 3Toluene 5,607 1 0 <40 <40 40trans-1,2-Dichloroethene 111 0 0 <100 <100 100Trichlorofluoromethane 590 0 0 <2,100 <2,100 2,100

Bromide 2.0 2.0 0.7 0.8 1.0 NABromate 0 0 0 0.3 0.3 0.5Iron (total) 20 2.0 10 0.3 0.3 1

Footnotes:

Concentrations are in micrograms per liter (g/L).(1) Calculated values based on estimates provided in Table J-1.(2) Estimated concentrations following AOP pre-treatment system. Refer to Table J-3 for calculation.(3) Concentrations are the maximum influent concentrations detected in the existing ISR system influent during system operation between 3/20/09 and 11/17/09.(4) Standard operation includes treating water from the AOP pre-treatment system and the existing ISR recovery wells. Estimated values are based on operation of both systems.(5) Contingency operation assumes the existing ISR recovery wells will be shut down; therefore, estimated values are based on treatment of the AOP pre-treatment system effluent only.(6) The City of St. Petersburg has provided a letter of intent to approve revisions to the current permit to include increases in flow rate to 100 gpm and increased discharge limits for the indicated compounds.

ISR - Interim Source RemovalPOTW - Publicly Owned Treatment Worksgpm - Gallons per minute

Expected Flow Rate From AOP Pre-Treatment System =Flow Rate From Existing ISR Recovery Wells =

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Page 1 of 1

60 gpm32 gpm







Influent (3)



Operation) (4)




Limits




Acetone 15,175 12,540 0 8,178 12,442 13,700 (6)



Footnotes:







Page 1 of 1

60 gpm32 gpm







Influent (3)



Operation) (4)




Limits




Acetone 15,175 12,540 0 8,178 12,442 13,700 (6)



Footnotes:





Table J-3Modified ISR System

AOP Pre-Treatment System Mass BalanceRaytheon Company


Page 1 of 1

Flow ID:

Parameters Units

Flow Rate (water, average) gpm 60 60 -- -- 60 60 60 60 1.8 (5) 1.8 (5) 0.09 1.7 -- -- --Flow Rate (water, instantaneous) gpm -- -- -- -- -- -- -- -- 106 (5) 106 20 20 -- -- --Flow Rate gpd -- -- -- 8.3 (2) -- -- -- -- -- -- 125 -- -- -- --Air Flow Rate SCFM -- -- 30 (1) -- -- -- -- -- -- -- -- -- 900 40 60Temperature ºF 72 - 180 72 - 120 -- -- 72 - 115 72 - 114 72 - 113 72 - 100 72 - 114 72 - 114 72 - 114 72 - 114 72 - 100 72 - 100 72 - 100Solids Generation cu.ft./day -- -- -- -- -- -- -- -- -- -- -- -- -- -- --

pH SU 6.0 6.0 -- 14.0 7.4 7.4 7.4 7.4 7.4 7.4 7.4 7.4 -- -- --Total suspended solids mg/L 30 30 -- -- 50 (3) 50 5 5 50 1,527 30,000 50 -- -- --Iron (total) mg/L 20.0 20 -- -- 20.0 20.0 2.0 2.0 20.0 611 12,000 20.0 -- -- --Iron (dissolved) mg/L 20.0 20 -- -- 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 -- -- --Bromide mg/L 2.0 2 -- -- 2.0 2.0 2.0 2.0 2.0 2.0 2.0 2.0 -- -- --Bromate mg/L 0.0 0 -- -- 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 -- -- --

1,1,1-Trichloroethane µg/L 4,310 4,310 -- -- 3,879 (4) 3,879 3,879 0 3,879 3,879 3,879 3,879 7.0 (6) 15.7 (6) 10.4 (6)1,1-Dichloroethene µg/L 13,789 13,789 -- -- 12,410 (4) 12,410 12,410 1 12,410 12,410 12,410 12,410 30.6 (6) 69.0 (6) 46.0 (6)cis-1,2-Dichloroethene µg/L 12,174 12,174 -- -- 10,957 (4) 10,957 10,957 1 10,957 10,957 10,957 10,957 27.1 (6) 60.9 (6) 40.6 (6)Vinyl chloride µg/L 4,997 4,997 -- -- 4,497 (4) 4,497 4,497 0 4,497 4,497 4,497 4,497 17.2 (6) 38.8 (6) 25.8 (6)Trichloroethene µg/L 44,178 44,178 -- -- 39,760 (4) 39,760 39,760 4 39,760 39,760 39,760 39,760 72.4 (6) 163.0 (6) 108.7 (6)1,1-Dichloroethane µg/L 6,318 6,318 -- -- 5,686 (4) 5,686 5,686 1 5,686 5,686 5,686 5,686 13.8 (6) 31.0 (6) 20.6 (6)1,4-Dioxane µg/L 15,767 15,767 -- -- 15,767 (4) 15,767 15,767 15,767 15,767 15,767 15,767 15,767 0.0 (6) 0.0 (6) 0.0 (6)

1,1,2-Trichloroethane µg/L 493 493 -- -- 444 (4) 444 444 2 444 444 444 444 0.8 (6) 1.8 (6) 1.2 (6)1,2,4-Trimethylbenzene µg/L 609 609 -- -- 548 (4) 548 548 0 548 548 548 548 1.1 (6) 2.5 (6) 1.6 (6)1,2-Dichloroethane µg/L 992 992 -- -- 893 (4) 893 893 2 893 893 893 893 2.2 (6) 4.9 (6) 3.2 (6)1,3,5-Trimethylbenzene µg/L 1,101 1,101 -- -- 991 (4) 991 991 0 991 991 991 991 2.0 (6) 4.4 (6) 3.0 (6)2-Butanone (MEK) µg/L 9,340 9,340 -- -- 8,873 (4) 8,873 8,873 7,076 8,873 8,873 8,873 8,873 5.7 (6) 31.4 (6) 20.9 (6)4-Methyl-2-pentanone (MIBK) µg/L 6,107 6,107 -- -- 5,802 (4) 5,802 5,802 555 5,802 5,802 5,802 5,802 11.9 (6) 14.8 (6) 9.9 (6)Acetone µg/L 15,175 15,175 -- -- 14,872 (4) 14,872 14,872 12,540 14,872 14,872 14,872 14,872 8.8 (6) 25.3 (6) 16.9 (6)Benzene µg/L 569 569 -- -- 512 (4) 512 512 0 512 512 512 512 1.6 (6) 3.5 (6) 2.4 (6)Carbon Disulfide µg/L 701 701 -- -- 631 (4) 631 631 0 631 631 631 631 2.0 (6) 4.5 (6) 3.0 (6)Chloroethane µg/L 496 496 -- -- 446 (4) 446 446 0 446 446 446 446 1.7 (6) 3.7 (6) 2.5 (6)Chloroform µg/L 12,973 12,973 -- -- 11,676 (4) 11,676 11,676 1 11,676 11,676 11,676 11,676 23.4 (6) 52.7 (6) 35.1 (6)Ethylbenzene µg/L 300 300 -- -- 270 (4) 270 270 0 270 270 270 270 0.6 (6) 1.4 (6) 0.9 (6)Isopropylbenzene µg/L 472 472 -- -- 425 (4) 425 425 0 425 425 425 425 0.8 (6) 1.9 (6) 1.3 (6)m,p-Xylene µg/L 426 426 -- -- 383 (4) 383 383 0 383 383 383 383 0.9 (6) 1.9 (6) 1.3 (6)Methylene chloride µg/L 13,043 13,043 -- -- 11,739 (4) 11,739 11,739 4 11,739 11,739 11,739 11,739 33.1 (6) 74.5 (6) 49.6 (6)Naphthalene µg/L 153 153 -- -- 138 (4) 138 138 6 138 138 138 138 0.2 (6) 0.6 (6) 0.4 (6)o-Xylene µg/L 254 254 -- -- 229 (4) 229 229 0 229 229 229 229 0.5 (6) 1.2 (6) 0.8 (6)Tetrachloroethene µg/L 1,514 1,514 -- -- 1,363 (4) 1,363 1,363 0 1,363 1,363 1,363 1,363 2.0 (6) 4.4 (6) 3.0 (6)Toluene µg/L 5,607 5,607 -- -- 5,046 (4) 5,046 5,046 1 5,046 5,046 5,046 5,046 13.1 (6) 29.5 (6) 19.7 (6)trans-1,2-Dichloroethene µg/L 111 111 -- -- 100 (4) 100 100 0 100 100 100 100 0.2 (6) 0.6 (6) 0.4 (6)Trichlorofluoromethane µg/L 590 590 -- -- 531 (4) 531 531 0 531 531 531 531 0.9 (6) 2.1 (6) 1.4 (6)

Footnotes:gpm - Gallons per Minutegpd - Gallons per DaySCFM - Standard Cubic Feet per MinuteºF - Fahrenheitcu.ft./day - Cubic Feet per Day

SU - Standard Unitmg/L - Milligrams per Literµg/L - Micrograms per LiterNE - Not Estimated at this TimeTSS - Total Suspended Solids

(1) 30 SCFM was the calculated volume to mix the tank using coarse bubble diffusers, volume required to oxidize iron was estimate to be approximately 5 SCFM(2) Sodium hydroxide usage is estimated based on usage in the ISR system which is 12 ml/minute at a flow rate of 33 gpm, the conversion was made to adjust for 60 gpm flow rate and units of gallons per day(3) TSS = TSS (from heating stream) - total iron + (2 X Dissolved Iron)(4) Assume that 10% of volatile compounds will be stripped in the aeration tank which is operated at an approximate air to water ratio of 4:1, removal rates for select compounds were decreased (1,4-dioxane, acetone, MEK, and MIBK)(5) Based on 3 filters beds, each backwashed once per day, 36-inch diameter bed, 106 gpm backwash rate x 8 minute (each bed) x 3 beds

2,545 gpd backwash water required, daily average = 1.8 gpm(6) calculated on separate sheet, units are ppmv

Other Compounds

Multi-Media Filter Effluent

Clean Backwash Water

From In-situ Thermal System

Air to Aeration Tank

Sodium Hydroxide

Aeration Tank Overflow

Multi-Media Filter Influent

Post Heat Exchanger

7 11Water to AOP

Treatment System

Backwash Solids

Chemicals of Concern

General Water Quality Parameters

1 3 4 5 62

Aeration Tank Vapors

8

Tank Vapors

14 1513Decant From

Backwash Tank

Air Stripper Vapors

12

Dirty Backwash Water

9 10

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AOP Treatment System Mass BalanceRaytheon Company


Page 1 of 1

Flow ID:

Parameters Units

Flow Rate (water, average) gpm 60 61 61 32 32 32 93 93 93 93 3.27 (4) 0.34 (5) 3.3 (4) 0.34 1.38 0 1.38 0.06 -- --Flow Rate (water, instantaneous) gpm -- -- -- -- -- -- -- -- -- -- 63, 188 74 -- 74 20 NA 20 -- -- --Flow Rate gpd -- -- -- -- -- -- -- -- -- -- -- -- -- -- -- NA -- 84 -- --Air Flow Rate (instantaneous) SCFM -- -- -- -- -- -- -- -- -- -- 38 (4) -- -- -- -- NA -- -- 4 max 8 maxTemperature ºF 72 - 100 72 - 100 72 - 100 75 75 75 73 - 94 73 - 94 73 - 94 73 - 94 73 - 94 73 - 94 73 - 94 73 - 94 73 - 94 NA 73 - 94 73 - 94 -- --Solids Generation cu.ft./day -- -- -- -- -- -- -- -- -- -- -- -- NA 0 -- -- --

pH SU 7.4 7.4 7.4 6.0 6.0 7.4 7.4 7.4 7.4 7.4 7.4 7.4 7.4 7.4 7.4 NA 7.4 7.4 -- --Total suspended solids mg/L 5 5 5 30 30 50 20 5 1 1 20 20 438 1,099 20 NA 20 30,000 -- --Iron (total) mg/L 2.0 2.0 2.0 10 10 10 5 0.3 0.3 0.3 5 5 101 254 5 NA 5 6,947 -- --Iron (dissolved) mg/L 0.0 0.0 0.0 10 10 0 0 0 0 0 0 0 0 0 0 NA 0 0 -- --Bromide mg/L 2.0 2.0 1.0 (2) 0.7 0.7 0.4 (2) 0.8 0.8 0.8 0.8 0.8 0.8 0.8 0.8 0.8 NA 0.8 0.8 -- --Bromate mg/L 0.0 0.0 0.3 (3) 0.0 0.0 0.3 (3) 0.3 0.3 0.3 0.3 0.3 0.3 0.3 0.3 0.3 NA 0.3 0.3 -- --

1,1,1-Trichloroethane µg/L 0 0 0 0 0 0 0 0 0 <200 0 0 0 0 0 NA 0 0 <1 (6) <1 (6)1,1-Dichloroethene µg/L 1 1 0 61 61 0 0 0 0 <7 0 0 0 0 0 NA 0 0 <1 (6) <1 (6)cis-1,2-Dichloroethene µg/L 1 1 0 480 480 0 0 0 0 <70 0 0 0 0 0 NA 0 0 <1 (6) <1 (6)Vinyl chloride µg/L 0 0 0 0 0 0 0 0 0 <1 0 0 0 0 0 NA 0 0 <2 (6) <2 (6)Trichloroethene µg/L 4 4 0 2,300 2,300 0 0 0 0 <3 0 0 0 0 0 NA 0 0 <1 (6) <1 (6)1,1-Dichloroethane µg/L 1 1 0 38 38 30 0 0 0 <70 0 0 0 0 0 NA 0 0 <1 (6) <1 (6)1,4-Dioxane µg/L 15,767 15,413 0 425 425 0 0 0 0 <3.2 0 0 0 0 0 NA 0 0 NA (6) NA (6)

1,1,2-Trichloroethane µg/L 2 2 0 0 0 0 0 0 0 <5 0 0 0 0 0 NA 0 0 <1 (6) <1 (6)1,2,4-Trimethylbenzene µg/L 0 0 0 0 0 0 0 0 0 <10 0 0 0 0 0 NA 0 0 <1 (6) <1 (6)1,2-Dichloroethane µg/L 2 2 0 0 0 0 0 0 0 <3 0 0 0 0 0 NA 0 0 <10 (6) <10 (6)1,3,5-Trimethylbenzene µg/L 0 0 0 0 0 0 0 0 0 <10 0 0 0 0 0 NA 0 0 <1 (6) <1 (6)2-Butanone (MEK) µg/L 7,076 7,021 7,021 0 0 0 4,615 4,615 4,615 <7,750 4,615 4,615 4,615 4,615 4,615 NA 4,615 4,615 <10 (6) <10 (6)4-Methyl-2-pentanone (MIBK) µg/L 555 550 550 0 0 0 362 362 362 <1,640 362 362 362 362 362 NA 362 362 NA (6) NA (6)Acetone µg/L 12,540 12,442 12,442 0 0 0 8,178 8,178 8,178 <13,700 8,178 8,178 8,178 8,178 8,178 NA 8,178 8,178 <10 (6) <10 (6)Benzene µg/L 0 0 0 0 0 0 0 0 0 <1 0 0 0 0 0 NA 0 0 <1 (6) <1 (6)Carbon Disulfide µg/L 0 0 0 0 0 0 0 0 0 <700 0 0 0 0 0 NA 0 0 <1 (6) <1 (6)Chloroethane µg/L 0 0 0 0 0 0 0 0 0 <12 0 0 0 0 0 NA 0 0 <2 (6) <2 (6)Chloroform µg/L 1 1 0 0 0 0 0 0 0 <70 0 0 0 0 0 NA 0 0 <1 (6) <1 (6)Ethylbenzene µg/L 0 0 0 0 0 0 0 0 0 <30 0 0 0 0 0 NA 0 0 <1 (6) <1 (6)Isopropylbenzene µg/L 0 0 0 0 0 0 0 0 0 <0.8 0 0 0 0 0 NA 0 0 <1 (6) <1 (6)m,p-Xylene µg/L 0 0 0 0 0 0 0 0 0 <20 0 0 0 0 0 NA 0 0 <1 (6) <1 (6)Methylene chloride µg/L 4 3 0 0 0 0 0 0 0 <5 0 0 0 0 0 NA 0 0 <1 (6) <1 (6)Naphthalene µg/L 6 6 0 0 0 0 0 0 0 <14 0 0 0 0 0 NA 0 0 <1 (6) <1 (6)o-Xylene µg/L 0 0 0 0 0 0 0 0 0 <20 0 0 0 0 0 NA 0 0 <2 (6) <2 (6)Tetrachloroethene µg/L 0 0 0 0 0 0 0 0 0 <3 0 0 0 0 0 NA 0 0 <1 (6) <1 (6)Toluene µg/L 1 0 0 0 0 0 0 0 0 <40 0 0 0 0 0 NA 0 0 <2 (6) <2 (6)trans-1,2-Dichloroethene µg/L 0 0 0 0 0 0 0 0 0 <100 0 0 0 0 0 NA 0 0 <1 (6) <1 (6)Trichlorofluoromethane µg/L 0 0 0 0 0 0 0 0 0 <2100 0 0 0 0 0 NA 0 0 <2 (6) <2 (6)

Footnotes:gpm - Gallons per Minutegpd - Gallons per DaySCFM - Standard Cubic Feet per MinuteºF - Fahrenheitcu.ft./day - Cubic Feet per DaySU - Standard Unitmg/L - Milligrams per Literµg/L - Micrograms per LiterNE - Not Estimated at this TimeTSS - Total Suspended Solids

(1) TSS = TSS (HiPOxTM Influent) + (2 X Dissolved Iron)(2) Based on bromide/bromate conversion (30-40%) observed in Interim Source Remediation System

(3) Based on bromate/bromide reduction observed in HiPOxTM technology laboratory testing completed by Applied Process Technology Inc.(4) Based on 3 filters beds, each backwashed once per day with a combination of air and water, followed by water only backwash sequence.

Air & Water Backwash: 48-inch diameter bed, 63 gpm backwash rate x 10 minute (each bed) x 3 beds = 1,890 gpd backwash water (630 gpd) required, on average = 1.31 gpm.38 scfm air scour rate x 10 minutes (each bed) x 3 beds = 1,140 scf per backwash or 380 scfd air sour required, on average = 0.79 scfm.Water Backwash: 48-inch diameter bed, 188 gpm backwash rate x 5 minutes (each bed) x 3 beds = 2,820 gp backwash water or 940 per day required, on average = 1.96 gpm.Total backwash water = 1.1 gpm daily average

(5) Based on 2 filters beds, each backwashed once every three days, 30-inch diameter bed, 74 gpm backwash rate x 10 minute (each bed) x 2 beds1,480 gallons of water required every third day, on average = 0.34 gpm

(6) Vapor concentration units are milligrams per cubic meter (mg/m3)

General Water Quality Parameters

Chemicals of Concern

Other Compounds

MMF Backwash

Solids

2824 25 262313 14 1510 11

T-1500 Influent from

Recovery Wells

AOP-200 Influent

Water From AOP Pre-Treatment

System

AOP-100 Influent

MMF Effluent LGAC Effluent

29

T-2300 Treated Vapor

Effluent

T-2200 Treated Vapor

Effluent

T-2000 Decant

Decant to T-1500

Decant to T-1300

27

Backwash Solids To Disposal

Catalytic Media Filter Backwash

Water

2212 18 19 20

Catalytic Media Filter Backwash

Solids

AOP-100 Effluent

MMF Backwash

Water

2116 17

Catalytic Media Filter Influent

Catalytic Media Filter Effluent

AOP-200 Effluent

G:\ENV\TF\901-1000\TF922\Reports\2010\RAPA 2010\Final FDEP RAPA\Appendix J\Tab #1\(7) Table J-4 (Tab 1)_MISR Mass Balance.xlsx ARCADIS

Tab 2

Modified ISR System – Piping & Instrumentation

Tab 3

Modified ISR System – AOP Pre-Treatment System Heat Exchanger

Page 1 of 1

Calc prepared by: M. SeppanenCalc checked by: J. PerellaDate: 01/28/2010

Considerations:

Tank volume = 2,000 gal

Solids Storage = 188 gal 6-inch Depth

Freeboard = 376 gal 12-inch Depth

Usable tank volume = Total tank volume - Solids storage - Freeboard

Usable tank volume = 1,436 gal

Process flow rate = 60 gpm In-Situ Thermal System Effluent

Total retention time = 24 min

Operation = 80 % Full

Design retention time = 19 min

Additional requirements = 0 gal

Calculate Required Tank Volume:

Retention time volume = Flow rate x Design retention time

1,149 gal

Minimum volume = Retention time volume + Additional requirements

1,149 gal

Tank Selection:

Cylindrical Tank:

Diameter = 8 feet

Sidewall Height = 10.5 feet

Usable Tank Volume = 1,436 gal

Available Tank Volume = 1,436 gal

Required Tank Volume = 1,149 gal

Volume Available > Volume Required therefore design is acceptable

HEAT EXCHANGER FEED TANK (T-100) SIZINGModified ISR System



G:\ENV\TF\901-1000\TF922\Reports\2010\RAPA 2010\Final FDEP RAPA\Appendix J\Tab #3\(1) Tab #3_T-100 Sizing.xlsx ARCADIS

Page 1 of 3

Total dynamic head calculation = Calc prepared by: M. Seppanenhead loss due to elevation change Calc checked by: J. Perellahead loss due to pipe friction Date: 1/28/2010head loss across misc. process componentsrequired discharge head

Calculate pipe size:

Where: v = Velocity (ft/sec)Q = Flow rate (gpm)r = Pipe radius (in)

Flow Rate Pipe Size Pipe ODWall

Thickness Pipe ID Area velocity(gpm) (in) (in) (in) (in) (ft2) (ft/sec)

60 2 2.375 0.154 2.067 0.023 5.5860 3 3.500 0.216 3.068 0.051 2.5360 4 4.500 0.237 4.026 0.088 1.47

*Pipe dimensions noted for Schedule 40 galvanized steel piping.Note: Design for velocity between 3 and 5 feet/sec to maintain sufficient scour velocity.

Calculate head loss (he) due to elevation change:

assume: Height from pump to discharge point = 15 feetHead loss, he = 15 feet

Calculate head loss due to pipe friction losses:

Step 1. There are multiple pipe sections with flow and pipe diameters shown below

Pipe Section 1 Nominal pipe diameter 1 = 3 inch

Flow (v1) = 60 gpm

Step 2. Calculate the friction factor for each pipe section using the Hazen-Williams formula

Hazen-Williams f = .2083 * (100/C)1.852 * (q1.852) / (D4.8655)Formula

f = Friction in head in feet of water per 100 ft of pipeC = Constant for inside roughness

(140 for new galvanized steel pipe, 150 for hdpe pipe)q = Flow rate (gal/min)D = Inside diameter of pipe (inches)

Nominal Diam (in)

ID (in)

ID w/ deposition (in)

1 1.049 0.9241.5 1.610 1.4852 2.067 1.9423 3.068 2.9434 4.026 3.9016 6.065 5.94

NOTE: a 0.0625 inch (1/16 inch) deposition on interior pipe wall is included in diameter for calculation - 1.003 - (2 x 0.0625) = 0.878 inch diameter

HEAT EXCHANGER FEED PUMP (P-100A/B) DESIGN CALCULATIONSModified ISR System - AOP Pre-Treatment System

Total Dynamic Head Calculation


sec60

min1*

)*( 2r

Qv

G:\ENV\TF\901-1000\TF922\Reports\2010\RAPA 2010\Final FDEP RAPA\Appendix J\Tab #3\(3) Tab #3_P-100A&B TDH.xlsx ARCADIS

Page 2 of 3




Friction factor for Pipe Section 1C = Pipe roughness factor 140 unitlessq = flow rate (gal/min) 60 gal/minD1 = Inner pipe diameter (inches) 2.943 inches (see NOTE)

Pipe Section friction factor 1.1 ft water / 100 feet of pipe

Step 3. Calculate the equivalent length of pipe for each section

Nominal Fitting size 1 in 1.5 in 2 in 3 in 4 in 6 in

90˚ Elbows 2.7 3.4 3.6 4.0 4.6 10.4Standard Tee (thru flow) 3.2 5.6 7.7 12.0 17.0 38.3Standard Tee (branch flow) 6.6 9.9 12.0 17.0 21.0 47.3Ball valve (full open) 1.6 2.3 2.9 4.3 5.5 12.3Check Valve 11.0 15.0 19.0 27.0 38.0 85.5Union 0.3 0.4 0.5 0.5 0.7 1.5Reducer (2/1) 1.0 1.5 1.5 3.0 4.0 9.0Expansion (1/2) 1.5 2.5 3.0 4.0 6.0 13.5

Equivalent lengths from reference: Civil Engineering Reference Manual, 9th Ed, Professional Publications, Inc., 2003; and "Flow of Fluids", Crane Technical Paper No. 410, 1988.

Pipe Section 1 - 3"

Item Qty. L (ft) Qty * LLinear Pipe (L1) 1 50 50Standard Tee (thru flow) 2 12 24Standard Tee (branch flow) 2 17 3490˚ Elbows 8 4 32Union 4 0.5 2Check Valve - Swing 1 27 27Ball valve (full open) 4 4.3 17

Equivalent Length: 186

Step 4. Determine pipe friction for each pipe section.

total pipe friction = total equivalent length x friction factor

Total Pipe Friction - Pipe Section 1total equivalent length = 186 feet

friction factor = 1.1 feet water / 100 feet of pipe

Total Pipe Friction = 2.1 feet

Step 5. Determine total pipe friction (all sections)

Total Pipe Friction - Pipe Section 1 = 2.1

Equivalent Length

Equivalent Length per Fitting (ft)


Page 3 of 3




Calculate Total Dynamic Head:

Head Loss Due to Change in Elevation 15 ft

Headless due to pipe friction 2.1 ft

Headless Across Misc. Process Components Heat Exchanger 25 ft

Required Discharge Pressure (0 psi) 0 ft

Total Dynamic Head Required - Calculated 42 ft

Design Safety Factor 25%

Total Dynamic Head Required - Design 53 feet

Pump Design Requirements:Flow 60 gpm

Total Dynamic Head 53 feet


Model: 3196 Size: 2X3-8 Group: MTi 60Hz RPM: 1750 Stages: 1

Job/Inq.No. : RAYTHEONPurchaser : ARCADISEnd User : ARCADIS Issued by : Rev. : 0Item/Equip.No. : P-100AB Quotation No. : RAPA PRETREATMENT Date : 02/03/2010Service :Order No. :

Operating Conditions Pump PerformanceLiquid: Water Published Efficiency: 46.0 % Suction Specific Speed: 8,693 gpm(US) ftTemp.: 180.0 deg F Rated Pump Efficiency: 46.0 % Min. Hydraulic Flow: 7.7 gpmS.G./Visc.: 1.000/1.000 cp Rated Total Power: 1.8 hp Min. Thermal Flow: N/AFlow: 60.0 gpm Non-Overloading Power: 2.6 hpTDH: 53.0 ft Imp. Dia. First 1 Stg(s): 7.1250 inNPSHa: NPSHr: 2.0 ftSolid size: Shut off Head: 56.7 ft% Susp. Solids(by wtg):

Vapor Press:

Max. Solids Size: 0.5000 inNotes: 1. The Mechanical seal increased drag effect on power and efficiency is not included, unless the correction is shown in the

appropriate field above. 2. Magnetic drive eddy current on power and efficiency is not included. 3. Elevated temperatureeffects on performance are not included. 4. Non Overloading power does not reflect v-belt/gear losses.

Page 1 of 2


I. Conditions:

Process Fluid: 60GPM of effluent from heating system to be cooled from 180º to 120ºF.Cooling Medium: Water at 40ºF. Assume a 45º maximum temperature rise.Cooler Design: 4-Pass design is selected to conserve water and energy usage.

II. Rate Flow Determination

Qp = M x C x Δt

Temperature of the inlet process water (T1) 180.0 ºF

Temperature of the outlet process water (T2) 120.0 ºF

Flow rate of process water 60.0 gpmMass flow rate of water in the heat exchanger (M) 30024 lb/hrSpecific heat of water ( C ) 1.0 Btu/lbºFTemperature difference of the process fluid ( Δ t) 60.0 ºFHeat Transfer (Qp) 1,801,440 Btu/hr

III. Determining cooling water flow rate

Temperature of the inlet cooling water (t1) 40.0 ºF

Temperature of the inlet outlet cooling water (t2) 85.0 ºF

Temperature difference of the cooling fluid (Δt) 45.00 ºFSpecific heat of water ( C ) 1.0 Btu/lbºFHeat Transfer (Qp) 1801440 Btu/hrCooling water mass flow rate (M) 40032 lb/hrCooling water flow rate (Qc) 80 gpm

IV. Determine Exchanger Surface area

Area = Qp/(U x (Cf x LMTD))

Where,

U = Overall Heat transmission Coefficient 275.0 (Btu/ft2 hr ºF)LMTD = Log Mean Temperature DifferenceCf = LMTD Correction Factor (4-Pass Hx) 0.67

Typical Overall heat Transmission Coefficient

Hot Fluid Cooling Fluid U

(Btu/ft2 hr ºF)Water Water 275-325Steam Water 300-500Steam Air 30-40

Heat Exchanger Design CalculationsModified ISR System



Calculation to select the right type of Heat exchanger.

G:\ENV\TF\901-1000\TF922\Reports\2010\RAPA 2010\Final FDEP RAPA\Appendix J\Tab #3\(5) Tab #3_HX Calc.xls ARCADIS

Page 2 of 2

Heat Exchanger Design CalculationsModified ISR System



LMTD = Log Mean Temperature Difference = (T1 -t2) - (T2 - t1)/ ln [(T1 -t2) / (T2 - t1)]

(T1 -t2) 95.0

(T2 - t1) 80.0

LMTD = Log Mean Temperature Difference = 87.3 ºF

Cf =

Required Surface area of the heat exchanger = 112 ft2

Required Surface area of the heat exchanger = 112 ft2

Based on the required surface area of the heat exchanger Model 08120 per foot from BASCO TYPE 500 Heat exchangers is selected.

Surface area of the selected heat exchanger 124.0 ft2

V. Check tube side velocity

Velocity should fall between 2 and 6 feet per second and should not exceed 8 feet per second.

Velocity factor for standard Tubing1/4" tubing = 9.663/8" tubing = 4.025/8" tubing = 1.47

Velocity factor of the selected model (Vf) with 3/8" tubing 1.47Flow rate of the cooling liquid 60.0 gpmNo of passes 4.0 noNo of tubes in the selected model 76 no

Velocity in the tube 4.6 ft/sec ok

G:\ENV\TF\901-1000\TF922\Reports\2010\RAPA 2010\Final FDEP RAPA\Appendix J\Tab #3\(5) Tab #3_HX Calc.xls ARCADIS

Basco/Whitlock Shell and Tube Heat Exchanger

1 JOB NO.

2 CUSTOMER ARCADIS REFERENCE NO.

3 ADDRESS TAMPA, FL PROPOSAL NO.

4 PLANT LOCATION AOP PRE-TREATMENT SYSTEM DATE 2/ 2/2010

5 SERVICE OF UNIT ITEM NO.

6 SIZE 08114 TYPE 500 (HORIZ.) (VERT.) CONNECTED IN

7 SQ.FT. SURFACE (GROSS) (EFF.) 118.1 SHELLS/UNIT ONE SQ.FT.SURF/SHELL (GROSS)

(EFF.) 118.1

8 PERFORMANCE OF ONE UNIT 9 SHELL SIDE TUBE SIDE

10 FLUID CIRCULATED WATER WATER

11 TOTAL FLUID ENTERING LB/HR 78.7 GPM 60.0 GPM

12 VAPOR LB/HR

13 LIQUID LB/HR 39391.9 29498.1

14 STEAM LB/HR

15 NON-CONDENSIBLES LB/HR

16 FLUID VAPORIZED OR CONDENSED LB/HR

17 STEAM CONDENSED LB/HR

18 SPECIFIC GRAVITY 1.00 0.98

19 VISCOSITY @ TEMP cP @ ºF 1.08 @ 62 0.43 @ 150

20 MOLECULAR WEIGHT

21 SPECIFIC HEAT BTU/LB-ºF 0.999 1.000

22 THERMAL CONDUCTIVITY BTU/HR-FT-ºF 0.352 0.376

23 LATENT HEAT – VAPORS BTU/LB

24 TEMPERATURE IN ºF 40.0 180.0

25 TEMPERATURE OUT ºF 85.0 120.0

26 OPERATING PRESSURE PSIA

27 NO. PASSES PER SHELL ONE FOUR

28 VELOCITY FT/SEC 5.82 4.65

29 PRESSURE DROP PSI 13.26 4.13

30 FOULING RESISTANCE (Min) ºF-FT²-HR/BTU 0.0010 0.0020

31 HEAT EXCHANGED 1769989. BTU/HR MTD CORRECTED 81.85 ºF

32 TRANSFER RATE – SERVICE 183.04 CLEAN BTU/HR-FT²-ºF

33 CONSTRUCTION 34 DESIGN PRESSURE PSIG 300 150

35 TEST PRESSURE PSIG 100 100

36 DESIGN TEMPERATURE (Max/Min) ºF 300 / +20 300 / +20

37 TUBES Stainless Steel NO. 76 OD 0.625" BWG 18 LENGTH 114 PITCH 0.75" Tri

38 SHELL Carbon Steel ID 8.071 OD 8.625" SHELL COVER (INTEG)(REMOV)

39 BONNET/CHANNEL Cast 304 Stainless CHANNEL COVER

40 TUBESHEET-STATIONARY Stainless Steel TUBESHEET-FLOATING

41 BAFFLES - CROSS Carbon Steel TYPE Seg. FLOATING HEAD COVER

42 BAFFLES - LONG TYPE IMPINGEMENT PROTECTION

43 TUBE SUPPORTS

44 TUBE TO TUBESHEET JOINT Mechanically Rolled

45 GASKETS Compressed Fiber PACKING

46 CONNECTIONS-SHELL SIDE IN 3 OUT 3 RATING NPT

47 BONNET/CHANNEL SIDE IN 2 OUT 2 RATING NPT

48 CORROSION ALLOWANCE – SHELL SIDE TUBE SIDE

49 CODE REQUIREMENTS Commercial Standard TEMA CLASS

50 OTHER

51 REMARKS

52

53

54

• API Basco • 2777 Walden Avenue, Buffalo, NY 14225 • (716) 684-6700 Fax: (716) 684-2129 (mai22104.doc)

• www.apiheattransfer.com

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4�� 1�� 1�� ,�� 4() �� 5�� )�� 5�� )��

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.��6�� 1�� )( �� "%�� !%�& ��$ �� "%�� 2%#�& ��$�

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8�� 1�� *�� +�� '�� 9��5�� :�� (+�)� /�� '�� 9��5�� *��

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��

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�� ISO-9001 Certified

Air Cooled Aluminum Heat Exchangers

91 North Street • P.O. Box 68

Arcade, New York 14009-0068

(716) 496-5755 • Fax: (716) 496-5776

�� ISO-9001 Certified

Basco®/Whitlock® Shell & Tube Heat Exchangers

2777 Walden Avenue

Buffalo, New York 14225

(716) 684-6700 • Fax: (716) 684-2129

�� Acme® Refrigeration Equipment

2300 West Marshall Drive

Grand Prairie, Texas 75051

(972) 647-2626 • Fax: (972) 641-1518

�� Plate Heat Exchangers and

Thermal Process Systems

2777 Walden Avenue

Buffalo, New York 14225

(716) 684-6700 • Fax: (716) 684-2129

�� .

ISO-9001 Certified

Plate Heat Exchangers and

Thermal Process Systems

P.O. Box 1580 D-75005 Bretten

Pforzheimer Strasse 46

D-75015 Bretten, Germany

49-7252-53101 • Fax: 49-7252-53201

� �� !!��"��#

$�� %%%# �� #��&��& �� ' �� #��&

�� !� "�# �$$

Tab 4

Modified ISR System – AOP Pre-Treatment System Influent Equalization and Iron Oxidation

Page 1 of 1


Considerations:

Useable tank volume = 18,000 gal

Process flow rate = 60 gpm Heat Exchanger Effluent







9,000 gal


9,000 gal

Tank Selection:

Rectangular Tank:

Length = 37.5 feet

Width = 8.5 feet

Height = 11 feet

Volume = 18,000 gal




INFLUENT EQUALIZATION TANK (T-200A) SIZINGModified ISR System



G:\ENV\TF\901-1000\TF922\Reports\2010\RAPA 2010\Final FDEP RAPA\Appendix J\Tab #4\(1) Tab #4_T-200A Sizing.xlsxEQ T-200A ARCADIS

Page 1 of 1

Calc prepared by: M. SeppanenCalc checked by: J. DarbyDate: 01/28/2010

Considerations:


Process flow rate = 60 gpm EQ Tank (T-200A) Overflow







16,200 gal


16,200 gal

Tank Selection:

Rectangular Tank:

Length = 37.5 feet

Width = 8.5 feet

Height = 11 feet

Volume = 18,000 gal




INFLUENT EQUALIZATION TANKS (T-200B/C) SIZINGModified ISR System



G:\ENV\TF\901-1000\TF922\Reports\2010\RAPA 2010\Final FDEP RAPA\Appendix J\Tab #4\(2) Tab #4_T-200B&C Sizing.xlsxEQ T-200B&C ARCADIS

To the best of our knowledge the technical data contained herein are true and accurate at the date of issuance and are subject to change without prior notice. No guarantee of accuracy is given or implied because variations can and do exist. NO WARRANTY OR GUARANTEE OF ANY KIND IS MADE BY BAKERCORP, EITHER EXPRESSED OR IMPLIED.

3020 OLD RANCH PARKWAY • SUITE 220 • SEAL BEACH, CA • 562-430-6262

Technical Information Manual

2.2.15

PRODUCT DATA SHEET February, 2008

EZ CLEAN FIXED AXLE SAFETY VAPOR TANK

GENERAL INFORMATION Vapor tight steel tank with two sealed top access hatches and pressure/vacuum relief valve. Smooth interior walls for easy cleaning. WEIGHTS AND MEASURES

» Capacity: ....... 480 BBL (20,160 gal.)

» Height: ....... 11’-2” (grade to roof deck) 14’-8” (grade to top of upright guardrails)

» Width : ....... 8’-6” (between side runners) » Length: ....... 39’-9” (front nose to outside of rear stairway) 37’-6” (tank only)

» Weight:

....... 24,480 lbs.

STRUCTURAL DESIGN

» Floor: ....... ¼”thick ASTM A36 carbon steel (V-bottom)

» Sides/Ends: ....... ¼” thick ASTM A36 carbon steel

» Roof Deck: ....... ¼” thick ASTM A36 carbon steel

» Wall Frame: ....... 3/16”x3”x5” ASTM A36 formed channel

» Roof Frame: ....... 3/16”x3”x5” ASTM A36 formed channel

» Skid Rails: ....... C8x11.5 structural channel

FEATURES

» Valves: ....... 1-Front &1-Rear: 6”- wafer butterfly valve. Cast iron body, Buna-N seat & seals, 316 SS stem, Nylon 11 coated ductile iron disk w/ plug and chain.

» Relief Valve: ....... 16 oz./in2 pressure setting, 0.4 oz./in2 vacuum setting; Buna-N seal

» Roof Deck Connections:

....... Vapor Recovery: 4”-150# flange (blinded) Gauging Port: 4” flange (blinded) with 2” threaded plugged port in blind flange.

» Side Manways: ....... One or two (depending on make of tank) on curb side of tank.

FEATURES – cont.

» Front Piping Connections:

....... Bottom Drain: 6”-150# flanged nozzle and butterfly valve Inlet/Outlet: 2 - 4”-150# raised face flange with blind flange (chained)

» Rear Piping Connections:


» Interior Access: ....... 2-50” long x 32” wide hinged vapor-proof marine-style hatches with neoprene gaskets and removable fall protection grid.

» Hatch and Manway Seals:

....... Neoprene gasket

» Roof Access Stairway:

....... Rear mounted – lower section folds up for transport and down for use. Stairway includes handrails.

» Guardrails: ....... Top deck, fold-down, 1¼” x 1¼” square tubing.

» Internal Ladder: ....... One; mounted below front-end interior access hatch on roof deck.

» Level Indication: ....... Ball style with 2-8” 304 SS floats with pointer-indicator on front endwall. Floor supports hold floats ½” off floor. [One 2” plugged connection for optional electronic gauge on top deck.]

» Axle: ....... 77½ track straight, non steer, 22,500# capacity.

» Suspension: ....... Silent Drive, 3 air-bags with manual release.

SURFACE DETAILS

» Exterior Coating: ....... High Gloss Polyurethane

» Interior Coating: ....... None

TESTS/CERTIFICATIONS

» Tests Performed: .......

Major repairs – hydrotest Scheduled- Level I, II and III inspections, including NESHAP testing

Page 1 of 3






60 2 2.375 0.154 2.067 0.023 5.5860 3 3.500 0.216 3.068 0.051 2.5360 4 4.500 0.237 4.026 0.088 1.47

*Pipe dimensions noted for Schedule 40 galvanized steel piping.Note: Design for velocity between 3 and 5 feet/sec to maintain sufficient scour velocity






Flow (v1) = 60 gpm





Nominal Diam (in)

ID (in)


1 1.049 0.9241.5 1.610 1.4852 2.067 1.9423 3.068 2.9434 4.026 3.9016 6.065 5.94


Modified ISR System - AOP Pre-Treatment SystemAERATION TANK FEED PUMP (P-200A/B) DESIGN CALCULATIONS



sec60

min1*

)*( 2r

Qv


Page 2 of 3









Equivalent lengths from reference: Civil Engineering Reference Manual, 9th Ed, Professional Publications, Inc., 2003;and "Flow of Fluids", Crane Technical Paper No. 410, 1988.

Pipe Section 1 - 3"

Item Qty. L (ft) Qty * LLinear Pipe (L1) 1 60 60Standard Tee (thru flow) 4 12 48Standard Tee (branch flow) 2 17 3490˚ Elbows 8 4 32Union 4 0.5 2Check Valve - Swing 1 27 27Ball valve (full open) 4 4.3 17









Equivalent Length



Page 3 of 3






Head Loss due to pipe friction 2.5 ft

Head Loss Across Misc. Process Components 0 ft











Vapor Press:



Page 1 of 3

RECIRCULATION PUMP (P-200C) DESIGN CALCULATIONS






40 1.5 1.900 0.145 1.610 0.014 6.1340 2 2.375 0.154 2.067 0.023 3.7240 3 3.500 0.216 3.068 0.051 1.69

*Pipe dimensions noted for Schedule 40 galvanized steel pipingNote: Design for velocity between 3 and 5 feet/sec to maintain sufficient scour velocity






Flow (v1) = 40 gpm





Nominal Diam (in)

ID (in)


1 1.049 0.9241.5 1.610 1.4852 2.067 1.9423 3.068 2.9434 4.026 3.9016 6.065 5.94

NOTE: a 0.0625 inch (1/16 inch) deposition on interior pipe wall is included indiameter for calculation - 1.003 - (2 x 0.0625) = 0.878 inch diameter

Modified ISR System - AOP Pre-Treatment SystemTotal Dynamic Head Calculation


sec60

min1*

)*( 2r

Qv

G:\ENV\TF\901-1000\TF922\Reports\2010\RAPA 2010\Final FDEP RAPA\Appendix J\Tab #4\(6) Tab #4_P-200C TDH.xlsx ARCADIS

Page 2 of 3

RECIRCULATION PUMP (P-200C) DESIGN CALCULATIONSModified ISR System - AOP Pre-Treatment System








Equivalent lengths from reference: Civil Engineering Reference Manual, 9th Ed, Professional Publications, Inc., 2003;and "Flow of Fluids", Crane Technical Paper No. 410, 1988

Pipe Section 1 - 1-1/2"

Item Qty. L (ft) Qty * LLinear Pipe (L1) 1 100 100Standard Tee (thru flow) 4 7.7 31Standard Tee (branch flow) 1 12 1290˚ Elbows 6 3.6 22Union 2 0.45 1Check Valve 1 19 19Ball valve (full open) 2 2.9 6









Equivalent Length



Page 3 of 3

RECIRCULATION PUMP (P-200C) DESIGN CALCULATIONSModified ISR System - AOP Pre-Treatment System





Head loss due to pipe friction 7.8 ft

Head loss Across Misc. Process Components 0 ft









Job/Inq.No. : RAYTHEONPurchaser : ARCADISEnd User : ARCADIS Issued by : Rev. : 0Item/Equip.No. : P-200C Quotation No. : RAPA PRETREATMENT Date : 02/03/2010Service :Order No. :


Vapor Press:



Page 1 of 1


Considerations:






Process flow rate = 60 gpm EQ Tank (T-300A) Effluent







4,628 gal


4,628 gal

Tank Selection:

Cylindrical Tank:

Diameter = 10.0 feet






AERATION TANK (T-300) SIZINGModified ISR System





2.4.4

PRODUCT DATA SHEET January, 2007

6500 GALLON POLY TANK (Original Style and Total Drain)

GENERAL INFORMATION This type of tank is not to be used for food applications. Potable water applications are generally not acceptable and must be reviewed by the Corporate office first for approval. WEIGHTS AND MEASURES

» Capacity: _ 6500 gallons (nominal)

» Height‡: _ 10’-6” (to top tangent line) 11’-11” (to top of dome) 12’-4” (to highest point on top lid)

» Diameter: :

_ 10’-0” (nominal)


3020 Old Ranch Parkway • Suite 220 • Seal Beach, CA • 562-430-6262

» Weight*:

_ Tank: 1700 lbs. – 1975 lbs. Pad: 400 lbs. - 450 lbs.

*Varies with origin of manufacture ‡ Does not include height of pad. Add four inches for pad thickness to determine heights from grade when pad is used. DESIGN PARAMETERS

» Tank Material:

_ High Density Polyethylene

» Design Pressure:

_ 0 psi – vented to atmosphere

» Design Vacuum:


» Spec. Gravity Limit:

_ Original Style – 1.65 Total Drain – 1.9

» Temp. Limit: _ 150° F » Certification: _ ASTM D1998 (not UL listed)

RESTRICTIONS

» Sulfuric Acid Storage:

_ • 80% concentration maximum • Use only tanks with equipment

numbers ≥ 7376 • Previously repaired tank cannot be

used (equipment number should have “W” at end)

• 100° F maximum temperature • Top fill only • Top manway must be open during

pneumatic filling of tank • Use flexible plumbing fixtures resistant

to sulfuric acid FEATURES

» Top Vent: _ 2” PVC U-vent (two threaded street elbows)

» Manway: _ Top mounted with 24” opening (34 inch diameter screw-on cover)

» Valves: _ 3” butterfly valve with PVC body and disc, Viton O-Ring seal and 316 SS stem.

» Ladder: _ Top mounted bracket for ladder hook-up. Ladder is not permanently mounted to tank.

» Piping Connections:

_ Inlet – 3” with butterfly valve Outlet – 3” with butterfly valve Top – 4” PVC adapter and PVC cap

MISCELLANEOUS

» Options: _ Secondary containment berm

Page 1 of 1


Determine amount of oxygen required to oxidize dissolved iron:

Input Water flow rate 60 gpmInput Ferrous iron concentration 20 mg/L Fe+3

Calc Amount of ferrous iron (1) 14.41 lbs/day Fe+3

Known mg O2 required to oxidize mg Fe+2 (2) 0.143 mg O2/mg Fe+3

Calc Amount of oxygen required to oxidize ferrous iron 2.06 lbs/day O2

Determine airflow rate required to oxidize ferrous iron:

Calc from above Amount of oxygen required to oxidize ferrous iron 2.06 lbs/day O2

Input Transfer efficiency (3) 2%Calc Pounds of oxygen injected 103.04 lbs/day O2

Known Density of oxygen 0.08 lbs/ft3 O2

Calc Free oxygen flow rate 1224.02 ft3/day O2

Calc Free oxygen flow rate 0.850 ft3/min O2

Calc Free air flow rate 4.05 ft3/min airCalc Free air flow rate 114.55 liters/min

Input Safety factor (4) 2

Calc Injected free air flow rate 8.095 ft3/min airCalc Injected free air flow rate 229.099 liters/min

NOTES:

(1) lbs/day = 8.34 x mg/L x MGD(2) 4 Fe+2 + 2H+ + O2 ---> 4Fe+3 + 2OH-, stochiometric = 1 O2 : 4 Fe+2, mass basis 1 O2 : 7 Fe+2

(Source: Montgomery, Water Treatment Principles and Design, page 340, 1985) (3) Professional judgment - contact tubing system similar to efficiency of 10-foot deep tank .(4) Selected to match design conditions of a similar system.

IRON OXIDATION DESIGN CALCULATIONModified ISR System - AOP Pre-Treatment System

Total Air Requirement Calculation


G:\ENV\TF\901-1000\TF922\Reports\2010\RAPA 2010\Final FDEP RAPA\Appendix J\Tab #4\(10) Tab #4_Air Rqmts - Fe Ox.xls ARCADIS

Page 1 of 2


I. Define System Parameters

a. Conveyance PipingInternal Diameter of Conveyance Piping 2.067 in (2-in. Nominal Dia., galv. steel)

0.17 ftMin. Flow Rate per Conveyance Line 36.0 ft3 / minFlow velocity 25.7 ft / sec

II. Define Flow Characteristics

a. Conveyance Piping

where:NRe = Reynolds Number

Internal Diameter of Conveyance Piping, D 2.067 in0.17 ft

AERATION BLOWER (B-100A/B) DESIGN CALCULATIONSModified ISR System



Calculate friction loss due to air flow through piping.

eeR

DN

mean velocity of flow, v 25.7 ft / secweight density of fluid (assume air), ρ 0.0752 lb / ft3

1.89E-05 kg / (m*sec)dynamic viscosity, e 1.27E-05 lb / (sec*ft)

Reynolds Number, N Re 26,260 (dimensionless)

(NRe < 2000 = Laminar, NRe > 4000 = Turbulent)

Flow is Turbulent

III. Determine Friction Factors

In the turbulent regime, the friction factor can be approximated by;Note: This equation applies for smooth piping onlyOther materials require friction factor obtained from Friction Factor chart


Friction Factor, f 6.22E-03 (dimensionless)

eeR

DN

32.0Re

125.00014.0

Nf

G:\ENV\TF\901-1000\TF922\Reports\2010\RAPA 2010\Final FDEP RAPA\Appendix J\Tab #4\(11) Tab #4_B-100 Calc.xls ARCADIS

Page 2 of 2

AERATION BLOWER (B-100A/B) DESIGN CALCULATIONSModified ISR System



IV. Determine Other Resistance Losses


Ball Valve 2 0.06 1 0.06Diaphragm Valve 2 6.5 1 6.590 Degree Elbow 2 0.57 6 3.42

Total K 9.98

V. Determine Pressure Loss/Drop


i. Conveyance Pipe Length, L 140 ftii. No vertical height change, therefore, Za-Zb = 0 20 ft [assumed]

iii. Gravity, g 32.2 ft / sec2

iv. gc 32.2 lb-ft / sec2-lbf

Pressure Drop, ∆Pa 25.61 lb / ft2

0.18 psi

4.9 in. water

csba

c gK

D

LfZZ

g

gP

2)4()(

2

Re

VI. Other Items

Coarse Bubble Diffuser 2.75 in. water [2.75 in wc / diffuser]

Water Depth above Diffusers 108 in. water

VII. Total Pressure Blower will be required to Generate

ΔPa 4.9 in. waterOther Items 110.8 in. waterSafety Factor 20%

Total Pressure Required 138.81 in. water


Becker Pumps Corp. • 100 East Ascot Lane • Cuyahoga Falls, Ohio 44223-3768 Ph. (330) 928-9966 • (888) 633-1083 • FAX: (330) 928-7065 • [email protected] • www.beckerpumps.com

KDT Series100% OIL-LESS COMPRESSORS

ISO 9001 Certified Compliant

The Becker KDT series is a line of 100% Oil-less, rotary vane, low pressure compressors. They are designed to operate on a continuous basis throughout a pressure range from atmospheric pressure to 22 PSIG.

Each KDT unit is a direct drive com-pressor and is supplied with a TEFC flange mounted electric motor. Each unit is equipped with inlet and discharge filters, a pressure regulating valve, and vibration isolators as

standard equipment, all of which are an integral part of the compressor.

The Becker KDT compressor is ideal for applications where air is the gas and where operation is in the low pressure range where high pressure compressors are less efficient. Applications for the KDT compressor include graphic arts,

soil remediation, pneumatic convey-ing, robotics and material handling,

packaging, and paper converting.

* @ 29.92" Hg Bar. Pr.; 68oF; 36% R.H.; 0.075#/ft3

1

4

6

8

12

50

20

30

40

60

70

120

90

80

KDT 3.140

0 2 4 6 8 10 12 14 16 2018 2210

9

7

5

3

2

SCFM*

SCFM*

SCFM*

SCFM*

BHP

BHP

BHP

BHP

KDT 3.100

KDT 3.80

KDT 3.60

FLO

W (

SCFM

*)

PO

WER

REQ

UIR

EMEN

TS (

HP

)

PRESSURE (PSIG)

100

110

10

11

JPERELLA

Line

JPERELLA

Line

JPERELLA

Line

JPERELLA

Text Box

36 CFM

JPERELLA

Text Box

5 psi

JPERELLA

Text Box

2.25 HP (Use 3HP Motor)

JPERELLA

Text Box

B-100 AERATION BLOWER

Becker Pumps Corp. • 100 East Ascot Lane • Cuyahoga Falls, Ohio 44223-3768 Ph. (330) 928-9966 • (888) 633-1083 • FAX: (330) 928-7065 • [email protected] • www.beckerpumps.com

3LIT0006 • 2/00

TECHNICAL DATA

KD

T 3.6

0K

DT

3.8

0K

DT

3.1

00

All data based on 60 Hz operation

KD

T 3.1

40

Top View

Side View

End View (Opposite Motor End)

Flow (SCFM @ 0 PSIG)

Horsepower

Speed (RPM)

Maximum Pressure (PSIG)

Weight (lbs.)—w/o motor

Weight (lbs.)—w/ motor**

Noise Level (Max. dBA)

Outlet size (BSP, inches)

Dimensional Dataa

b

b1

e

e1

g

g1

g2

h

h1

h3

h4

i

k2

kL

o

48

71/2*

1740

22

108

265*

76

1

12.83

7.5

3.75

5.43

2.56

13.9

7.68

5.55

6.38

11.38

12.28

12.9

3.78

17.64

30

1.81

95

12*

1740

22

172

368*

84

11/2

15.67

9.65

4.82

7.5

3.75

18.5

8.78

9.06

6.38

11.7

13.0

13.25

5.5

22.17

36.6

2.36

69

10*

1740

22

156

323*

78

11/2

15.67

9.65

4.82

7.5

3.75

18.5

8.78

9.06

6.38

11.7

13.0

13.25

5.5

22.17

34.15

2.36

Manufacturer reserves right to alter data without notice.* Operation at lower pressure may use smaller motor.** May vary with motor type and manufacturer

39

5*

1740

22

104

191*

74

1

12.83

7.5

3.75

5.43

2.56

13.9

7.68

5.55

6.38

11.38

12.28

12.9

3.78

17.64

28.2

1.81

1 - Inlet Port2 - Discharge Port3 - Pressure Relief Valve4 - Vibration Isolators

g

g1 g2

h3 h1

h4

b1

b4

a i

K2

3

1

12mm dia.

h

oe

2

8mm thds.

(Inches)

e1 e1

KL**

JPERELLA

Line

JPERELLA

Line

JPERELLA

Line

JPERELLA

Line

JPERELLA

Line

JPERELLA

Line

JPERELLA

Text Box

Model KDT 3.60 w/ 3HP Motor

TAN

KS

&TA

NK

AC

C.

531For A Quote Call 1-800-877-4472

50th Anniversary Product Catalog

DOUBLE WALL CONTAINMENT - MINI-BULK TANKS

Diameter(in.)

Optional Elevation StandsPart

Number

Double Wall Containment Mini-BulkSmaller dual-containment tanks provide added safety and environment protection in moreconfined or remote storage locations. The advanced double wall tank design is enclosed toprohibit foreign matter from entering the secondary containment tank, and a unique octagonalshape provides optimal spacing and sealing surface for the industry’s most reliable transition fitting.

Features:• Available in HDLPE and XLPE resin packages.• Primary tank is available in both closed and open-top designs.• Secondary tank provides 115-120% of inner tank’s capacity,complies with CRF-264.193.

• Transition fitting allows side safe installation and long-term sealingpower through both walls of the tank.

• Large flat surface area provides ample space for a variety offitting sizes and styles.

• Rib reinforced flat-top design provides ample surface space for chemical feedpump mounting.

• Narrow diameter provides location versatility to fit through most any doorway.• Forklift and pallet jack accessible design on 275, 360 and 500 gallon models.• Optional top draw tube assembly.• Optional 2” vent provides vacuum relief for interior tank.• Optional all-poly elevation stands create more room for plumbing and othersystem requirements without using additional floor space.

Snyder

BottomClearance

(in.)137023 22 12 376.00

137001023 22 18 434.00169023 30 12 568.00

169001023 30 18 651.00173023 36 12 682.00

173001023 36 18 785.00175023 42 12 796.00

175001023 42 18 914.00176023 48 12 948.00

176001023 48 18 1,089.00

PartNumber

TankSize(Gals.)

Dimensions (In.)Diameter Height

List PriceEa. ($)

Double Wall Containment Tanks Mini-BulkPart

Number

XLPE HDPEPrimaryTank Specific

Gravity

ManwayFill(in.)

35 19 36 1.9 6 100020042 537.00 100020045 423.0060 253⁄4 403⁄4 1.9 14 100030042 636.00 100030045 500.00120 33 49 1.9 14 598000042 1,076.00 598000045 888.00150 333⁄4 60 1.9 14 100040042 1,220.00 100040045 1,024.00275 47 631⁄4 1.9 14 100050042 1,800.00 100050045 1,502.00360 53 601⁄4 1.9 14 100060042 2,130.00 100060045 1,864.00500 48 65 1.9 14 100080042 2,884.00 100080045 2,239.00

Shownwith Tank

Shown with OptionalEquipment

List PriceEa. ($)

List PriceEa. ($)• All plastic corrosion resistant.

• Plastic stands elevate tanks off the floor12 to 18 inches forfitting and piping clearance.

• Heavy-duty plastic stand is corrosionproof and available for both flat and conebottom tanks.

Tank Stand Features:

Industri

al

Industri

al

ASTM

ASTM

Grade

Grade

Tanks.qxd:Tanks 1/26/09 3:00 PM Page 531

Koflo Corporation309 CARY POINT DR.CARY, IL 60013

CUSTOMER:

DATE:

SCALE:

MODEL NO:

APPROVED BY DRAWN BY

REVISED

REVISED

REVISED

DRAWING NUMBER:

NONE

7/10/06

NJF

KD-985TYPICAL LOW PRESSURE LOSS DESIGN FLANGE MOUNTED MIXER WITH FNPT INJECTION PORT

5/30/08

"B" HOLES "C" DIAMETER ON A "D" D.B.C.

150 LB. RAISED FACE FLANGED ENDS

KOFLO STATIC MIXER CONSTRUCTED OFSCHEDULE 40 OR 10 PIPE WITH *____ FIXED LOW PRESSURE LOSS DESIGN MIXING ELEMENTS

"A"(Inches)

NOTE: SCH 40 IS USED FOR CARBON STEEL MIXERS SCH 10 IS USED FOR SS/ALLOY MIXERS 3" AND LARGER

"E"

FNPT INJECTION PORT "F" SIZE OR AS SPECIFIED

DIRECTIONOF FLOW

Tab 5

Modified ISR System – AOP Pre-Treatment System Filtration and Solids Settling

Page 1 of 1


Considerations:






Process flow rate = 60 gpm Aeration Tank Effluent




Additional requirements = 2,600 gal Backwash Decant



1,800 gal


4,400 gal

Tank Selection:

Cylindrical Tank:







FILTER FEED TANK (T-400) SIZINGModified ISR System





2.4.4






» Diameter: :

_ 10’-0” (nominal)



» Weight*:



» Tank Material:


» Design Pressure:


» Design Vacuum:





RESTRICTIONS














MISCELLANEOUS


Page 1 of 3

FILTER FEED PUMPS (P-300A/B) DESIGN CALCULATIONS






60 2 2.375 0.154 2.067 0.023 5.5860 3 3.500 0.216 3.068 0.051 2.5360 4 4.500 0.237 4.026 0.088 1.47






Pipe Section 1-3" Nominal pipe diameter 1 = 3 inch

Flow (v1) = 60 gpm





Nominal Diam (in)

ID (in)


1 1.049 0.9241.5 1.610 1.4852 2.067 1.9423 3.068 2.9434 4.026 3.9016 6.065 5.94




sec60

min1*

)*( 2r

Qv


Page 2 of 3

FILTER FEED PUMPS (P-300A/B) DESIGN CALCULATIONSModified ISR System - AOP Pre-Treatment System




Pipe Section 1 friction factor 1.1 ft water / 100 feet of pipe





Pipe Section 1 - 3"

Item Qty. L (ft) Qty * LLinear Pipe (L1) 1 100 100Standard Tee (thru flow) 4 12 48Standard Tee (branch flow) 2 17 3490˚ Elbows 16 4 64Union 8 0.5 4Check Valve 2 27 54Ball valve (full open) 8 4.3 34







Equivalent Length



Page 3 of 3

FILTER FEED PUMPS (P-300A/B) DESIGN CALCULATIONSModified ISR System - AOP Pre-Treatment System







Head loss due to pipe friction 4 ft

Head loss Across Misc. Process Components Multi-Media Filter 35 ft

Air Stripper 24 ftFlow meter 12 ft








Model: 3196 Size: 1.5X3-6 Group: STi 60Hz RPM: 3520 Stages: 1



Vapor Press:



Page 1 of 3

BACKWASH PUMP (P-300C) DESIGN CALCULATIONS






110 3 3.500 0.216 3.068 0.051 4.64110 4 4.500 0.237 4.026 0.088 2.70110 6.00 6.625 0.280 6.065 0.201 1.19







Flow (v1) = 110 gpm





Nominal Diam (in)

ID (in)


1 1.049 0.9241.5 1.610 1.4852 2.067 1.9423 3.068 2.9434 4.026 3.9016 6.065 5.94




sec60

min1*

)*( 2r

Qv


Page 2 of 3

BACKWASH PUMP (P-300C) DESIGN CALCULATIONSModified ISR System - AOP Pre-Treatment System









Pipe Section 1 - 3"

Item Qty. L (ft) Qty * LLinear Pipe (L1) 1 100 100Standard Tee (thru flow) 6 12 72Standard Tee (branch flow) 2 17 3490˚ Elbows 4 4 16Check Valve 1 27 27Ball valve (full open) 6 4.3 26









Equivalent Length



Page 3 of 3

BACKWASH PUMP (P-300C) DESIGN CALCULATIONSModified ISR System - AOP Pre-Treatment System





Head loss due to pipe friction 9.7 ft

Head loss Across Misc. Process Components Static Mixer 10 ft

Multi-Media Filter 35 ftFlow meter 12 ft








Model: 3196 Size: 1.5X3-6 Group: STi 60Hz RPM: 3520 Stages: 1

Job/Inq.No. : RAYTHEONPurchaser : ARCADISEnd User : ARCADIS Issued by : Rev. : 0Item/Equip.No. : P-300C Quotation No. : RAPA PRETREATMENT Date : 02/03/2010Service :Order No. :


Vapor Press:



Multi-Media Filter Design CalculationsModified ISR System



Page 1 of 1

Calc prepared by: M. Seppanen

Calc checked by: J. Perella

Date: 1/28/2010

Assume:

Filter sizing is based on hydraulic loading

8 - 15 gpm/ft2

Process Flow Rate = 60 gpm

Design Loading Rate 5.0 gpm/ft2

Filtration Area Required = 12.0 ft2

Number of online vessels = 3

Filtration area per vessel = 4.0 ft2

Calculated diameter of vessel = 2.3 ft

Selected vessel diameter = 3.0 ft

Filtration Area per vessel = 7.1 ft2

Actual Loading Rate = 2.8 gpm/ft2

Water Loading Rate = 15 gpm/ft2

Time per vessel = 8 min

Backwash Flow Rates:

Water = 106 gpm

Backwash Volumes:

Volume of Backwash Required per Vessel= 848 gpm

Total Volume of Backwash Required = 2,544 gpm

Calculate size of Multi-Media Filter units:

Recommended hydraulic loading for media

Calculate diameter of Multi-Media Filter:

Selected design requirement specifications:

Backwash Requirements

G:\ENV\TF\901-1000\TF922\Reports\2010\RAPA 2010\Final FDEP RAPA\Appendix J\Tab #5\(7) Tab #5_Pre AOP MMF Calcs.xlsx ARCADIS

Page 1 of 1


Considerations:


21-Days Solids Storage = 2,625 gal 125 gallons per day


Input Volume = 2545 gal Daily Backwash Volume

Additional Requirements = 0 gal


Total input volume = Daily Backwash Volume + Additional Requirements

2,545 gal

Minimum required volume = Total input volume + Solids storage + Freeboard

5,789 gal

Tank Selection:

Cylindrical Tank:



Volume = 6,500 gal




BACKWASH TANK (T-800) SIZINGModified ISR System





2.4.4






» Diameter: :

_ 10’-0” (nominal)



» Weight*:



» Tank Material:


» Design Pressure:


» Design Vacuum:





RESTRICTIONS














MISCELLANEOUS


Page 1 of 3

DECANT PUMP (P-600) DESIGN CALCULATIONS






30 1.5 1.900 0.145 1.610 0.014 4.6030 2 2.375 0.154 2.067 0.023 2.7930 3 3.500 0.216 3.068 0.051 1.27






Pipe Section 1 Nominal pipe diameter 1 = 1.5 inch

Flow (v1) = 30 gpm





Nominal Diam (in)

ID (in)


1 1.049 0.9241.5 1.610 1.4852 2.067 1.9423 3.068 2.9434 4.026 3.9016 6.065 5.94




sec60

min1*

)*( 2r

Qv

G:\ENV\TF\901-1000\TF922\Reports\2010\RAPA 2010\Final FDEP RAPA\Appendix J\Tab #5\(12) Tab #5_P-600 TDH.xlsx ARCADIS

Page 2 of 3

DECANT PUMP (P-600) DESIGN CALCULATIONSModified ISR System - AOP Pre-Treatment System









Pipe Section 1 - 1-1/2"

Item Qty. L (ft) Qty * LLinear Pipe (L1) 1 150 150Standard Tee (thru flow) 2 5.6 11Standard Tee (branch flow) 0 9.9 090˚ Elbows 6 3.4 20Union 2 0.39 1Check Valve 1 15 15Ball valve (full open) 2 2.3 5









Equivalent Length



Page 3 of 3

DECANT PUMP (P-600) DESIGN CALCULATIONSModified ISR System - AOP Pre-Treatment System






Head loss Across Misc. Process Components ft








ITTGoulds Pumps1SC Submersible

Water Pump

GouldsPumpsisabrandofITTCorporation.

www.goulds.com

Engineered for life

Residential Water Systems

Features

■ Casing: AISI 304 SS. Corrosion resistant, non-toxic, non-leaching.

■ Impeller: FDA compliant, glass filled Noryl®. Corrosion and abrasion resistant.

■ Mechanical Seal: Silicon/carbide sealing faces; all metal components of AISI type 300 stainless steel running in protected oil chamber.

■ Elastomers: BUNA-N.

■ Motor Shell and Lifting Handle: Constructed of AISI type 304 series stainless steel.

■ Shaft: AISI type 304 stainless steel high strength keyed pump shaft with impeller locking cap screw.

■ Discharge: 11⁄4" NPT vertical discharge connection.

■ Suction Strainer: Detachable for easy clean out.

�

ITT GOuLDs PuMPsResidential Water Systems

0 �50

CAPACITY

TOTA

L D

YNA

MIC

HEA

D

FEET

U.S. GPM

100

50

150

�010 �00

�0

40

METERS

0 � 4� 6 m3/hr

60

5 15

51

�00

�5

7 8

1SC51E-H

1SC51C-F

1SC51D-G

1SC51C-A

1SC51D-B

1SC51E-C

1 HP3/4 HP1/2 HP

1 HP

3/4 HP

1/2 HP

aPPLICatIONs

Submersible water pumps designed for pumping out of reservoirs and storage tanks:• Homes and farms• Mobile home parks and motels• Schools and hospitals• Municipal applications• Industrial applications• Commercial applications

sPeCIFICatIONs

Pump:

• 11⁄4" NPT discharge and open suction.

• Maximum suspended solids 1⁄8".

• Capacities: to 35 U.S. GPM (7.9 m3/h).

• Total heads: to 240 feet TDH (70 m).

• Temperature: 104ºF (40ºC) continuous 140ºF (60ºC) intermittent.

• Maximum submergence: to 65 feet (20 m).

• Continuous duty rated, non-overloading motor.Motor:

• Single phase: 3450 RPM, 115 and 230 V, 60 Hz.

• Three phase: 3450 RPM, 230 V, 60 Hz.

• Non-overloading.

• Class F insulation.

• Thermal overload protection: built-in with automatic reset on single phase.

• Three phase models require external overloads in panel.

• Power cord: All 30' long.Single phase – 16/3, with 115 V or 230 V plugThree phase – 16/4 STO, bare leads

NOTE: See accessory section for separate control panels.

JPERELLA

Line

JPERELLA

Line

JPERELLA

Text Box

Pretreatment P-600 AOP P-500

�


DIMeNsIONs

MeCHaNICaL Data

NPT 11⁄4

L

5"

“L” Dimensions Discharge Series HP Phase in inches Size

1⁄2 1,3 191⁄8

1SC 3⁄4 1,3 201⁄8 11⁄4

1 1,3 213⁄4

Series Number of HP Volts Phase Maximum RPM Weight Stages Amps (lbs.) 1SC51C0AA 115 1 10.6

1SC51C1AA 1⁄2 230 4.5

1SC51C3AA 3 3 3.0 31 1SC51C0FA 115 1 10.7

1SC51C1FA 1⁄2 230 4.5

1SC51C3FA 3 3.0

1SC51D1BA 1 5.4 3450

1SC51D3BA 4 3⁄4 230 3 3.5 33 1SC51D1GA 1 5.3

1SC51D3GA 3 3.5

1SC51E1CA 1 6.4

1SC51E3CA 5 1 230 3 4.1 38 1SC51E1HA 1 6.8

1SC51E3HA 3 4.3

ITT

GouldsPumpsandtheITTEngineeredBlocksSymbolareregisteredtrademarksandtradenamesofITTCorporation.

NorylisaregisteredtrademarkofGEPlastic.

SPECIFICATIONS ARE SUBJECT TO CHANGE WITHOUT NOTICE.

B1SC August, 2007©2007ITTCorporation

Engineered for life


Component Material Outer Casing and Upper Support Stainless Steel (AISI 304)

Motor Casing Stainless Steel (AISI 304)

Suction Strainer Stainless Steel (AISI 304)

Motor Shaft Stainless Steel (AISI 304)

Impeller Noryl

Diffuser Stainless Steel (AISI 304)

Upper Cover Technopolymer

Mechanical Seal Housing Technopolymer

Lower Bearing Support Aluminum Die Cast

Lower Bearing Urethane Resin

Elastomers Buna-N

Lower Mechanical Seal Silicon Carbide/Silicon Carbide

Upper Lip Seal Nitrile Rubber

Polymer CalculationsModified ISR System


Raytheon Company St. Petersburg, Florida

Page 1 of 1

M. Seppanen

J. Darby

1/28/2010

Flow rate = 106 gpm

Polymer dosage = 15 ppmv Jar Test Results

Specific gravity of polymer = 1.015

Polymer weight = 8.465 lbs/gal

Polymer flow rate = 6.0 mL/min

Backwash flow rate = 106 gpm


Duration of backwash = 8 min

Volume of polymer per vessel = 0.05 L

Number of vessels = 3

Total Volume of polymer = 0.14 L

Backwash Frequency = 7 Backwash cycles/week

Total Volume of polymer per week = 1.01 L/week

0.27 gal/week

Total Volume of polymer per week 0.27 gal/week

Calculate Volume of Polymer Required per Week:

Calculate Polymer Flow Rates for the Multi-Media Filter Backwash Cycle:

Calculate Volume of Polymer Required:

Calc prepared by:

Calc checked by:

Date:

G:\ENV\TF\901-1000\TF922\Reports\2010\RAPA 2010\Final FDEP RAPA\Appendix J\Tab #5\(14) Tab #5_PreAOP Polymer Calc.xlsx ARCADIS

©2006, General Electric Company. All rights reserved. *Trademark of General Electric Company; may be registered in one or more countries.

Fact Sheet

PFW957EN 0606

Europe/Middle East/Africa Heverlee, Belgium +32-16-40-20-00

Asia/Pacific Shanghai, China +86-21-5298-4573

Find a contact near you by visiting gewater.com or e-mailing [email protected].

Americas Watertown, MA +1-617-926-2500

Global Headquarters Trevose, PA +1-215-355-3300

PolyFloc* AS1002 High Molecular Weight Flocculant• Easy-to-feed polymeric flocculant

• Convenient, true liquid

• Reduces floc carryover

• Approved for potable use

Description and Use

PolyFloc AS1002 is a liquid, weakly anionic, high molecular weight, polymeric flocculant, which is designed to function in industrial treatment programs as a coagulant aid, or flocculant, in clarification, thickening, and softening processes. The product is chlorine resistant. NSF certification for potable applications is pending.

PolyFloc AS1002 is true liquid, high molecular weight flocculant. This polymer is ideal for remote plant operations or small volume usage because it does not require extensive feed and makedown equipment.

A fast-settling floc is formed when PolyFloc AS1002 is applied to warm or hot lime/soda softeners, cold lime softeners, and influent clarification systems. Floc carryover is reduced, resulting in a cleaner effluent.

PolyFloc AS1002 is also an excellent sludge dewatering aid producing clean filtrate, high solids capture, and a drier cake. Applications to many types of industrial sludges have been successful, including blast furnace sludge dewatering applications.

Treatment and Feeding Requirements

PolyFloc AS1002 is an easy-to-feed liquid that does not require any special makedown procedures. Poly-Floc AS1002 can be fed neat with any suitable high viscosity gear pump or diluted with water to any con-venient concentration. Diluted product may be fed by a pump, eductor, or by gravity flow to a point where good mixing, but not violent agitation, of the treated water occurs. High speed mixing decreases the activ-

ity of the polymer. Pumps used to transfer the solution to the point of application should be positive dis-placement gear or piston pumps.

To minimize corrosion and contamination by corro-sion products, liquid-side components of tanks, pumps, and piping should be constructed of stainless steel, polyethylene, or polyvinyl chloride. Mild steel is acceptable only in systems where contamination by corrosion products is not a critical problem.

General Properties

Physical properties of PolyFloc AS1002 are shown on the Material Safety Data Sheet, a copy of which is available on request.

Packaging Information

PolyFloc AS1002 is a liquid product, available in a vari-ety of containers. Consult your GE representative for delivery and packaging alternatives.

Storage and Handling

Store PolyFloc AS1002 at moderate temperatures of 40 to 90°F (4 to 32°C), and protect from freezing. The recommended shelf life of the product is six months.

Spilled polymer is very slippery. Small amounts of spilled polymer can be washed down with copious amounts of water. Large spills should be contained and absorbed on inert material, then disposed as solid waste, prior to flushing with water.

Safety Precautions

A Material Safety Data Sheet containing detailed in-formation about this product is available upon re-quest.

Material Safety Data Sheet Issue Date: 28-JAN-2008 Supercedes: 28-JAN-2008

POLYFLOC AS1002

1 IdentificationIdentification of substance or preparationPOLYFLOC AS1002

Product Application AreaFlocculant.

Company/Undertaking IdentificationGE Betz, Inc.4636 Somerton RoadTrevose, PA 19053T 215 355-3300, F 215 953 5524

Emergency Telephone(800) 877-1940

Prepared by Product Stewardship Group: T 215-355-3300 Prepared on: 28-JAN-2008

2 Hazard(s) identification

******************************************************************************** EMERGENCY OVERVIEW CAUTION May cause slight irritation to the skin. May cause slight irritation to the eyes. Mists/aerosols may cause irritation to upper respiratory tract. DOT hazard is not applicable Odor: Slight; Appearance: Colorless To Light Yellow, Liquid Fire fighters should wear positive pressure self-contained breathing apparatus(full face-piece type). Proper fire-extinguishing media: dry chemical, carbon dioxide, foam or water ******************************************************************************** POTENTIAL HEALTH EFFECTS ACUTE SKIN EFFECTS: Primary route of exposure; May cause slight irritation to the skin. ACUTE EYE EFFECTS: May cause slight irritation to the eyes. ACUTE RESPIRATORY EFFECTS: Mists/aerosols may cause irritation to upper respiratory tract.

Page 1Substance or Preparation: POLYFLOC AS1002

INGESTION EFFECTS: May cause slight gastrointestinal irritation. TARGET ORGANS: No evidence of potential chronic effects. MEDICAL CONDITIONS AGGRAVATED: Not known. SYMPTOMS OF EXPOSURE: May cause redness or itching of skin.

3 Composition / information on ingredients

Information for specific product ingredients as required by the U.S. OSHA HAZARD COMMUNICATION STANDARD is listed. Refer to additional sections of this MSDS for our assessment of the potential hazards of this formulation. HAZARDOUS INGREDIENTS: This product is not hazardous as defined by OSHA regulations. No component is considered to be a carcinogen by the National Toxicology Program, the International Agency for Research on Cancer, or the Occupational Safety and Health Administration at OSHA thresholds for carcinogens.

4 First-aid measures

SKIN CONTACT: Wash thoroughly with soap and water. Remove contaminated clothing. Get medical attention if irritation develops or persists. EYE CONTACT: Remove contact lenses. Hold eyelids apart. Immediately flush eyes with plenty of low-pressure water for at least 15 minutes. Get medical attention if irritation persists after flushing. INHALATION: If nasal, throat or lung irritation develops - remove to fresh air and get medical attention. INGESTION: Do not feed anything by mouth to an unconscious or convulsive victim. Do not induce vomiting. Immediately contact physician. Dilute contents of stomach using 2-8 fluid ounces (60-240 mL) of milk or water. NOTES TO PHYSICIANS: No special instructions

5 Fire-fighting measures


FIRE FIGHTING INSTRUCTIONS: Fire fighters should wear positive pressure self-contained breathing apparatus (full face-piece type). EXTINGUISHING MEDIA: dry chemical, carbon dioxide, foam or water HAZARDOUS DECOMPOSITION PRODUCTS: oxides of carbon and sulfur FLASH POINT: > 200F > 93C P-M(CC)

6 Accidental release measures

PROTECTION AND SPILL CONTAINMENT: Ventilate area. Use specified protective equipment. Contain and absorb on absorbent material. Place in waste disposal container. Flush area with water. Wet area may be slippery. Spread sand/grit. DISPOSAL INSTRUCTIONS: Water contaminated with this product may be sent to a sanitary sewer treatment facility,in accordance with any local agreement,a permitted waste treatment facility or discharged under a permit. Product as is - Incinerate or land dispose in an approved landfill.

7 Handling and storage

HANDLING: Normal chemical handling. STORAGE: Keep containers closed when not in use. Protect from freezing. Shelf life 135 days.

8 Exposure controls / personal protection

EXPOSURE LIMITS This product is not hazardous as defined by OSHA regulations. ENGINEERING CONTROLS: adequate ventilation PERSONAL PROTECTIVE EQUIPMENT: Use protective equipment in accordance with 29CFR 1910 Subpart I RESPIRATORY PROTECTION: A RESPIRATORY PROTECTION PROGRAM THAT MEETS OSHA’S 29 CFR 1910.134 AND ANSI Z88.2 REQUIREMENTS MUST BE FOLLOWED WHENEVER WORKPLACE CONDITIONS WARRANT A RESPIRATOR’S USE. USE AIR PURIFYING RESPIRATORS WITHIN USE LIMITATIONS ASSOCIATED WITH THE EQUIPMENT OR ELSE USE SUPPLIED AIR-RESPIRATORS. If air-purifying respirator use is appropriate, use any of the following particulate respirators: N95, N99, N100, R95, R99, R100, P95, P99 or P100. SKIN PROTECTION: rubber, butyl, viton or neoprene gloves -- Wash off after each use. Replace as necessary. EYE PROTECTION: splash proof chemical goggles


9 Physical and chemical properties

Specific Grav.(70F,21C) 1.015 Vapor Pressure (mmHG) ~ 18.0 Freeze Point (F) 32 Vapor Density (air=1) < 1.00 Freeze Point (C) 0 Viscosity(cps 70F,21C) 2000 % Solubility (water) 100.0 Odor Slight Appearance Colorless To Light Yellow Physical State Liquid Flash Point P-M(CC) > 200F > 93C pH As Is (approx.) 4.1 Evaporation Rate (Ether=1) < 1.00 Percent VOC: 0.0 NA = not applicable ND = not determined

10 Stability and reactivity

STABILITY: Stable under normal storage conditions. HAZARDOUS POLYMERIZATION: Will not occur. INCOMPATIBILITIES: May react with strong oxidizers. DECOMPOSITION PRODUCTS: oxides of carbon and sulfur INTERNAL PUMPOUT/CLEANOUT CATEGORIES: "A"

11 Toxicological information

Oral LD50 RAT: >2,000 mg/kg NOTE - Estimated value Dermal LD50 RABBIT: >2,000 mg/kg NOTE - Estimated value

12 Ecological information

AQUATIC TOXICOLOGY Daphnia magna 48 Hour Static Acute Bioassay (pH adjusted) LC50= 25466; No Effect Level= 8700 mg/L Fathead Minnow 96 Hour Static Acute Bioassay (pH adjusted) LC50= 30944; No Effect Level= 15500 mg/L BIODEGRADATION No Data Available.

13 Disposal considerations


If this undiluted product is discarded as a waste, the US RCRA hazardous waste identification number is : Not applicable. Please be advised; however, that state and local requirements for waste disposal may be more restrictive or otherwise different from federal regulations. Consult state and local regulations regarding the proper disposal of this material.

14 Transport information

DOT HAZARD: Not Applicable PROPER SHIPPING NAME: DOT EMERGENCY RESPONSE GUIDE #: Not applicable Note: Some containers may be DOT exempt, please check BOL for exact container classification

15 Regulatory information

TSCA: All components of this product are included on or are in compliance with the U.S. TSCA regulations. CERCLA AND/OR SARA REPORTABLE QUANTITY (RQ): No regulated constituent present at OSHA thresholds FOOD AND DRUG ADMINISTRATION: 21 CFR 176.110 (acrylamide - acrylic acid resins) All ingredients comprising this product are authorized by FDA for the manufacture of paper and paperboard that may contact aqueous and fatty foods as per 21 CFR 176.170(a) (4). USDA FOOD PLANT APPROVALS: G1 SARA SECTION 312 HAZARD CLASS: Product is non-hazardous under Section 311/312 SARA SECTION 302 CHEMICALS: No regulated constituent present at OSHA thresholds SARA SECTION 313 CHEMICALS: No regulated constituent present at OSHA thresholds CALIFORNIA REGULATORY INFORMATION CALIFORNIA SAFE DRINKING WATER AND TOXIC ENFORCEMENT ACT (PROPOSITION 65): No regulated constituents present MICHIGAN REGULATORY INFORMATION No regulated constituent present at OSHA thresholds

16 Other information

NFPA/HMIS CODE TRANSLATION Health 1 Slight Hazard Fire 0 Minimal Hazard Reactivity 0 Minimal Hazard Special NONE No special Hazard


(1) Protective Equipment B Goggles,Gloves (1) refer to section 8 of MSDS for additional protective equipment recommendations. CHANGE LOG EFFECTIVE DATE REVISIONS TO SECTION: SUPERCEDES --------- --------------------- ---------- MSDS status: 30-JAN-1997 ** NEW ** 12-MAY-1997 15 30-JAN-1997 06-MAY-1998 ;EDIT:9 12-MAY-1997 27-MAY-1999 15 06-MAY-1998 21-SEP-1999 15 27-MAY-1999 11-FEB-2002 4,16 21-SEP-1999 28-JAN-2008 4,5,7,8,10 11-FEB-2002



CUSTOMER:

DATE:

SCALE:

MODEL NO:


REVISED

REVISED

REVISED

DRAWING NUMBER:

NONE

7/10/06

NJF


5/30/08




"A"(Inches)


"E"


DIRECTIONOF FLOW

Tab 6

Modified ISR System – AOP Pre-Treatment System Air Stripping

QED Air Stripper Model ver. 2.01 2/15/2010

Site DataName: Maija Seppanen e-mail: maija.seppanen@arcadis-

us.comProject: Raytheon RAPAUnits: English Altitude: 0 ftAir Temp: 90 F Flow: 60 gpmWater Temp: 72 FStripper: EZ-Tray 16.x - Click for details Stripper Air Flow: 850 cfmStripper Max Flow: 150 gpm

Water ResultsContaminant Influent

(ppb)Target (ppb)

4-Tray Results (ppb)

4-Tray %Removal

6-Tray Results (ppb)

6-Tray %Removal

1,1,1-trichloroethane 4310 0 < 1 100.000 < 1 100.0001,1,2-trichloroethane 493 0 12.8 97.404 2.4 99.5131,1-dichloroethane 6318 0 2.7 99.957 < 1 100.0001,1-dichloroethylene 13789 0 < 1 100.000 < 1 100.0001,2,4-trimethylbenzene 609 0 < 1 100.000 < 1 100.0001,2-dichloroethane 992 0 15.2 98.468 2.1 99.7881,3,5-trimethylbenzene 1101 0 < 1 100.000 < 1 100.0001,4-dioxane 15767 0 15363.8 2.557 15363.8 2.5572-butanone (MEK) 9340 0 7462.1 20.106 7448.6 20.2512-hexanone (MBK) 6107 0 42.2 99.309 3.8 99.938acetone 15175 0 12805.1 15.617 12796.2 15.676benzene 569 0 < 1 100.000 < 1 100.000c-1,2-dichloroethylene 12174 0 3.0 99.975 < 1 100.000carbon disulfide 701 0 < 1 100.000 < 1 100.000chloroethane 496 0 < 1 100.000 < 1 100.000chloroform (trichloromethane) 12973 0 13.8 99.894 < 1 100.000ethylbenzene 300 0 < 1 100.000 < 1 100.000isopropylbenzene 472 0 < 1 100.000 < 1 100.000m-xylene 426 0 < 1 100.000 < 1 100.000methylene chloride 13043 0 51.7 99.604 3.5 99.973naphthalene 153 0 15.6 89.804 6.6 95.686o-xylene 254 0 < 1 100.000 < 1 100.000t-1,2-dichloroethylene 111 0 < 1 100.000 < 1 100.000tetrachloroethylene (PERC,PCE) 1514 0 < 1 100.000 < 1 100.000toluene 5607 0 2.1 99.963 < 1 100.000trichloroethylene (TCE) 44178 0 3.5 99.992 < 1 100.000trichlorofluoromethane 590 0 < 1 100.000 < 1 100.000vinyl chloride (chloroethylene) 4997 0 < 1 100.000 < 1 100.000

Air ResultsContaminant 4-Tray

(ppmV)4-Tray (lb/hr)

6-Tray (ppmV)

6-Tray (lb/hr)

Page 1 of 3QED Stripper Model

2/15/2010http://64.9.214.199/cgi-bin/cmod_run.pl

CWorden

Line

1,1,1-trichloroethane 7.6390 0.12948 7.6393 0.129491,1,2-trichloroethane 0.8511 0.01443 0.8695 0.014741,1-dichloroethane 15.0893 0.18973 15.0955 0.189811,1-dichloroethylene 33.6308 0.41426 33.6313 0.414271,2,4-trimethylbenzene 1.1974 0.01829 1.1980 0.018301,2-dichloroethane 2.3339 0.02935 2.3651 0.029741,3,5-trimethylbenzene 2.1652 0.03307 2.1660 0.033081,4-dioxane 1.0820 0.01211 1.0820 0.012112-butanone (MEK) 6.1585 0.05642 6.2027 0.056822-hexanone (MBK) 14.3171 0.18221 14.4076 0.18336acetone 9.6481 0.07120 9.6840 0.07147benzene 1.7215 0.01709 1.7223 0.01709c-1,2-dichloroethylene 29.6851 0.36566 29.6922 0.36575carbon disulfide 2.1771 0.02106 2.1772 0.02106chloroethane 1.8175 0.01490 1.8178 0.01490chloroform (trichloromethane) 25.6675 0.38934 25.6940 0.38974ethylbenzene 0.6680 0.00901 0.6681 0.00901isopropylbenzene 0.9285 0.01418 0.9285 0.01418m-xylene 0.9484 0.01279 0.9487 0.01280methylene chloride 36.1666 0.39030 36.3009 0.39175naphthalene 0.2536 0.00413 0.2701 0.00440o-xylene 0.5651 0.00762 0.5657 0.00763t-1,2-dichloroethylene 0.2707 0.00333 0.2707 0.00333tetrachloroethylene (PERC,PCE) 2.1586 0.04549 2.1587 0.04549toluene 14.3831 0.16839 14.3884 0.16845trichloroethylene (TCE) 79.4960 1.32715 79.5021 1.32725trichlorofluoromethane 1.0155 0.01773 1.0155 0.01773vinyl chloride (chloroethylene) 18.9044 0.15012 18.9046 0.15013

NotesCopyright -- QED Treatment Equipment, PO Box 3726, Ann Arbor, MI 48106.

PH-> 1-800-624-2026 or 1-734-995-2547, FX-> 1-734-995-1170. E-mail->[email protected]. WEB->www.qedenv.com.

The QED modeler estimates unit performance for the listed contaminants. Results assume -

1. dissolved-phase contaminant within a water matrix 2. clean stripper air 3. no surfactants, oil, grease or other immiscible phase(s) in the influent 4. unit operated within the given parameters and as instructed in the O&M

manual

Stripper performance shall meet or exceed either the required effluent concentration(s) or effluent estimates, whichever is greater, for the conditions supplied and assumes the influent concentrations of each contaminant are less than 25% solubility in water. QED makes no claim of the model's accuracy beyond the 25% solubility in water limit.



Contact UsFill out your contact and project information and click Send to have a QED Treatment application specialist contact you.

Name - Maija Seppanen

Company - Company

Phone - Phone Fax - Fax

e-mail - [email protected] - Raytheon RAPA

Application Notes

Send Reset

Save Data

Use the following URL to reconstruct your data form for future remodeling with changes. This URL can be saved in any text file for record keeping and later retrieval. This run's URL:

http://64.9.214.199/cgi-bin/remodel.pl?u=e&tw=72&ta=90&f=60&a=0&s=16.x&n=Maija&[email protected]&p=Rayth&c=9,4310;13,493;15,6318;16,13789;23,609;27,992;29,1101;33,15767;36,9340;40,6107;55,15175;63,569;81,12174;84,701;89,496;91,1



Sliding Tray, High-EfficiencyAir Strippers for VOC Removal

800-624-2026www.qedenv.com

Air flows up through perforatedtrays creating a turbulent froth zonewith a high air-to-liquid surface areafor mass transfer of volatile organiccompounds (VOCs)

Additional space required by conventionalstacking tray air strippers.

E-Z Tray®

Conventional air strippers needmore than twice the accessand tray removal space than E-Z Tray® air strippers.

Hinged door optionallows for easy accesswithout door removal.

Flow rates available from1 to 1,000 gpm.

Front access hatches sealtight and are removedquickly with hand-knobs.

Split-tray option reduces maximumtray weight to only 28 lbs., even on the 1,000 gpm unit!

Front access slide-out trays allowunit maintenance by one person.

E-Z Trayaccessarea

Flow Rates from 1 to 1,000 gpm and Options to Fit Every Treatment Project

The E-Z Tray® Air Stripper (U.S. Patent Number5,518,668) is a sliding tray, stainless steel air stripperused to remove volatile organic compounds (VOC)from contaminated groundwater and waste streams.The exclusive design of the E-Z Tray stripper results invery high removal efficiencies in an easier to maintainprocess unit.

Any air stripping process subject to fouling conditionshas to contend with periodic cleaning in order toretain treatment efficiencies and capacity. Tower airstrip pers can become maintenance headaches whenthe tower packing becomes clogged and cementedtogether with bio-fouling or precipitants. When theperforated trays in stacking tray air strippers becomefouled they require major disassembly, cranes orhoists, and lots of room.

Unlike these traditional types of air strippers, QED’s E-Z Tray air strippers use removable, lightweight, front slide-out trays. This unique feature providesmany advantages, including one person cleaning andless building space.

E-Z Tray air strippers are available in configurationswith 4 or 6 trays, with maximum flow rates from 1-25 gpm (4-100 Lpm) all the way up to 1,000 gpm(3,784 Lpm).

NEW – High Capacity Process Air StrippersThese air strippers are engineered to serve in larger,process-type projects involving multiple treatmentstages, where they are an effective component oflarge-scale water or wastewater processes in

E-Z Tray

• Single personcleaning

• Easy processmonitoring andinspection, even while inoperation

• Reducedfootprint forinstallation andmaintenance

• High removalefficiencieseasier tomaintain

• Easily modeledonline bycustomer tohelp processevaluation

E-Z Tray AdvantagesTower AirStrippers

• Condition ofpacking andliquid and airflow distribu-tion are verydifficult toobserve

• Small footprintbut very tallstructurerequired

• More difficultto keep atdesignperformance

• More complexprocessassistancerequired

Stacking Tray AirStrippers

• Major disassemblysteps and crewneeded

• Difficult toimpossible toobserve air andliquid flowdistribution duringoperation

• Lots of spaceneeded fordisassembly, toaccess all sidesand to lift andstore tray stages

• More difficult tokeep at designperformance

• Online modelernot offered

Easier tray cleaning andsuperior technical supportmake E-Z Tray® air strippersa smart choice!

manufacturing, refining, chemical processing andother industries. They can act as a pre-treatment stagefor other process elements, such as large aerobicbiotreatment units, removing VOCs at much lowerairflow rates to reduce the costs of off-gas treatment.

All of this combined with the easier maintenance andsmaller footprint of QED's sliding tray air strippers,has led E-Z Tray to become the preferred choice formajor remediation and process stream projects in theU.S. and abroad.

The QED VOC Removal AdvantageProven equipment, expert help with its selection and installation, and support you can count on when you need it

Air Stripper SpecificationsModel Maximum Dry Operating Shell Dimension TraysNo. Flow Range Weight Weight (LxWxH) Per Tier

4.4 1-50 gpm (4-189 Lpm) 630 lbs. (286 kg) 985 lbs. (447 kg) 29 x 27 x 82 in. (74 x 69 x 208 cm) 4 x 29 lbs. (4 x 13 kg)

4.6 1-50 gpm (4-189 Lpm) 780 lbs. (354 kg) 1,219 lbs. (553 kg) 29 x 27 x 102 in. (74 x 69 x 259 cm) 6 x 29 lbs. (6 x 13 kg)




8.6 1-75 gpm (4-284 Lpm) 1,182 lbs. (536 kg) 1,956 lbs. (887 kg) 49 x 27 x 102 in. (124 x 69 x 259 cm) 6 x 50 lbs. (6 x 23 kg)

12.4 1-120 gpm (4-454 Lpm) 1,165 lbs. (528 kg) 2,105 lbs. (955 kg) 73 x 27 x 82 in. (185 x 69 x 208 cm) 4 x 60 lbs. (4 x 447 kg)

12.6 1-120 gpm (4-454 Lpm) 1,442 lbs. (654 kg) 2,606 lbs. (1,182 kg) 73 x 27 x 102 in. (185 x 69 x 259 cm) 6 x 60 lbs. (6 x 447 kg)




24.6 1-250 gpm (4-946 Lpm) 2,599 lbs. (1,179 kg) 4,926 lbs. (2,234 kg) 73 x 52 x 104 in. (185 x 132 x 264 cm) 12 x 60 lbs. (12 x 27 kg)

48.4 1-500 gpm (1,893 Lpm) 5,000 lbs. (2,268 kg) 12,500 lbs. (5,670 kg) 98 x 71 x 84 in. (249 x 180 x 213 cm) 16 x 60 lbs. (16 x 27 kg)

48.6 1-500 gpm (1,893 Lpm) 5,500 lbs. (2,495 kg) 13,000 lbs. (5,897 kg) 98 x 71 x 104 in. (249 x 180 x 264 cm) 24 x 60 lbs. (24 x 27 kg)

96.4 1-1,000 gpm (3,785 Lpm) 11,000 lbs. (4,990 kg) 25,000 lbs. (11,340 kg) 142 x 98 x 84 in. (361 x 249 x 213 cm) 32 x 60 lbs. (32 x 27 kg)

96.6 1-1,000 gpm (3,785 Lpm) 11,500 lbs. (5,216 kg) 30,000 lbs. (13,608 kg) 142 x 98 x 104 in. (361 x 249 x 264 cm) 48 x 60 lbs. (48 x 27 kg)Standard construction is 304 SS, other alloys upon request. *Allow additional space for accessory components. (blower, piping, etc.)

Exclusive Online PerformanceModeler has been developedto assist you in selecting themost effective air strippingpackage for your groundwatercleanup project

E-Z Tray®

Model 24.4E-Z Tray®

Model 16.4E-Z Tray®

Model 6.4

CWorden

Line

count on when you need it

Active Nominal Additional SpaceArea Air Flow for Tray Removal*2.8 ft.2 (0.26 m2) 210 cfm (5.95 m3/min) 27 in. (69 cm)

2.8 ft.2 (0.26 m2) 210 cfm (5.95 m3/min) 27 in. (69 cm)

3.8 ft.2 (0.35 m2) 320 cfm (9.06 m3/min) 35 in. (89 cm)

3.8 ft.2 (0.35 m2) 320 cfm (9.06 m3/min) 35 in. (89 cm)

5.6 ft.2 (0.52 m2) 420 cfm (11.89 m3/min) 47 in. (119 cm)

5.6 ft.2 (0.52 m2) 420 cfm (11.89 m3/min) 47 in. (119 cm)

8.8 ft.2 (0.82 m2) 600 cfm (16.99 m3/min) 71 in. (180 cm)

8.8 ft.2 (0.82 m2) 600 cfm (16.99 m3/min) 71 in. (180 cm)

11.1 ft.2 (1.03 m2) 850 cfm (24.07 m3/min) 47 in. (119 cm)

11.1 ft.2 (1.03 m2) 850 cfm (24.07 m3/min) 47 in. (119 cm)

17.5 ft.2 (1.63 m2) 1,300 cfm (36.81 m3/min) 72 in. (183 cm)

17.5 ft.2 (1.63 m2) 1,300 cfm (36.81 m3/min) 72 in. (183 cm)

27 ft.2 (2.51 m2) 2,600 cfm (73.62 m3/min) 72 in. (183 cm)

27 ft.2 (2.51 m2) 2,600 cfm (73.62 m3/min) 72 in. (183 cm)

54 ft.2 (5.02 m2) 5,200 cfm (147.25 m3/min) 2 x 72 in. (2 x 183 cm)*

54 ft.2 (5.02 m2) 5,200 cfm (147.25 m3/min) 2 x 72 in. (2 x 183 cm)*

Try it for yourself today! Use our exclusiveonline stripper modeler atwww.qedenv.com/model/model.htmlto spec the exact size and configuration foryour project. Then talk to a QED applicationsspecialist toll-free at (800) 624-2026for fast, free system design assistance and a price quote.

E-Z Tray®

Model 96.6

How it WorksAs contaminated groundwater enters throughthe top of the air stripper, millions of airbubbles are forced by blower pressure upthrough the perforated trays. This creates aturbulent froth zone with an extremely highair-to-liquid surface area for mass transfer ofvolatile organic compounds (VOCs) from liquidto air. Using the froth instead of a conventionaltower packing delivers high VOC removalefficiencies even under fouling conditions, andis easier to inspect and maintain.

CWorden

Line

6095 Jackson RoadAnn Arbor, MI 48106-3726USA

800-624-2026T: 734-995-2547F: [email protected]

The World Leader in Air-Powered RemediationFor Remediation, Landfills and Groundwater Sampling

CODE 2336 4/09

Visit qedenv.com/air-strippers to view and use the exclusive OnlinePerformance Modeler, which allows you to model your process conditions andselect the most efficient air stripping package for your VOC removal project.You can also view case studies where E-Z Tray air strippers were the topchoice in successful projects.

QED Quality Control,Manufacturing Standardsand Customer ServiceExperienced site owners, including major oilcompanies, are increasingly choosing E-Z Tray®

air strippers from QED due to their uniquefeatures and solid technical support, including:

• Lower long-term O&M costs due to easiertray maintenance than tower-type orstacking tray air strippers.

• Lightweight, slide-out trays don’trequire hoists, regardless of the size ofthe air stripper.

• E-Z Tray air strippers need less buildingspace, which can lower building costs.

• QED’s staff and resources are #1 in airstripper technical and service support,including for unusual applications.

• Online Performance Modeler tool available 24/7 to help you select theproper air stripper.

• QED quote & delivery times are quickand dependable.

1565 Alvarado StreetSan Leandro, CA 94577USA

800-624-2026T: 510-346-0400F: [email protected]

QED EZ-Tray Model 16.4 - Front View

BLOWER

46

51.5

93

89

GRAVITYDRAIN4" PIPE

PUMP

CONTROL PANEL

Copyright QED Environmental Systems, Inc., 2001

QED EZ-Tray Model 16.4 - Top View

GRAVITYDRAIN

AREA OF TRAYEXTRACTION

AREA OF TRAYEXTRACTION

BLOWER

INLETPUMP

DISCHPUMP

CONTROL PANEL

47.25

93

51.5

AIR EXHAUST8" PIPE

WATER INLET4" FNPT

Copyright QED Environmental Systems, Inc., 2001

Page 1 of 3









St. Petersburg, FloridaRaytheon Company


AIR STRIPPER BLOWERS (B-200A/B) DESIGN CALCULATIONSModified ISR System


eeR

DN


1.89E-05 kg / (m*sec)1.27E-05 lb / (sec*ft)



Flow is Turbulent





eeR

DN

32.0Re

125.00014.0

Nf

G:\ENV\TF\901-1000\TF922\Reports\2010\RAPA 2010\Final FDEP RAPA\Appendix J\Tab #6\(4) Tab #6_B-200A&B Calc.xls ARCADIS

Page 2 of 3






i. Flow Resistance due to Sudden Expansion6" Blower outlet expands to 8" conveyance line

Internal Diameter of Conveyance Piping, d1 6.065 inInternal Diameter of Conveyance Piping, d2 7.981 in

Resistance, K1 0.21 (dimensionless)

ii. Fittings Size (in) K-Value Quantity Total K-Value

Butterfly Valve 8 0.63 3 1.89Diaphragm Valve 8 5.1 1 5.190 Degree Elbow 8 0.42 10 4.2

Total K 11.40


KL

fZZgP

)4()(2

22

2115.0

d

dK






0.21 psi

5.9 in. water

VI. Other Items

Air Stripper 4 in. water [loss per tray]24 in. water [total loss - 6 trays]

Actuated Flow Control Valve (Electric) 10 in. water [assumed]

Discharge into a Pressurized Line 10 in. water [assumed]

Air Stripper Inlet Screen 2 in. water [assumed]

csba

c gK

D

LfZZ

g

gP

2)4()( Re


Page 3 of 3




VII. Total Pressure Blower will be required to Generate

ΔPa 5.9 in. waterOther Items 46.0 in. waterSafety Factor 15%

Total Pressure Required 59.73 in. water


PRESSURE BLOWERS

BULLETIN 451JANUARY, 2001

• Static pressures to 58”WG• Capacities to 5200 CFM• Temperatures to 600̊ F.

ARRANGEMENT 4

ARRANGEMENT 10

ARRANGEMENT 8

For greater pressures and capacities: see Type HP Pressure Blowers

7660 QUINCY STREET–WILLOWBROOK,ILLINOIS 60521-5596TEL: [630] 794-5700•FAX: [630] 794-5776•WEB: http://www.nyb.com •E-MAIL: [email protected]

PAGE 2

DESIGN FEATURES

• Pressures to 58”WG.

• Capacities to 5200 CFM.

• Stable performance . . . the pressure curveremains stable from wide-open to closed-off . . .fan instability, or pulsation, is eliminated evenwhen “turn-down” approaches zero flow.

• Efficiency . . . advanced wheel and aerodynamichousing design combine for air-handling efficiencysuperior to conventional radial-wheel designs.

• Wide performance range . . . choice of 13 wheeldiameters and five outlet sizes enable efficientfan selection across a broad range of volumes andpressures.

• Choice of arrangements . . . direct-drive and belt-drive.

• Wide application range . . . designed for continuousoperation in combustion, cooling, conveying, drying,and various process systems.

CONSTRUCTION FEATURES

• All-welded steel housings . . . heavy-gauge hous-ings are rigidly braced to prevent “flexing” at highpressures.

• Flanges . . . continuously welded flanges matchANSI Class 125/150 hole pattern.

• Balance . . . all wheels are precision-balancedprior to assembly . . . fans with motors and drivesmounted by nyb are final-balanced at the speci-fied running speed.

• Shafting . . . straightened to close tolerance to min-imize “run-out” and ensure smooth operation.

• Inlet configuration . . . a choice of three inlet typesallows units to be tailored to specific applicationrequirements.

• Lifting eyes . . . standard on all units for ease ofhandling and installation.

• Finish . . . medium-green industrial coating.

... for process systems

© Copyright 2001 by The New York Blower Company.® Registered trademark of The New York Blower Company.

BLOWERS

PRESSURE

Arrangement 1 Pressure Blower with plain pipe inlet.

Arrangement 4 Pressure Blower with Venturi inlet.

Arrangement 8 Pressure Blower

with motor, coupling guard,and shaft and bearing guard.

The New York Blower Company certifies thatthe Pressure Blowers shown herein arelicensed to bear the AMCA Seal. The ratingsshown are based on tests and procedures per-formed in accordance with AMCA Publication211 and comply with the requirements of theAMCA Certified Ratings Program.

PRESSURE BLOWERS

WHEEL

PAGE 3

ALUMINUM

STANDARD

The unique Pressure Blower wheel is designedto provide efficient performance and reducedsound levels . . . the dual-taper design conceptyields typical efficiencies up to 10 percentagepoints greater than conventional straight radialwheels. Riveted high-strength aluminum alloyblades and side plates minimize overhungwheel weight and starting inertia. Ductile-iron,taper-lock hubs make wheels easily removable.Welded steel and stainless steel wheels are alsoavailable . . . see page 5.

Recommended for belt-driven applications only.Wheel is mounted onshaft mounted in heavy-duty bearings.

Max. airstream temperature:200˚F.–aluminum wheel.300˚F.–steel wheel.600˚F.–heat fan.

ARRANGEMENT 1

A compact direct-driveunit with a minimumnumber of moving partsfor ease of maintenance.Wheel is mounted directlyon motor shaft.

Max. airstream temperature:180˚F.

ARRANGEMENT 4

Direct-drive arrangementsimilar to Arrangement 1,but with integral motorpedestal . . . fan shaft isconnected to the motorshaft with a flexible cou-pling.


ARRANGEMENT 8

Enclosed belt-drive ar-rangement. Ideal for out-door applications. Wheelmounted on shaftmounted in heavy-dutybearings.


ARRANGEMENT 10

ARRANGEMENTSStandard aluminum wheel.

MATERIAL SPECIFICATIONSU. S. STANDARD SHEET GAUGE TO 7 GAUGE

FLANGEDIMENSIONS

[INCHES]† Holes straddle centerline.

ANSI Class 125/150 hole pattern.Flange thickness 3/8”

WHEEL WEIGHTSAND INERTIA [WR2=LBS.–FT.2]

PAGE 10

DIMENSIONS [INCHES] Dimensions not to be used for construction unless certified.

Wheeldia.

Wheeldia.

Wheeldia.

Scrollandsides

Outletsize

Inletflange

AArr.4

B JJ L MNNArr.8

Motorframe

Arr. 4, 8

A

H

C D F GArr. 8

Arrangement

Arr. 8

8

Arr. 8Arr. 4

4

Arr. 4Arr. 10

10

RArr.

4, 8 10

Housing Shaft dia. Bearings Drive keySide platesSide plates Arrangement Arr. 1 Arrangement Arrangement

Drive Inlet Driveend

In-board1, 10 888 1010

Fan weight*Arrangement

84 10

SArr.

84

Arr. 10 Arr. 10 Arr. 10 Arr. 10 Arr. 10 Arr. 10K N S T U V W

14-1819-2223-26

14-18

12

10

8

8

6

8

6

143-145182-184

182-184

182-184

182-184

182-184

182-184

213-215

213-215

213-215

213-215

213-215

213-215

213-215

254-256

254-256

254-256

254-256

254-256

284-286

284-286

284-286

284-286324-326

324-326 291⁄4281⁄4291⁄4263⁄426

26

26

26

26

263⁄4

263⁄4243⁄4

243⁄4

243⁄4

243⁄4

243⁄4

24

24

24

24

23

23

193⁄419

19 181⁄4

181⁄4

181⁄4

173⁄4

173⁄4

173⁄4

213⁄4

23

23 39

39

38

375⁄8

38

331⁄2

375⁄8

361⁄8

331⁄2

361⁄8

311⁄8 55⁄8

61⁄8

61⁄8

7

7

71⁄4 71⁄4

71⁄4 71⁄4103⁄4

103⁄4

85⁄8

85⁄8

85⁄8

85⁄8

85⁄8

85⁄8

65⁄8

65⁄8 37⁄8

41⁄2

5

5

41⁄2

41⁄2

41⁄2

37⁄8

37⁄8

33⁄8

33⁄843⁄8

51⁄2

51⁄2

61⁄4

61⁄4

63⁄4

63⁄4 231⁄2

231⁄2

191⁄2

191⁄2

191⁄2

191⁄2

191⁄2

141⁄8

141⁄8

141⁄8

141⁄8

141⁄8

141⁄8

141⁄8

141⁄8

141⁄8

85⁄8

85⁄8 15 145165

230

165185190235

240

290

315

190

260

290

320

300

350

375

390 550

540

535

450

430

515

495440425420320315510

490

400

395

320

315

395

295 205

305

210

310

390

215

315

400

325

405

410

15

15

15

17191⁄4

191⁄4

245⁄8

245⁄8

245⁄8

253⁄8

253⁄8

253⁄8

161⁄2

161⁄2

161⁄2

161⁄2

161⁄2

161⁄2

183⁄4

183⁄4

183⁄4

183⁄4

183⁄4241⁄4247⁄8

241⁄8

51⁄8

51⁄8

55⁄8

55⁄8

61⁄4

61⁄4

61⁄4

61⁄4

37⁄8

5

5

63⁄4

63⁄4

63⁄4

63⁄4

371⁄4

371⁄4

331⁄4

321⁄4

321⁄4

267⁄8

267⁄8

267⁄8

267⁄8

213⁄8

317⁄8

317⁄8

261⁄2

261⁄2

25

25

241⁄219 391⁄2

417⁄8

417⁄8443⁄8

443⁄8

443⁄8

471⁄2

471⁄2

471⁄2

471⁄2513⁄4543⁄8

543⁄8

543⁄8567⁄8

567⁄8 463⁄8 277⁄8

277⁄8463⁄8437⁄8

437⁄8431⁄8427⁄8421⁄8

421⁄8

363⁄4

363⁄4

363⁄4

363⁄4

341⁄2

341⁄233

341⁄2

423⁄442

42

365⁄8

365⁄8343⁄8355⁄8333⁄8

333⁄8

333⁄8

317⁄8

317⁄8

317⁄8

531⁄4

513⁄4

397⁄8

397⁄8

421⁄2

421⁄2455⁄8441⁄2475⁄8

475⁄8

517⁄8

517⁄853

19

19

173⁄4

173⁄4

19193⁄4

143-145182-184143-145

143-145

04

06

08

10

12

19-22

14-18

19-22

23-26

15-18

19-22

23-26

19-22

23-26

14-18 10 10 10 17⁄16 17⁄16 A A A A 3⁄8 3⁄819-22 10 10 10 17⁄16 17⁄16 B B A B 3⁄8 3⁄823-26 10 10 7 111⁄16 17⁄16 B C A B 3⁄8 3⁄8

23-26

191⁄2235⁄8265⁄8

21275⁄8275⁄8

135⁄8161⁄2191⁄2

113⁄4147⁄8175⁄8

143⁄8171⁄2205⁄8

123⁄4151⁄2181⁄4

31⁄241⁄241⁄2

222626

173⁄8197⁄8197⁄8

87⁄8107⁄8107⁄8

91⁄8107⁄8107⁄8

93⁄8121⁄4121⁄4

93⁄4113⁄4113⁄4

10113⁄4113⁄4

81⁄41111

101⁄41313

KArr.8

31⁄4

31⁄4

27⁄8

27⁄8

27⁄8

27⁄8

33⁄8

33⁄8

33⁄8

31⁄4

31⁄4

37⁄827⁄8

33⁄8

33⁄8

* Bare fan weight, pounds, is approximate for units with aluminum wheels, less motors. For units with steel wheels,add the difference in wheel weights from the table at left.

Tolerance: ± 1⁄8”

Tolerance: ± 1⁄8”

14041406

Size AluminumWt.[lbs.] WR2

SteelWt.[lbs.] WR2

19.25 11.222.3 11.2

52.0 30.2461.0 35.48

50.0 26.8958.5 31.46

48.0 23.7956.0 27.75

46.0 20.9353.5 24.35

34.0 14.1640.0 16.66

32.5 12.3338.0 14.42

31.0 10.6736.5 12.56

29.5 9.1634.5 10.72

22.0 6.1326.0 7.25

21.0 5.2224.5 6.09

20.0 4.4123.0 5.07

19.0 3.6821.5 4.16

18.0 3.0420.5 3.46

19.0 10.2221.9 11.0

18.75 9.2921.9 10.8

18.5 8.4221.7 10.6

12.75 5.3115.6 5.4

12.5 4.7415.5 5.3

12.25 4.2215.3 5.2

12.0 3.7315.1 5.1

9.5 2.6512.4 2.6

9.25 2.312.2 2.6

9.0 1.9812.1 2.5

8.75 1.6911.8 2.4

8.5 1.4311.7 2.4

15041506, 1508

16041606, 1608

17041706, 1708

18041806, 18081904, 19061908, 19102004, 20062008, 20102104, 21062108, 21102204, 22062208, 22102306, 23082310, 23122406, 24082410, 24122506, 25082510, 25122606, 26082610, 2612

Flange I. D. O. D. Bolt Holes†size circle No. - Size

04 4 9 71⁄2 8 - 3⁄4”06 6 11 91⁄2 8 - 7⁄8”08 8 131⁄2 113⁄4 8 - 7⁄8”10 10 16 141⁄4 12 - 1”12 12 19 17 12 - 1”

A–200 Series Ball B–22400 Series Roller C–300 Series Ballnyb reserves the right to substitute bearings of equal rating.

Arr. 10 motor lim.ODP TEFC C-NW215T256T256T

215T254T254T

165⁄8185⁄8185⁄8

PAGE 11

DRAWINGS Dimensions not to be used for construction unless certified.

L

A

B

FD

G

CJJM

H

UT

UT

R S

9/16" DIA. HOLES

INLETVENTURI

INLETPLAIN PIPE

JJ-3/8"

LCHOUSING

JJ-3/8"

Arrangement

4PRESSUREBLOWERS

1 1/4"

UT

SR

H

JJ

MJJ-5/16" JJ-3/8"

F

UT

D

9/16" DIA. HOLES

B

A

L

NN

G

C

K

12 1/4"

LCHOUSING

INLETVENTURI

INLETPLAIN PIPE

Arrangement

8PRESSUREBLOWERS

NH

MJJ-3/8" JJ-3/8"

WTV

B

WTV

D F

R

A

S

SIZES 19–26: 3/4" DIA. HOLESSIZES 14–18: 9/16" DIA. HOLES

L

C

G

KJJ

LCHOUSING

INLETVENTURI

INLETPLAIN PIPE

Arrangement

10PRESSUREBLOWERS

The New York Blower Company has a policy of continuous product developmentand reserves the right to change designs and specifications without notice.

Housings are reversible and rotatable in 221⁄2˚ increments except Down Blast and Bottom Angular Down which require special construction.Arrangement 10 fans Sizes 19–22 are not rotatable in the field.

CBeears

L A B F D G C JJ M H U T U T R S 9/16" DIA. HOLES INLET VENTURI INLET PLAIN PIPE JJ-3/8" L C HOUSING JJ-3/8" Arrangement 4 PRESSURE BLOWERS

CBeears

The New York Blower CompanyFan-to-SizeFan Selection Data

Project:Location:Contact:

Fan Tagging: 012810-02C2

Fan DesignProduct: Type HP Pressure Blower Arrangement: 4Size/Model: 28506 Drive type: DirectWheel Type: AluminumWheel Material: AluminumWheel Width: 100.0 % Wheel Diameter: 100.0 %

Operating ConditionsVolume Flow Rate: 850 CFM Fan Speed: 3500 rpmFan Static Pressure: 61.2 in wg Fan Input Power: 17.1 bhpOutlet Velocity: 4337 ft/min VP/SP ratio: 0.0192Altitude (above mean sea level): 0 ft Operating Temperature: 70 Deg FOperating Inlet Airstream Density: 0.0750 lb/ft3Static Efficiency: 47.70% Mechanical Efficiency: 48.62%Maximum Operating Temperature: 70 Deg F Maximum Safe Operating Speed: 3600 rpm

Sound Power Level Ratings Levels expressed in dB (power levels reference 10^(-12) watts)Center Frequency (Hz): 63 125 250 500 1000 2000 4000 8000Octave Bands: 1 2 3 4 5 6 7 8 OverallTotal Fan Power Levels*: 102.9 104.9 102.8 105.7 105.8 102.7 96.7 92.7 112.3Inlet Power Levels**: 99.9 101.9 99.8 102.7 102.8 99.7 93.7 89.7 109.3Outlet Power Levels**: 99.9 101.9 99.8 102.7 102.8 99.7 93.7 89.7 109.3

*As corrected for point of operation (location on fan curve)**Unsilenced Inlet and Outlet power ratings are 3 dB lower than total fan power levels under the assumption that "half" of the sound power can be attributed to each opening. Silenced power ratings include this 3 dB reduction as well as the silencer attenuation. Estimated Sound Pressure Levels Expressed in dB (pressure levels reference 2x10-7 microbar) Directivity/Reflection Factor (Q) is 2, hemispherical radiation; Distance is 3 ft.; A-weighting is in use.

The estimated sound pressure level outside the fan due to an open inlet OR outlet is 99.6 dBA at 3.0 feet. The estimated sound pressure level outside the fan when BOTH inlet and outlet are ducted is 91.2 dBA at 3.0 feet (Housing Radiated Noise). Your Representative:Baltus Incorporated6020 W Maple Road Suite 504West Bloomfield, MI 48322Phone: (248) 851-6420Fax: (248) 851-6694E-Mail: [email protected]

Version: 1.77.30-R (October 2007) Printed: 02/03/2010 PDF. Calc Mode: 3

Static PressurePower

0

10

20

30

40

50

60

0

5

10

15

20

25

30

35

0 500 1000 1500 2000 2500 3000

The New York Blower CompanyFan-to-Size

Type HP Pressure Blower Volume Flow Rate: 850 CFM Temp.: 70 Deg F28506 Aluminum Fan Static Press.: 61.2 in wg Altitude: 0 ftArr.: 4 Speed: 3500 rpm Density: 0.0750 lb/ft3

Power: 17.1 bhp Outlet Velocity: 4337 ft/minTag: 012810-02C2

Copyright ©1999 The New York Blower Company. Phone: (248) 851-6420Baltus, Inc. [v1.77.30-R -- October 2007] Date Printed: 2/3/2010 Baltus IncorporatedCustomer: Your Sales Representative:

Fan

Sta

tic P

ress

ure

(in w

g)Fan Input P

ower (bhp)

Volume Flow Rate (CFM)

Version: 1.77.30-R (October 2007) Printed: 02/03/2010 PDF. Calc Mode: 3

Page 1 of 1


Considerations:




Usable tank volume = 856 gal

Process flow rate = 60 gpm Air Stripper Effluent







684 gal


684 gal

Tank Selection:

Cylindrical Tank:

Diameter = 7.2 feet

Total Tank Height = 4.3 feet

Usable Tank Volume = 856 gal

Available Tank Volume = 856 gal

Required Tank Volume = 684 gal


AIR STRIPPER DISCHARGE TANK (T-700) SIZINGModified ISR System




Page 1 of 3

AIR STRIPPER DISCHARGE PUMPS (P-400A/B) DESIGN CALCULATIONS






60 2 2.375 0.154 2.067 0.023 5.5860 3 3.500 0.216 3.068 0.051 2.5360 4 4.500 0.237 4.026 0.088 1.47







Flow (v1) = 60 gpm





Nominal Diam (in)

ID (in)


1 1.049 0.9241.5 1.610 1.4852 2.067 1.9423 3.068 2.9434 4.026 3.9016 6.065 5.94




sec60

min1*

)*( 2r

Qv


Page 2 of 3

AIR STRIPPER DISCHARGE PUMPS (P-400A/B) DESIGN CALCULATIONSModified ISR System - AOP Pre-Treatment System









Pipe Section 1 - 3"

Item Qty. L (ft) Qty * LLinear Pipe (L1) 1 1,400 1,400Standard Tee (thru flow) 6 12 72Standard Tee (branch flow) 2 17 3490˚ Elbows 12 4 48Union 6 0.5 3Check Valve 2 27 54Ball valve (full open) 6 4.3 26

Equivalent Length: 1,637



Total Pipe Friction - Pipe Section 1total equivalent length = 1,637 feet





Equivalent Length



Page 3 of 3

AIR STRIPPER DISCHARGE PUMPS (P-400A/B) DESIGN CALCULATIONSModified ISR System - AOP Pre-Treatment System






Head loss Across Misc. Process Components Flow meter 12 ft











Vapor Press:



Tab 7

Modified ISR System – AOP Pre-Treatment System Tank Venting

Page 1 of 2










TANK VENT BLOWER (B-300) DESIGN CALCULATIONSModified ISR System




eeR

DN

1.89E-05 kg / (m*sec)1.27E-05 lb / (sec*ft)



Flow is Turbulent





eeR

DN

32.0Re

125.00014.0

Nf


Page 2 of 2

TANK VENT BLOWER (B-300) DESIGN CALCULATIONSModified ISR System





i. Flow Resistance due to Sudden ExpansionNot applicable

Internal Diameter of Conveyance Piping, d1 3.068 inInternal Diameter of Conveyance Piping, d2 3.068 in

Resistance, K1 0.00 (dimensionless)

ii. Fittings Size (in) K-Value Quantity Total K-Value

Butterfly Valve 3 0.81 2 1.62Diaphragm Valve 3 6.1 1 6.190 Degree Elbow 3 0.54 8 4.32

Total K 12.04


csba

c gK

D

LfZZ

g

gP

2)4()(

2

Re

22

2115.0

d

dK






0.02 psi

0.6 in. water

VI. Other Items

Actuated Flow Control Valve (Electric) 10 in. water [assumed]

Discharge into a Pressurized Line 10 in. water [assumed]

VII. Total Vacuum Blower will be required to Generate

ΔPa 0.6 in. water

Other Items 20.0 in. waterSafety Factor 15%

Total Vacuum Required 23.74 in. water


B-9

DR 303M & CP 303MRegenerative BlowerFEATURES• Manufactured in the USA – ISO 9001 compliant• CE compliant – Declaration of Conformity on file• Maximum flow: 55 SCFM• Maximum pressure: 45 IWG• Maximum vacuum: 3.4" Hg (42 IWG)• Standard motor: 0.5 HP, TEFC• Cast aluminum blower housing, impeller

& cover; cast iron flanges (threaded)• UL & CSA approved motor with permanently

sealed ball bearings• Inlet & outlet internal muffling• Quiet operation within OSHA standardsMOTOR OPTIONS• International voltage & frequency (Hz)• Chemical duty, high efficiency, inverter duty

or industry-specific designs• Various horsepowers for application-specific needsBLOWER OPTIONS• Corrosion resistant surface treatments & sealing options• Remote drive (motorless) models• Slip-on or face flanges for application-specific needsACCESSORIES (See Catalog Accessory Section)• Flowmeters reading in SCFM• Filters & moisture separators• Pressure gauges, vacuum gauges & relief valves• Switches – air flow, pressure, vacuum or temperature• External mufflers for additional silencing• Air knives (used on blow-off applications)• Variable frequency drive package

BLOWER PERFORMANCE AT STANDARD CONDITIONSAIR FLOW RATE (M3/MIN)

INC

HE

S O

F W

ATE

R

PS

IG

PRESSURE

AIR FLOW RATE (SCFM)

600500400300200

80604020

MO

TOR

WIN

DIN

GTE

MP

RIS

E °

C

PO

WE

RIN

PU

TW

ATT

S

BLO

WE

RA

IR T

EM

PR

ISE

°C

AIR FLOW RATE (M3/MIN)

3

INC

HE

S O

F W

ATE

R

INC

HE

S O

F M

ER

CU

RY

SUCTION


MO

TOR

WIN

DIN

GTE

MP

RIS

E °

C

PO

WE

RIN

PU

TW

ATT

S

BLO

WE

RA

IR T

EM

PR

ISE

°C

MM

OF

WA

TER

0 10 20 30 40 50

0.5 1.0 1.5 2.0

60 70

750

500

250

1000

2

1

1.5

MM

OF

WA

TER

0 10 20 30 40 50

0.5 1.0 1.5 2.0

60 70

750

500

250

1000

1.0

0.5

6050403020

600500400300200

80604020

6050403020

60 Hz

50 Hz

60 Hz

50 Hz

55

45

35

25

15

5

-55

-45

-35

-25

-15

-5

2.0 41250 1250

Rev. 2/04

SUCTION

60 Hz

50 Hz

0

10

20

30

40

50

0 10 20 30 40 50 60 70


INC

HE

S O

F W

AT

ER

0

200

400

600

800

1000

1200

0 0.5 1 1.5 2

AIR FLOW RATE (m3/MIN)

mm

H2O

AMETEK Technical and Industrial Products, Kent, OH 44240 • e mail: [email protected] • internet: www.ametektmd.com

ROTRON Regenerative Blowers

SectionB 2004.qxd 6/26/04 10:37 AM Page B-9

JPERELLA

Line

JPERELLA

Line

JPERELLA

Text Box

B-300 Tent Vent Blower

Scale CAD drawing available upon request.

Specifications subject to change without notice. Please consult your Local Field Sales Engineer for specification updates.

B-10

DR 303M & CP 303MRegenerative Blower

1 Rotron motors are designed to handle a broad range of world voltages and power supply variations. Our dual voltage 3 phase motors arefactory tested and certified to operate on both: 208-230 /415-460 VAC-3 ph-60 Hz and 190-208/380-415 VAC-3 ph-50 Hz. Our dualvoltage 1 phase motors are factory tested and certified to operate on both: 104-115/208-230 VAC-1 ph-60 Hz and 100-110 /200-220VAC-1 ph-50 Hz. All voltages above can handle a ±10% voltage fluctuation. Special wound motors can be ordered for voltages outside ourcertified range.

2 Maximum operating temperature: Motor winding temperature (winding rise plus ambient) should not exceed 140°C for Class F rated motorsor 120°C for Class B rated motors. Blower outlet air temperature should not exceed 140°C (air temperature rise plus inlet temperature).Performance curve maximum pressure and suction points are based on a 40°C inlet and ambient temperature. Consult factory for inlet orambient temperatures above 40°C.

3 Maximum blower amps corresponds to the performance point at which the motor or blower temperature rise with a 40°C inlet and/orambient temperature reaches the maximum operating temperature.

SPECIFICATIONS

A .68 INCH DIAMETER CONNECTOR HOLE

B CAPACITOR LOCATION ON SINGLE PHASE MOTORS

DIMENSIONS: INMM

TOLERANCES: .XX ± .082

(UNLESS OTHERWISE NOTED)

Same as DR303AE72M –

038842except addChemical

Processing (CP)

features from catalog

inside front cover

MODEL DR303AE9M DR303AE72M DR303AE86M CP303FA91MLRPart No. 038841 038842 038843 080148Motor Enclosure – Shaft Material TEFC – CS TEFC – CS TEFC – CS ChemTEFC – SSHorsepower 0.5 0.5 0.5Voltage 1 115/230 208-230/460 575Phase – Frequency 1 Single - 60 Hz Three - 60 Hz Three - 60 HzInsulation Class 2 F F FNEMA Rated Motor Amps 6.2/3.1 1.3-1.2/0.6 0.6Service Factor 1.25 1.25 1.25Locked Rotor Amps 21/10.5 10-9.2/4.6 4.2Max. Blower Amps 3 6/3 1.63/0.83 0.7Recommended NEMA Starter Size 0/00 00/00 00Shipping Weight 40 lb (18.2 kg) 36 lb (16.3 kg) 35 lb (15.9 kg)

Rev. 2/04

AMETEK Technical and Industrial Products, Kent, OH 44240 • e mail: [email protected] • internet: www.ametektmd.com

ROTRON Regenerative Blowers

SectionB 2004.qxd 6/26/04 10:37 AM Page B-10

JPERELLA

Line

JPERELLA

Line

JPERELLA

Line

JPERELLA

Line

JPERELLA

Text Box

B-300 0.5HP Motor

Tab 8

Modified ISR System – AOP Pre-Treatment System Scrubber Blow-Down System

Page 1 of 1

Calc prepared by: J. DarbyCalc checked by: J. PerellaDate: 2/5/2010

Considerations:

Process flow rate = 15 gpm

Minimum retention time = 60 min

Free board requirement = 1 foot

Height of discharge fitting = 0.75 foot

Calculate Tank Volume:

Retention time volume = Flow rate x Retention time

900 gal

Tank Dimensions:

Selected diameter = 6 feet

Usable volume = 900 gal

Calculated height = 4.3 feet

Freeboard requirement = 1 feet

Height of discharge fitting = 0.75 feet

Required height = 6.0 feet

Selected height = 6.0 feet

Tank Selection:

Vertical Cylindrical Tank Diameter = 6 feet

Height = 6 feet

Volume = 170 ft3

Volume = 1,268 gal

Nominal Volume = 1,200 gal

Scrubber Blow-Down Tank (T-1100) SizingModified ISR System



G:\ENV\TF\901-1000\TF922\Reports\2010\RAPA 2010\Final FDEP RAPA\Appendix J\Tab #8\(1) Scrubber T-1100 Sizing.xlsx ARCADIS

Page 1 of 3

TRANSFER PUMP (P-900) DESIGN CALCULATIONSAOP Pre-Treatment System

Calc prepared by: J. DarbyCalc checked by: J. PerellaDate: 2/5/10

Total dynamic head calculation = head loss due to elevation changehead loss due to pipe frictionhead loss across misc. process componentsrequired discharge head



Flow Rate Pipe Size Pipe OD Wall Thickness Pipe ID Area velocity(gpm) (in) (in) (in) (in) (ft2) (ft/sec)

15 1 1.315 0.133 1.049 0.006 5.4215 1.5 1.900 0.145 1.610 0.014 2.3015 2 2.375 0.154 2.067 0.023 1.39







Flow (v1) = 15 gpm


Flow (v2) = 15 gpm


Hazen-Williams Formula f = .2083 * (100/C)1.852 * (q1.852) / (D4.8655)


(140 for new carbon steel pipe)q = Flow rate (gal/min)D = Inside diameter of pipe (inches)



sec60

min1*

)*( 2r

Qv

G:\ENV\TF\901-1000\TF922\Reports\2010\RAPA 2010\Final FDEP RAPA\Appendix J\Tab #8\(2) P-900 TDH.xlsx ARCADIS

Page 2 of 3




Nominal Diam (in) ID (in)ID w/ deposition

(in)

1 1.003 0.8781.5 1.452 1.3272 1.826 1.7013 2.691 2.5664 3.460 3.3356 5.460 5.335








90˚ Elbows 2.7 3.4 3.6 4.0 4.6 10.4Standard Tee (thru flow) 3.2 5.6 7.7 12.0 17.0 38.3Standard Tee (branch flow) 6.6 9.9 12.0 17.0 21.0 47.3Ball valve (full open) 1.6 2.3 2.9 4.3 5.5 12.3Check Valve - Spring and Swing 11.0 15.0 19.0 27.0 38.0 85.5Union 0.3 0.4 0.5 0.5 0.7 1.5Reducer (2/1) 1.0 1.5 1.5 3.0 4.0 9.0Expansion (1/2) 1.5 2.5 3.0 4.0 6.0 13.5

Equivalent lengths from reference: Civil Engineering Reference Manual, 9th Ed, Professional Publications, Inc., 2003; and"Flow of Fluids", Crane Technical Paper No. 410, 1988.

Pipe Section 1 - 1.5" - pump discharge to LPGAC

Item Qty. L (ft) Qty * LLinear Pipe (L1) 1 20 20

Standard Tee (thru flow) 2 3.2 6Standard Tee (branch flow) 0 6.6 0Union 4 0.3 1.290˚ Elbows 8 2.7 21.6Check Valve - Swing 1 11 11Expansion (1.5 x 1) 2 1.5 3.0Ball valve (full open) 4 1.6 6



Equivalent Length


Page 3 of 3




Pipe Section 2 - 2" - LPGAC, pump discharge to south end of Building E, tie-in to Mod. ISR discharge

Item Qty. L (ft) Qty * LLinear Pipe (L1) 1 2,500 2,000

Union 4 0.5 2.090˚ Elbows 8 3.6 28.8Check Valve - Swing 0 19 0



Total pipe friction = Total equivalent length x Friction factor

Total Pipe Friction - Pipe Section 1Total equivalent length = 70 feet

Friction factor = 4.2 feet water / 100 feet of pipe


Total Pipe Friction - Pipe Section 2Total equivalent length = 2,031 feet




Total Pipe Friction - Pipe Section 1+2 = 28.7




Head loss Across Misc. Process Components LPGAC-1 35 ft 1 psi = 2.31 ftLPGAC-2 23 ft

Flow Meter 12 ft







Equivalent Length


1 NPT

D1

D2

L3

L1

L2

2

65⁄16

3⁄8 DRAIN

3⁄8FILL VENT

3⁄82 HOLES

3⁄4

M1

71⁄16 85⁄16

315⁄16

57⁄8

M2

1⁄24 HOLES

CAPACITORCOVER ONSINGLE PHASEONLY

7⁄8

TECHNICAL MANUAL

SSV Series VerticalMulti-StagePumps

G&LSeriesSSV

300 LB. FLANGE

4

General Characteristics2-pole

SSV Product Range 1SV 2SV 3SV 4SV 33SV 46SV 66SV 92SV Nominal Flow (GPM) 15 30 60 85 150 220 350 450 Flow Range (GPM) 2 – 22 6 – 40 11 – 75 17 – 110 30 – 195 45 – 285 70 – 420 90 – 580 Max. Head (Ft) 1100 945 1005 930 1125 1210 850 715 Max. Working Pressure (PSI) 2 360 PSIG 1 360 / 580 PSIG Temperature Range -20ºF to 250ºF (-30ºC to -121ºC) Motor Power (HP) ½ – 5 HP ¾ – 5 HP 2 – 15 HP 5 – 20 HP 3 – 60 HP 7½ – 75 HP 10 – 75 HP 15 – 75 HP Max. Pump Efficiency 44% 58% 64% 67% 76% 78% 78% 80% Material of Construction SVA AISI 304SS – – – – SVB AISI 304SS Cast Iron / AISI 316L SVC AISI 304SS – – – – SVD AISI 316LSS Cast Stainless Steel / AISI 316L Connection Sizes

SVA – Oval NPT 1" NPT 1¼" NPT 1½" NPT

–

– – – –

(female) (female) (female) SVB – Round ANSI 1¼" 1¼" 2" 2" 2½" 3" 4" 4" Size/Class 300# 300# 300# 300# 125/250# 1325/250# 125/250# 125/250# SVC – Top/Bottom Round 1¼" 1¼" 2" 2"

– – – –

ANSI – Size/Class 300# 300# 300# 300# SVD – Round ANSI 1¼" 1¼" 2" 2" 2½" 3" 4" 4" Size/Class 300# 300# 300# 300# 150/300# 150/300# 150/200# 150/300# Optional Connections (on request)

Victaulic (PJE) 1¼" 1¼" 2" 2"

– – – –

(Victaulic) (Victaulic) (Victaulic) (Victaulic)

1 Some staging may have MAWP of 580 psi (40 bar). 2 See pages 53-60 for specific details.

SVA1SV, 2SV, 3SV

SVB, SVD1SV, 2SV, 3SV, 4SV

SVC1SV, 2SV, 3SV, 4SV

VICTAULIC1SV, 2SV, 3SV, 4SV

SVB, SVD33SV, 46SV, 66SV, 92SV

6

SSV Product Line Numbering System for 1 – 4SV

The various versions of the SSV line are identified by a product code number on the pump label. This number is also the catalog number for the pump. The meaning of each digit in the product code number is shown below.Note: Not all combinations are possible. Consult your G&L distributor.

Example Product Code2 SV A 1 D 2 B 1 H

Options: H = Horizontal mount, refer to back cover VIC = Victaulic connections (1SVB/D – 4SVB/D only)

Mechanical Seal Options:

Number of Stages: B = 2 D = 4 F = 6 H = 8 K = 10 M = 12 P = 14 R = 16 V = 20 Z = 24 C = 3 E = 5 G = 7 J = 9 L = 11 N = 13 Q = 15 T = 18 X = 22

Driver: (50 Hz, no single phase number 0, 1, 4) 1 = 1 PH, ODP 3 = 575V, ODP 5 = 3 PH, TEFC 7 = 3 PH, XP 9 = 3 PH, TEFC with premium efficiency 2 = 3 PH, ODP 4 = 1 PH, TEFC 6 = 575V, TEFC 8 = 575V, XP 0 = 1 PH, XP

HP Rating: C = 1⁄2 E = 1 G = 2 J = 5 L = 10 N = 20 D = 3⁄4 F = 11⁄2 H = 3 K = 71⁄2 M = 15 P = 25

Hertz/RPM: 1 = 60 Hz, 3500 RPM 3 = 60 Hz, 3500 RPM, 380 V 5 = 60 Hz, 3500 RPM, 220-380 V, D.O.L. 2 = 50 Hz, 2900 RPM, 190-380 V, (50 Hz motor) 4 = 50 Hz, 2900 RPM, 460 V 6 = 60 Hz, 3500 RPM, 380 V, Y-DELTA 7 = 60 Hz, 1750 RPM, 208-230, 460 V

Material and Suction/Discharge: A = 304 stainless steel, in-line NPT threaded oval flange connections (1, 2, 3 only) B = 304 stainless steel, in-line ANSI flange (1, 2, 3, 4SV) C = 304 stainless steel, top/bottom ANSI flange connections D = 316 stainless steel, in-line ANSI flange

Product Line: Stainless Vertical

Nominal Flow: 1 = 15 GPM 2 = 28 GPM 3 = 55 GPM 4 = 86 GPM

Code No. Rotary Stationary Elastomer Reference Application 0 High Temp. General Carbon Silicon Viton Service 4 Silicon Carbide Carbide Graphite Filled Graphite 6 High Temp. Filled EPR Boiler Feed Carbon

Abrasive

Rating Plate 1, 2, 3 and 4SV

G&L PumpsSSV™

CATALOG NUMBER

GPM FEET RPM

DO NOT OPERATE AT CLOSED DISCHARGE

Goulds Pumps, ITT Industries, Inc. 8

2

5

3

7

4

1

6

1 Goulds Catalog Number 2 Capacity Range 3 TDH Range 4 Rated Speed 5 Rated Horsepower 6 Maximum Operating Pressure 7 Maximum Operating Temperature 8 Pump Serial Number

JPERELLA

Text Box

PUMP MODEL: 1SVD1FSD1H

19

1SV Curve 3500 RPM

0

100

200

300

400

500

600

700

0 10 15 25 US GPM

FEET

TOTA

L D

YNA

MIC

HEA

D

CAPACITY

30

40

50

EFF

%

1100

1SV 60 Hz3500 RPM

0

0.5

HP/

STA

GE

0 5 m3/h

0

50

100

150

200

250

300

350

METERS

1000

800

900

0

8

12

20

4321

10

6

kW/S

TAG

E

0

.30

.20

.10

5

4

2

0.25

NPS

Hr

0

2

3

1

(m) (ft)

2 – 16 STAGES

18 – 22 STAGES*

* For vertical shaft installation only.

22 STAGE

20 STAGE

18 STAGE

16 STAGE

13 STAGE

11 STAGE

9 STAGE

8 STAGE

7 STAGE

6 STAGE

5 STAGE

4 STAGE

3 STAGE

2 STAGE

Eff.

BHP

15 STAGE

JPERELLA

Line

JPERELLA

Line

JPERELLA

Line

JPERELLA

Text Box

0.33 HP/Stage => 1.32HP use 1.5HP motor

JPERELLA

Text Box

126' TDH

JPERELLA

Rectangle

JPERELLA

Text Box

PUMP MODEL: 1SVD1FSD1H

CWorden

Typewritten Text

Your Mobile Water Treatment Specialists

7500 Boone Ave N, Suite 101, Brooklyn Park, MN 55428 Ph: 800-526-4999 Fax: 763-315-4614 www.carbonair.com Customer: ARCADIS, Tampa, FL Site: Unknown Date: 2/5/10 Design Basis: Water flow rate: 15 gpm Water temperature: 120 oF (from wet scrubber) Critical contaminant: TCE Influent concentration: 50 ppb Effluent criteria: < 1 ppb (assumed for ND) Water Quality: Chloride 1,700-12,000 ppm Recommendations: Liquid Phase Carbon Adsorbers Two FRP PC3 vessels in series, each with 250 lbs of carbon

The FRP vessels are recommended in order to avoid corrosion due to the high chloride. The lead and lag vessels are predicted to last 30 and 120 days, respectively. Recommend

changing out the lead vessel every 90 days. Note:

Chloride will not be effectively adsorbed by carbon and will have no adverse effect on the adsorption of non-polar organic compounds such as TCE. The high water temperature of 120 oF will increase the solubility of TCE in water and consequently will reduce the adsorbability of TCE onto carbon.

CONFIDENTIALITY NOTICE: Reproduction, disclosure, or distribution of any parts of this document is strictly prohibited without a written approval from Carbonair.

LIQUID-PHASE CARBON ADSORPTION MODEL CALCULATIONS

CARBONAIR ENVIRONMENTAL SYSTEMS

7500 BOONE AVENUE NORTH, SUITE 101

BROOKLYN PARK, MN 55428

PHONE: 800-526-4999

FAX: 763-315-4614

CARBON ADSORBERS: PC3

NO OF ADSORBERS IN SERIES: 1

TOTAL MASS OF CARBON (LBS): 250.00

FLOW RATE (GPM): 15.000

HYDRAULIC LOADING (GPM/SQ.FT): 6.3159

EMPTY BED CONTACT TIME (MIN.): 4.5435

DESIGN COMPOUND: TCE (120 F)

EXPECTED INFLUENT CONCENTRATION (PPB): 50.000

MODEL INFLUENT CONCENTRATION (PPB): 50.000

EFFLUENT CRITERIA (PPB): 1.0000

EFFECTIVE K-VALUE (%): 50.000

TIME(DAYS) VOLUME TREATED(GAL) EFF. CONC.(PPB)

5.0 108000. 0.0000

10.0 216000. 0.0000

15.0 324000. 0.0225

20.0 432000. 0.0759

25.0 540000. 0.2277

30.0 648000. 0.6064 BREAKTHROUGH

35.0 756000. 1.4180

40.0 864000. 2.8386

45.0 972000. 4.8516

50.0 1080000. 7.2420

55.0 1188000. 9.7850

60.0 1296000. 12.3006

65.0 1404000. 14.7117

70.0 1512000. 16.9811

75.0 1620000. 19.0984

80.0 1728000. 21.0658

85.0 1836000. 22.8937

90.0 1944000. 24.5925

95.0 2052000. 26.1721

100.0 2160000. 27.6421

105.0 2268000. 29.0125

110.0 2376000. 30.2933

115.0 2484000. 31.4906

120.0 2592000. 32.6117

Note: The model influent concentration results from the

impact of the other background compounds, which is

determined by using a competitive adsorption model

DISCLAIMER: ACTUAL RESULTS MAY VARY SIGNIFICANTLY FROM

THE MODEL. THE MODEL IS BASED ON THE ASSUMPTIONS THAT

THE FLOW RATE AND INFLUENT CONCENTRATION ARE CONSTANT,

AND ONLY THE CONTAMINANTS PROVIDED TO CARBONAIR ARE

PRESENT IN THE WATER. VARYING OPERATING CONDITIONS CAN

HAVE ADVERSE EFFECTS ON CARBON ADSORPTIVE CAPACITY.

THE PREDICTED BED LIFE IS NOT GUARANTEED.

LIQUID-PHASE CARBON ADSORPTION MODEL CALCULATIONS

CARBONAIR ENVIRONMENTAL SYSTEMS

7500 BOONE AVENUE NORTH, SUITE 101

BROOKLYN PARK, MN 55428

PHONE: 800-526-4999

FAX: 763-315-4614

CARBON ADSORBERS: PC3

NO OF ADSORBERS IN SERIES: 2

TOTAL MASS OF CARBON (LBS): 500.00

FLOW RATE (GPM): 15.000

HYDRAULIC LOADING (GPM/SQ.FT): 6.3159

EMPTY BED CONTACT TIME (MIN.): 9.0869

DESIGN COMPOUND: TCE (120 F)

EXPECTED INFLUENT CONCENTRATION (PPB): 50.000

MODEL INFLUENT CONCENTRATION (PPB): 50.000

EFFLUENT CRITERIA (PPB): 1.0000

EFFECTIVE K-VALUE (%): 50.000

TIME(DAYS) VOLUME TREATED(GAL) EFF. CONC.(PPB)

10.0 216000. 0.0000

20.0 432000. 0.0000

30.0 648000. 0.0000

40.0 864000. 0.0000

50.0 1080000. 0.0000

60.0 1296000. 0.0000

70.0 1512000. 0.0000

80.0 1728000. 0.0000

90.0 1944000. 0.0140

100.0 2160000. 0.0656

110.0 2376000. 0.2458

120.0 2592000. 0.8576 BREAKTHROUGH

130.0 2808000. 2.3719

140.0 3024000. 4.9095

150.0 3240000. 8.0677

160.0 3456000. 11.4139

170.0 3672000. 14.7078

180.0 3888000. 17.8383

190.0 4104000. 20.7704

200.0 4320000. 23.4838

210.0 4536000. 25.9837

220.0 4752000. 28.2780

230.0 4968000. 30.3755

240.0 5184000. 32.2903

Note: The model influent concentration results from the

impact of the other background compounds, which is

determined by using a competitive adsorption model

DISCLAIMER: ACTUAL RESULTS MAY VARY SIGNIFICANTLY FROM

THE MODEL. THE MODEL IS BASED ON THE ASSUMPTIONS THAT

THE FLOW RATE AND INFLUENT CONCENTRATION ARE CONSTANT,

AND ONLY THE CONTAMINANTS PROVIDED TO CARBONAIR ARE

PRESENT IN THE WATER. VARYING OPERATING CONDITIONS CAN

HAVE ADVERSE EFFECTS ON CARBON ADSORPTIVE CAPACITY.

THE PREDICTED BED LIFE IS NOT GUARANTEED.

Pressure Drop for PC 3F

0.00.51.01.52.02.53.03.54.04.5

0 2 4 6 8 10 12 14 16 18 20

Flow Rate (gpm)

Pres

sure

Dro

p (p

si)

Tab 9

Modified ISR System – AOP Treatment System Sodium Sulfite Contactor System

©MMVI NORWECO, INC.

220 REPUBLIC STREETNORWALK, OHIO, USA 44857-1156TELEPHONE (419) 668-4471FAX (419) 663-5440www.norweco.com

PROGRESS THROUGH SERVICE SINCE 1906

BIO-MAX® DECHLORINATION TABLETS

SPECIFICATIONSTablet Size 2 5/8" diameter,

1" thickApprox. Tablet Weight 5 oz. (140 grams)Active Ingredient Sodium Sulfite

( Na2SO3 )Active Ingredient 92%Inert Ingredients 8%Appearance and odor Blue-green tablet with

herbal odorD.O.T. Designation Non-Hazardous

GENERAL INFORMATIONBio-Max dechlorination tablets provide a convenient to usesource of concentrated sodium sulfite to instantly removechlorine from wastewater, potable water and process water.Containing 92% sodium sulfite and 8% inert ingredients,Bio-Max dechlorination tablets assist plant operators inmeeting stringent chlorine discharge limitations in a low cost,low maintenance, environmentally safe manner. Formulatedfor use in all major gravity or pressure rated tablet feeders,several patent pending inert compounds are blended intoBio-Max tablets during production. These compounds havea synergistic effect with the sulfite, resulting in a tablet withexceptional integrity and a precisely regulated dissolve rate.

A single chemical feed tube filled with 21 Bio-Max tabletswill remove 1 ppm chlorine from over 400,000 gallons of wateror wastewater without affecting dissolved oxygen levels orreleasing irritating and potentially dangerous treatmentchemicals into the environment. For a 15,000 GPD water orwastewater facility, this means up to 26 days of treatmentbefore new tablets must be loaded into the feed tubes. Alsoideal for periodic flows typical of USEPA storm watercompliance related activities, Bio-Max dechlorination tabletsare not affected by long periods of no flow conditions andcan be repeatedly immersed in water and dried down withno loss of integrity or performance.

Pound for pound, Bio-Max dechlorination tablets are 30%more effective in removing chlorine than ascorbic acid tabletsor slurries. This means less chemical consumption, lessmaintenance and of course, reduced operating costs for aslong as you operate your system. Available in 48 lb.resealable pails, Norweco’s Bio-Max tablets offer plantowners and operators the best way to meet stringent chlorinedischarge requirements.

ADVANTAGES92% concentrated sodium sulfiteCompletely eliminates both free and combined chlorineFor use in all types of tablet feedersCost effective treatment for high flow systemsNo effect on dissolved oxygen or pHVery low maintenance requiredNo mixing of chemicals or solutions

Bio-Max dechlorination tablets are available from your localNorweco dealer or distributor in conveniently packaged, childresistant 48 lb. resealable polyethylene pails with a whitebase and a blue-green lid.

CAUTIONBio-Max dechlorination tablets are a strongreducing agent containing sodium sulfite. Directcontact with most oxidizing agents such asBio-Sanitizer disinfecting tablets, swimmingpool tablets or any other chlorine containingcompound is extremely dangerous. Water orwastewater being treated with Bio-Maxdechlorination tablets should be at or near aneutral pH. If water or wastewater has anavailable chlorine level greater than 20 ppm ora water temperature greater than 100° F, donot use any mixture containing sodium sulfiteor other reducing agents. A reaction may occurwhich could generate heat and chlorine gas.Care must be taken in the handling and storageof Bio-Max tablets. Store only in sealed originalcontainer and in a well-ventilated area. Readthe product container label carefully prior to use.Keep out of the reach of children. This productshould not be used to treat water intended forhuman consumption.

DISTRIBUTED LOCALLY BY:

DECHLORINATION TABLETS

GENERAL SPECIFICATIONSBio-Max dechlorination tablets shall be formulated to serve as a source of concentrated sodium sulfite for the removal of chlorinein water, wastewater and process water. The slow and consistent release of concentrated sodium sulfite from Bio-Max tabletsshall allow their use in a variety of applications such as meeting National Pollution Discharge Elimination System (NPDES)criteria, and phase two storm water discharge requirements. The tablets shall be 2 5/8" diameter, 1" in thickness with anapproximate weight of 140 grams. Proprietary beveled edges incorporated into the tablets will stabilize the slow release ofsodium sulfite. Bio-Max dechlorination tablets shall contain a minimum of 92% sodium sulfite as an active ingredient and 8%patent pending inert ingredients. Ascorbic acid tablets or liquid sodium metabisulfite systems require the mixing of irritatingchemicals into a pumpable slurry which exposes operators to potentially hazardous conditions and shall not be considered forthis application.

TABLET PROPERTIES AND USAGEBio-Max dechlorination tablets shall release sodium sulfite in direct correlation to the velocity of the incoming flow. This shallallow design engineers and system operators to precisely regulate the sulfite dose, and in turn, the dechlorination process formaximum effectiveness and minimum operating cost. Patent pending inert ingredients added to Bio-Max tablets shall maintainthis predictable chemical dose at intermittent peak flow factors as high as four, and shall provide reliable elimination of chlorineeven when the significant runoff period is six hours. Bio-Max tablets shall be an ideal product for municipal storm watertreatment which requires treatment capacity for high or pressurized flow and then an extended time of no flow conditions. Byincorporating commercial feeders such as Norweco’s Bio-Dynamic tablet feeders, or constructing custom units, the consistentdosage of Bio-Max tablets will allow effective and controlled dechlorination for a wide variety of applications.

PRODUCT APPLICATIONBio-Max dechlorination tablets shall be incorporated into the treatment process following the chlorine contact tank or finaltankage. As Bio-Max tablets stop the disinfection process by eliminating chlorine, no bacterial sampling shall be performed onthe effluent or water stream following the addition of Bio-Max tablets. The dechlorination system can be designed so the entireflow needing dechlorination contacts the Bio-Max tablets or in a bypass arrangement where a percentage of flow is directed atthe tablets, is saturated with the sulfite, and then blended into the remainder of the flow. While the cost effective performanceof Bio-Max tablets is optimized with Norweco’s Bio-Dynamic tablet feeders in gravity flow applications, the tablets can provideexceptional dechlorination with field constructed feed systems or in conjunction with the various brands of pressure typefeeders. Check your feeder’s operating manual for further details.

DESIGN DATATablet Size 25/8" diameter, 1" thick Inert Ingredient Content 8%Approximate Tablet Weight 5 oz. (140 grams) U.S. DOT Hazard Class Non-hazardousActive Ingredient Sodium Sulfite – Na

2SO

3Appearance Characteristics Blue-Green Tablet with Herbal Odor

Active Ingredient Content 92% Special Design Features Beveled Edges

PRODUCT DOSAGEUnder gravity flow conditions, the sulfite dose from Bio-Max tablets shall be 6.75 mg/L at 70° F. Significant variations intemperature or flow velocity may have an impact on tablet dose. Adjustment of dosing equipment will be required upon start-up.Chlorine residuals prior to dechlorination fluctuate based on upstream treatment processes and conditions. Monitoring ofchlorine residual levels prior to dechlorination is recommended to insure consistent performance of the dechlorination system.Once steady performance of the upstream treatment process and dechlorination system is established only minor adjustmentsof the feeder shall be required. A single feed tube of Bio-Max dechlorination tablets shall remove up to 3.8 mg/L availablechlorine, with no excess sodium sulfite. To estimate average tablet usage, multiply plant flow in liters (l) per day by 6.75 mg/L,then divide this product by 1,000 and again by 140. The final result will be the number of Bio-Max dechlorination tablets used perday of operation. Consult your tablet feeder’s operational manual for further information.

PRODUCT STORAGEBio-Max dechlorination tablets are a strong reducing agent. Tablets should be stored in a cool, dry, well-ventilated area, awayfrom heat or flame. Avoid storage in areas subject to direct sunlight or temperatures in excess of 140° F. Stock should berotated on a first-in, first-out basis. Bio-Max dechlorination tablets must be stored in their original container with the lid tightlyclosed. Do not allow moisture to enter the pail during storage or while removing tablets for use. Moisture contamination mayaffect tablet integrity and performance. Do not reuse the empty container.

SAFETY INSTRUCTIONSBefore handling Bio-Max tablets, carefully read the container label and the Product Storage, Tablet Handling, Caution and FirstAid sections of these instructions. Do not add Bio-Max tablets to a feed tube containing any other product, particularly oil andpetroleum products or swimming pool chlorine. Such action may cause a violent reaction leading to fire or explosion. Do notcontaminate food or feed during the use, storage or disposal of Bio-Max tablets or the cleaning of chemical feed equipment.Always wear rubber gloves and either safety goggles or a face shield when handling Bio-Max tablets or working with any tabletfeeder or feed tube. Avoid contact with skin, eyes, mouth, respiratory system or clothing. Keep this product only in its tightlyclosed original container. Store only in a cool, dry, well-ventilated area.

TABLET HANDLINGUse only clean, dry utensils. Do not add Bio-Max dechlorination tablets to any device containing remnants of any other product– contact with oxidizers, such as Bio-Sanitizer disinfecting tablets or any other tablets used for chlorination can cause fire andthe release of toxic gas. Read the entire Bio-Max tablet container label and these instructions carefully before handling thisproduct. Use only in well-ventilated areas. Bio-Max tablets are not rated a hazardous substance by the U.S. DOT or USEPA,but necessary care should be taken in the use and handling of the tablets. Collected material can be dissolved in water,exercising caution as the solution can get hot. Dispose of dissolved material in any appropriate industrial waste collectionsystem. Consult local, state and federal regulatory agencies before disposing of any material.

FEED TUBE LOADING INSTRUCTIONS1. Remove feed tube from dispenser housing.2. Remove protective cap from feed tube; place cap in a clean, dry area.3. Remove any tablet residue by gently tapping feed tube on concrete or stone

surface. If tablets other than Bio-Max have been used, rinse tube and capwith fresh water until clean and allow to dry before proceeding.

4. Hold tube, slotted end up, at a 45° angle and slide Bio-Max dechlorinationtablets into the tube, one tablet at a time.

5. Ensure that all tablets lie flat, on top of one another, in the feed tube.6. Use your gloved hand to retain tablets inside the open end of the inverted

tube while filling.7. Carefully return tube to upright position.8. Replace the cap securely.9. Place tube back into housing, slotted end down.10. Be sure feed tube is fully engaged and rests evenly on the floor of the housing.11. If the tablet feeder incorporates multiple feed tubes, consult the manufacturer’s instructions to determine the correct

number of tubes to be filled and their placement.

CAUTIONDo not mix Bio-Max dechlorination tablets with acids or oxidizing agents such as Bio-Sanitizer disinfecting tablets or othertablets used for chlorination – fire or explosion could result. Keep out of the reach of children. Avoid contact with skin, eyes,mouth, respiratory system or clothing – failure to do so may cause irritation on contact. Wear rubber gloves and either safetygoggles or a face shield when handling this product. Product will form Sodium Sulfide at 600° C. At 900° C Sulfur Dioxide isformed. Inert ingredients could support combustion. Use self-contained breathing apparatus for fire fighting.

FIRST AID INSTRUCTIONSIf contact with skin occurs, wash with water for 15 minutes. If irritation persists, seek medical attention.If eye contact occurs, flush with water for at least 15 minutes. Get immediate medical treatment.If swallowed, promptly drink large quantities of water or milk. Induce vomiting. Avoid alcohol. Call physician immediately.If inhaled, move victim to fresh air. If difficulty in breathing persists, get immediate medical attention.In case of fire, immediately evacuate the area and notify the fire department.

MATERIAL SAFETY DATA SHEET EMERGENCY TELEPHONE: (800) 424-9300

BIO-MAX® DECHLORINATION TABLETS DATE PREPARED: JANUARY 2009

NOTE: THIS PRODUCT IS NOT RATED A HAZARDOUS MATERIAL BY THE U.S. DEPARTMENT OF TRANSPORTATION OR THE U.S.ENVIRONMENTAL PROTECTION AGENCY. THE FOLLOWING DATA IS FOR INFORMATIONAL PURPOSES ONLY.

I. PRODUCT IDENTIFICATION

TRADE NAME Bio-Max®CHEMICAL Sodium SulfiteCHEMICAL ABSTRACT SYSTEM NO. CAS #7757-83-7CHEMICAL DESCRIPTION ReducerFORMULA Na

2SO

3

U.S. DOT SHIPPING NAME Non-Hazardous Tablets, Item NM503401U.S. DOT HAZARD CLASS Non-Hazardous

II. INGREDIENTS

HAZARDOUS INGREDIENTS NoneNON-HAZARDOUS INGREDIENTS Sodium Sulfite 92%

Inert Ingredients 8% (Includes sustained release agents)

III. PHYSICAL DATA

BOILING POINT AT 760 mm Hg Decomposes at 900° CFREEZING/MELTING POINT Not ApplicableSOLUBILITY IN H

2O; % BY WEIGHT 25% at 80° C

SPECIFIC GRAVITY OF TABLET 2.63 (H2O = 1)

APPROXIMATE TABLET DENSITY 125 lbs./ft3

pH OF SOLUTION AlkalineVOLUME % VOLATILE Not ApplicableAPPEARANCE AND ODOR Blue-Green Tablet with Mild Odor

IV. FIRE AND EXPLOSION DATA

FLASH POINT Not ApplicableFLAMMABLE LIMITS IN AIR Not ApplicableEXTINGUISHING MEDIA Use extinguishing media appropriate for burning material. Compatible with water fog, spray foam or CO

2.

SPECIAL FIRE FIGHTING PROCEDURES NIOSH/MSHA-Approved, positive pressure, self-contained breathing apparatus with full face piece.UNUSUAL FIRE & EXPLOSION HAZARD At 600° C, Sodium Sulfide is formed. At 900° C, Sulfur Dioxide is formed. Inert ingredients could support combustion by burning,

yielding carbon dioxide and water. Use self-contained breathing apparatus for fire fighting.

V. HEALTH HAZARD DATA

ACUTE TOXICITY DATA (ANIMAL)LC 50 INHALATION See effects of overexposure.LD 50 ORAL 2825 MG/KG (Rabbit)LD 50 DERMAL See effects of overexposure.LC 50 AQUATIC Very high concentrations will chemically deplete dissolved oxygen necessary for aquatic life.

CHRONIC TOXICITY Sodium Sulfite may cause allergic reactions in sensitive individuals. Contact with strong acids or high temperatures maygenerate Sulfur Dioxide, which is toxic, corrosive, and hazardous.

VI. EFFECTS OF OVEREXPOSURE

PERMISSIBLE No permissible exposure limits have been established by OSHA.ACUTE

INHALATION Inhalation of product dust or solution may cause respiratory tract irritation.EYE Dust or solution may burn eyes on contact.SKIN Product dust or solution may result in skin irritation upon prolonged contact.INGESTION Ingestion may irritate gastrointestinal tract. Toxic if taken in large doses.

VII. EMERGENCY AND FIRST AID PROCEDURES

INHALATION Remove to fresh air. If not breathing, resuscitate and administer oxygen if readily available. Seek medical attention immediately.EYE CONTACT Immediately flush with large amounts of water for fifteen (15) minutes, rinsing eye thoroughly. Get medical attention.SKIN CONTACT Wash with plenty of soap and water for fifteen (15) minutes. Remove contaminated clothing. If skin irritation occurs, get medical attention. Wash

clothing before reuse.INGESTION If conscious, drink large quantities of water or milk and induce vomiting. Call a physician immediately. Avoid alcohol.

If unconscious, or in convulsions, seek medical attention immediately. Do not give anything by mouth to an unconscious person.

VIII. STEPS FOR MATERIAL SPILL

Spills exceeding 100 pounds should be reported to the local authorities.1. Contain all spilled material, wearing appropriate protective equipment.2. Place spilled material in clean, dry containers for disposal. Do not flush to surface water.

WASTE DISPOSAL METHODNot rated a hazardous substance by USEPA. Collected material can be dissolved in water, exercising caution. Dissolved material may be discharged into an appropriateindustrial waste collection system but consult local, state, and federal regulating agencies before disposing of any material.

IX. SPECIAL PROTECTION INFORMATION

RESPIRATORY PROTECTION If dusty conditions are encountered, use NIOSH/MSHA respirator with acid gas cartridge and dust pre-filter.VENTILATION Store and use in a well-ventilated area.EYE PROTECTION Chemical safety goggles.GLOVES Natural or synthetic rubber.OTHER PROTECTIVE EQUIPMENT Boots, aprons, or chemical suits as required to prevent skin contact.

THIS MATERIAL SAFETY DATA SHEET IS OFFERED SOLELY FOR YOUR INFORMATION, CONSIDERATION AND INVESTIGATION. NORWALK WASTEWATER EQUIPMENT COMPANY PROVIDES NOREPRESENTATIONS OR WARRANTIES, EITHER EXPRESSED OR IMPLIED, AND ASSUMES NO RESPONSIBILITY FOR THE ACCURACY OR COMPLETENESS OF THE DATA CONTAINED HEREIN.

220 REPUBLIC STREETNORWALK, OHIO, USA 44857-1156TELEPHONE (419) 668-4471FAX (419) 663-5440www.norweco.com

DISTRIBUTED LOCALLY BY:

Norweco®, Norweco.com®, Singulair®, Modulair®, Travalair®, Lift-Rail®, Microsonic®, Bio-Dynamic®, Bio-Sanitizer®, Bio-Neutralizer®, Bio-Kinetic®,Bio-Static®, Bio-Gem®, Bio-Regeneration®, Bio-Perc®, Blue Crystal®, ClearCheck®, ChemCheck®, Service Pro®, Grease Buster® and “BUSTER”logo® are registered trademarks of Norwalk Wastewater Equipment Company, Inc.

©MMVI NORWECO, INC.

ADDITIONAL CHEMICAL PRODUCTS FROM NORWECO

BIO-DYNAMIC® TABLET FEEDERSBio-Dynamic tablet feeders are a technological advancement in self-contained dry chemical dosing systems for the treatment ofwater or wastewater. A low cost, low maintenance and extremely effective method of chemical treatment, Bio-Dynamic feeders

have no mechanical components and require no electricity. The safety, accuracyand reliability provided by Bio-Dynamic feeders outperform gas, liquid and ultravioletsystems. With fourteen different models, Bio-Dynamic feeders have multipleinstallation options that provide maximum flexibility, including direct burial, in-lineand contact chamber mounting. Riser assemblies are available to eliminate theneed for a manhole or separate enclosure during direct burial installations. Fullyserviceable from finished grade, riser assemblies eliminate the need for confinedspace entry equipment required by OSHA regulations. Direct burial models includetrim lines that allow height adjustment on site for each installation. Molded inletand outlet hubs allow the Bio-Dynamic feeder to be directly connected to treatmentsystem piping without the need for a separate drop box. The tiered flow deck ofthe Bio-Dynamic feeder accommodates variable, intermittent and surge hydraulicflows into the system. The flow deck directs liquid to the feed tubes during lowflows and disperses liquid velocity throughout the feeder during peak flows, resultingin consistent chemical application. Chemical dosage is further controlled byinterchangeable weir plates or an optional sluice that can be completely adjustedfrom a 1" to 3" outlet width. The sluice can be adjusted during tablet feederoperation using only a standard socket wrench with extension. All models are

backed by a ten year limited warranty. Standard components include one-piece feed tubes with twist lock caps, adjustable inletbaffle, molded inlet and outlet hubs, molded mounting feet and interchangeable outlet weir plates.

BIO-LOGICAL® DISINFECTING TABLETSBio-Logical disinfecting tablets are a new type of biocide formulated exclusively for low flow water and wastewater disinfection.This patent pending blend of isocyanurates and buffering agents quickly eliminate bacteria without the use of concentratedoxidizing chemicals. Safe and effective to use in all dry tablet feeders, Bio-Logical tablets are not considered an oxidizer underUnited States Department of Transportation or International Marine Standards. This allows for quick and economical shipmentof product direct to your customers anywhere in the world. Bio-Logical disinfecting tablets are ideal for use with potable watersystems, cisterns, individual home aerobic treatment systems, commercial wastewater treatment systems, sand filters andMarine Sanitation Devices. Bio-Logical tablets are available in 6-tablet bags and 5 lb., 35 lb. and 90 lb. resealable pails.

BIO-GEM® ORGANIC DIGESTERA blend of bacteria, enzymes and natural growth accelerators, Bio-Gem organic digester effectively digests grease, fats andoils in wastewater treatment systems, lift stations, septic tanks, sand filters, drain lines and commercial grease traps. Whenused as directed, Bio-Gem liquid will quickly and effectively convert common grease, fats and oils into carbon dioxide andwater. This organic digestion process is much more effective and reliable than compounds that merely emulsify the grease,fats and oils, sending the problem to downstream treatment processes. Regular use of Bio-Gem liquid will reduce odors,stabilize effluent quality, reduce system maintenance and minimize tank pump-out frequency. Packaged in one or five galloncontainers and 55 gallon drums, Bio-Gem organic digester is environmentally safe and works in aerobic or anaerobic conditions.

Page:

1/5

MEMO

To:

Joe DarbyCopies:

David Liles

From:

Todd Thornton

Date: ARCADIS Project No.:

February 15, 2010 TF000922.0048.00001

Subject:

Raytheon Permanganate-Sulfite Lab Study Results

Background

This lab project was intended to test the theoretical molar relationship in the oxidation-reduction (redox) reaction between permanganate and sulfite. The theoretical redox reaction is shown below.

2MnO4- + 3SO3

2- → 2MnO2 + 3SO42- + 2OH-

The spectator cations are not shown in the equation since they have no influence on the redox reaction. From the balanced redox reaction above, the molar relationship between permanganate and sulfite is 2:3.

In addition to validating the molar relationship between sulfite and permanganate, a series of non-quantitative additions of sulfite was tested to examine the residual permanganate concentrations. Theoretically, the purple color imparted by the permanganate in solution will lighten and eventually turn clear upon sufficient addition of sulfite to reduce the Mn(VII). Insufficient additions of sulfite should reduce the permanganate concentration and thereby only lighten the color of the solution. The change in concentration can be measured using visible spectroscopy and Beer’s law which related absorbance of visible light to the concentration of the analyte (A = εBC, where A = absorbance, ε = molar absorbtivity, B = cell path length, C = concentration).

ARCADIS G&M of North Carolina, Inc.

4915 Prospectus Drive

Suite F

Durham

North Carolina 27713

Tel 919.544.4535

Fax 919.544.5690

ARCADIS, Inc.

Page:

2/5

Experimental

A stock 1000 mg/L sodium permanganate solution was prepared by diluting 2.5 g 40% sodium permanganate solution to 1000 mL using deionized water. The concentration of the stock solution was verified using the NaMnO4 standardization in method 4500-KMnO4 from Standard Methods for the Examination of Water and Wastewater. Using the stock solution, five solutions of varying concentration were created by dilution with deionized water. These solutions were then analyzed by visible spectroscopy to create a calibration curve for future permanganate measurements.

A 100 mL sample of the stock permanganate solution was taken and to it 104 mg of received sodium metabisulfite was added directly. After mixing, there was no visible change in the color of the permanganate solution even though sufficient sulfite (SO3

2-) ions had been added to completely react with the permanganate ions in solution. A second attempt was made, this time adding the 104 mg of sodium metabisulfite to 50 mL deionized water to ensure that the sodium metabisulfite completely dissolved. After swirling, no visible crystals were observed in the water. The solution was added to a fresh 100 mL sample of the stock permanganate solution and swirled. Again, there was no visible change in color.

At this point the experiment was repeated once more, this time using reagent grade sodium sulfite (Na2SO3) that was available in the lab. A 50 mL sample of the stock permanganate solution was combined with 76 mg of sodium sulfite which had been dissolved in 20 mL of deionized water. Immediately the solution changed color from purple to brown. Due to the brown color, the solution could not be analyzed by spectroscopy for residual permanganate. Approximately 1 mL of 20% sulfuric acid was added to the solution to precipitate the Mn. This resulted in a “soft” brown solid falling out of solution leaving a clear supernatant.

The original experiment was then conducted using the reagent grade sodium sulfite. 50 mL aliquots of the stock permanganate solution were taken and varying amounts of sodium sulfite were added to each one by dissolving the sulfite salt into 1-2 mL of deionized water. Once mixed, 3 drops of concentrated sulfuric acid was added to the solution and mixed. A 5-10 mL sample of the supernatant was collected and analyzed in the spectrophotometer for permanganate.

Data and Results

The prepared stock permanganate solution was titrated with sodium oxalate per standard water and wastewater method 4500. The titration was performed three times with a resulting average concentration of 1029 mg/L.

Page:

3/5

A series of five dilutions were prepared to generate a calibration curve for the spectrophotometer. This data is shown in Table 1.

Table 1 Calibration Data

Calibration Point

MnO4used(mL)

MnO4Concentration

(mg/mL)

%T A

C1 0.1 0.0021 93 0.03C2 0.5 0.010 67 0.17C3 1.0 0.021 46 0.34C4 1.5 0.031 32 0.49C5 2.0 0.041 23 0.64

Absorbance is calculated from the %T reading through the formula A = -log10(%T/100). The plot of the absorbance vs. concentration curve is shown in Figure 1.

Figure 1 Calibration Curve

Page:

4/5

Once permanganate samples were reacted with selected molar quantities of sodium sulfite and acidified to precipitate the Mn, samples of supernatant were collected and analyzed in the spectrophotometer. The concentration of the residual permanganate was calculated from the calibration curve. This data is presented in Table 2.

Table 2 Permanganate-Sulfite Reaction Data

Molar % required

SO3

Moles SO3

added

Na2SO3needed

(mg)

Na2SO3added(mg)

%T D.F APermanganate Concentration

(mg/mL)% MnO4 reacted

100 3 68.5 69 100 1 0.00 -0.001 1.0066 2 45.7 47 3 1 1.52 0.098 0.9050 1.5 34.3 35 18 10 0.74 0.474 0.5325 0.75 17.1 16 9.5 10 1.02 0.653 0.360 0 0 0 68 100 0.17 1.018 0.00

D.F. = dilution factorA = absorbance

As a control, the stock permanganate solution was analyzed (shown as the 0 required SO3). The measured concentration (1018 mg/L) is consistent with the calculated concentration from titration (1029 mg/L). This solution was acidified with sulfuric acid just as the samples had been and re-analyzed to ensure there were no effects on the permanganate concentration by the acid. The acidified permanganate solution resulted in the same measured %T, so the acid was verified to have no effect.

Conclusion

The percent permanganate reacted correlates very well with the molar percent sulfite added. The exception noted in the 66 molar percent sulfite addition is most likely due to approaching the end of the calibration curve. From the data it is clear that the molar relationship of permanganate and sulfite in this redox reaction is 2:3, which corresponds to a mass relationship of 1.33 Na2SO3/NaMnO4. Additionally, when less than the molar requirement for sulfite is added, residual permanganate will remain in solution.

As this redox reaction occurs and permanganate is removed from the solution, manganese dioxide (MnO2) is generated. From the balanced redox equation it is apparent that for each mole of NaMnO4 that reacts with Na2SO3 there will be one mole of MnO2 produced. On a mass basis, 0.6 units MnO2 is created for every 1 unit NaMnO4 reacted. Examples of expected MnO2 concentrations at various permanganate levels are shown in Table 3.

Page:

5/5

Table 3 Expected MnO2 Concentrations at Various Initial MnO4 Levels

Flow rate (GPM)

NaMnO4concentration

(mg/L)NaMnO4(lbs/day)

Na2SO3 demand (lbs/day)

MnO2produced (lbs/day)

MnO2concentration

(mg/L)

8 1 0.096 0.128 0.0576 0.68 10 0.961 1.28 0.576 68 100 9.61 12.8 5.76 608 500 48.0 63.9 28.8 3008 1000 96.1 127.8 57.6 600

Tab 10

Modified ISR System – AOP Treatment System Influent Equalization and Advanced Oxidation Process

Page 1 of 1


Considerations:


Process flow rate = 60 gpm AOP Pre-Treatment System Effluent




Additional requirements = 6,190 gal Backwash Tank



9,000 gal


15,190 gal

Tank Selection:

Rectangular Tank:

Length = 37.5 feet

Width = 8.5 feet

Height = 11 feet

Volume = 18,000 gal




INFLUENT EQUALIZATION TANK (T-1300) SIZINGModified ISR System







2.2.15




» Capacity: ....... 480 BBL (20,160 gal.)



» Weight:

....... 24,480 lbs.

STRUCTURAL DESIGN







FEATURES






FEATURES – cont.















SURFACE DETAILS






VAPOR PHASE GAC VESSEL DESIGN CALCULATIONSModified ISR System



Page 1 of 2

M. Seppanen

J. Darby

1/28/2010

Assume:

No active aeration within tank T-1300

The only airflow is from tank venting during filling periods

Filling period is the difference between the high and low set points in the EQ tank

During filling period the system flow rate will be equal to the AOP pre-treatment system effluent rate

The air discharge rate has been estimated to be 60 gpm on a daily basis

The air in the tank will be in equilibrium with the influent groundwater concentrations

System Flow Rate = 60 gpm8.0 CFM

0.227 m3/min

ModelMaximum

Flow (CFM)

Amount of Carbon

(lbs)

Design Pressure

(psi)

G-1S 100 200 10G-2S 300 170 10G-3S 500 140 10

Source: Carbtrol Corporation

VPGAC Selection:G-1S 55 gallon drum

Maximum flow = 100 CFMRequired flow = 8.0 CFMAmount of Carbon 200 lbs

Convert air concentrations from ppmv to µg/m3:


Conc 2 =

Where: Conc 1 = Air concentration in parts per million by volume (ppmv)

Conc 2 = Air concentration in (µg/m3)

MW = Molecular weight of compound (g/mol)

Temp = Air temperature in degrees Kelvin (298.15)

R = Universal gas constant (0.08205 atm*L/mol*K)

Calc prepared by:

Calc checked by:

Date:

Calculate size of VPGAC unit to treat off-gasses from Influent Tank T-1300:

VPGAC vessel design requirements:

VPGAC Vessel Specifications:

Estimate VPGAC Usage

RTemp

MWConc

*

*1000*1

G:\ENV\TF\901-1000\TF922\Reports\2010\RAPA 2010\Final FDEP RAPA\Appendix J\Tab #10\(3) Tab #10_VPGAC Calcs.xlsx ARCADIS




Page 2 of 2

Calculate VOC Flow Rate:

Mass flow rate (lb/day) =

Conversions: 2.2 kg = 1 lb

1,440 min = 1 day

1 kg = 1,000,000 µg

VOC Flow Rate (lbs/day)

0.00

0.00

0.01

0.00

0.00

0.00

0.01

0.00

0.00

0.04

Total potential lbs of VOCs = 0.1 lbs/day

Average VPGAC Loading Rate = 0.1 lb/lb

Potential VPGAC Use Rate = 1 lbs/day

Assume:

Amount of VPGAC in G-1S = 200 lbs

Potential Vapor-Phase GAC Use = 1 lbs/day

Estimated Time for Carbon Breakthrough = 285 days

Trichloethene

Xylenes 0.000

1,1-Dichloroethane 0.000 0.000 0

1,1-Dicholoethene 0.001 0.003 12

Equilibrium Air Concentration

(ppmv)


(µg/m3)

Chloroethane 0.000 0.000 0

Vinyl Chloride 0.000 0.002 5

CompoundInfluent Concentration

(mg/L)

2

1,1,1-Trichloroethane 0.000 0.001 3

0.004 0.003 17

cis-1,2-Dichloroethene 0.001 0.001 2

Toluene 0.001 0.000

Calculate Estimated Time for Carbon Breakthrough:

0.000 0

1,4-Dioxane 15.8 0.016 58

440,1**)000,000,1

1(*2.2*2 airQConc





Page 1 of 2

M. Seppanen

J. Darby

1/28/2010

Assume:

No active aeration within tank T-1500

The only airflow is from tank venting during filling periods

Filling period is the difference between the high and low set points in the EQ tank

During filling period the recovery well network will pump approx 2 gpm more than the HiPOx unit

The air discharge rate has been estimated to be 2 gpm on a daily basis

The air in the tank will be in equilibrium with the influent groundwater concentrations

System Flow Rate = 2 gpm0.3 CFM

0.008 m3/min

ModelMaximum

Flow (CFM)

Amount of Carbon

(lbs)

Design Pressure

(psi)

G-1S 100 200 10G-2S 300 170 10G-3S 500 140 10

Source: Carbtrol Corporation

VPGAC Selection:G-1S 55 gallon drum

Maximum flow = 100 CFMRequired flow = 0.3 CFMAmount of Carbon 200 lbs



Conc 2 =

Where: Conc 1 = Air concentration in parts per million by volume (ppmv)

Conc 2 = Air concentration in (µg/m3)

MW = Molecular weight of compound (g/mol)

Temp = Air temperature in degrees Kelvin (298.15)

R = Universal gas constant (0.08205 atm*L/mol*K)

VPGAC Vessel Specifications:

Estimate VPGAC Usage

VPGAC vessel design requirements:

Calc prepared by:

Calc checked by:

Date:

Calculate size of VPGAC unit to treat off-gasses from Influent Tank T-1500:

RTemp

MWConc

*

*1000*1





Page 2 of 2

Calculate VOC Flow Rate:

Mass flow rate (lb/day) =

Conversions: 2.2 kg = 1 lb

1,440 min = 1 day

1 kg = 1,000,000 µg

VOC Flow Rate (lbs/day)

0.00

0.00

0.00

0.02

0.00

0.00

0.23

0.00

0.00

0.00

Total potential lbs of VOCs = 0.3 lbs/day

Average VPGAC Loading Rate = 0.1 lb/lb

Potential VPGAC Use Rate = 3 lbs/day

Assume:

Amount of VPGAC in G-1S = 200 lbs

Potential Vapor-Phase GAC Use = 3 lbs/day



Xylenes 0.000 0.00 0

1,4-Dioxane 0.425 0.00 1

Trichloethene 2.300 2 9,614

Vinyl Chloride 0.000 0.00 0

Toluene 0.001 0.00 3

1,1,1-Trichloroethane 0.001 0.00 6

1,1-Dicholoethene 0.061 0.02 63

cis-1,2-Dichloroethene 0.480 0.22 884

Chloroethane 0.000 0.00 0

1,1-Dichloroethane 0.038 0.02 97

CompoundInfluent Concentration

(mg/L)


(ppmv)


(µg/m3)

440,1**)000,000,1

1(*2.2*2 airQConc


Tab 11

Modified ISR System – AOP Treatment System Filtration and Solids Settling

Page 1 of 3







92 3 3.500 0.216 3.068 0.051 3.8892 4 4.500 0.237 4.026 0.088 2.2592 6 6.625 0.280 6.065 0.201 0.99







Flow (v1) = 92 gpm


Flow (v2) = 92 gpm


Flow (v3) = 92 gpm





Nominal Diam (in)

ID (in)


1 1.003 0.8781.5 1.452 1.3272 1.826 1.7013 2.691 2.5664 3.460 3.3356 5.460 5.335




FILTER FEED PUMP (P-1100A/B) DESIGN CALCULATIONSModified ISR System - AOP Treatment System



sec60

min1*

)*( 2r

Qv


Page 2 of 3











Equivalent lengths from reference: Civil Engineering Reference Manual, 9th Ed, Professional Publications, Inc., 2003; and"Flow of Fluids", Crane Technical Paper No. 410, 1988.

Pipe Section 1 - 3"

Item Qty. L (ft) Qty * LLinear Pipe (L1) 1 10 10Standard Tee (thru flow) 1 12 12.0Check Valve - Swing 1 27 27Ball valve (full open) 1 4.3 4.390˚ Elbows 3 4.0 12.0Expansion (3"x4") 1 4.0 4.0


Pipe Section 2 - 4"

Item Qty. L (ft) Qty * LLinear Pipe (L1) 1 350 350Standard Tee (thru flow) 6 17 102Standard Tee (branch flow) 4 21 84Union 8 0.7 5.290˚ Elbows 20 4.6 92Check Valve - Swing 4 38 152Ball valve (full open) 10 5.5 55


Pipe Section 3 - 6"

Item Qty. L (ft) Qty * LLinear Pipe (L1) 1 2,500 2,500Union 8 1.5 11.790˚ Elbows 4 10.35 41.4Check Valve - Swing 1 85.5 85.5



Total pipe friction = Total equivalent length x Friction factor







Equivalent Length


Equivalent Length

Equivalent Length


Page 3 of 3




Total Pipe Friction - Pipe Section 3Total equivalent length = 2,639 feet




Total Pipe Friction - Pipe Section 1+2+3 = 18.8




Head loss Across Misc. Process Components Catalytic Media Filter 35 ft 1 psi = 2.31 ft

Multi-Media Filter 20 ftLPGAC-1 23 ftLPGAC-2 12 ft

Flow Meter (plant) 10 ftFlow Meter (discharge) 10 ft









Job/Inq.No. : RAYTHEONPurchaser : ARCADISEnd User : ARCADIS Issued by : Rev. : 0Item/Equip.No. : P-1100AB Quotation No. : RAPA AOP Date : 02/04/2010Service :Order No. :


Vapor Press:



Page 1 of 3

Calc prepared by: M. SeppanenCalc checked by: J. PerellaDate:






106 3 3.500 0.216 3.068 0.051 4.47106 4 4.500 0.237 4.026 0.088 2.60106 6 6.625 0.280 6.065 0.201 1.14

*Pipe dimensions noted for Schedule 40 galvanized steel pipingNote: Design for velocity between 3 and 5 feet/sec to maintain sufficient scour velocity






Flow (v1) = 106 gpm


Flow (v2) = 106 gpm





Nominal Diam (in)

ID (in)


1 1.003 0.8781.5 1.452 1.3272 1.826 1.7013 2.691 2.5664 3.460 3.3356 5.460 5.335

NOTE: a 0.0625 inch (1/16 inch) deposition on interior pipe wall is included indiameter for calculation - 1.003 - (2 x 0.0625) = 0.878 inch diameter



BACKWASH PUMP (P-1200) DESIGN CALCULATIONSModified ISR System - AOP Treatment System



Raytheon Company

sec60

min1*

)*( 2r

Qv

G:\ENV\TF\901‐1000\TF922\Reports\2010\RAPA 2010\Final FDEP RAPA\Appendix J\Tab #11\

(3) Tab #11_P‐1200 TDH.xlsx ARCADIS

Page 2 of 3




Raytheon Company






Equivalent lengths from reference: Civil Engineering Reference Manual, 9th Ed, Professional Publications, Inc., 2003; an"Flow of Fluids", Crane Technical Paper No. 410, 1988

Pipe Section 1 - 3"

Item Qty. L (ft) Qty * LLinear Pipe (L1) 1 10 10Standard Tee (thru flow) 1 12 12Check Valve - Swing 1 27 27Ball valve (full open) 1 4.3 4.390˚ Elbows 1 4.0 4.0Expansion (3"x4") 1 4.0 4.0


Pipe Section 2 - 4"

Item Qty. L (ft) Qty * LLinear Pipe (L1) 1 150 150Standard Tee (thru flow) 6 17 102Standard Tee (branch flow) 3 21 63Union 3 0.7 2.090˚ Elbows 6 4.6 27.6Check Valve - Swing 1 38 38Ball valve (full open) 6 5.5 33



Total pipe friction = Total equivalent length x Friction facto








Total Pipe Friction - Pipe Section 1+2 = 11.4





Equivalent Length

Equivalent Length



Page 3 of 3




Raytheon Company

Head loss Across Misc. Process Components Catalytic Media Filter 45 ft 1 psi = 2.31 ft

Static Mixer 20 ftFlow Meter 12 ft









Model: 3196 Size: 2X3-8 Group: 3196MTI 60Hz RPM: 3000 Stages: 1

Job/Inq.No. : RAYTHEONPurchaser : ARCADISEnd User : ARCADIS Issued by : Rev. : 0Item/Equip.No. : P-1200 Quotation No. : RAPA AOP Date : 02/04/2010Service :Order No. :


Vapor Press:



CATALYTIC MEDIA FILTER DESIGN CALCULATIONSModified ISR System



Page 1 of 1



Date: 1/28/2010

Assume:


3 - 5 gpm/ft2










Bed Depth and Media Contact Time:

Minimum bed depth = 36 inches


Flow rate per vessel = 30.7 gpm

4.11 ft3/min

Media contact time = 9.2 min

With Air Scour:

Step 1: Air Loading Rate = 3 SCFM/ft2



Step 2: Water Loading Rate = 15 gpm/ft2



Step 1: Air = 38 SCFM

Water = 63 gpm

Step 2: Water = 188 gpm

Backwash Volumes:

Volume of Backwash Required per Vessel= 1,570 gpm


Calculate size of Catalytic Media Filter units:


Calculate diameter of Catalytic Media Filter:



G:\ENV\TF\901-1000\TF922\Reports\2010\RAPA 2010\Final FDEP RAPA\Appendix J\Tab #11\(5) Tab #11_LayneOx Calcs.xlsx ARCADIS

Multi-Media Filter Design CalculationsModified ISR System



Page 1 of 1



Date: 1/28/2010

Assume:


8 - 15 gpm/ft2













Water = 74 gpm

Backwash Volumes:

Volume of Backwash Required per Vessel= 740 gpm





Calculate diameter of Multi-Media Filter:

Calculate size of Multi-Media Filter units:

G:\ENV\TF\901-1000\TF922\Reports\2010\RAPA 2010\Final FDEP RAPA\Appendix J\Tab #11\(9) Tab #11_Media Filter Calcs.xlsx ARCADIS

INDUSTRIALPRESSURIZED

WATER MANAGEMENT SYSTEMS, INC. IN-LINE

Yardney high rate automatic backwashing Multi-Media filters are designed for enhanced capacity water filtration. These permanent media automatic backwashing filters will remove organic and/or inorganic suspended solids down to 5-10 microns in size and will entrap greater amounts of suspended solid contaminants than sand media filters. Through the use of automatically controlled backwashing, the filter will operate “on line” for extended periods of time prior to the short backwashing cycle. Automatic filter operation is monitored on both elapsed time as well as pressure differential. When the

controller “calls” for a backwash as a result of pressure differential or elapsed time, the backwashing function utilizes a portion of the clean filtered water produced by the system to clean the media. Single tank systems utilize unfiltered water for backwashing. Optional external backwash water sourcing systems are available for both single and multiple tank systems.

EXCELLENT FOR SUSPENDED SOLIDS REMOVAL DOWN TO 5-10 MICRONSUNITS SHIPPED COMPLETELY ASSEMBLED ON STRUCTURAL SKIDS 3M SCOTCHKOTE 134 FUSION BONDED EPOXY LININGS 60” DEEP SAND MEDIA TANK SHELLS ARE STANDARD AUTOMATIC BACKWASH VALVES IN CAST IRON, STAINLESS TRIM- (AIR OR WATER POWERED) SOLID STATE CONTROLS WITH INTEGRAL ADJUSTABLE PRESSURE DIFFERENTIAL SWITCH. FLANGED OR GROOVED OPTIONS AVAILABLE FOR INLET AND OUTLET CONNECTIONS REMOVEABLE TYPE 304 STAINLESS UNDER-DRAINS IDEAL FOR RAW WATER FILTRATION OR PRE-TREATMENT OF R.O. OR D.I. SYSTEMS AND IN-LINE DISPOSABLE CARTRIDGE OR BAG FILTERS EASY INSTALLATION AND START-UP ASME CODE STAMP AVAILABLE (OPTIONAL) NEMA 4X CONTROLS HOUSING AVAILABLE (OPTIONAL) FILTERED WATER BACKWASH ON MULTIPLE TANK SYSTEMS

Yardney Water Management Systems, Inc. 6666 Box Springs Blvd., Riverside, CA U.S.A.

Phone: (951) 656-67l6 or (800) 854-4788 Fax (951) 656-3867 Website: www.yardneyfilters.com Email: [email protected]

LIT-MM UNITS BROCHURE-002-1206

INDUSTRIAL IN-LINE PRESSURIZED MULTI-MEDIA FILTRATION SYSTEMS

WATER MANAGEMENT SYSTEMS, INC.

ENGINEERING & SIZING DATA FOR SINGLE & MULTIPLE TANK SYSTEMS MULTI-MEDIA FILTRATION SYSTEMS – 60” SIDE SHELL TANKS DESIGNED FOR HIGH QUALITY FILTRATION APPLICATIONS

FOR REMOVAL OF SUSPENDED SOLIDS DOWN TO 5-10 MICRONS IN SIZE

Service Flow rates

Approximate Shipping

Weight Lbs. Approximate Space

Requirement

Model Number

Normal Flow

Range GPM

Peak Flow Rate GPM

Total Filtration

Area (Sq. Ft.)

Dia. X Side Shell

(Inches)

Multi- Media Cu. Ft.

Back-Wash GPM

Inlet/Outlet Size

Back-wash Line Size

StandardMaximum Working Pressure Equip. Media

Approximate Operating

Weight Lbs. Length Width HeightMM-2460-1A 16-47 63 3.15 24 X 60 12.0 47 2" 2" 100 PSI 465 1210 2200 3' 1" 2' 4" 8' 0" MM-2460-2A 32-95 126 6.30 24 X 60 24.0 47 3" 2" 100 PSI 875 2468 4500 4' 5" 2' 4" 8' 6" MM-2460-3A 48-142 189 9.45 24 X 60 36.0 47 3" 2" 100 PSI 1330 3578 6750 6' 9" 2' 4" 8' 6" MM-3060-1A 25-74 98 4.91 30 X 60 20.0 74 3" 3" 100 PSI 680 2116 3650 4' 8" 2' 9" 8' 6" MM-3060-2A 50-147 196 9.82 30 X 60 40.0 74 4" 2" 100 PSI 1140 4205 7050 5' 5" 2' 9" 8' 8" MM-3060-3A 75-221 294 14.73 30 X 60 60.0 74 4" 2" 100 PSI 1740 5846 10,600 8' 3" 2' 9" 8' 8" MM-3660-1A 35-107 142 7.10 36 X 60 28.5 107 3" 3" 100 PSI 840 3022 5150 4' 8" 3' 3" 8? 10"MM-3660-2A 70-213 284 14.20 36 X 60 57.0 107 4" 4" 100 PSI 1485 5617 10,100 6' 5" 3' 3" 9' 3" MM-3660-3A 105-320 426 21.30 36 X 60 85.5 107 4" 4" 100 PSI 2420 8364 15,350 9' 9" 3' 3" 9' 3" MM-4860-1A 63-189 252 12.60 48 X 60 51.5 189 4" 4" 80 PSI 1160 5138 9150 5' 7" 4' 3" 9? 10"MM-4860-2A 126-378 504 25.20 48 X 60 103.0 189 6" 4" 80 PSI 2360 10,101 18,300 8' 5" 4' 3" 10' 2"MM-4860-3A 189-567 756 37.80 48 X 60 154.5 189 6" 4" 80 PSI 3450 15,064 27,300 12' 9" 4' 3" 10' 2"MM-4860-4A 252-756 1008 50.40 48 X 60 206.0 189 8" 4" 80 PSI 5070 20,002 36,850 17' 1" 4' 3" 10' 4"MM-4860-5A 315-945 1260 63.00 48 X 60 257.5 189 10" 4" 80 PSI 6060 25,065 45,850 22? 2” 4' 3" 10' 2"MM-4860-6A 378-1134 1512 75.60 48 X 60 309.0 189 10" 4" 80 PSI 7150 30,028 54,850 26? 6” 4' 3" 10' 2"MM-5460-1A 80-239 318 15.91 54 X 60 65.5 239 4" 4" 80 PSI 1350 6423 11,400 5? 10” 4? 9” 10? 4”MM-5460-2A 160-477 636 31.82 54 X 60 131.0 239 6" 4" 80 PSI 2710 12,746 22,850 9? 4” 4? 9” 10? 8”MM-5460-3A 240-716 954 47.73 54 X 60 196.5 239 6" 4" 80 PSI 4080 17,366 34,250 14? 2” 4? 9” 10? 8”MM-5460-4A 320-955 1272 63.64 54 X 60 262.0 239 8" 4" 80 PSI 5540 25,417 45,750 19? 9” 4? 9” 10? 10”MM-5460-5A 400-1193 1590 79.55 54 X 60 327.5 239 10" 4" 80 PSI 6940 31,740 57,200 24? 7” 4? 9” 10? 8”

MM-5460-6A 480-1432 1908 95.46 54 X 60 393.0 239 10" 4" 80 PSI 8320 38,088 68,650 29? 5” 4? 9” 10? 8”

Single Tank Models I.D. – 1A Multiple Tank Models I.D. – 2A, 3A, 4A, 5A, 6A STANDARD MEDIA SPECIFICATIONS:Gravel Pack: ½” X ¾” crushed rock Garnet: INTERFACE MEDIA Garnet: WORKING MEDIA Anthracite: PRE-FILTER MEDIA

NOTE: For optional media grades, consult factory. NOTE: Media shipping weight includes gravel pack. NOTE: For higher working pressure operation

requirements, consult factory.

Standard Systems Include: Filtered water backwash on multi-tank systemsAll interior surfaces fusion epoxy coated with 3M Scotchkote 134Advanced solid-state automation with elapsed timer and pressure differential controlSkid mounted on structural steel skidLiquid-filled stainless steel pressure gaugesGrooved coupling in/out standard (flanged available – consult factoryAutomatic diaphragm operated non-corrosive brass or cast iron valvesSystems provided with interconnecting pipingRemovable type 304 stainless steel cross-flow underdrain standardASME code stamped available – consult factoryFiltration media is included in the system definition and pricing.

?Excellence In Filtration For A Better World”

Yardney Water Management Systems, Inc. 6666 Box Springs Blvd., Riverside, CA U.S.A.

Phone: (951) 656-67l6 or (800) 854-4788 Fax (951) 656-3867 Website: www.yardneyfilters.com Email: [email protected]

LIT-MM UNITS BROCHURE-002-1206

Page 1 of 1


Considerations:


21-Days Solids Storage = 1,764 gal 84 gallons per day

Daily Input Volume = 4,710 gal Catalytic Media Backwash

Daily Input Volume = 493 gal Multi-Media Backwash

Additional Requirements = 0 gal


Total input volume = Daily Backwash Volume + Additional Requirements

5,203 gal

Minimum required volume = Total input volume + Solids storage

10,407 gal

Tank Selection:

Rectangular Tank:

Length = 37.5 feet

Width = 8.5 feet

Height = 11 feet

Volume = 18,000 gal




BACKWASH TANK (T-2000) SIZINGModified ISR System







2.2.15




» Capacity: ....... 480 BBL (20,160 gal.)



» Weight:

....... 24,480 lbs.

STRUCTURAL DESIGN







FEATURES






FEATURES – cont.















SURFACE DETAILS






Page 1 of 3

DECANT PUMP (P-1300) DESIGN CALCULATIONS






30 1.5 1.900 0.145 1.610 0.014 4.6030 2 2.375 0.154 2.067 0.023 2.7930 3 3.500 0.216 3.068 0.051 1.27







Flow (v1) = 30 gpm





Nominal Diam (in)

ID (in)


1 1.049 0.9241.5 1.610 1.4852 2.067 1.9423 3.068 2.9434 4.026 3.9016 6.065 5.94


Modified ISR System - AOP Treatment SystemTotal Dynamic Head Calculation


sec60

min1*

)*( 2r

Qv


Page 2 of 3

DECANT PUMP (P-1300) DESIGN CALCULATIONSModified ISR System - AOP Treatment System









Pipe Section 1 - 2"

Item Qty. L (ft) Qty * LLinear Pipe (L1) 1 150 150Standard Tee (thru flow) 2 5.6 11Standard Tee (branch flow) 1 9.9 1090˚ Elbows 8 3.4 27Union 2 0.39 1Check Valve 1 15 15Ball valve (full open) 3 2.3 7









Equivalent Length



Page 3 of 3

DECANT PUMP (P-1300) DESIGN CALCULATIONSModified ISR System - AOP Treatment System






Head loss Across Misc. Process Components 0 ft








ITTGoulds Pumps1SC Submersible

Water Pump

GouldsPumpsisabrandofITTCorporation.

www.goulds.com

Engineered for life


Features

■ Casing: AISI 304 SS. Corrosion resistant, non-toxic, non-leaching.

■ Impeller: FDA compliant, glass filled Noryl®. Corrosion and abrasion resistant.

■ Mechanical Seal: Silicon/carbide sealing faces; all metal components of AISI type 300 stainless steel running in protected oil chamber.

■ Elastomers: BUNA-N.

■ Motor Shell and Lifting Handle: Constructed of AISI type 304 series stainless steel.

■ Shaft: AISI type 304 stainless steel high strength keyed pump shaft with impeller locking cap screw.

■ Discharge: 11⁄4" NPT vertical discharge connection.

■ Suction Strainer: Detachable for easy clean out.

�


0 �50

CAPACITY

TOTA

L D

YNA

MIC

HEA

D

FEET

U.S. GPM

100

50

150

�010 �00

�0

40

METERS

0 � 4� 6 m3/hr

60

5 15

51

�00

�5

7 8

1SC51E-H

1SC51C-F

1SC51D-G

1SC51C-A

1SC51D-B

1SC51E-C

1 HP3/4 HP1/2 HP

1 HP

3/4 HP

1/2 HP

aPPLICatIONs

Submersible water pumps designed for pumping out of reservoirs and storage tanks:• Homes and farms• Mobile home parks and motels• Schools and hospitals• Municipal applications• Industrial applications• Commercial applications

sPeCIFICatIONs

Pump:

• 11⁄4" NPT discharge and open suction.

• Maximum suspended solids 1⁄8".

• Capacities: to 35 U.S. GPM (7.9 m3/h).

• Total heads: to 240 feet TDH (70 m).

• Temperature: 104ºF (40ºC) continuous 140ºF (60ºC) intermittent.

• Maximum submergence: to 65 feet (20 m).

• Continuous duty rated, non-overloading motor.Motor:

• Single phase: 3450 RPM, 115 and 230 V, 60 Hz.

• Three phase: 3450 RPM, 230 V, 60 Hz.

• Non-overloading.

• Class F insulation.

• Thermal overload protection: built-in with automatic reset on single phase.

• Three phase models require external overloads in panel.

• Power cord: All 30' long.Single phase – 16/3, with 115 V or 230 V plugThree phase – 16/4 STO, bare leads

NOTE: See accessory section for separate control panels.

JPERELLA

Line

JPERELLA

Line

JPERELLA

Text Box

Pretreatment P-600 AOP P-1300

CWorden

Typewritten Text

�


DIMeNsIONs

MeCHaNICaL Data

NPT 11⁄4

L

5"

“L” Dimensions Discharge Series HP Phase in inches Size

1⁄2 1,3 191⁄8

1SC 3⁄4 1,3 201⁄8 11⁄4

1 1,3 213⁄4

Series Number of HP Volts Phase Maximum RPM Weight Stages Amps (lbs.) 1SC51C0AA 115 1 10.6

1SC51C1AA 1⁄2 230 4.5

1SC51C3AA 3 3 3.0 31 1SC51C0FA 115 1 10.7

1SC51C1FA 1⁄2 230 4.5

1SC51C3FA 3 3.0

1SC51D1BA 1 5.4 3450

1SC51D3BA 4 3⁄4 230 3 3.5 33 1SC51D1GA 1 5.3

1SC51D3GA 3 3.5

1SC51E1CA 1 6.4

1SC51E3CA 5 1 230 3 4.1 38 1SC51E1HA 1 6.8

1SC51E3HA 3 4.3

ITT

GouldsPumpsandtheITTEngineeredBlocksSymbolareregisteredtrademarksandtradenamesofITTCorporation.

NorylisaregisteredtrademarkofGEPlastic.

SPECIFICATIONS ARE SUBJECT TO CHANGE WITHOUT NOTICE.

B1SC August, 2007©2007ITTCorporation

Engineered for life


Component Material Outer Casing and Upper Support Stainless Steel (AISI 304)

Motor Casing Stainless Steel (AISI 304)

Suction Strainer Stainless Steel (AISI 304)

Motor Shaft Stainless Steel (AISI 304)

Impeller Noryl

Diffuser Stainless Steel (AISI 304)

Upper Cover Technopolymer

Mechanical Seal Housing Technopolymer

Lower Bearing Support Aluminum Die Cast

Lower Bearing Urethane Resin

Elastomers Buna-N

Lower Mechanical Seal Silicon Carbide/Silicon Carbide

Upper Lip Seal Nitrile Rubber




Page 1 of 2

M. Seppanen

J. Darby

1/28/2010

Air/Water Scour: Flow rate = 63 gpm


Specific gravity of polymer = 1.015

Polymer weight = 8.465 lbs/gal


Water Only: Flow rate = 188 gpm



Flow rate = 74 gpm



Air Scour: Backwash flow rate = 63 gpm



Volume of polymer = 0.04 L

Water Only: Backwash flow rate = 188 gpm



Volume of polymer = 0.05 L

Calc prepared by:

Calc checked by:

Date:

Calculate Polymer Flow Rates for the Catalytic Media Backwash Cycle:

Calculate Volume of Polymer Required for the Catalytic Media Filters:

Calculate Polymer Flow Rates for the Multi-Media Backwash Cycle:

G:\ENV\TF\901-1000\TF922\Reports\2010\RAPA 2010\Final FDEP RAPA\Appendix J\Tab #11\(16) Tab #11_AOP Polymer Calc.xlsx ARCADIS




Page 2 of 2

Combined: Total Volume of polymer per vessel = 0.09 L



Backwash flow rate = 74 gpm



Volume of polymer per vessel = 0.04 L



Cataltyic Media Filters:




0.49 gal/week

Multi-Media Filters:




0.07 gal/week

Total Volume of polymer per week = 0.56 gal/week

Calculate Total Volume of Polymer Required per Week:

Calculate Volume of Polymer Required for the Mulit-Media Filters:

G:\ENV\TF\901-1000\TF922\Reports\2010\RAPA 2010\Final FDEP RAPA\Appendix J\Tab #11\(16) Tab #11_AOP Polymer Calc.xlsx ARCADIS

©2006, General Electric Company. All rights reserved. *Trademark of General Electric Company; may be registered in one or more countries.

Fact Sheet

PFW957EN 0606

Europe/Middle East/Africa Heverlee, Belgium +32-16-40-20-00

Asia/Pacific Shanghai, China +86-21-5298-4573

Find a contact near you by visiting gewater.com or e-mailing [email protected].

Americas Watertown, MA +1-617-926-2500

Global Headquarters Trevose, PA +1-215-355-3300

PolyFloc* AS1002 High Molecular Weight Flocculant• Easy-to-feed polymeric flocculant

• Convenient, true liquid

• Reduces floc carryover

• Approved for potable use

Description and Use

PolyFloc AS1002 is a liquid, weakly anionic, high molecular weight, polymeric flocculant, which is designed to function in industrial treatment programs as a coagulant aid, or flocculant, in clarification, thickening, and softening processes. The product is chlorine resistant. NSF certification for potable applications is pending.

PolyFloc AS1002 is true liquid, high molecular weight flocculant. This polymer is ideal for remote plant operations or small volume usage because it does not require extensive feed and makedown equipment.

A fast-settling floc is formed when PolyFloc AS1002 is applied to warm or hot lime/soda softeners, cold lime softeners, and influent clarification systems. Floc carryover is reduced, resulting in a cleaner effluent.

PolyFloc AS1002 is also an excellent sludge dewatering aid producing clean filtrate, high solids capture, and a drier cake. Applications to many types of industrial sludges have been successful, including blast furnace sludge dewatering applications.

Treatment and Feeding Requirements

PolyFloc AS1002 is an easy-to-feed liquid that does not require any special makedown procedures. Poly-Floc AS1002 can be fed neat with any suitable high viscosity gear pump or diluted with water to any con-venient concentration. Diluted product may be fed by a pump, eductor, or by gravity flow to a point where good mixing, but not violent agitation, of the treated water occurs. High speed mixing decreases the activ-

ity of the polymer. Pumps used to transfer the solution to the point of application should be positive dis-placement gear or piston pumps.

To minimize corrosion and contamination by corro-sion products, liquid-side components of tanks, pumps, and piping should be constructed of stainless steel, polyethylene, or polyvinyl chloride. Mild steel is acceptable only in systems where contamination by corrosion products is not a critical problem.

General Properties

Physical properties of PolyFloc AS1002 are shown on the Material Safety Data Sheet, a copy of which is available on request.

Packaging Information

PolyFloc AS1002 is a liquid product, available in a vari-ety of containers. Consult your GE representative for delivery and packaging alternatives.

Storage and Handling

Store PolyFloc AS1002 at moderate temperatures of 40 to 90°F (4 to 32°C), and protect from freezing. The recommended shelf life of the product is six months.

Spilled polymer is very slippery. Small amounts of spilled polymer can be washed down with copious amounts of water. Large spills should be contained and absorbed on inert material, then disposed as solid waste, prior to flushing with water.

Safety Precautions

A Material Safety Data Sheet containing detailed in-formation about this product is available upon re-quest.

Material Safety Data Sheet Issue Date: 28-JAN-2008 Supercedes: 28-JAN-2008

POLYFLOC AS1002

1 IdentificationIdentification of substance or preparationPOLYFLOC AS1002

Product Application AreaFlocculant.

Company/Undertaking IdentificationGE Betz, Inc.4636 Somerton RoadTrevose, PA 19053T 215 355-3300, F 215 953 5524

Emergency Telephone(800) 877-1940

Prepared by Product Stewardship Group: T 215-355-3300 Prepared on: 28-JAN-2008

2 Hazard(s) identification

******************************************************************************** EMERGENCY OVERVIEW CAUTION May cause slight irritation to the skin. May cause slight irritation to the eyes. Mists/aerosols may cause irritation to upper respiratory tract. DOT hazard is not applicable Odor: Slight; Appearance: Colorless To Light Yellow, Liquid Fire fighters should wear positive pressure self-contained breathing apparatus(full face-piece type). Proper fire-extinguishing media: dry chemical, carbon dioxide, foam or water ******************************************************************************** POTENTIAL HEALTH EFFECTS ACUTE SKIN EFFECTS: Primary route of exposure; May cause slight irritation to the skin. ACUTE EYE EFFECTS: May cause slight irritation to the eyes. ACUTE RESPIRATORY EFFECTS: Mists/aerosols may cause irritation to upper respiratory tract.


INGESTION EFFECTS: May cause slight gastrointestinal irritation. TARGET ORGANS: No evidence of potential chronic effects. MEDICAL CONDITIONS AGGRAVATED: Not known. SYMPTOMS OF EXPOSURE: May cause redness or itching of skin.

3 Composition / information on ingredients

Information for specific product ingredients as required by the U.S. OSHA HAZARD COMMUNICATION STANDARD is listed. Refer to additional sections of this MSDS for our assessment of the potential hazards of this formulation. HAZARDOUS INGREDIENTS: This product is not hazardous as defined by OSHA regulations. No component is considered to be a carcinogen by the National Toxicology Program, the International Agency for Research on Cancer, or the Occupational Safety and Health Administration at OSHA thresholds for carcinogens.

4 First-aid measures

SKIN CONTACT: Wash thoroughly with soap and water. Remove contaminated clothing. Get medical attention if irritation develops or persists. EYE CONTACT: Remove contact lenses. Hold eyelids apart. Immediately flush eyes with plenty of low-pressure water for at least 15 minutes. Get medical attention if irritation persists after flushing. INHALATION: If nasal, throat or lung irritation develops - remove to fresh air and get medical attention. INGESTION: Do not feed anything by mouth to an unconscious or convulsive victim. Do not induce vomiting. Immediately contact physician. Dilute contents of stomach using 2-8 fluid ounces (60-240 mL) of milk or water. NOTES TO PHYSICIANS: No special instructions

5 Fire-fighting measures


FIRE FIGHTING INSTRUCTIONS: Fire fighters should wear positive pressure self-contained breathing apparatus (full face-piece type). EXTINGUISHING MEDIA: dry chemical, carbon dioxide, foam or water HAZARDOUS DECOMPOSITION PRODUCTS: oxides of carbon and sulfur FLASH POINT: > 200F > 93C P-M(CC)

6 Accidental release measures

PROTECTION AND SPILL CONTAINMENT: Ventilate area. Use specified protective equipment. Contain and absorb on absorbent material. Place in waste disposal container. Flush area with water. Wet area may be slippery. Spread sand/grit. DISPOSAL INSTRUCTIONS: Water contaminated with this product may be sent to a sanitary sewer treatment facility,in accordance with any local agreement,a permitted waste treatment facility or discharged under a permit. Product as is - Incinerate or land dispose in an approved landfill.

7 Handling and storage

HANDLING: Normal chemical handling. STORAGE: Keep containers closed when not in use. Protect from freezing. Shelf life 135 days.

8 Exposure controls / personal protection

EXPOSURE LIMITS This product is not hazardous as defined by OSHA regulations. ENGINEERING CONTROLS: adequate ventilation PERSONAL PROTECTIVE EQUIPMENT: Use protective equipment in accordance with 29CFR 1910 Subpart I RESPIRATORY PROTECTION: A RESPIRATORY PROTECTION PROGRAM THAT MEETS OSHA’S 29 CFR 1910.134 AND ANSI Z88.2 REQUIREMENTS MUST BE FOLLOWED WHENEVER WORKPLACE CONDITIONS WARRANT A RESPIRATOR’S USE. USE AIR PURIFYING RESPIRATORS WITHIN USE LIMITATIONS ASSOCIATED WITH THE EQUIPMENT OR ELSE USE SUPPLIED AIR-RESPIRATORS. If air-purifying respirator use is appropriate, use any of the following particulate respirators: N95, N99, N100, R95, R99, R100, P95, P99 or P100. SKIN PROTECTION: rubber, butyl, viton or neoprene gloves -- Wash off after each use. Replace as necessary. EYE PROTECTION: splash proof chemical goggles


9 Physical and chemical properties

Specific Grav.(70F,21C) 1.015 Vapor Pressure (mmHG) ~ 18.0 Freeze Point (F) 32 Vapor Density (air=1) < 1.00 Freeze Point (C) 0 Viscosity(cps 70F,21C) 2000 % Solubility (water) 100.0 Odor Slight Appearance Colorless To Light Yellow Physical State Liquid Flash Point P-M(CC) > 200F > 93C pH As Is (approx.) 4.1 Evaporation Rate (Ether=1) < 1.00 Percent VOC: 0.0 NA = not applicable ND = not determined

10 Stability and reactivity

STABILITY: Stable under normal storage conditions. HAZARDOUS POLYMERIZATION: Will not occur. INCOMPATIBILITIES: May react with strong oxidizers. DECOMPOSITION PRODUCTS: oxides of carbon and sulfur INTERNAL PUMPOUT/CLEANOUT CATEGORIES: "A"

11 Toxicological information

Oral LD50 RAT: >2,000 mg/kg NOTE - Estimated value Dermal LD50 RABBIT: >2,000 mg/kg NOTE - Estimated value

12 Ecological information

AQUATIC TOXICOLOGY Daphnia magna 48 Hour Static Acute Bioassay (pH adjusted) LC50= 25466; No Effect Level= 8700 mg/L Fathead Minnow 96 Hour Static Acute Bioassay (pH adjusted) LC50= 30944; No Effect Level= 15500 mg/L BIODEGRADATION No Data Available.

13 Disposal considerations


If this undiluted product is discarded as a waste, the US RCRA hazardous waste identification number is : Not applicable. Please be advised; however, that state and local requirements for waste disposal may be more restrictive or otherwise different from federal regulations. Consult state and local regulations regarding the proper disposal of this material.

14 Transport information

DOT HAZARD: Not Applicable PROPER SHIPPING NAME: DOT EMERGENCY RESPONSE GUIDE #: Not applicable Note: Some containers may be DOT exempt, please check BOL for exact container classification

15 Regulatory information

TSCA: All components of this product are included on or are in compliance with the U.S. TSCA regulations. CERCLA AND/OR SARA REPORTABLE QUANTITY (RQ): No regulated constituent present at OSHA thresholds FOOD AND DRUG ADMINISTRATION: 21 CFR 176.110 (acrylamide - acrylic acid resins) All ingredients comprising this product are authorized by FDA for the manufacture of paper and paperboard that may contact aqueous and fatty foods as per 21 CFR 176.170(a) (4). USDA FOOD PLANT APPROVALS: G1 SARA SECTION 312 HAZARD CLASS: Product is non-hazardous under Section 311/312 SARA SECTION 302 CHEMICALS: No regulated constituent present at OSHA thresholds SARA SECTION 313 CHEMICALS: No regulated constituent present at OSHA thresholds CALIFORNIA REGULATORY INFORMATION CALIFORNIA SAFE DRINKING WATER AND TOXIC ENFORCEMENT ACT (PROPOSITION 65): No regulated constituents present MICHIGAN REGULATORY INFORMATION No regulated constituent present at OSHA thresholds

16 Other information

NFPA/HMIS CODE TRANSLATION Health 1 Slight Hazard Fire 0 Minimal Hazard Reactivity 0 Minimal Hazard Special NONE No special Hazard


(1) Protective Equipment B Goggles,Gloves (1) refer to section 8 of MSDS for additional protective equipment recommendations. CHANGE LOG EFFECTIVE DATE REVISIONS TO SECTION: SUPERCEDES --------- --------------------- ---------- MSDS status: 30-JAN-1997 ** NEW ** 12-MAY-1997 15 30-JAN-1997 06-MAY-1998 ;EDIT:9 12-MAY-1997 27-MAY-1999 15 06-MAY-1998 21-SEP-1999 15 27-MAY-1999 11-FEB-2002 4,16 21-SEP-1999 28-JAN-2008 4,5,7,8,10 11-FEB-2002



CUSTOMER:

DATE:

SCALE:

MODEL NO:


REVISED

REVISED

REVISED

DRAWING NUMBER:

NONE

7/10/06

NJF


5/30/08




"A"(Inches)


"E"


DIRECTIONOF FLOW

Tab 12

Modified ISR System – AOP Treatment System Granular Activated Carbon

LIQUID-PHASE GAC VESSEL DESIGN CALCULATIONSModified ISR System



Page 1 of 2

M. Seppanen

J. Darby

1/28/2010

Assume: LPGAC vessel sizing is based on chemical adsorption and hydraulic loading.

The amount of volatile organic compounds to the LPGAC vessel in the influent stream is

expected to be minimal. The orientation of the LPGAC vessels are two vessels in series

3 - 8 gpm/ft2










COCs: 1,1 - Dichloroethane (1,1-DCA) = 10 μg/L

Total VOCs in Influent = 0.010 mg/L

0.011 lbs/day

Carbon usage =

Where,

Co = Contaminant concentration (mg/L)

Q = Process flow rate (Lpm)

t = Time (day)

k = Adsorption Capacity @ 1ppm (mg/g carbon)

η = Efficiency (%)

Calc prepared by:

Calc checked by:

Date:

Calculate Carbon Usage Rate:

Calculate size of aqueous phase granular activated carbon (GAC) units:

Incoming VOCs (Based on Mass Balance and ISR Operation):

Calculate diameter of LPGAC vessel:


Design is based on hydraulic loading

Recommended hydraulic loading for carbon

)1

(*)**

( 0

k

tQC

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LIQUID-PHASE GAC VESSEL DESIGN CALCULATIONSModified ISR System



Page 2 of 2

1,1 - DCA Concentration at Mid Process point 1 = (C0) = 0.010 mg/L

Process Flow Rate = (Q) = 348 L/min

Adsorption capacity 2 = (k) = 7.5 mg/g carbon

Efficiency = (η) = 5 %

Time = (t) = 1,440 min

Carbon usage rate for 1,1-DCA: 13,372 g carbon/day

29.5 lb carbon/day

Mass of carbon in vessel = 2,500 lb



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Tab 13

Modified ISR System – General Arrangement Plans

Tab 14

Modified ISR System – Building Containment Curb

Page 1 of 2


Calculate Volume of Tanks and Process Equipment within Containment:

Equipment Name Volume (gal) No. Units Total Volume (gal)

Heat Exchanger Feed Tank (T-100) 2,145 1 2,145Heat Exchanger (HX-100A/B) 10 2 20Influent Equalization Tank (T-200A/B/C) 20,160 3 60,480Aeration Tank (T-300) 6,500 1 6,500Filter Feed Tank (T-400) 6,500 1 6,500Multi-Media Filters (T-500A/B/C) 370 3 1,110Air Stripper (T-600A/B) 250 2 500Air Stripper Discharge Tank (T-700) 1,100 1 1,100Backwash Holding Tank (T-800) 6,500 1 6,500Polymer Tank (T-900) 5 1 5Sodium Hydroxide Tank (T-1000) 275 1 275Scrubber Blow-Down Tank (T-1000) 1,000 1 1,000Scrubber Blow-Down LPGAC (T-1100A/B) 160 1 160

Subtotal = 86,295 gallons

Calculate Volume of Required Containment:

The total containment volume required shall be the larger volume from either Method 1 or 2 below:

Method 1:

Total Volume = 10% of Total Volume of Tanks and Process Equipment

Volume of Tanks and Process Equipment 86,295 gallons10% 8,630 gallons

Total Method 1 = 8,630 gallons

Method 2:


CONTAINMENT VOLUME CALCULATIONModified ISR System


Total Volume = 110% Volume of the Largest Tank

Volume of Largest Tank 20,160 gallons110% 22,176 gallons


Calculate Volume of Containment Available:

Containment Volume = (Containment Area - Equipment Area) x Containment Curb Depth

Length (feet) Width (feet) Total Area (ft2)Containment Area 85 80 6,800

Subtotal = 6,800 ft2

Equipment Name Area (ft2) * % under curb Displacement Area (ft2)Heat Exchanger Feed Tank (T-100) 44 100% 44Heat Exchanger (HX-100A/B) 36 50% 18Influent Equalization Tank (T-200A/B/C) 960 100% 960Aeration Tank (T-300) 79 100% 79Filter Feed Tank (T-400) 79 100% 79Multi-Media Filters (T-500A/B/C) 30 30% 9Air Stripper (T-600A/B) 70 20% 14Air Stripper Discharge Tank (T-700) 41 100% 41Backwash Tank (T-800) 79 100% 79Polymer Tank and Pump (T-900) 16 100% 16Sodium Hydroxide Tank (T-1000) 12 100% 12Scrubber Blow-Down Tank (T-1000) 25 50% 13Scrubber Blow-Down LPGAC (T-1100A/B) 20 50% 10Pump Skids (7) 63 50% 32Blower Skids (3) 27 50% 14

Subtotal = 1,418

* measurements from Modified ISR System AOP Pre-treatment System Layout: Figure J-5, Tab #11

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Page 2 of 2


CONTAINMENT VOLUME CALCULATIONModified ISR System


Containment Area 6,800 square feetEquipment Area 1,418 square feet

Subtotal = 5,382 square feetDepth 0.75 feet (Curb 9" high)Estimated Floor Slope 0.17 feetCorrected Depth 0.67 feet

Total = 3,588 cubic feetConversion 7.48 gallons/cubic foot

Containment Volume Available 26,839 gallons

Containment Volume Available 26,839 gallonsContainment Volume Required 22,176 gallons


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Page 1 of 2


Calculate Volume of Tanks and Process Equipment within Containment:

Equipment Name Volume (gal) No. Units Total Volume (gal)

Influent Equalization Tank (T-1300) 20,160 1 20,160Influent Equalization Tank (T-1500) 20,160 1 20,160Filter Feed Tank (T-1400) 6,500 1 6,500Filter Feed Tank (T-1600) 6,500 1 6,500Catalytic Media Filters (T-1700A/B/C) 750 3 2,250Multi-Media Filters (T-1800A/B) 370 2 740LPGAC (T-1900A/B/C) 2,200 3 6,600Backwash Tank (T-2000) 20,160 1 20,160Polymer Storage Tank (T-2100) 5 1 5AOP Unit (AOP-100) 150 1 150AOP Unit (AOP-200) 250 1 250AOP-100 Unit pH Control Unit 500 1 500Hydrogen Peroxide Tank 1,500 1 1,500Sodium Permanganate Solution Tanks 530 1 530

Subtotal = 86,005 gallons

Calculate Volume of Required Containment:

The total containment volume required shall be the larger volume from either Method 1 or 2 below:

Method 1:

Total Volume = 10% of Total Volume of Tanks and Process Equipment

Volume of Tanks and Process Equipment 86,005 gallons10% 8,601 gallons


Method 2:

Total Volume = 110% Volume of the Largest Tank

Volume of Largest Tank 20,160 gallons110% 22,176 gallons


Calculate Volume of Containment Available:

Containment Volume = (Containment Area - Equipment Area) x Containment Curb Depth

Length (feet) Width (feet) Total Area (ft2)Containment Area 118 68 8,024

Subtotal = 8,024 ft2

Equipment Name Area (ft2) * % under curb Displacement Area (ft2)Influent Equalization Tank (T-1300) 344 100% 344Influent Equalization Tank (T-1500) 344 100% 344Filter Feed Tank (T-1400) 79 100% 79Filter Feed Tank (T-1600) 79 100% 79Catalytic Media Filters (T-1700A/B/C) 63 30% 19Multi-Media Filters (T-1800A/B) 19 30% 6LPGAC (T-1900A/B/C) 147 30% 44Backwash Tank (T-2000) 344 100% 344AOP Unit (AOP-100) 320 100% 320AOP Unit (AOP-200) 204 100% 204Control Panels 70 30% 21Vapor Phase Carbon Vessels (3) 25 30% 8VSA Oxygen Skid 36 100% 36AOP-100 Unit Chiller 10 100% 10AOP-200 Unit Chiller 7 100% 7Hydrogen Peroxide Tank 76 100% 76AOP-100 Unit pH Control Unit 35 100% 35AOP-100 Unit Feed Pump Skid 11 100% 11Polymer Skid 9 100% 9Pump Skids (4 pumps) 16 50% 8Sodium Permanganate System Building 204 100% 204

Subtotal = 2,206


Modified ISR SystemAOP Treatment System

CONTAINMENT VOLUME CALCULATION

Raytheon Company

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Page 2 of 2

Modified ISR SystemAOP Treatment System

CONTAINMENT VOLUME CALCULATION

Raytheon Company

* measurements from Modified ISR System AOP System Layout: Figure J-6, Tab #9

Containment Area 8,024 square feetEquipment Area 2,206 square feet

Subtotal = 5,818 square feetDepth 0.75 feet (Curb 9" high)Estimated Floor Slope 0.17 feetCorrected Depth 0.67 feet

Total = 3,879 cubic feetConversion 7.48 gallons/cubic foot

Containment Volume Available 29,014 gallons

Containment Volume Available 29,014 gallonsContainment Volume Required 22,176 gallons


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Tab 15

Modified ISR System – Support Equipment

JPERELLA

Rectangle

JPERELLA

Rectangle

JPERELLA

Text Box

A-100 Model SF 1

JPERELLA

Text Box

A-200 Model SF 11

Tab 16

Modified ISR System – Process and Instrumentation


AOP Pre-Treatment SystemControl Logic TableRaytheon Company


PROCESS UNIT DEVICE ID DEVICE TYPE SET POINT RESPONSE (1) COMMENT

LS-100 Level Switch 1. 56 inches - high / high level Alarm - Notify Operator.

AOP pre-treatment system shut down (2). Critical alarm to Thermal System PLC - disable transfer of groundwater and condensate.

LE/LT-100 Level Transmitter 1. 12 inches - low level 2. 40 inches - operating level3. 48 inches - high level4. 52 inches - high / high level

1. Alarm - Notify Operator; Disable operation of heat exchanger feed pumps (P-100A/B).2. PLC controls P-100A/B pump speed to maintain specified water level in tank.3. Alarm - Notify Operator.4. Critical alarm to Thermal System PLC - disable transfer of groundwater and condensate.

HS-100A/B HOA selector switch 1. Hand2. Auto3. Off

1. The pump shall operate regardless of the status of alarms and interlocks.2. The pump shall be subject to control devices, interlocks and alarms.3. The pump shall not operate.

VFD-100A/B Variable Frequency Drive PLC adjustable set point The purpose is to maintain a constant water level in the heat exchanger feed tank (T-100). Tank level data will be monitored and transmitted to PLC by LE/LT-100.

YI-100A/B Status Indicator On/Off 1. Indicates status of P-100A/B. A discord alarm will occur if P-100A or P-100B is engaged to run and the return input from the auxiliary contact is not made.2. Notify Operator.

TE/TT-100A Temperature transmitter Indication only 4-20mA signal sent to PLC, PLC to track temperature reading. The purpose is to monitor influent temperature to heat exchanger (HX-100A/B). Data to be used to determine heat exchanger performance.

TE/TT-100B Temperature transmitter PLC adjustable set point to detect temperature in the heat exchanger effluent line.

High temperature response:1. >140 F - Shut down power to Pumps P-100A/B, Critical alarm to Thermal System PLC, Notify Operator.2. 130 - 140F - Slow speed of Pump P-100A/B 10%, delay 15 minutes and then re-assess, Notify operator, Notification alarm to Thermal System PLC3. 120 - 130 F - Notify Operator.

TE/TT-100C Temperature transmitter PLC adjustable set point to detect temperature in the chilled water feed line.

1. 4-20mA signal sent to PLC, PLC to track temperature reading.2. Temperatures >50 F, Notify Operator.

TE/TT-100D Temperature transmitter Indication only 1. 4-20mA signal sent to PLC, PLC to track temperature reading.2. Temperatures >95 F, Notify Operator.

The purpose is to monitor water temperature returned to TerraTherm's system. Data to be used to determine heat exchanger performance.

LS-1100 Level Switch 1. 64 inches - high / high level 1. Alarm - Notify Operator.2. Critical alarm to Thermal System PLC - disable transfer of scrubber blow-down water.

LE/LT-1100 Level Transmitter 1. 12 inches - low level 2. 16 inches 3. 48 inches - operating level4. 54 inches - high level5. 60 inches - high / high level

1. Alarm - Notify Operator. 2. Disable operation of transfer pump (P-900).3. PLC controls P-900 pump speed to maintain specified water level in tank.4. Alarm - Notify Operator.5. Critical alarm to Thermal System PLC - disable transfer of scrubber blow-down water.

HS-900 HOA selector switch 1. Hand2. Auto3. Off


VFD-900 Variable Frequency Drive PLC adjustable set point The purpose is to maintain a constant water level in the scrubber blow-down tank (T-1100). Tank level data will be monitored and transmitted to PLC by LE/LT-1100.

YI-900 Status Indicator On/Off 1. Indicates status of P-900. A discord alarm will occur if P-900 is engaged to run and the return input from the auxiliary contact is not made.2. Notify Operator.

LPGAC Vessels (T-1200A/B)

PIT-1200A/B;DPI-1200

Pressure Transmitter, Differential Pressure Indicator

PLC adjustable set point to detect pressure at the inlet and outlet of the LPGAC vessels.

Low pressure at PIT-1200A:1. Shut down power to Pump P-900.2. Notify Operator.3. Flashing strobe light.High pressure at PT-1200A:1. Shut down power to Pump P-900.2. Notify Operator.3. Flashing strobe light.High differential pressure response:1. Notify Operator.

The purpose is to optimize operation of the GAC filters. Low pressure may indicate leakage and high pressure indicates membranes and/or piping may be plugged. High differential pressure indicates changeout of carbon is required.

Treatment System - Figure J-4Heat Exchanger Feed Tank (T-100)

Heat Exchanger(HX-100A/B)Chilled Water Feed and Return Lines

Heat Exchanger Feed Pumps (P-100A/B)

Heat Exchanger (HX-100A/B) Process Water Line

Scrubber Blow-Down Tank (T-1100)

Transfer Pump (P-900)

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Scrubber Blow-Down Effluent Piping

FE/FIT-100 Totalizing flow meter with indicating transmitter

NA 4-20mA signal sent to PLC, PLC to calculate flow rate and track totalizer reading.

LS-200A Level Switch 1. 122 inches - high / high level Alarm - Notify Operator.


LE/LT-200A Level Transmitter 1. 24 inches - low level 2. 20 inches 3. 80 inches - operating level4. 100 inches - high level5. 112 inches - high / high level

1. Alarm - Notify Operator; Disable operation of aeration tank feed pumps (P-200A/B). 2. Notify Operator.3. PLC controls P-200A/B pump speed to maintain specified water level in tank.4. Alarm - Notify Operator. Begin overflow to influent EQ tanks (T-200B/C).5. Disable operation of heat exchanger feed pumps (P-100A/B). Critical alarm to Thermal System PLC - disable transfer of groundwater and condensate.

FV-200A Flow Valve On/Off Flow Valve FV-200A opens or closes depending on the control device and alarms it is subject to. FV-200A shall fail closed in the event of AOP pre-treatment system shut down.

The purpose is to control the flow of compressed air to the pneumatic actuated valves associated with EQ tank operation.

LS-200B/C Level Switch 1. 122 inches - high / high level Alarm - Notify Operator.


LE/LT-200B/C Level Transmitter 1. 24 inches - low level 2. 96 inches - operating level3. 108 inches - high level4. 116 inches - high / high level

1. Alarm - Notify Operator; Disable operation of recirculation pump (P-200C).2. Enable operation of recirculation pump (P-200C). PLC controls P-200C pump speed to maintain a constant flow of recycled water to influent EQ tank (T-200A).3. Alarm - Notify Operator. 4. Disable operation of heat exchanger feed pumps (P-100A/B). Critical alarm to Thermal System PLC - disable transfer of groundwater and condensate.

FV-200B/C Flow Valve On/Off Flow Valve FV-200B/C opens or closes depending on the control device and alarms it is subject to. FV-200B/C shall fail closed in the event of AOP pre-treatment system shut down.




VFD-200A/B Variable Frequency Drive PLC adjustable set point The purpose is to maintain a constant water level in the influent EQ tank (T-200A). Tank level data will be monitored and transmitted to PLC by LE/LT-200A.


HS-200C HOA selector switch 1. Hand2. Auto3. Off


VFD-200C Variable Frequency Drive PLC adjustable set point The purpose is to maintain a constant recycled water flow rate to influent EQ tank (T-200A). Tank level data will be monitored and transmitted to PLC by LE/LT-200A/B/C.

YI-200C Status Indicator On/Off 1. Indicates status of P-200C. A discord alarm will occur if P-200C is engaged to run and the return input from the auxiliary contact is not made.2. Notify Operator.

Aeration Tank (T-300) Influent Line

AE/AIT-300 pH Sensor 1. pH = 6.0 - low level2. pH = 7.6 - high level

Data will be used to control the speed of the sodium hydroxide metering pump (P-700) and ensure the correct pH is maintained in the aeration tank (T-300).


Shut down AOP pre-treatment system components downstream of EQ tanks T-200A/B/C (3). LE/LT-300 Level Transmitter 1. display/record tank water level

2. 108 inches - high / high level 1. 4-20 mA signal sent to PLC to display/record tank water level2. Critical alarm - Notify operator, disable aeration feed tank pumps (P-200A/B).

Influent EQ Tanks(T-200B/C)

Treatment System - Figure J-5Influent Equalization (EQ) Tank (T-200A)

Aeration Tank(T-300)

Aeration Tank Feed Pumps (P-200A/B)

Recirculation Pump (P-200C)






Aeration Tank Blower (B-100A/B)

VFD-B-100A/B Variable Frequency Drive PLC adjustable set point The purpose is to maintain a constant air flow rate to the aeration tank (T-300).

HS-B-00A/B HOA selector switch 1. Hand2. Auto3. Off


YI-B-100A/B Status Indicator On/Off 1. Indicates status of blower B-100A/B. A discord alarm will occur if B-100A/B is engaged to run and the return input from the auxiliary contact is not made.2. Notify Operator.

PI/PIT-B-100A/B Pressure transmitter PLC adjustable set point to detect pressure in the aeration tank blower discharge lines

Low pressure response:1. Shut down power to blower B-100A/B.2. Notify Operator.3. Flashing strobe light.High pressure response:1. Shut down power to blower B-100A/B.2. Notify Operator.3. Flashing strobe light.

Low pressure may indicate leakage and high pressure indicates piping may be plugged.



P-700 operation will be dependant upon pH in the aeration tank (T-300) influent line.



Shut down AOP pre-treatment system components downstream of EQ tanks T-200A/B/C (3). LE/LT-400 Level Transmitter 1. 12 inches - low level

2. 20 inches - low level3. 64 inches - operating level4. 100 inches - high level5. 108 inches - high / high level

1. Alarm - Notify Operator; Disable operation of filter feed pumps (P-300A/B). 2. Notify Operator of low level. 3. PLC controls P-300A/B pump speed to maintain specified water level in tank.4. Alarm - Notify Operator.5. Critical alarm - Notify Operator; Disable operation of aeration tank feed pumps (P-200A/B).



YI-300A/B Status Indicator On/Off 1. Indicates status of P-300A/B. A discord alarm will occur if P-300A/B is engaged to run and the return input from the auxiliary contact is not made.2. Notify Operator.

PI/PIT-300A/B Pressure transmitter PLC adjustable set point to detect pressure in the filter feed pump discharge line.

Low pressure response (<10 psi): (1) shut down power to Pumps P-300A/B, Notify Operator, flashing strobeMid-Pressure response (40-50 psi): (1) Notify OperatorHigh pressure response (>50 psi): (1) Shut down power to pumps P-300A/B, (2) Notify operator, (3) flashing strobe light


VFD-300C Variable Frequency Drive PLC adjustable set point. The purpose is to maintain a constant backwash flow rate through the multi-media filters (T-500A/B/C).

HS-300C HOA selector switch 1. Hand2. Auto3. Off


Pump operation shall be tied to differential pressure switches (DPI-500). Run permissive based on level in filter feed tank (T-300) and backwash tank (T-800). Do not operate if P-300A/B is engaged.

YI-300C Status Indicator On/Off 1. Indicates status of P-300C. A discord alarm will occur if P-300C is engaged to run and the return input from the auxiliary contact is not made.2. Notify Operator.

Backwash Pump (P-300C)

Sodium Hydroxide Metering Pump (P-700)

Filter Feed Pumps (P-300A/B)

Treatment System - Figure J-6Filter Feed Tank (T-400)






PI/PIT-500A/B/C;DPI-500


PLC adjustable set point to detect pressure in the multi-media filter piping.

High pressure response (>20 psi): Notify Operator, warning.High-High Pressure response (>50 psi): (1) Notify Operator, backwash required.

The purpose is to notify the operator when backwash may be required.

LS-800 Level Switch 1. 114 inches - high / high level Alarm - Notify Operator.Shut down backwash pump (P-300C)

LE/LT-800 Level Transmitter 1. display/record tank water level 2. 102 inches - high level3. 108 inches - high / high level

1. 4-20 mA signal sent to PLC to display/record tank water level. 2. Alarm - Notify Operator.3. Critical alarm - Notify Operator; Disable operation of backwash pump (P-300C) and polymer metering pump (P-500).



P-600 shall operate based on water level in the backwash tank (T-800) and filter feed tank (T-400).




Pump operation will be dependant upon backwash cycle operation. Pump will only operate when backwash pump (P-300C) operates.



1. The compressor shall operate regardless of the status of alarms and interlocks.2. The compressor shall be subject to control devices, interlocks and alarms.3. The compressor shall not operate.

YI-100 Status Indicator On/Off 1. Indicates status of A-100. A discord alarm will occur if A-100 is engaged to run and the return input from the auxiliary contact is not made.2. Notify Operator.

KV-100 Timer Valve Manual set point Drain valve on air receiver tank will open or close depending on a set timer.PI/PIT-A100 Pressure transmitter 70 psi Low pressure response (<10 psi): (1) Notify Operator. Low pressure may indicate leakage and high pressure indicates

piping may be plugged.

Air Stripper(T-600A/B)

PI/PIT-600A/B Pressure transmitter PLC adjustable set point. Low pressure response:1. Shut down power to pumps P-300A/B and blowers B-200A/B.2. Notify Operator.3. Flashing strobe light.High pressure response:1. Shut down power to pumps P-300A/B and blowers B-200A/B.2. Notify Operator.3. Flashing strobe light.

The purpose is to optimize operation of the air stripper. Low pressure may indicate leakage and high pressure indicates piping may be plugged.

VFD-B-200A/B Variable Frequency Drive PLC adjustable set point. The purpose is to maintain a constant air flow rate to the air strippers (T-600A/B).

HS-B-200A/B HOA selector switch 1. Hand2. Auto3. Off


YI-B-200A/B Status Indicator On/Off 1. Indicates status of B-200A/B. A discord alarm will occur if B-200A/B is engaged to run and the return input from the auxiliary contact is not made.2. Notify operator

NOTE: not all valving for the Multi-media filter is shown on the PID. Valving will be controlled by a PLC that is part of the MMF system. Full control logic and valve sequencing for backwashing is not

presented within this control logic table.

Decant Pump (P-600)

Backwash Tank (T-800)

Multi-Media Filters (T-500A/B/C)

Treatment System - Figure J-7

Polymer Metering Pump (P-500)

Air Compressor (AC-100)

Air Stripper Blower (B-200A/B)






VFD-B-300 Variable Frequency Drive PLC adjustable set point. The purpose is to maintain a constant air flow rate to the air strippers (T-600A/B).

HS-B-300 HOA selector switch 1. Hand2. Auto3. Off


YI-B-300 Status Indicator On/Off 1. Indicates status of B-200A/B. A discord alarm will occur if B-200A/B is engaged to run and the return input from the auxiliary contact is not made.2. Notify Operator.

PI/PIT-B-300 Pressure transmitter PLC adjustable set point. Low pressure response:1. Shut down power to blower B-300.2. Notify Operator.3. Flashing strobe light.High pressure response:1. Shut down power to blower B-300.2. Notify Operator.3. Flashing strobe light.


PI/PCV-100 On/Off Manual set point. PCV-100 opens or closes depending on the pressure in the line. The PLC will modulate valve PCV-100 to maintain a consistent pressure at PIT-600C. The purpose is to control the pressure in the vapor discharge line to achieve a consistent flow rate from the airstripper blower (B-200A/B) and the vent blower (B-300).

PI/PIT-600C Pressure transmitter PLC adjustable set point Pressure data will be transferred to PLC, and the PLC will modulate valve PCV-100 to maintain a constant pressure at PIT-600C Low pressure response:1. Notify Operator.High pressure response:1. Shut down power to Pumps P-300A/B/C and Blower B-200A/B 2. Notify Operator. 3. Flashing strobe light.


PI/PIT-600D Pressure transmitter PLC adjustable set point. Record/transmit pressure data to PLC


Shut down AOP pre-treatment system components downstream of EQ tanks T-200A/B/C (3). LE/LT-700 Level Transmitter 1. 10 inches - low level

2. 14 inches3. 24 inches - operating level4. 28 inches - high level5. 32 inches - high / high level

1. Alarm - Notify Operator; Disable operation of air stripper discharge pumps (P-400A/B).2. Alarm - low level: Notify Operator. 3. PLC controls P-400A/B pump speed to maintain specified water level in tank.4. Alarm - high level - Notify Operator.5. Critical alarm - Notify Operator; Disable operation of filter feed pumps (P-300A/B).

VFD-400A/B Variable Frequency Drive PLC adjustable set point. The purpose is to maintain a constant water level in the air stripper discharge tank (T-700). Tank level data will be monitored and transmitted to PLC by LE/LT-700.



YI-400A/B Status Indicator On/Off 1. Indicates status of P-400A/B. A discord alarm will occur if P-400A/B is engaged to run and the return input from the auxiliary contact is not made.2. Notify Operator.



PI/PIT-400 Pressure transmitter PLC adjustable set point to monitor pressure in pipeline between AOP pre-treatment system and AOP treatment system.

Low pressure response:1. Shut down power to Pumps P-400A/B.2. Notify Operator.3. Flashing strobe light.High pressure response:1. Shut down power to Pumps P-400A/B.2. Notify Operator.3. Flashing strobe light.


Air Stripper Discharge Tank(T-700)

Vapor Discharge Line

AOP Pre-Treatment System Effluent Line

Air Stripper Discharge Pumps (P-400A/B)

Tank Vent Blower (B-300)






LS-800A Level switch 1. 6 inches - low level 2. 18 inches - high level

1. Low level response - Sump Pump (P-800) will turn off.2. High level response - Sump Pump (P-800) will turn on.

HS-800A HOA selector switch 1. Hand2. Auto3. Off


YI-800A Status Indicator On/Off 1. Indicates status of P-800. A discord alarm will occur if P-800 is engaged to run and the return input from the auxiliary contact is not made.2. Notify Operator.

Containment Area Leak Sensor

LS-800B Level switch 1. 2 inches - high level 1. Indicates leak in treatment area. AOP pre-treatment system shut down (2). Critical Alarm - Notify Operator.

Footnotes: (1) All analog values (level, flow, pressure, etc.) shall be recorded for the purpose of historical trending and data analysis. (2) AOP pre-treatment system shut down - if AOP pre-treatment system shutdown is identified as response, the following will occur: a. All motors will be de-energized b. Flow valves FV-200A/B/C will fail closed c. Audible alarm will sound in the plant area and in the plant office d. A red stack light in the plant will illuminate e. The operator will be notified via cell phone text message (3) AOP pre-treatment system components will be shut down downstream of the EQ Tanks T-200A/B/C. Response is the same as (2) above. AOP - Advanced Oxidation Process EQ - Equalization NA - Not Applicable PLC - Programmable Logic Controller VFD - Variable Frequency Drive

Sump Pump (P-800)



AOP Treatment SystemControl Logic TableRaytheon Company



FE/FIT-XXX Totalizing flow meter with indicating transmitter


PIT-XXXA Pressure Transmitter (water level in well)

PLC adjustable set point Display and track water level within the recovery well:1. Recovery pump speed may be controlled by PLC to maintain select water level within the well.

The purpose is to optimize operation of the recovery well pumps.

PIT-XXX Pressure Transmitter (recovery piping line pressure)

PLC adjustable set point Low pressure response:1. Shut down power to Pumps P-XXX.2. Notify Operator.High pressure response:1. Shut down power to Pumps P-XXX.2. Notify Operator.

The purpose is to optimize operation of the recovery well pumps. Low pressure may indicate leakage and high pressure indicates the pump and/or piping may be plugged.

LS-XXX Level Switch (water level in the recovery well vault

1. 2 inches - high level High level response:1. Stop Extraction Well Pumps P-XXXX.2. Notify Operator.

VFD-XXX Variable Frequency Drive PLC adjustable set point The pump VFD may be controlled to maintain a select water level within the well.

HS-XXX HOA selector switch 1. Hand2. Auto3. Off


YI-XXX Status Indicator On/Off 1. Indicates status of P-XXX. A discord alarm will occur if P-XXX is engaged to run and the return input from the auxiliary contact is not made.2. Notify Operator.


AOP treatment system shut down (2). Critical alarm - disable transfer of pre-treated groundwater from the AOP pre-treatment system.

LE/LT-1300 Level Transmitter 1. 24 inches - low / low level 2. 30 inches - low level3. 80 inches - operating level4. 100 inches - high level5. 112 inches - high / high level

1. Alarm - Notify Operator; Disable operation of AOP feed pump (P-1000). 2. Alarm - Notify Operator - low level warning.3. PLC controls AOP feed pump (P-1000) speed to maintain specified water level in tank.4. Alarm - Notify Operator - high level warning.5. Critical alarm - disable operation of recovery well pumps.

FV-1300 Flow Valve On/Off Flow Valve FV-1300 opens or closes depending on the control device and alarms it is subject to. FV-1300 shall fail closed in the event of AOP treatment system shut down.



Treatment system shut down (2). Critical alarm - disable operation of recovery well extraction pumps.

LE/LT-1500 Level Transmitter 1. 24 inches - low / low level 2. 30 inches - low level3. 80 inches - operating level4. 100 inches - high level5. 112 inches - high / high level

1. Alarm - Notify Operator; Disable operation of AOP feed pump (P-1000). 2. Alarm - Notify operator - low level warning.3. PLC controls AOP feed pump (P-1000) speed to maintain specified water level in tank.4. Alarm - Notify Operator - high level warning.5. Critical alarm - disable operation of recovery well pumps.

FV-1500 Flow Valve On/Off Flow Valve FV-1500 opens or closes depending on the control device and alarms it is subject to. FV-1500 shall fail closed in the event of AOP treatment system shut down.




VFD-1000 Variable Frequency Drive PLC adjustable set point The purpose is to maintain a constant water level in the heat exchanger feed tank (T-100). Tank level data will be monitored and transmitted to PLC by LE/LT-100.

PLC programmable timer.

YI-1000 Status Indicator On/Off 1. Indicates status of P-110A/B. A discord alarm will occur if P-110A or P-110B is engaged to run and the return input from the auxiliary contact is not made.2. Notify Operator.

PI/PIT-1000 Pressure transmitter PLC adjustable set point to detect pressure in the AOP feed pump discharge line.

Low pressure response:1. Shut down power to Pumps P-1000.2. Notify Operator.3. Flashing strobe light.High pressure response:1. Shut down power to Pumps P-1000.2. Notify Operator.3. Flashing strobe light.


Treatment System - Figure J-8

AOP Feed Pump(P-1000)

Recovery Wells(Each Well)

Recovery Well Pumps (P-XXX)

Influent EQ Tank (T-1500)

Influent Equalization (EQ) Tank (T-1300)






LS-1500A Level switch 1. 6 inches - low level 2. 18 inches - high level

1. Low level response - Sump Pump (P-1500) will turn off.2. High level response - Sump Pump (P-1500) will turn on.

HS-1500A HOA selector switch 1. Hand2. Auto3. Off


YI-1500A Status Indicator On/Off 1. Indicates status of P-1500. A discord alarm will occur if P-1500 is engaged to run and the return input from the auxiliary contact is not made.2. Notify Operator.

LS-1500B Level switch 1. 2 inches - low level 1. Indicates potential leak within treatment system or build-up of rainwater in the containment area. Notify Operator.

LS-1500C Level switch 1. 6 inches - high level 1. Indicates potential leak within treatment system or build-up of rainwater in the containment area. AOP treatment system shut down (2). Critical Alarm - Notify Operator.


AOP treatment system shut down (2). LE/LT-1400 Level Transmitter 1. 12 inches - low level


1. Alarm - Notify Operator; Disable operation of filter feed pumps (P-1100A/B). 2. Alarm - Notify Operator - low level warning.3. PLC controls filter feed pumps (P-1100A/B) speed to maintain specified water level in tank.4. Alarm - Notify Operator - high level warning.5. Critical alarm - disable operation of AOP-100.


AOP treatment system shut down (2). LE/LT-1600 Level Transmitter 1. 12 inches - low level


1. Alarm - Notify Operator; Disable operation of filter feed pumps (P-1100A/B). 2. Alarm - Notify Operator - low level warning.3. PLC controls filter feed pumps (P-1100A/B) speed to maintain specified water level in tank.4. Alarm - Notify Operator - high level warning.5. Critical alarm - disable operation of AOP-100.



VFD-1100A/B Variable Frequency Drive PLC adjustable set point The purpose is to maintain a constant water level in the filter feed tanks (T-1400 and T-1600). Tank level data will be monitored and transmitted to PLC by LE/LT-1400 and LE/LT-1600.


PI/PIT-1100A/B Pressure transmitter PLC adjustable set point to detect pressure in the aeration tank feed pump discharge line.

Low pressure response (<10 psi): (1) shut down power to Pumps P-1100A/B, Notify Operator, flashing strobe.Mid-Pressure response (40-50 psi): (1) Notify Operator.High pressure response (>50 psi): (1) Shut down power to pumps P-1100A/B, (2) Notify operator, (3) flashing strobe light.


VFD-1200 Variable Frequency Drive PLC adjustable set point The purpose is to maintain a constant backwash flow rate through the catalytic and multi-media filters.



Pump operation shall be tied to differential pressure switches (DPI-1700 and DPI-1800). Run permissive based on level in filter feed tanks (T-1400 and T-1600) and backwash tank (T-2000). Do not operate if P-1100A/B is engaged.


PI/PIT-1700A/B/C;DPI-1700


PLC adjustable set point to detect pressure in the catalytic media filter piping.




1. The compressor shall operate regardless of the status of alarms and interlocks.2. The compressor shall be subject to control devices, interlocks and alarms.3. The compressor shall not operate.

YI-200 Status Indicator On/Off 1. Indicates status of A-200. A discord alarm will occur if A-200 is engaged to run and the return input from the auxiliary contact is not made.2. Notify Operator.

KV-200 Timer Valve Manual set point Drain valve on air receiver tank will open or close depending on a set timer.PI/PIT-A100 Pressure transmitter 70 psi Low pressure response (<10 psi): (1) Notify operator. Low pressure may indicate leakage and high pressure indicates

piping may be plugged.

Air Compressor (A-200)

Treatment System - Figure J-9Filter Feed Tank (T-1400)

Catalytic Media Filters (T-1700A/B/C)

Filter Feed Pumps (P-1100A/B)

Filter Feed Tank (T-1600)

Backwash Pump (P-1200)



Containment Area Leak Sensors

Sump Pump (P-1500)






PI/PIT-1800A/B;DPI-1800


PLC adjustable set point to detect pressure in the multi-media filter piping.



GAC Vessels (F-1900A/B/C)

PIT-1900A/B/C;DPI-1900


PLC adjustable set point to detect pressure at the inlet and outlet of the GAC vessels




1. Flow monitoring data as required by City POTW permit. 2. Flow = 95 - 100 gpm (high flow alarm) 3. Flow > 100gpm (high flow alarm)

1. Data transmitted and recorded by PLC as required by City POTW permit. 2. Notify Operator - high flow warning.

3. Shutdown of AOP Treatment System (2) .

AE/AIT-700 pH Sensor 1. pH monitoring data as required by City POTW permit. 2. pH < 5.5 (low pH alarm) 3. pH = 5.5 - 6.0 (low pH warning) 4. pH = 9 - 11 (high pH warning) 5. pH >11.0 (high pH alarm)

1. Data transmitted and recorded by PLC as required by City POTW permit.

2. Shutdown of AOP Treatment System (2) . 3. Notify Operator. 4. Notify Operator.

5. Shutdown AOP Treatment System (2) .


AOP treatment system shut down (2). LE/LT-200- Level Transmitter 1. display/record tank water level

2. 102 inches - high level3. 108 inches - high / high level

1. 4-20 mA signal sent to PLC to display/record tank water level. 2. Alarm - Notify Operator.3. Critical alarm - Notify Operator; Disable operation of backwash pump (P-300C) and polymer metering pump (P-500).



P-13 shall operate based on water level in the backwash tank (T-2000) and influent EQ tank (T-1300).




Pump operation will be dependant upon backwash cycle operation. Pump will only operate when backwash pump (P-1200) operates.


Footnotes: (1) All analog values (level, flow, pressure, etc.) shall be recorded for the purpose of historical trending and data analysis. (2) AOP treatment system shut down - if AOP treatment system shutdown is identified as response, the following will occur: a. All motors will be de-energized b. Flow valves FV-1300 and FV-1500 will fail closed c. Audible alarm will sound in the plant area and in the plant office d. A red stack light in the plant will illuminate e. The operator will be notified via cell phone text message

AOP - Advanced Oxidation Process EQ - Equalization NA - Not Applicable PLC - Programmable Logic Controller VFD - Variable Frequency Drive

Polymer Metering Pump (P-1400)

Treatment System - Figure J-10Multi-Media Filters (T-1800A/B)

Backwash Tank (T-2000)

Decant Pump (P-1300)

AOP Treatment System Effluent Piping




Tab 17

Modified ISR System – Sampling Port Locations

Table J-7Sample Port LocationsModified ISR System


Page 1 of 2

Sample Location Purpose of SampleCompliance Sample

(Yes/No)

AOP Pre-Treatment System Influent

Composite of in-situ thermal system recovery well network - collected from the heat exchanger discharge line. Sample will be used to evaluate source recovery rates and determine concentrations of COCs in the AOP pre-treatment system influent.

Yes

Aeration Tank EffluentSample will be used to evaluate performance of the aeration tank and verify oxidation of dissolved iron in the groundwater.

No

Multi-Media Filter EffluentMulti-media effluent - sample will be used to determine filter efficiency to remove particles and optimize backwash frequency.

No

Air Stripper EffluentAir stripper effluent - sample will be used to assess the performance of the air stripper unit and determine concentrations of COCs in the AOP treatment system influent.

No

VPGAC Effluent

Passive venting from the AOP treatment system influent equalization tanks will be monitored with an organic vapor analyzer. Samples will be used to demonstrate air emissions compliance and estimate the time required for COC break-through of the carbon unit.

Yes

AOP-100 IntermediateSample will be used to evaluate performance of the AOP unit, and

verify and update destruction curve/ model for the HiPOxTM system.No

AOP-100 Effluent

AOP effluent - sample will be used to assess the performance of the AOP unit and update destruction curve/model generated for the

HiPOxTM system. Results will be used to determine influent solids loading to the catalytic media filters.

No



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Table J-7Sample Port LocationsModified ISR System


Page 2 of 2

Catalytic Media Filter Effluent

Catalytic media effluent - sample will be used to determine filter efficiency to remove/oxidized iron and other particles. Results will be used to optimize backwash frequency, and determine the influent solids loading for the multi-media filter.

No

Multi-Media Filter EffluentMulti-media effluent - sample will be used to determine filter efficiency to remove particles that may break through the catalytic media filter, and optimize backwash frequency.

No

Primary LPGAC Vessel Effluent

Effluent of the lead carbon vessel - sample will be used to determine the time and volume of water required for COC break-through, and optimize the LPGAC change out frequency.

No

Secondary LPGAC Vessel Effluent(Treated Water Discharge - POTW)

Effluent of the lag carbon vessel - sample will be used to show compliance with the City IWD Permit.

Yes

Settled SolidsSolids sample will be collected from the backwash tank prior to off-site disposal. Sample will be representative of settled solids and will be used to develop a waste profile for off-site disposal of generated solids.

Yes

Footnotes:VPGAC - Vapor-Phase Granular Activated CarbonAOP - Advanced Oxidation ProcessLPGAC - Liquid Phase Granular Activated Carbon

POTW - Publicly Owned Treatment WorksCOC - Constituents of Concern

IWD - Industrial Wastewater Discharge

G:\ENV\TF\901-1000\TF922\Reports\2010\RAPA 2010\Final FDEP RAPA\Appendix J\Tab #17\Tab J-7 - Sample Port Locations.xlsx ARCADIS

Tab 18

Modified ISR System – Air Emission Calculations

Page 1 of 2

Calc prepared by: M. SeppanenChecked by: J. Darby

Date: 1/17/10

Determine emissions from air stripper exhaust using the following equations:

Emissions = Cremoved * QW gpm * 3.79 L/gal * 1 g/106 g * 1 lb/454.5 g * 1440 min/day

Cout = Cin * Air Stripper Removal Efficiency

Cremoved = Cin - Cout

Where: Cin = Concentration of contaminant in the liquid (mg/L)

Cout = Concentration of contaminant in the liquid effluent of the air stripper (mg/L)

Cremoved = Concentration of contaminant removed from the liquid and transferred to the

vapor phase (mg/L)QW = Liquid flow rate = 60 gpm

QA = Air flow rate = 900 SCFM

Conversions:lbs/day to mg/m3 = mg/m3 = lbs/day * (453,600 mg/lbs) * (1/Q minutes/ft3) * (1 day/1440 minutes) * (35.3 ft3/m3)

ppmv = (mg/m3)*(273.15 + °C) / (12.187)(MW)

ppmv = ppm by volume mg/m3 = milligrams of gaseous pollutant per cubic meter of ambient air

MW = molecular weight of the gaseous pollutant°C = ambient air temperature in degrees Centigrade

Notes:1 The design maximum groundwater concentrations from the In-situ Thermal System were used to estimate off-gas emissions.2 Concentrations determined using QED air stripper model EZ-Tray 16.6, modeled at an air:water ratio of 110:1, water temperature of 72 F, assume 4 trays.


Calculation of Off-Gas Emissions from Air StripperModified ISR System

AOP Pre-treatment System

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Page 2 of 2

Volatile Organic Compounds

Design Maximum Concentration from

Heating System 1 (g/L)

Air Stripper Removal

Efficiency 2

(%)

Cremoved

(g/L)

Cout

(g/L)

Unabated Emissions

(lb/day)

Vapor Concentration

(mg/m3) MW

Vapor Concentration

(ppmv)Chemicals of Concern1,1,1-Trichloroethane 4,310 99.99% 4,310 0.43 3.11E+00 38.4 133.4 7.01,1-Dichloroethene 13,789 99.99% 13,788 1.38 9.93E+00 122.7 96.9 30.6cis-1,2-Dichloroethene 12,174 99.99% 12,172 1.22 8.77E+00 108.4 96.9 27.1Vinyl chloride 4,997 99.99% 4,997 0.50 3.60E+00 44.5 62.5 17.2Trichloroethene 44,178 99.99% 44,173 4.42 3.18E+01 393.2 131.4 72.41,1-Dichloroethane 6,318 99.99% 6,317 0.63 4.55E+00 56.2 99.0 13.81,4-Dioxane 15,767 0.00% 0.0 15,767 0.00E+00 0.0 88.1 0.0

Other Compounds1,1,2-Trichloroethane 493 99.51% 491 2.4 3.54E-01 4.4 133.4 0.81,2,4-Trimethylbenzene 609 99.99% 609 0.06 4.39E-01 5.4 120.2 1.11,2-Dichloroethane 992 99.79% 989 2.08 7.13E-01 8.8 99.0 2.21,3,5-Trimethylbenzene 1,101 99.99% 1,101 0.11 7.93E-01 9.8 120.2 2.02-Butanone (MEK) 9,340 20.25% 1,891 7,449 1.36E+00 16.8 72.1 5.74-Methyl-2-pentanone (MIBK) 6,107 90.44% 5,523 584 3.98E+00 49.2 100.2 11.9Acetone 15,175 15.68% 2,379 12,795 1.71E+00 21.2 58.1 8.8Benzene 569 99.99% 568 0.06 4.10E-01 5.1 78.1 1.6Carbon Disulfide 701 99.99% 701 0.1 5.05E-01 6.2 76.1 2.0Chloroethane 496 99.99% 496 0.05 3.57E-01 4.4 64.5 1.7Chloroform 12,973 99.99% 12,971 1.30 9.35E+00 115.5 119.4 23.4Ethylbenzene 300 99.99% 300 0.03 2.16E-01 2.7 106.2 0.6Isopropylbenzene 472 99.99% 472 0.05 3.40E-01 4.2 120.2 0.8m,p-Xylene 426 99.99% 426 0.04 3.07E-01 3.8 106.2 0.9Methylene chloride 13,043 99.97% 13,039 3.91 9.39E+00 116.1 84.9 33.1Naphthalene 153 95.69% 147 6.61 1.06E-01 1.3 128.2 0.2o-Xylene 254 99.99% 254 0.03 1.83E-01 2.3 106.2 0.5Tetrachloroethene 1,514 99.99% 1,514 0.15 1.09E+00 13.5 165.8 2.0Toluene 5,607 99.99% 5,607 0.56 4.04E+00 49.9 92.1 13.1trans-1,2-Dichloroethene 111 99.99% 111 0.01 7.96E-02 1.0 96.9 0.2Trichlorofluoromethane 590 99.99% 590 0.06 4.25E-01 5.2 137.4 0.9

Total Air Emissions 9.79E+01 281

Total Emissions = 97.94 lbs/day

Allowable Emissions = 13.7

Allowable Emissions Exceeded = Yes

lbs/day

G:\ENV\TF\901-1000\TF922\Reports\2010\RAPA 2010\Final FDEP RAPA\Appendix J\Tab #18\(1) Air Stripper Emissions.xlsx ARCADIS

Page 1 of 2

Calc prepared by: M. SeppanenChecked by: J. Darby

Date: 1/17/10

Determine emissions from aeration tank using the following equations:

Emissions = Cremoved * QW gpm * 3.79 L/gal * 1 g/106 g * 1 lb/454.5 g * 1440 min/day

Cout = Cin * Aeration Tank Removal Efficiency

Cremoved = Cin - Cout

Where: Cin = Concentration of contaminant in the liquid (mg/L)

Cout = Concentration of contaminant in the liquid effluent of the aeration tank (mg/L)

Cremoved = Concentration of contaminant removed from the liquid and transferred to the

vapor phase (mg/L)QW = Liquid flow rate = 60 gpm

QA = Air flow rate = 40 SCFM

Conversions:lbs/day to mg/m3 = mg/m3 = lbs/day * (453,600 mg/lbs) * (1/Q minutes/ft3) * (1 day/1440 minutes) * (35.3 ft3/m3)

ppmv = (mg/m3)*(273.15 + °C) / (12.187)(MW)

ppmv = ppm by volume mg/m3 = milligrams of gaseous pollutant per cubic meter of ambient air

MW = molecular weight of the gaseous pollutant°C = ambient air temperature in degrees Centigrade

Notes:1 The design maximum groundwater concentrations from the In-situ Thermal System were used to estimate off-gas emissions.2 Concentrations determined using QED air stripper model EZ-Tray 16.6, modeled at an air:water ratio of 110:1, water temperature of 72 F, assume 4 trays.


Calculation of Off-Gas Emissions from Aeration Tank (T-300)Modified ISR System

AOP Pre-treatment System

G:\ENV\TF\901-1000\TF922\Reports\2010\RAPA 2010\Final FDEP RAPA\Appendix J\Tab #18\(2) Aeration Tank Emissions.xlsx ARCADIS

Page 2 of 2

Volatile Organic Compounds

Design Maximum Concentration from

Heating System 1 (g/L)

Aeration Tank

Removal

Efficiency 2

(%)

Cremoved

(g/L) Cout (g/L)

Unabated Emissions

(lb/day)

Vapor Concentration

(mg/m3) MW

Vapor Concentration

(ppmv)

Chemicals of Concern1,1,1-Trichloroethane 4,310 10.00% 431 3,879.30 3.11E-01 86.3 133.4 15.71,1-Dichloroethene 13,789 10.00% 1,379 12,410.36 9.93E-01 276.2 96.9 69.0cis-1,2-Dichloroethene 12,174 10.00% 1,217 10,956.25 8.77E-01 243.8 96.9 60.9Vinyl chloride 4,997 10.00% 500 4,497.53 3.60E-01 100.1 62.5 38.8Trichloroethene 44,178 10.00% 4,418 39,760.08 3.18E+00 884.8 131.4 163.01,1-Dichloroethane 6,318 10.00% 632 5,686.26 4.55E-01 126.5 99.0 31.01,4-Dioxane 15,767 0.00% 0.0 15,767 0.00E+00 0.0 88.1 0.0

Other Compounds1,1,2-Trichloroethane 493 10.00% 49 444.0 3.55E-02 9.9 133.4 1.81,2,4-Trimethylbenzene 609 10.00% 61 548.46 4.39E-02 12.2 120.2 2.51,2-Dichloroethane 992 10.00% 99 892.40 7.14E-02 19.9 99.0 4.91,3,5-Trimethylbenzene 1,101 10.00% 110 990.77 7.93E-02 22.0 120.2 4.42-Butanone (MEK) 9,340 5.00% 467 8,873 3.36E-01 93.5 72.1 31.44-Methyl-2-pentanone (MIBK) 6,107 5.00% 305 5,801 2.20E-01 61.2 100.2 14.8Acetone 15,175 2.00% 303 14,871 2.19E-01 60.8 58.1 25.3Benzene 569 10.00% 57 511.66 4.10E-02 11.4 78.1 3.5Carbon Disulfide 701 10.00% 70 631.3 5.05E-02 14.0 76.1 4.5Chloroethane 496 10.00% 50 446.52 3.57E-02 9.9 64.5 3.7Chloroform 12,973 10.00% 1,297 11,675.29 9.35E-01 259.8 119.4 52.7Ethylbenzene 300 10.00% 30 270.39 2.16E-02 6.0 106.2 1.4Isopropylbenzene 472 10.00% 47 424.62 3.40E-02 9.4 120.2 1.9m,p-Xylene 426 10.00% 43 383.56 3.07E-02 8.5 106.2 1.9Methylene chloride 13,043 10.00% 1,304 11,739.05 9.40E-01 261.2 84.9 74.5Naphthalene 153 10.00% 15 138.00 1.10E-02 3.1 128.2 0.6o-Xylene 254 10.00% 25 228.67 1.83E-02 5.1 106.2 1.2Tetrachloroethene 1,514 10.00% 151 1,362.31 1.09E-01 30.3 165.8 4.4Toluene 5,607 10.00% 561 5,046.66 4.04E-01 112.3 92.1 29.5trans-1,2-Dichloroethene 111 10.00% 11 99.48 7.96E-03 2.2 96.9 0.6Trichlorofluoromethane 590 10.00% 59 530.77 4.25E-02 11.8 137.4 2.1

Total Air Emissions 9.87E+00 646

Total Emissions = 9.87 lbs/day

Allowable Emissions = 13.7 lbs/day

Allowable Emissions Exceeded = No

G:\ENV\TF\901-1000\TF922\Reports\2010\RAPA 2010\Final FDEP RAPA\Appendix J\Tab #18\(2) Aeration Tank Emissions.xlsx ARCADIS

Tab 19

Modified ISR System – Electrical Load Calculation

Page 1 of 1

Calc prepared by: J. DarbyCalc checked by: A. CardosoDate: 2/24/10

AOP Pre-Treatment SystemEquipment Name Tag HP Voltage AMP KVA kW1

Heat Exchanger Feed Pump 1 P-100A 3 460 4.8 2.21 3.06Heat Exchanger Feed Pump 2 P-100B 3 460 4.8 2.21 3.06Aeration Tank Feed Pump 1 P-200A 1.5 460 2.6 1.20 1.66Aeration Tank Feed Pump 2 P-200B 1.5 460 2.6 1.20 1.66Recirculation Pump P-200C 2 460 3.4 1.56 2.16Filter Feed Pump 1 P-300A 7.5 460 11.0 5.06 7.00Filter Feed Pump 2 P-300B 7.5 460 11.0 5.06 7.00Backwash Feed Pump P-300C 7.5 460 11.0 5.06 7.00Air Stripper Feed Pump 1 P-400A 3 460 4.8 2.21 3.06Air Stripper Feed Pump 2 P-400B 3 460 4.8 2.21 3.06Polymer Feed Pump P-500 0.25 115 5.8 0.67 0.67Decant Pump P-600 0.5 115 9.8 1.13 1.13Sodium Hydroxide Feed Pump P-700 0.25 115 5.8 0.67 0.67Aeration Blower 1 B-100 3 460 4.8 2.21 3.06Aeration Blower 2 B-100 3 460 4.8 2.21 3.06Air Stripper Blower 1 B-200A 10 460 14.0 6.44 8.91Air Stripper Blower 2 B-200B 10 460 14.0 6.44 8.91Tank Vent Blower B-300 0.5 460 1.0 0.46 0.64Air Compressor A-100 2 460 3.4 1.56 2.16Misc Load MISC NA 115 130.4 15.00 12.00

Total KVA = 64.75AMP at 460V Service = 140.76

Amp. Service (125% Round UP) = 180.0Maximum kW = 79.9

Average kW2 = 41.7AOP Treatment SystemEquipment Name Tag HP Voltage AMP KVA kW1

AOP Feed Pump (Existing) P-1000 2 230 6.8 1.56 2.16Filter Feed Pump 1 P-1100A 15 460 21.0 9.66 13.37Filter Feed Pump 2 P-1100B 15 460 21.0 9.66 13.37Backwash Feed Pump P-1200 15 460 21.0 9.66 13.37Polymer Feed Pump P-1400 0.25 115 5.8 0.67 0.92Decant Pump P-1300 0.5 115 9.8 1.13 1.56Sump Pump (Existing) P-1500 1 115 16.0 1.84 2.55Extraction Pump RW-2 RW-2 1 230 3.6 0.83 1.15Extraction Pump RW-3 RW-3 1 230 3.6 0.83 1.15Extraction Pump RW-4 RW-4 1 230 3.6 0.83 1.15Extraction Pump RW-5 RW-5 1 230 3.6 0.83 1.15Air Compressor 1 A-100 15 460 21.0 9.66 13.37Misc Load MISC NA 115 130.4 15.00 12.00AOP-100 System 3 AOP-100 NA 230 28.3 6.50 5.20AOP-200 System AOP-200 NA 460 56.5 26.00 20.80

Total KVA = 94.65AMP at 460V Service = 205.76

Amp. Service (125% Round UP) = 260.0Maximum kW = 103.3

Average kW 4 = 66.6Notes:1 three phase = kW = KVA x power-factor x 1.73 (power factor = 0.8) single phase = kW = KVA

and Misc loads. 50% of A-100, 20% of P-700, and 10% of P-200C, P-300C, P-500, and P-600.

oxygen generator, ozone generator, and chiller. AOP-100 System is assumed to have 4 times the power usage as AOP-200 System (increased size plus oxygen generator)4 Average power usage includes, 100% operation of P-1000, P-1100A, RW-2, RW-3, RW-4, RW-5, Misc Loads,

AOP-100, and AOP-200. 50% operation of A-100, 10% operation of P-1200, P-1400, P-1300, and P-1500.

2 Average power usage includes, 100% operation of P-100A, P-200A, P-300A, P-400A, B-100, B-200A, B-300,

Electrical Load CalculationModified ISR SystemRaytheon Company


3 AOP System is assumed to operate feed pump, chemical pumps (sodium hydroxide and hydrogen peroxide),

G:\ENV\TF\901-1000\TF922\Reports\2010\RAPA 2010\Final FDEP RAPA\Appendix J\Tab #19\Raytheon Load Calc_MISR.xls ARCADIS

Tab 20

Modified ISR System – Operation and Maintenance Plan

Table J-8Start-up and Proof of Performance Monitoring Program

Modified ISR System Raytheon Company


Page 1 of 1

Analyte VOC 1,4-dioxane Bromide Bromate Iron TSS COD Alkalinity pH

USEPA Method 8260B 8260 SIM 300.0 300.0 200.7 SM 2540D SM 5220D SM 2320B Field

X X X X X X X X XMultiples samples throughout testing period.

Aeration Tank Effluent X X XMultiples samples throughout testing period.

Multi-Media Filter Effluent (T-500A/B/C) X X X X XMultiples samples throughout testing period. Sample will be used to monitor influent conditions to the air stripper.

X X XMultiples samples throughout testing period. Sample will be used to monitor influent conditions to AOP-100.

X X X X X Complete set for each tested condition.

X X X X X Complete set for each tested condition.

X X X X X XOne set for combined effluent. Results will be used to obtain approval for POTW discharge.

X X X During POTW discharge.

X X X During POTW discharge.

X X During POTW discharge.

Footnotes:USEPA - United States Environmental Protection AgencyVOC - Volatile Organic CompoundsCOD - Chemical Oxygen DemandIWD - Industrial Wastewater DischargeSIM - Selective Ion MonitoringPOTW - Publicly Owned Treatment WorksAOP - Advanced Oxidation ProcessLPGAC - Liquid-Phase Granular Activated CarbonMMF - Multi-Media Filters

(1) - IWD Permit Suite includes parameters specified by the City POTW discharge permit.

AOP-100 Intermediate

AOP-100 Effluent

Filter Feed Tank(2) (T-1400)

Catalytic Media Filter Effluent (T-1700A/B/C)

Multi-Media Filter Effluent (T-1800A/B/C)

(2) - Combined effluent from operating conditions evaluated during testing period will be stored in the Filter Feed Tank until analytical results indicate treated water is acceptable for discharge.For continuous operation, any time there is a significant change of greater than 30 percent of the present flow, and for AOP operating settings of greater than 25 percent of current process flow rate or chemical dose/feed rate, a new proof of performance testing will be conducted.

Secondary LPGAC Effluent(Treated Water Discharge)

Start-Up and Proof of Performance Testing

Air Stripper Effluent

Sample Location CommentsIWD Permit

Suite(1)

Influent to heat exchanger feed tank (T100)

G:\ENV\TF\901-1000\TF922\Reports\2010\RAPA 2010\Final FDEP RAPA\Appendix J\Tab #20\(1) Table J-8 (Tab #20)_Startup and proof monitoring.xlsx ARCADIS

Table J-9Process Monitoring Plan and Reporting Schedule

Modified ISR SystemRaytheon Company


Page 1 of 1

Year>

Month > 2 3 4 5 6 7 8 9 10 11 12

Week > 2 3 4 - - - - - - - - - - -

Days > 1 2 3 4 5 - - - - - - - - - - - - - -

Monitoring Plan - Sample LocationAnalytical

Suite(*)

Aeration Tank Feed Pump Discharge 1 X X X X X X X X X X X X X X X X X X X

Filter Feed Pump Discharge 2 X X X X X X

Post Multi-Media Filters 2 X X X X X X

Air Stripper Discharge Pump 3 X X X X X X X X X X X X X X X X X X X

Decant Pump Discharge 2 X X

Backwash Solids (to disposal) 2

RW-2 3 X X X X

RW-3 3 X X X X

RW-4 3 X X X X

RW-5 3 X X X X

AOP-200 Feed Pump Discharge 1 X X X X X X X X X X X X X X X X X X X

Post AOP-200 1 X X X X X X X X X X X X X X X X X X X

Post EQ Tank (2 Tanks) 4 X X X X X X X X X X X X X X X X X X X


X

X

X

X

X

X

1

1

Year 1 (Modified ISR System operations are expected to be 6 -12 months)

X


X

Post AOP-100 1 X X X X X X X X X X X X X X X X X X X

Filter Feed Pump Discharge 2 X X X X X X

Post Catalytic Media Filters 2 X X X X X X

Post Multi-Media Filters 2 X X X X X X

Intermediate GAC 3 X X X X

Post GAC (Final Effluent) 5 X X X X X X X X X X X X X X X X X X X

Post VPGAC (2 Vessels) 6 X X X X X X X X X X X X X X

X X X X X X X X X X X X X X X X X X X



AOP-100 Feed Pump Discharge (part of HiPOxTM) X X X X X X X X X X X X X X X X X X X

Filter Feed Pump Discharge X X X X X X X X X X X X X X X X X X X

Quarterly Reports A X X X X

X X X X X X X X X X X



X

X

X

X

Volume Measurements - Minimum Frequency

X

Aeration Tank Feed Pump Discharge

Air Stripper Discharge Pump

AOP-200 Feed Pump Discharge

Treated Water Discharge

Reporting

IWD Permit Periodic Compliance Reports B

Continuous

Footnotes:VPGAC - Vapor-Phase Granular Activated CarbonAOP - Advanced Oxidation ProcessLPGAC - Liquid-Phase Granular Activated CarbonPOTW - Publicly Owned Treatment WorksIWD - Industrial Wastewater DischargeUSEPA - United States Environmental Protection AgencyVOC - Volatile Organic CompoundSIM - Selective Ion Monitoring(*) - Analytical Suites:

1

2 USEPA Method 200.7 iron and Method SM 2540D total suspended solids.3 USEPA Method 8260B VOCs and USEPA Method 8260 SIM 1,4-dioxane.

4

5 Parameters specified by the City of St. Petersburg POTW - IWD Permit.6 Field measurement using Photoionization Detector (PID).

B Submittal to City of St. Petersburg. In accordance with IWD Permit, reports are due 30 days after the last day of the month in which the samples were collected.

A Submittal to the Florida Department of Environmental Protection (FDEP) within 60 days of the end of the reporting period.

USEPA Method 8260B VOCs; USEPA Method 8260 SIM 1,4-dioxane; USEPA Method 300.0 bromide/bromate; USEPA Method 200.7 iron.

USEPA Method 8260B VOCs; USEPA Method 8260 SIM 1,4-dioxane; USEPA Method 300.0 bromide/bromate; USEPA Method 200.7 iron, RCRA Metal Method 200.8.

G:\ENV\TF\901-1000\TF922\Reports\2010\RAPA 2010\Final FDEP RAPA\Appendix J\Tab #20\(2) Table J-9 (Tab #20)_Schedule.xlsx ARCADIS

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