TM001[1]

TM 001_Process_v1 080709.docx

TECHNICAL MEMORANDUM

To: Aladdin Shaikh, City of Bill Moorhead, City of Anaheim

From: Michael Moore, MWH

c.c: Team

Subject: Process Design of City of Anaheim Recycling Demonstration Project

INTRODUCTION The City of Anaheim provides potable water to approximately 350,000 people within a 50 square mile area. This results in a potable water demand of approximately 75,000 acre(AFY) and 64-80% of this demand is met from the production wells. In order to augment the water supply, the City is in process of building a 100,000 gpd tertiary wastewater treatment plathat will produce water that meets Department of Public Health (CDPH). recycling facility (WRF), which will consist of Membrane Bioreactor (MBR), ozodisinfection. This technical memorandum will describe the preliminary process design of this demonstration recycling plant.

PROJECT BACKGROUNDCurrently the City of Anaheim wastewater generated within the City’s service areas is collected and treated by Orange County Sanitation District’s (OCSD) Regional Wastewater Treatment Facilitiesact as a scalping plant by collecting and treating wastewater fronear the intersection of Oak Street and Lemon Street, just northwest of the City Hall West (CHW) parking structure. The effluent wastewater quality produced by the new WRF will comply with all applicable federal, state and lotreatment process will include an influent diversion pump station, fine screening, nitrification and denitrification tanks, membrane filtration system, ozonation system, UV disinfection system, odor control facility and a clearwell. The water recycling demonstration project will be built in two phases with ultimate treatment capacity of 130,410 gpd in order to produce 100,000 gpd of reclaimed waterproject will consist of designing and buildi

v1 080709.docx

TECHNICAL MEMORANDUM

, City of Anaheim

Bill Moorhead, City of Anaheim Date: August

, MWH Reference: 1007151

Process Design of City of Anaheim Demonstration Project

Document No: TM-00

The City of Anaheim provides potable water to approximately 350,000 people within a 50 square in a potable water demand of approximately 75,000 acre

80% of this demand is met from the production wells. In order to augment the water supply, the City is in process of building a 100,000 gpd tertiary wastewater treatment plathat will produce water that meets the Title 22 water quality requirements of California Department of Public Health (CDPH). MWH was selected by the City to design this

, which will consist of Membrane Bioreactor (MBR), ozoThis technical memorandum will describe the preliminary process design of this

PROJECT BACKGROUND of Anaheim does not have any water recycling facilities

wastewater generated within the City’s service areas is collected and treated by Orange County Sanitation District’s (OCSD) Regional Wastewater Treatment Facilities. The proposedact as a scalping plant by collecting and treating wastewater from the Lemon Street Trunk Sewer near the intersection of Oak Street and Lemon Street, just northwest of the City Hall West (CHW) parking structure. The effluent wastewater quality produced by the new WRF will comply with all applicable federal, state and local health and water quality requirements. treatment process will include an influent diversion pump station, fine screening, nitrification and denitrification tanks, membrane filtration system, ozonation system, UV disinfection system,

cility and a clearwell.

The water recycling demonstration project will be built in two phases with ultimate treatment in order to produce 100,000 gpd of reclaimed water

project will consist of designing and building a 70,955 gpd facility and Phase 2 of the project

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August 8, 2009

1007151

001

The City of Anaheim provides potable water to approximately 350,000 people within a 50 square in a potable water demand of approximately 75,000 acre-feet per year

80% of this demand is met from the production wells. In order to augment the water supply, the City is in process of building a 100,000 gpd tertiary wastewater treatment plant

Title 22 water quality requirements of California MWH was selected by the City to design this water

, which will consist of Membrane Bioreactor (MBR), ozonation and UV This technical memorandum will describe the preliminary process design of this

does not have any water recycling facilities and hence the wastewater generated within the City’s service areas is collected and treated by Orange County

proposed WRF will m the Lemon Street Trunk Sewer

near the intersection of Oak Street and Lemon Street, just northwest of the City Hall West (CHW) parking structure. The effluent wastewater quality produced by the new WRF will

cal health and water quality requirements. The treatment process will include an influent diversion pump station, fine screening, nitrification and denitrification tanks, membrane filtration system, ozonation system, UV disinfection system,

The water recycling demonstration project will be built in two phases with ultimate treatment in order to produce 100,000 gpd of reclaimed water. Phase 1 of the

gpd facility and Phase 2 of the project

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TM-001 Preliminary Process Design August 7, 2009

TM 001_Process_v1.docxocess_V1.docx 2 of 36

will increase the treatment capacity to 130,410 gpd. Table 1 shows the details of the flow-rates during each phase of the design. As shown, a fine screen will require a spray water flow-rate of 10,000 gpd to clean the screen and carry the screenings to the adjacent sewer. Since the treated water will be used as the spray/conveyance water, the treatment process units will be designed to treat this additional volume. Since MBR systems use membrane filtered water for backwashing and chemical cleaning of the membranes, approximately 15% of the treated water will be consumed for this function. In addition, waste activated sludge (WAS) volumes needs to be accounted for when calculating the gross production capacity of the process units. The gross treatment capacity of the treatment train was calculated by taking into account recycled water end user demand, fine-screen spray/conveyance water, backwash/cleaning water for membranes and WAS volume.

Table 1 – Estimated Flow-rates for the Water Recycling Plant

Flow-rates, gpd

Design Flow

Average Demand

Max Day

Demand

Screen Spray Water

WAS

MBR Backwash Water/CIP

Water

Total Average

Total Peak

Supplemental Potable Water

Required

Phase 1 50,000 58,000 110,000 10,000 1,700 9,255 70,955 121,700 50,745

Phase 2 100,000 107,000 193,000 10,000 3,400 17,010 130,410 206,400 75,990

For fine-screen, spray/conveyance water flow-rate needs to be maintained at 10,000 gpd Backwash/CIP water volume will be about 15% of the total volume produced by membranes

INFLUENT WASTEWATER CHARACTERIZATION In order to characterize influent wastewater, several grab and composite samples were collected over a period of two weeks. Since the MBR system will be designed as a scalping plant, flow-rate to the plant will generally remain constant throughout the day. The primary purpose of the sampling was to determine the variations in the contaminant loading rate to the plant. 24-hr time composite samples were collected to determine average, maximum month, maximum week and maximum day organic loading rates. Table-2 shows the water quality sampling plan that was implemented for influent wastewater characterization. The wastewater samples were collected from trunk sewer near Oak and Lemon Street. The project team awaiting final lab results for the last few samples.



Table 2 - Influent Wastewater Characterization Parameters

Grab 24-hr composite Diurnal (2-hr composite)

COD COD COD

TSS TSS TSS

VSS VSS VSS

TKN TKN TKN

TP TP TP

BOD BOD

NH3-N NH3-N

PO4-P PO4-P

Alkalinity Alkalinity

pH pH

ffCOD

sCOD

TDS

Results obtained from sampling and water quality analyses are summarized in Table 3. The maximum week concentrations for COD, TKN and TP were calculated at 972, 75 and 8.6 mg/L respectively based on results from 24-hr composite samples. Probability plots were prepared to determine the maximum week and maximum month concentrations for each contaminant. Figure-1 shows the probability plots for COD, BOD, TKN and TP concentrations measured in 24-hr composite samples. Once the project team receives additional results from other sampling events, these tables and plots will be updated accordingly. Influent wastewater quality results received from the lab are shown in Appendix A.

Table 3 – Influent Wastewater Quality based on 24-hr Composite Samples

BOD COD TKN NH3-N TP PO4-P pH

Total Alkalinity

as CaCO3 TSS VSS

Max Day 488 996 76 36 9 5 8 524 508 454 Max Week 474 972 75 36 8.6 4.7 7.9 520 499 443 Max Month 428 890 71 35 8.3 4.5 7.5 503 465 405 Minimum 160 390 49 13 6.0 2.6 6.3 310 99 84 Maximum 490 1000 76 36 8.7 4.8 8.0 525 510 456

Median 230 600 62 28 6.7 3.5 7.0 450 284 236



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Figure 1 – Probability Plot for Influent COD, BOD, TKN and TP Concentrations

TARGET EFFLUENT WATER QUALITY REQUIREMENTS The recycled water produced from the WRF will comply with the recycled water quality criteria specified in Title 22 and the Water Reclamation Requirements and Monitoring and Reporting Program issued by the Regional Board as part of the City’s Master Reclamation Permit. Table-4 specifies the effluent water quality criteria for the WRF.

Table 4 – Effluent Water Quality Requirements

Parameter Concentration Unit Standard BOD < 10 mg/L Annual Average

Nitrate-N 5 mg/L Monthly Average

Turbidity < 0.1 NTU Annual Average

Total Coliform 2.2 MPN/100 mL 7-day median

Total Dissolved Solids < 1,000 mg/L Annual Average

Total Suspended Solids < 10 mg/L Annual Average

Effluent from the WRF will be considered as disinfected tertiary recycled water. The later is defined per CCR Title 22, Section 60301.230 as a filtered and subsequently disinfected wastewater that meets the following criteria: a) The filtered wastewater has been disinfected by either:

(1) A chlorine disinfection process following filtration that provides a CT (the product of total chlorine residual and modal contact time measured at the same point) value of not

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less than 450 milligram-minutes per liter at all times with a modal contact time of at least 90 minutes, based on peak dry weather design flow; or (2) has been demonstrated to inactivate and/or remove 99.999 percent of the plaque forming units of F-specific bacteriophage MS2, or polio virus in the wastewater. A virus that is atleast as resistant to disinfection as polio virus may be used for purposes of the demonstration.

b) The median concentration of total coliform bacteria measured in the disinfected effluent does not exceed an MPN of 2.2 per 100 milliliters utilizing the bacteriological results of the last seven days for which analyses have been completed and the number of total coliform bacteria does not exceed an MPN of 23 per 100 milliliters in more than one sample in any 30 day period. No sample shall exceed an MPN of 240 total coliform bacteria per 100 milliliters. Title 22 also specifies sampling procedures. Sampling provisions per CCR, Title 22, Section 60321 include the following: a) The daily total coliform bacteria samples shall be taken from the disinfected effluent and shall be analyzed by an approved laboratory. b) Disinfected tertiary recycled water shall be continuously sampled for turbidity using a continuous turbidity meter and recorder following filtration. Compliance with the daily average operating filter effluent turbidity shall be determined by averaging the levels of recorded turbidity taken at four-hour intervals over a 24-hour period. Compliance with turbidity requirements pursuant to not exceeding an average of 2 NTU within a 24-hour period, 5 NTU more than 5 percent of the time within a 24-hour period and 10 NTU at any time; shall be determined using the levels of recorded turbidity taken at intervals of no more than 1.2-hours over a 24-hour period. c) Should the continuous turbidity meter and recorder fail, grab sampling at a minimum frequency of 1.2-hours may be substituted for a period of up to 24-hours. d) The results of daily average turbidity determinations shall be reported to the Regional Board. Reporting provisions per CCR, Title 22, Section 60329 include the following: a) Operating records maintained should include: at minimum, all analyses specified in the reclamation criteria, operational problems, plant and equipment breakdowns, any diversions of disinfected tertiary recycled water from the use site and any diversions of raw or partially treated wastewater from the plant, and all corrective or preventive action taken. b) Minimum reporting requirements to the Regional Board: results of daily total coliform bacteria monitoring, running 7-day median calculation, maximum daily coliform reading for previous month(s), minimum daily chlorine residual, results of four hour turbidity readings, average effluent turbidity (24 hour period), 95 percentile effluent turbidity (24 hour period), daily maximum turbidity reading, and daily CT compliance determinations.



PROCESS DESCRIPTION The proposed treatment process flow diagram shown in Figure-2 consists of MBR, ozone and UV treatment processes. The detailed layout of individual unit processes and a full copy of the process flow diagram, equipment list and preliminary chemical volume calculations are shown in Appendix B. Wastewater from the trunk sewer will be pumped to the WRF using chopper/grinder pumps in order to avoid any clogging in the transfer line. Wastewater will be treated using a fine screen at the WRF and distributed by gravity to the pre-anoxic zone of the MBR process. The MBR process will be designed as a 4-stage Bardenpho process with pre-anoxic and post-anoxic zones to achieve low effluent Total Nitrogen (TN) concentration. The facility will be designed with provisions for carbon addition in the post-anoxic zone in order to achieve low effluent nitrate concentration. As specified in the draft design report prepared by PBS&J, an external tubular configuration membrane system (commercial name DynaLift) will be used for filtration. This configuration offers several benefits specific to this facility. The DynaLift membrane system is located outside of the biological process tanks, which simplifies chemical cleaning as the membranes do not have to be removed from the biological process tanks. In addition, since the membrane modules can be drained and filled with cleaning chemicals, the chemical cleaning process does not require lifting the membrane modules out of the tank. Membrane filtered effluent will be collected in a 500-gallon equalization tank that will serve as a feed tank to the ozonation system. The purpose of providing the equalization tank is to allow the use of booster pump to feed the ozonation system and to allow for continuous flow to the ozonation system while the membranes are being backwashed. Since the membrane effluent will have a pressure of less than 2 psi, a booster pump will feed the membrane treated water to the ozonation system, where the water will be treated further to remove residual color, odor and to provide disinfection. The selected ozonation system is Title 22 approved system. It will be designed to deliver sufficient dose and contact time to achieve effluent water quality standards that comply with Title 22 water quality standards for tertiary disinfected water. Ozonated effluent will then be passed through the UV unit, which will serve as a secondary barrier against microbial contaminants. Each of the unit treatment processes will be described in detail in the following sections. Each unit process will be equipped with instrumentation and control devices (factory supplied panels) provided by the vendors and communication from each unit process will be set up with the SCADA system.



Figure 2 - Proposed Process Flow Diagram for the Water Recycling Facility

FINE SCREENING Membrane clogging due to hair and fibrous materials can result in loss of membrane area and productivity of the membrane filtration system. In order to avoid this problem, raw wastewater is always filtered by a fine screen before being fed to the bioreactors and the membrane modules. The project team will use a center feed perforated rotating drum screen with openings of 1 mm.

Design Specifications and Power Requirements The proposed drum screen is manufactured by Waste Tech, based in Spartanburg, SC and the specifications of screen are presented in Table 5. The detailed specifications for the fine screen equipment are shown in Appendix C.



Table 5 – Specifications for Fine Screen

Parameter Value

Manufacturer Waste Tech Inc.

Model RDS-OF-30

Type Rotating Perforated Drum Screen

Perforations (mm) 1 mm

Length x Width x Height (feet) 5.9 x 2.9 x 4.3

Power requirement, HP (kW) 0.5 (0.37)

Design flow-rate (gpd) 150,000

Spray water flow-rate (gpm) 15

Spray water pressure (psi) 60

The Waste Tech rotating drum screen incorporates a feed distribution head box for effective flow distribution and an internally screw auger with individual dewatering cells which dewaters and transports the separated solids out of the drum. Depending on the size of the screen the drum is direct drive, cog fear drive or trunnion driven. The influent to the drum is distributed over a large area of the drum to ensure efficient use of the drum open area. As the drum rotates, fluid passes through the perforations and the solids are removed and dewatered from the drum by the fixed transport screw. Since the enclosed perforated drum screen has no seals or slots, all flow must pass through the perforations, which prevents bypass or carryover of solids to the downstream process. An automatic Integral Overflow System (IOS) within the screen equipment provides an alarm indication when screen is clogged in order to prevent raw wastewater from contaminating the filtered effluent. Separate overflow connection allows raw wastewater to be diverted to the sewer in the event of screen being clogged. Treated water from the clearwell will be used periodically (usually every 15-20 minutes for 10-15 seconds) as spray water for the spray system to wash away biological slimes, grease, etc. A mechanical brush continuously cleans the outside of the screen whereas the spray water is used as a secondary mechanism to clean the drum. The system shall be equipped with controls to provide both manual and automatic operation. Controls shall be housed in a NEMA 4X enclosure complete with HOA Switch for screen drive, ON/OFF Lights, Fail Lights, Overflow Alarm Light, Main Disconnect with panel mounted disconnect lockable in the off position. All necessary starters, breakers, fuses, timers and relays for Automatic and Manual Control.

Scope of Supply & Equipment Warranty The supplier shall furnish one RDS-OF-30 perforated drum screen with NEMA 4X controls, spares, anchor bolts, site service and provide delivery to site. The supplier shall also furnish, boxed for storage and clearly marked, the following spare parts: two complete trunnion wheel assemblies. The screen equipment is warranted for 2 years after installation.



MEMBRANE BIOREACTOR Membrane Bioreactor (MBR) process is an advanced wastewater treatment process which uses membranes for solids separation instead of clarifiers. Use of membrane for solids separation allows the process to operate at high MLSS concentration (8,000-12,000 mg/L) irrespective of sludge settling characteristics and provides superior effluent water quality. Operation at high MLSS also reduces the required bioreactor volume and use of membrane replaces the need for clarifiers and media filters thereby reducing the overall footprint of the plant. Typically, a well operated MBR process with intact membranes will produce effluent with BOD and TSS below detection levels and turbidity of <0.2 NTU. Since MBRs are usually designed to operate at higher sludge retention times (SRT), effluent is fully nitrified and effluent ammonia concentrations are maintained at < 0.5 mg/L-N. MBR process can be categorized as either submerged or external depending on if the vacuum or pressure is used to produce permeate. Submerged MBR systems are more frequently used in municipal wastewater application since external MBR systems are perceived to be more energy intensive. The external MBR process requires a higher recirculation flow-rate for cross-flow pumping to provide enough hydrodynamic shear for membrane scouring. But high flux operation and recent advances in external MBR systems such as air-lift assisted cross-flow pumping have made external MBR systems competitive to submerged MBR systems. External MBR systems also offer an advantage in ease of cleaning since it is not required to lift the module out of the membrane tank for chemical cleaning.

BIOLOGICAL PROCESS CONFIGURATION MBR systems are usually designed using the MLE process with dual recycle configuration. Since the recycle stream from the membrane tank has high dissolved oxygen (DO) concentration (3-5 mg/L), it is usually diverted to aeration tank instead of to the anoxic tank. Denitrification is then achieved by having an internal recycle from aeration to anoxic tank. Recycle flow from aeration to membrane tank is dictated by the desired MLSS concentration in the membrane tank, which is usually 10,000-12,000 mg/L. Alternatively, when designed with single recycle configuration, a larger anoxic tank volume is required to quench the DO from the membrane to anoxic recycle stream. The project team proposes to install a MBR process with single recycle configuration with allowance to split the membrane recycle flow to aerobic and pre-anoxic zones. Screened influent will pass to the pre-anoxic tank to utilize influent BOD for denitrification process. Mixed liquor will flow by gravity from the pre-anoxic tank to the aeration tank for nitrification. Nitrified effluent from the aeration tank will then flow by gravity to the post-anoxic tank for additional denitrification. The process will be designed with provision for addition of MicroCg (agriculturally derived carbon source) to the post-anoxic zone to achieve low effluent nitrate concentration (< 5 mg/L NO3-N).

Denitrified wastewater from the post-anoxic tank will be pumped to the membrane tank for filtration. The recycle flow-rate from the post-anoxic tank to the external membrane system will



vary from 12-15 times the influent flow-rate. Since the recycle stream from the membrane tank has high DO concentration (3-5 mg/L), provisions will be made to split the membrane recycle flow such that the recycle flow can be diverted to either pre-anoxic tank or aerobic tank or both. Such provision will allow maintaining anoxic conditions in the pre-anoxic tank by diverting part of the membrane recycle flow to aerobic tank if DO concentration in the recycle stream is high. The biological process is designed with an SRT of 20 days and detailed calculations for pumps, blowers and mixers sizing are shown in Appendix D. A BioWin model was prepared to predict effluent water quality and bioreactor conditions at steady state as well as to simulate different contaminant loading conditions. Results from BioWin modeling are also shown in Appendix D. The results shown from BioWin modeling are currently based on maximum week concentrations only determined from the 24-hour composite samples. Designing to the maximum week loading will ensure meeting the maximum month requirement for effluent nitrate. The project will further simulate diurnal fluctuations in organic loading rate when the results for the diurnal sampling are received. Model runs for annual average, maximum month and maximum day loadings will also be verified at that time. Based on the steady state analysis, the proposed biological process design will achieve effluent nitrate concentration of < 5 mg/L-N on a monthly average basis.

Table 6 – Biological Treatment Process Design Parameters

Parameter Value Design SRT (days) 20 Design Volumes

Pre‐anoxic 26,030 Aerobic 43,926 Post‐anoxic 17,896

Design HRT, Total (hours) 16 Aerobic MLSS (mg/L) 9,000 Process Air (scfm) 400 Membrane Scouring Air (scfm) 130



Design Specifications and Power Requirements Design specifications for biological process equipment and membrane filtration equipment are shown in Table 7 and detailed calculations are shown in Appendix D.

Table 7 – Mixers and Blower Design Specifications

Parameter Value Pre-Anoxic Tank Submersible Mixer

Wetted Volume (ft3) 1,791 Mixer Design Power Input (HP/1000 ft3) 1 Selected Motor Size (HP) 3.0

Post-Anoxic Tank Submersible Mixer Wetted Volume (ft3) 1,176 Mixer Design Power Input (HP/1000 ft3) 1 Selected Motor Size (HP) 2.0

Process Blower Process Air Flow-rate (scfm) 200 Power, ideal (HP) -5 Selected Motor Size (HP) 7.5

Membrane Feed Pump Design Flow-rate (gpm) 1,025 System Head (ft.) 21 Selected Motor Size (HP) 10.0

Membrane Permeate Pump Design Flow-rate (gpm) 60 System Head (ft.) 33 Selected Motor Size (HP) 1.0

Membrane Backwash Pump Design Flow-rate (gpm) 616 System Head (ft.) 95 Selected Motor Size (HP) 25.0

Membrane Scouring Air Blower Process Air Flow-rate (scfm) 60 Power, ideal (HP) -2 Selected Motor Size (HP) 3.0



MEMBRANE FILTRATION In accordance to the draft engineering report prepared by PBS&J (June 8, 2009), the membrane system to be specified is the DynaLift membrane system provided by Parkson Corporation (Fort Lauderdale, FL). As part of the preliminary process design, the project team requested Parkson Corporation provide the following information associated with the DynaLift system:

• Scope of supply • equipment specifications, • membrane design criteria, • warranty information, • list of reference plants.

As part of this request, the project team provided Parkson influent water quality and effluent water goals, along with the preliminary biological process design parameters. During a follow up conversation with Parkson’s MBR Group Manger, the project team was asked to contact Norit X-Flow (Enshede, Netherlands) to obtain the requested information regarding the DynaLift membrane system. Norit X-Flow is the membrane manufacturer and developer of the technology (commercial name AirLift MBR) used in the DynaLift membrane system. After further discussions with Norit, it was explained to the project team that Parkson is no longer an authorized supplier of the DynaLift technology. Based on further discussions with Norit X-Flow, the project team was informed that Dynatec Systems, Inc. (Burlington, NJ) was the original and current authorized representative of the DynaLift technology in the United States. Dynatec has been providing membrane systems for wastewater treatment applications for 30 years with many small capacity (<200,000 gpd) industrial and municipal DynaLift MBR systems currently operating in the United States. Based on discussions with Dynatec, the DynaLift system design they provide is similar to Parkson’s design with the major difference being the feed and product header configuration. After speaking with the Dynatec representative and qualifying their experience and knowledge of the municipal DyanLift MBR technology, the project team has selected this firm to provide the membrane equipment for the City of Anaheim MBR facility. Table 8 summarizes Norit’s MBR plants currently operating in the United States and overseas.



Table 8 Municipal MBR Plants Utilizing X-Flow Tubular Membrane Modules

Location System Supplier Plant Name Start Up Capacity (MGD)

Naples, FL, United States

Parkson Port of the Islands WRF

2007 0.15

Delaware, United States

Parkson Millsboro WRF 2009 1.0

North Carolina United States

Parkson Stump Point WRF 2009/2010 0.1

Maryland, United States

Dynatec Glen Meadows 2004 0.12

Michigan, United States

Dynatec Saddle Ridge 2003 0.03

Michigan, United States

Dynatec Grand Traverse 2005 0.10

Dubai UAE Veolia Palm Jumeirah 2007/2008 4.5 Vienna, Austria

VA Tech NA 1999 0.03

Ootmarsum, Netherlands

NMT NA 2005/2006 1.0

Tables 9, 10 and 11 provide preliminary information received from Norit and Dynatec related to the membrane specifications, membrane system configuration, and membrane design parameters, respectively associated with the DynaLift technology for the given application. Appendix E provides general drawings and preliminary flow diagrams for the DynaLift membrane system.



Table 9 - Membrane Specifications

Parameter Value Membrane & Module Manufacturer & Model Norit ‐ X Flow (38 PRV, F4385) Configuration Tubular / External Nominal Pore Size (micrometer) 0.03 Absolute Pore Size (micrometer) 0.05 Inner Tube Diameter (mm) 5.2 Membrane Material Polyvinylidene Fluoride (PVDF) Active Membrane Area per Module (m2) 29 Maximum Backwash Pressure (bar) 1 Trans‐Membrane Pressure Range (bar) 0.07‐0.34 Maximum Temperature (Deg C) 40

pH Range 2‐10

Table 10 - Membrane System Configuration

Parameter Value Membrane Skid Configuration (Phase 1) Number of skids 1 Number of installed UF Modules per skid 10 Max. Spare Modules per skid 2 Gross Product Flow, Train A (gpd) 80000 Skid footprint, ft (LXWXH) 10.2X2.6X14.8 Membrane Skid Configuration (Phase 2) Number of skids added 1 Number of installed UF Modules per skid 10 Max. Spare Modules per skid 2 Gross Product Flow, Train A/Train B (gpd) 65,000/65,000 Skid footprint, ft (LXWXH) 10.2X2.6X14.8



Table 11 - Membrane Design Parameters

Parameter Value Max Gross Flux (GFD) 25‐30 Filtration Time (min) 9 Backwash Duration (s) 15 Backwash Flow per module (gpm) 44 Drain Sequence Frequency per skid (hr/DS) 1 Drain Sequence Duration per skid (s) 30 Drain Volume per module (gallons) 42 Chemical Enhanced Backwash Frequency per skid (days/CEB) 7 Chemical Cleaning with Re‐circulation Frequency per skid (day/CCR) 30 Recovery during max. flux (%) 84.3

Airlift (SCFM) per module 6

Scope of Supply & Equipment Warranty An example of a typical pro-rated lifetime membrane warranty provided by Norit is provided in Appendix E. In general, the terms of the warranty replace a membrane element found to be defective in the first 12 months at no cost to the owner. However, membranes identified to be defective after 12 months are replaced at a prorated charge calculated as follows: Pro-rated membrane replacement = New Membrane Cost x Months of Beneficial Use Total Membrane element warranty period (36 months) The warranty is also subject to a number of conditions related to the operation and performance documentation. In addition to membrane warranty, Dynatec will provide manufacturer warranty on all equipment associated with the membrane system (i.e. blowers, pumps, valves, chemical dosing systems, gauges, etc.). A complete scope of supply, equipment list, and budgetary cost estimate for the DynaLift membrane system is currently being prepared by Dynatec and will be incorporated into the overall engineering estimate of the plant in the final TM.



OZONATION Ozonation is an alternative disinfection technology for reuse applications. Like chlorine, ozonation is also considered a chemical disinfection process. However, ozone is a much stronger disinfectant than chlorine, and does not produce DBPs such as trihalomethanes (THMs) and haloacetic acids (HAAs). Other DBPs may be formed from ozonation (bromate), but this process depends on the bromide concentration in the water (expected to be low in this case) may be successfully controlled by pH adjustment and peroxide addition. For long time, UV has dominated the disinfection market due to the very short contact times required to achieve the desired inactivation goals. Ozone, on the other hand, is a gas sparingly soluble in water, which requires longer contact time to dissolve and become effective for disinfection. For this reason, the traditional ozonation process requires large contact basins with multiple contact chambers. Ozone is bubbled in the first 2-3 chambers and additional contact/reaction time is provided by the subsequent chambers. The contact time (CT) requirements for disinfection are met when the effluent leaves the last chamber. However, for applications of the size required at the WRF, alternative ozonation systems are available. Pressurized plug-flow tubular reactors, where ozone can be added in sequential steps, allow ozone to dissolve faster in water, and to utilize it more efficiently than using contact basins (i.e., by increasing dissolution in water, ozone losses to air are reduced). Under these conditions, ozone can compete effectively with UV to achieve the required disinfection goals for recycled water. Other advantages of ozonation over the UV process include providing higher dissolved oxygen (DO) to the effluent, as well as leaving a measurable residual to confirm the required disinfection goals, both advantageous conditions for recycled water applications. Successful implementation of this technology for Title 22 applications has been reported by Applied Process Technologies (APT) and their product known as the HiPOx® reactor. Data from prior applications indicate that when the objective is achieving disinfection equivalent to the irradiation of a 100 mJ/cm2 UV dose, the HiPOx reactor can achieve this same objective in a more cost effective manner. To accommodate the plant extension during the second phase of this project, the capacity of the proposed reactor can be easily doubled to 100,000 gpd (nominal) by using a pipeline array extension and an extra ozone generator. An extra generator may be also added later for redundancy. The selected ozone reactor has two more important advantages over UV:

• Substantial improvement to effluent water quality, especially with respect to odor and

color. • Removal of trace contaminants, such as endocrine disruptors (EDCs), and pharmaceutical

and personal care products (PPCPs), especially when used in conjunction with hydrogen peroxide for advanced oxidation (AOP)



Design Specifications and Power Requirements The design specifications for APT’s HiPOx ozonation system are shown in Table 8. Detailed specifications and calculations for the ozonation equipment are shown in Appendix F.

Table 8 – Specifications for APT’s HiPOx Ozonation System

Parameter Value Manufacturer & Model APT

Model HiPOx

Design Flow-rate (MGD) 0.13

Expected Ozone Demand (mg/L) 4.0

Desired Ozone Residual (mg/L) 0.5

Contact Time (mg-L/min) 1.0

Total Ozone Dose - Transferred (mg/L) 5.0

Total Ozone Requirement - daily, with contingency (ppd) 5.4

Liquid Oxygen Requirements (ft3/d) 1.4

Number of Ozone Generators (including standby) 2

Power Requirements (kW) 15

Scope of Supply and Equipment Warranty The following equipments will be provided as skid-mounted system, pre-assembled, pre-tested, and fully automated as much as possible:

• Ozone dissolution system (injection point, mixers) with pipeline contactor • Influent flow conveyance (pump, flow meter, manual control valve) • Ozone generator (air-cooled ozone generator) • Control panel with PLC/OIT • Off-gas collection system (vent valve, ozone destruct) • Dissolved ozone residual analyzer

ULTRAVIOLET DISINFECTION The TrojanUVFit™ is an UV system from Trojan Technologies for wastewater reuse and high level disinfection applications. The TrojanUVFitTM system is ideal for piped systems and delivers effective chemical-free disinfection in a pressurized reactor. This configuration is well-suited for media or membrane filtered effluent where effluent is already under pressure. The UV system uses low-pressure high intensity amalgam lamps to provide an energy-efficient solution.



The proposed UV system has a compact reactor design which minimizes footprint and headloss while ensuring that maintenance activities such as lamp replacement are is performed quickly and safely. Design Specifications and Power Requirements The design specifications for the proposed UV disinfection system are shown in Table 9 and detailed information/specifications for the proposed UV system are shown in Appendix G. Since the ozone system will be designed for both color removal as well as disinfection, the UV system will be designed and operated at a minimum dose. The UV transmittance (UVT) is expected to be higher (80%) since the water is treated with membrane and ozone before being passed to the UV system. In the event of membrane integrity failure or ozone system failure, the WRF effluent pumps (to the clearwell) will be turned off. Since the MBR and ozonation system (combined) will be designed to meet Title 22 standards, the UV system will be operated at a minimal dose of 40 mJ/cm2.

Table 9 – Design Specifications for TrojanUVFit UV Disinfection System

Parameter Value Manufacturer Trojan Technologies

Model TrojanUVFit - 04AL20

UV Transmittance 80% minimum

Total Suspended Solids (mg/L) 5

Design UV Dose (mJ/cm2) 40

Number of SS316L Reactors 1

Number of Lamps per Reactor Chamber 4

Sleeve Wiping Automatic Mechanical

Power Requirements (kW) 2

Scope of Supply & Equipment Warranty

• Trojan Technologies warrants all components of the system (excluding UV lamps) against faulty workmanship and materials for a period of 12 months from date of start-up or 18 months after shipment, whichever comes first.

• UV lamps purchased are warranted for 12,000 hours of operation or 3 years from shipment, whichever comes first. The warranty is pro-rated after 9,000 hours of operation. This means that if a lamp fails prior to 9,000 hours of use, a new lamp is provided at no charge.

• Electronic ballasts are warranted for 5 years, pro-rated after 1 year.



ODOR CONTROL The new WRF is intended to be a high profile demonstration project. The facility is surrounded by high use public buildings and open spaces. Thus the complete capture and treatment of odors and the prevention of any foul odors from the facility impacting the public is an essential part of making the WRF successful. All odor control systems contain the following elements:

• Ventilation of working areas: • Capture and collection of foul air; • Treatment of the air to remove odorous compounds; and • Exhaust of the treated air.

All four of these elements play a key role in preventing odor impacts to the public.

Regulatory Requirements The following laws and agencies regulate various portions of the odor control and emission process:

• City of Anaheim municipal code – odorous emissions • South Coast Air Quality Management District (SCAQMD) – emissions • National Fire Protection Agency (NFPA) – ventilation of process areas; and • Occupational Health and Safety Administration (OSHA) – ventilation of worker occupied

areas. Chapter 18.48 of NFPA Standard 820 governs operations of recycling facilities. Section 060 paragraph 140 states the following: “All uses shall be conducted in a manner so as not to be objectionable by reason of noise, odor, dust, fumes, smoke, vibrations, or other similar causes.” The NFPA Standard 820 provides standards of ventilation established to prevent fire and explosion within wastewater treatment facilities. The ventilation rates for various areas of WWTPs depend on the type of electrical equipment used in those areas. The Anaheim WRF facility will be completely enclosed in a single building. The anoxic, aeration, and post anoxic areas will be in tanks below the building and there will be openings between the areas the rest of the building. The NFPA ventilation standard for enclosed aeration zones is 12 air changes per hour if the electrical equipment has a National Electrical Code (NEC) rating of Division 2 Class I Group D. If the equipment is rated Division 1 there are no ventilation requirement. While the mixing equipment in the anoxic zones may be Division 1 rated, all of the equipment in the working areas of the building will be Division 2. Thus a minimum ventilation rate of 12 air changes per hour throughout the building may be required. NFPA also has standards for the odor control areas. With Division 2 electrical equipment a minimum of six air changes per hour in the areas out to three feet surrounding any potential leak.



Because the odor control area is not isolated from the rest of the facility the12 air changes per hour standard discussed above will govern. OSHA does not provide specific ventilation standards but rather sets limits for worker exposure to specific compounds. In wastewater treatment applications hydrogen sulfide is the most common among these compounds. Worker exposure to hydrogen sulfide is limited to 20 ppm. Most of the process equipment such as the screen and MBR are self contained equipment and will be ventilated. The anoxic, aeration and post anoxic areas are tanks below the floor of the building. The only access to these areas will be through hatches in the floor. This configuration of the tanks and the limited access means these areas must be governed by the rules of confined space entry. Confined space entry requires workers to have respirators and thus the OASHA limits for concentration of hydrogen sulfide do not apply in these areas. As confined spaces these areas will have to be equipped with the following gas detectors and associated alarms located at the entrances:

• Hydrogen sulfide; • Oxygen; and • Methane.

Ventilation and Emission Capture/Collection In addition to the regulatory requirements discussed above there are other considerations in the sizing and arrangement of the ventilation and air collection systems. The foremost concern at the WRF is to prevent odors from escaping the facility and impacting the public in the surrounding areas. Process equipment in the building such as the inlet screen and MBR will be self contained and ventilated. The equipment will have small maintenance hatches that will need to remain closed for operation. Each anoxic and aeration tank will have a single three by three foot access hatch. Each post anoxic tanks will have two of these hatches. At least one of these hatches for each tank will need to be open occasionally and possibly be left open for extended periods. It is vital that enough air be pulled down through the hatches when they are open to prevent odors from escaping. For hatches located inside a building away from suction caused by wind passing over the hatches a capture velocity of 100 ft/min will be sufficient to prevent odor from escaping the tanks. Table 10 outlines the ventilation requirements for the various process equipment and areas as well as the sizing criteria. Detailed sizing calculations for odor control are shown in Appendix H.



Table 10 – Ventilation Requirements for Various Process Equipments

Area/Equipment Sizing Criteria Required Airflow

Inlet screen 12 ACH inside screen 11 cfm Anoxic Tank 1 and 2 100 ft/min capture velocity

across the opening of one hatch per tank

1,800 cfm

Aeration Tanks 1 and 2 100 ft/min capture velocity across the opening of one hatch per tank plus the maximum amount of aeration air added to each tank

1,800 + 400 = 2,200 cfm

Post Anoxic Tanks 1 and 2 100 ft/min capture velocity across the opening of one hatch per tank

1,800 cfm

MBR Scour air 130 cfm Odor Control Area 6 ACH in the area surrounding

the collection fans and treatment equipment (a total foot print of 26’ x 20’ x 10’ high)

520 cfm

Total 6,461 cfm

The total volume of the building is approximately 254,000 ft3. The required airflow to achieve 12 air changes per hour in the building is 4,875 cfm. The air collected from the process areas will need to be gathered from the building in order to provide the capture velocity across the hatch openings. Thus the process air collection of approximately 6,500 cfm is greater than the minimum 4,875 cfm required for 12 air changes per hour in the building. The odor control system will be sized for 6,500 cfm which will provide approximately 16 air changes per hour in the building. In addition to the amount of air collected the location of the inlets for makeup air and the collection points are important. The following are general good engineer practice when locating makeup air inlets and foul air collection points: Whenever possible enclose the odors and collect foul air as close to the odors source as possible;

• Drag fresh air past worker areas; • Avoid pulling foul air past worker areas; and • Avoid short circuiting the collection of odors by placing the collection port too close to

the makeup air inlet. In the proposed ventilation scheme fresh air will be introduced into the building through roof mounted inlets. This air will become the makeup air for the tanks and will be introduced to the tanks through louvered intakes located near the hatches. Air will be collected from the tanks at the opposite end of the tanks from the inlets. Air will also be collected from the inlet screen and the MBR directly. Air will be collected from near the floor in the odor control area. This



collection point will be located as far away from the overhead door as possible. This scheme incorporates all of the four elements listed above and will provide vital capture of odors thus preventing them from escaping the facility when doors or hatches are opened.

Foul Air Treatment There is a wide variety of odor control technologies available but these can be grouped into the following general types:

• Absorption filters – carbon and iron sponge filers; • Biofilters – organic and inorganic media filters; • Biotrickling filters and bioscrubbers; • Wet chemical scrubbers; • Chemical dosing of the wastewater; and • Regenerative thermal oxidation.

Of these technologies biotrickling filters, bioscrubbers, wet chemical scrubber and chemical dosing of the wastewater can be eliminated from consideration. Biotrickling filters, bioscrubbers and wet chemical scrubbers generally target hydrogen sulfide with some removal of other odorous compounds. Thus they do not provide the highest level of odor reduction. In this application and location the highest level of odor removal is essential. In addition chemical scrubbers require frequent delivery of caustic chemicals that require operator training and special handling. Given the close proximity to the high traffic public areas such chemical deliveries would be impractical and undesirable. Several different chemicals can be dosed into the wastewater flow to prevent the formation and release of odorous compounds. These chemicals generally target hydrogen sulfide generation but will reduce other sulfide compounds depending on the chemical used. However, as with wet chemical scrubbers, many of these compounds are corrosive or otherwise harmful and require care in handling and storage. Again the proximity of the facility to the general public makes the delivery, storage and use of such chemicals impractical and undesirable.

Treatment Technologies

Iron sponges can also be eliminated from consideration. These filters collect hydrogen sulfide and leave other odorous compounds in the air stream thus not achieving the maximum odor removal. Regenerative thermal oxidizers (RTOs) are very effective in removing a wide range of odorous compounds, however they are seldom used in wastewater application. The foul airstream is wet and relatively cool. The energy required to achieve compound destruction in an RTO makes their cost of operation prohibitive. The two remaining technologies are biofilters and carbon filters. Both are very effective at removing odors but they function very differently. In a biofilter odorous compounds are absorbed into a thin moisture layer on the surface of the media. The compounds are then oxidized by microorganisms in the moisture layer. The byproducts are mineral salts, carbon



dioxide and water. Depending on the material used for the media there can be a residual odor from the media itself. This is true of organic media biofilters that are composed mostly of wood or bark nuggets. Biofilter require a relatively large footprint compared to other control technologies. For the Anaheim WRF a minimum footprint of approximately 1,100 ft2 would be required. In addition the media must be replaced every three years and this generally requires the use of earth moving equipment. This type periodic operation is not well suited to the WRF location. In an activated carbon filter odorous compounds are adsorbed onto surface of the carbon media. The media has high porosity which provides an enormous amount of available adsorption surface area. There are three generic types of carbon media, Plain carbon also known as virgin carbon, caustic impregnated carbon and catalytic carbon. Both catalytic and impregnated carbon are treated to improve their ability to remove hydrogen sulfide and thus extend the life of the carbon in airstreams with high concentrations of hydrogen sulfide. Plain or virgin carbon is better suited for light hydrogen sulfide loading and higher VOC removal. Hydrogen sulfide is normally found in the early stages of wastewater treatment. At the WRF most of the hydrogen sulfide would be expected to be released from the inlet screen and the anoxic tanks. These areas represent about 30% of the total air collected in the facility. Thus there is ample dilution of any hydrogen sulfide collected. For this application where maximum odor reduction is required, removal of the greatest number of volatile compounds will provide the best overall odor removal. There are several advantages to carbon filters. They have a small footprint, and are completely enclosed in a vessel. The major drawback to carbon filters is the need to frequently replace the media. However the replacement process is relatively neat compared to that of a biofilter. Table 11 and Table 12 list the advantages and disadvantages of biofilters and carbon filter respectively:

Table 11 - Advantages and Disadvantages a biofilter

Advantages Disadvantages Less frequent media replacement Highly effective odor removal Inexpensive operation

Large foot print Residual odor from media Heavy equipment required for media replacement and replacement is messy More frequent oversight required for irrigation and weed control

Table 12 - Advantages and disadvantages of the carbon filters

Advantages Disadvantages Smaller footprint Highly effective odor removal Completely enclosed Easier and cleaner media replacement

More frequent media replacement Very high media cost but less media required



Based on the above analysis the small footprint, enclosed vessels and the neater maintenance make the carbon filter the clear choice for the Anaheim WRF. Exhaust of Treated Air The air exhausting from the carbon filters will be highly treated and have very little odor. However, it must be noted that no odor control system can produce 100% odor free air 100% of the time. There can be upsets in operation normal reductions in removal efficiency just before the media must be replaced. There is a backup unit in place to provide continual treatment during maintenance operation.

The odor control system will be a carbon filter system with plain or virgin carbon media. The system will treat 6,500 cfm. The system will have the following components:

• One duty carbon filter and one standby unit with each unit 10 feet in diameter. The filter will have either two horizontal media beds each three feet thick as shown in Figure 1.1 or a radial bed filter as shown in Figure 1.2.

• One duty fan and on standby fan to collect the foul air and send it through the carbon filter. The fan will be rated for 6,500 cfm at16 in.w.c.

• Due to the limited space available the collection fans will be equipped with inlet boxes to reduce turbulence entering the fan that would otherwise reduce the efficiency of the fan operation.

ELECTRICAL AND CONTROL SYSTEMS This section describes the electrical and control systems for the WRF building.

Incoming Power to the Water Recycling Facility MWH and the City of Anaheim Electrical Staff shall coordinate the work to provide an incoming power feed to the new Water Recycling Facility (WRF) adjacent to City Hall East. The work shall consist of the design and construction of conduits, wires, Motor Control Center, fittings and other necessary appurtenances to furnish an incoming power feed to the site that is in compliance with local City standards and the NEC. The incoming electrical power feed shall originate from the existing Civic Center Main Switchgear located south of the WRF. A 400 ampere circuit breaker, matching the existing manufacturer, shall be installed in the available space within the Civic Center Main Switchgear. The power wiring shall utilize an existing 5-inch conduit that originates from the Civic Center Main Switchgear and runs to the Maintenance Room located in the Parking Structure east of City Hall East. MWH and City of Anaheim Electrical Staff shall determine the exact routing of this existing conduit and coordinate the location of where to intercept this raceway to continue its routing to the new WRF. The incoming power feed shall be terminated at a Motor Control Center (MCC) located within the WRF. The MCC shall be enclosed in a non walk-in NEMA 4X enclosure to prevent the possibility of exposure to water and/or other harsh chemicals that may



be present in the building. The incoming power feed, designed by MWH and coordinated with City of Anaheim Electrical Staff, shall power this MCC, which in turn, shall deliver power throughout the WRF and the new Diversion Structure. MWH shall coordinate the proper number and size of breakers, starters and panel boards provided within this MCC. Bus size and approximately 20 percent extra space for future breakers and starters shall be designed to account for future loads at the WRF. Power for the site shall be distributed from the MCC (MCC) in the Electrical Room of the new WRF. Electric power shall be distributed from the MCC to all equipment, valves and instruments located in the WRF and new Diversion Structure. The equipment manufacturers shall provide local control panels with their equipment which house the starters for their respective equipment if possible. Otherwise starters and controls for this equipment shall be located within the MCC. The MCC shall distribute auxiliary power to the WRF via a step down transformer and 120/208, 3 phase lighting panel located within the MCC.

Communications to the WRF All controls shall be hardwired or networked to a PLC within the WRF. This PLC shall be tied into the existing City’s communication system via fiber optic using utilizing TCP/IP (Ethernet) Protocol. The City of Anaheim already has an existing fiber optic network infrastructure. The probable location for network interface will be to City Hall East which will be adjacent to the WRF. Coordination with the City of Anaheim Telecom Group shall determine the exact location for interfacing with the existing ethernet fiber optic system. The fiber optic system shall provide two way communications with City Hall, Lenain Water Treatment Plant and other locations as required. The WRF will be monitored remotely by City staff at the Lenain Treatment Plant via SCADA. Alarms and control notifications will be sent to the Lenain Treatment Plant and elsewhere as required.

Power Feed to Diversion Structure Power to the Diversion Structure shall originate from the MCC within the WRF. The Variable Frequency Drives and controls for these pumps shall be housed within this MCC. Each pump within the diversion structure shall have a power feed in a 1” conduit from the Motor Control Center to a local disconnect switch at the manhole. These local disconnect switches shall be rated NEMA 4X due to the outside environment where they will be mounted. Another 1” conduit shall be routed from the local disconnect switch to each pump within the diversion structure.

Communications to the Diversion Structure

A PLC shall be provided at the Diversion Structure for communication interface with the WRF. The City has standardized on General Electric RX3i PLCs which are capable of direct Ethernet interface. All process parameters and alarms at the Diversion Structure shall interface with City’s network via an Ethernet fiber optic link.

Power Feed to Booster Pump at City Hall West



MWH and the City of Anaheim Electrical Staff shall coordinate the work to provide power to a small booster pump. The booster pump is responsible for boosting pressure to the toilets on floors 2 through 11 in the City Hall West Building. There are two options to provide power to this pump. The first option is to provide a starter in the existing Motor Control Center MCC-A, located in the basement of the City Hall West Building. New conduit and wire shall be routed from the Motor Control Center MCC-A to the booster pump through the ceiling. The controls for this pump would be located at MCC-A. Another option would be to install a 480, 3-phase breaker in Panel board LSLB located in the basement of the City Hall West Building, and route new conduit and wire to a Local Control Panel near the pump. The controls for this pump would be housed in this Local Control Panel.

Communications to the booster pump station A PLC shall be provided at the Booster Pump Station for communication interface with the City Hall West. All process parameters and alarms at the Booster Pump Station shall interface with City’s network via an Ethernet fiber optic link. The fiber optic link will probably interface directly to the nearest Remote Terminal Unit (RTU) in City Hall West. Coordination with the City of Anaheim Telecom Group shall determine the exact location for interfacing with the existing Ethernet fiber optic system.

STRUCTURAL CONSIDERATIONS The City of Anaheim has formally adopted the 2007 California Building Code (CBC) with City specific amendments. The structural design of RWBR WWTP will be governed by these codes. In specific, the following list of codes will be used by MWH to complete the detailed structural design.

• Concrete – ACI 350-06: Code requirements for Environmental Engineering Concrete Structures

• Masonry – ACI 530-05: Building Code Requirements for Masonry Structures • Steel – AISC 13th Ed: Steel Construction Manual

The geotechnical design requirements and recommendations are forth coming. These requirements and recommendations will set forth the design criteria lateral soils pressures, allowable soils bearing pressures and the general site-specific Seismic design parameters. The RWBR WWTP is to be constructed on the North-East corner of the existing City Hall building. It will be placed in between the existing City Hall building and an existing electrical duct bank. The new WWTP will be approximately 20 feet from the North wall of City Hall. This close proximity to the existing City hall and the electrical duct bank will introduce some challenges during the construction phase of the project. Based on the limited information provided in the pre-design report, the construction excavation for the WWTP is expected to extend below grade approximately 20 to 25 feet. Specially designed shoring will need to be designed and installed to limit any settlement of the existing building, interruption of the electrical duct bank and to keep the soils in place between the existing building and the new



construction. MWH recommends that a qualified shoring consultant be contracted by the contractor to design and install this shoring once the final location and depth of the WWTP has been determined and in accordance with the design parameters that will be specified in the geotechnical report.

APPENDICES:

A: Water Quality Results from Lab B: WRF Plant Layout and Process Flow Diagram C: Information and Specifications for Fine Screen D: Equipment Sizing Calculations and BioWin Modeling Results E: Information and Specifications/Warranty for Norit/Dynatec Membrane System F: Information, Specifications and Calculations for Ozonation System G: Information and Specifications for UV System H: Calculations for Odor Control System

HISTORY: Draft Issued: 08/07/09



APPENDIX A

Water Quality Results from Lab



APPENDIX B

WRF Plant Layout, Process Flow Diagram, Equipment List and Preliminary Chemical Volume Calculations

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B C D E F G H J N O P Q S T U V W X Y Z AA AB AC AD AE AF AG AH AI AJRevision: 0 Prepared By: JGC/CDG Checked By:Revision: Prepared By: Checked By:

EQUIPMENT LIST WITH MOTORS Revision: Prepared By: Checked By:Revision: Prepared By: Checked By:Revision: Prepared By: Checked By:

PHASE I (0.08 MGD) PHASE 2 (0.13 MGD)Connected Duty Ave. Ops. Average Connected Duty Ave. Ops. Average Motor Comments

Rev Seq Unit Sub-Station

Major Process

Sub- process

Sub-Process Description Equipment Desciption Equip Dsgntr

Motor Encl.

Supply Voltage

Thermal Protection

Moisture Sensor

Number HP / unit Total Number Total Factor Load Number HP / unit Total Number Total Factor Load (Note 1)Type

Influent Pump Station Influent Pumps P TEFC 480 Y Y 2 1.5 3 1 1.5 1 1.5 2 3 6 1 3 1 3 VFC Non-Clog Sewer Pump 60HZFine Screen Station Fine screen SC TEFC 480 N N 1 1 1 1 1 0.5 0.5 1 1 1 1 1 0.75 0.75 CSAnoxic Tanks Anoxic Tank Submersible Mixers MX TEFC 480 Y Y 1 3 3 1 3 1 3 2 3 6 2 6 1 6 CSAeration Tanks Internal Recycle Pumps P TEFC 480 Y Y 1 2 2 1 2 1 2 2 2 4 2 4 1 4 VFC Aeration Tanks Process Blower BL TEFC 480 N N 2 7.5 15 1 7.5 1 7.5 3 7.5 22.5 2 15 1 15 VFCPost Anoxic Tanks Post Anoxic Tank Submersible Mixers MX TEFC 480 Y Y 1 2 2 1 2 1 2 2 2 4 2 4 1 4 CSPost Anoxic Tanks Membrane Feed Pumps P TEFC 480 Y Y 1 7.5 7.5 1 7.5 1 7.5 2 7.5 15 2 15 1 15 VFCMBR Membrane Blower BL TEFC 480 N N 1 3 3 1 3 1 3 2 3 6 2 6 1 6 CS Connected as power suply to panel: 1 phase, 60 HZMBR Membrane Permeate Pumps P TEFC 480 Y Y 1 1 1 2 2 1 2 2 1 2 2 2 1 2 VFCMBR Backwash Pump P TEFC 480 Y Y 1 1 1 1 1 0.03 0.03 1 1 1 1 1 0.06 0.06 CSOzone Treatment Ozone Skid OZ TEFC 230 Y Y 1 30 30 1 30 1 30 2 30 60 2 60 1 60 NA Connected as power supply to panel: 230 v, 100 A, 1 phaseUV Disinfection UV Skid UV TEFC 240 Y Y 1 2 2 1 2 1 2 1 2 2 1 2 1 2 NAClearwell Water Reuse Pumps P TEFC 480 Y Y 2 5 10 1 5 1 5 2 15 30 1 15 1 15 VFC Non-Clog Sewer Pump 60HZ, 3 phaseOdor Control Station Blowers BL TEFC 480 N N 2 30 60 1 30 1 30 2 30 60 1 30 1 30 CS 6000 cfm, 27 BHP, Pressure: 14" WCCOD Feed Station Sugar Feed Pump P TEFC 120 N N 1 0.25 0.25 1 0.25 0 0 1 0.25 0.25 1 0.25 0 0 SCR Drive 3 AMPpH System Feed Station PH Feed Pump P TEFC 120 N N 1 0.25 0.25 1 0.25 0 0 1 0.25 0.25 1 0.25 0 0 SCR Drive 3 AMPChlorine Station Chlorine Feed Pumps P TEFC 120 N N 1 0.25 0.25 1 0.25 1 0.25 1 0.25 0.25 1 0.25 1 0.25 SCR Drive 3 AMPCitric Acid Station Citric Acid Feed Pumps P TEFC 120 N N 1 0.25 0.25 1 0.25 0 0 1 0.25 0.25 1 0.25 0 0 CS 3 AMPBuilding Misc Auxillary Loads NA TEFC 480 N N 1 45 45 1 45 0.5 22.5 1 45 45 1 45 0.5 22.5 NA 45 kva transformerBuilding Misc Roll Up Door NA TEFC 480 N N 1 1 1 1 1 0 0 1 1 1 1 1 0 0 CS

Building Misc Air Conditioning Unit AC TEFC 480 Y N 1 10 10 1 10 0.5 5 1 10 10 1 10 0.5 5 CS

• Air Handling Unit - 6,000 cfm @ 1.0” w.c. External Static Pressure, 5 hp and 460V-3P60Hz• Circulating Pump - 32 gpm @ 40 ft TDH, ¾ hp and 460V-3Ph-60Hz • Electric Unit Heater- 15 KW capacity and 460V-3Ph-60Hz (Typical of 2).

Building Misc Air Compressor C TEFC 480 N N 1 0.5 0.5 1 0.5 0.3 0.15 1 0.5 0.5 1 0.5 0.5 0.25 CS

TOTAL (hp) PHASE 1 198 155 123.93 PHASE 2 277 221.5 191

Total (kW) 148 116 92 207 165 142

Total (kVA) 185 144 116 258 206 178

\\7.3\CALC_Equipment List_Rev 1.xlsx Overall Page 1 of 1

ANAHEIM DEMO RECYCLE PLANTMEMBRANE BIOREACTOR

7/16/2009 Calc. By: Z. HiraniChecked By: J. CiccotelliChecked Date: 7/17/2009

INTRODUCTIONChlorine and citric acid calcs for cleaning membranesAcetic acid calcs for determing external carbon addition to reduce nitrate concentrationActivated carbon calcs for odor controlResidual chlorine calcs

Chlorine for cleaning membrane Comments

Stock chlorine concentration 12.5 % 125000 mg/L

Desired concentration of chlorine 1000 mg/L

Volume of chlorine required per module 45 gallons 170.1 L

Number of membrane modules to be cleaned 20

Total volume of cleaning solution 882 gallons 3335 L

Volume of stock solution to use per cleaning 7 gallons

Cleaning frequency 4 per month

Total stock solution to store for 1 month 28 gallons

Tote volume 55 gallons

No. totes on site 1 tote

Citric Acid for cleaning membrane

Stock citric acid concentration 100 %

Desired concentration of citric acid 1000 mg/L

Volume of citric acid required per module 45 gallons 170.1 L

Number of membrane modules to be cleaned 20

Total volume of cleaning solution 882 gallons 3335 L

Mass of stock concentration to use per cleaning 3.3 kg 7.3 lbs

Cleaning frequency 4 per month

Total stock solution to store for 1 month 29 lbs

Powdered bag size 55 lbs

No. bags on site 1 bags

Acetic Acid (CH3COOH) to further reduce nitrate

Stock acetic acid concentration 20 % 200000 mg/L

COD value of stock solution 214000 mg/L

Nitrate to be reduced 4 mg/L-N

COD/NO3-N ratio 6

Nitrate to be removed per day 1965600 mg/d

COD required per day 11793600 mg/d

Volume of COD required per day 15 gallons

Volume of stock acetic acid required per day 14 gallons

No. days storage 14 days

Total stock solution for storage period 191 gallons



Activated Carbon Calcs

Air flow-rate to be treated 500 cfm

Contact time per vessel 5 seconds 0.08 min

Approximate volume required 41.7 ft3

Face velocity criteria 20 ft/min max

Area of vessel 25.0 ft2

Diameter of vessel 5.6 ft

Selected diameter 6 ft

Media depth 1.7 ft

Selected Media depth 3 ft

Specific gravity of activated carbon 0.5

Density of activated carbon 30 lb/ft3 480.6 kg/m3

Actual volume of activated carbon 85 ft3

Mass of activated carbon required 2543 lbs

Residual Chlorine Calcs

Flow to be chlorinated 0.13 MGD 130000 gpd

Stock chlorine concentration 12.5 % 125000 mg/L

Desired concentration of chlorine dose 2 mg/L

Chlorine injection flow-rate 2.08 gpd





MicroC to further reduce nitrate

COD value of stock solution 670000 mg/L Obtained from vendor

Nitrate to be reduced 4 mg/L-N

COD/NO3-N ratio 6

Nitrate to be removed per day 1965600 mg/d

COD required per day 11793600 mg/d

Volume of stock solution required per day 5 gallons



END CALCULATION



APPENDIX C

Information and Specifications for Fine Screen

The Waste Tech Rotating Drum Screen incorporates a feed distribution headbox for effective flow distribution and an internally screw auger with individual dewatering cells which dewaters and transports the separated solids out of the drum. Depending on the size of the screen the drum is direct drive, cog gear drive or trunnion driven. The influent is controlled into the drum by means of various inlet pipe designs, selection based on the type of material processed, which distributes the influent over a large area of the drum to ensure efficient use of the drum open area. As the drum rotates fluids pass through the perforations and forward to treatment. Solids are removed and dewatered from the drum by the fixed transport screw.

The Perforated Screen is effectively cleaned by means of a friction drive rotating brush and intermittent spray system. The Waste Tech RDS is fully enclosed with removable inspection covers to prevent splashing and leaks and are designed to create a hygienic working environment in the area the screens are located and comes standard equipped with a pipe connection for odor control.

When combined with our screenings washer press fitted with drainage perforations matching the drum perforation we can guarantee matching capture efficiency of solids to prevent bypass of solids to the downstream process. Screenings are washed and compacted to 80%+ volume reduction

Special Features:Automatic Integral Overflow System (IOS) with alarm indication to prevent dirty influent from contaminating the filtered effluent. Separate overflow connection allows dirty flow to be diverted to back to the pump station.

IOS System automatically activates spray system with hot or cold water to wash away biological slimes, grease, etc….

Various influent distribution pipe designs for specific applications

The enclosed perforated drum screen has no seals or slots – all flow must pass through the perforations – therefore we can guarantee no bypass or carryover of solids to the downstream process.

Special perforation design and cleaning system allow perforations down to 0.6mm guaranteed not to clog with screenings.

Low water usage due to special designed drum cleaning system – water is the secondary cleaning method, not the primary cleaning method

Perforated drum available from 3 mm to 0.6 mm

The Waste Tech RDS stainless steel perforated drums are stronger and more efficient than wedge wire or mesh drum screens

Operator Safety – all rotating parts are covered and the unit is totally enclosed to prevent contact with material.

All removable covers are bolted down or fitted with safety switches to detect removal

Combined with our screenings washer press provides a complete high performance screenings capture, washing and dewatering system

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Special Applications:Membrane Biological Reactors (MBR)Effectively removes short chain fibers that create ropes which hang on the hollow fiber membranes and reduce efficiency causing frequent back flushing and failure of the membranes.

Waste-Tech RDS with 1 mm perforations are ideal for screening raw sewage ahead of MBR plants. Waste-Tech RDS efficiently remove up to +95% inert solids, including fibers and hair. Waste-Tech RDS with 0.6 mm to 3 mm perforations offer flow capacities up to 50 mgd (larger capacities available).

Guarantee no carryover of solids

Sludge ThickenerBy adding polymer to waste activated sludge (WAS) or mixed primary and secondary sludges, a Waste Tech RDS can dewater the sludge from 0.5 -2% DS to 4-10% DS. This will save money on less transport or by using a lower capacity belt press.

Typical ApplicationsThe Waste Tech RDS is also used in a variety of other applications including: - Raw Sewage Screen, Sludge dewatering, Pulp and Paper Mills, Fiberglass, Poultry, Fish Processing, Vegetable Preparation, Slaughterhouses – any application requiring liquid solids separation between 0.6 mm to 3 mm

All models are of stainless steel and have the following options:

optional hole perforation from 0.6 mm (0.02 inches) to 3 mm (0.12 inches)varying types of inlet pipes for water or sludge with or without overflow system varying speeds variable inclines available low weight and small footprint low energy consumptionlow water usage304, 316 stainless steel – special alloys available hygienically encased with optional ventilation connection

Screen Model Length (mm) Width (mm) Height (mm) HP (kw)RDS-9 48.5 (1230) 23.5 (600) 40 (1020) 1/3 (0.25)RDS-30 71 (1810) 34.5 (880) 51 (1290) 1/2 (0.37)RDS-90 109 (2770) 34.5 (880) 59 (1500) 3/4 (0.55)RDS-135 114 (2900) 49 (1250) 75 (1900) 3/4 (0.55)RDS-290 157 (3990) 62 (1570) 94.5 (2400) 1.5 (1.1) *Dimensions are to the nearest 0.5 inch

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101 Zima Park Drive (29301)P.O. Box 6128

Spartanburg, SC 29304, USAPh: 864.576.0660 • Fax: 864.587.5761

www.kuesterszima.com

For additional information call847.367.5150 or 864.587.5714

ROTOSIEVEFILTER DRUM SCREEN SPECIFICATION

1. GENERAL

The Contractor shall furnish and install one (1) Model No. RDS –OF- 30 ROTOSIEVE ROTARY DRUM SCREEN suited for screening wastewater from a process plant. Each unit shall be a rotating screen which is internally fed. The rotating action of the screen shall cause the captured solids to roll up into an agglomerate which shall be conveyed to the discharge end of the screen by internal flights. The screen assembly shall include a perforated cylindrical screen element, splash guards, inlet headbox assembly, base frame, trunnion wheels, drive system, internal/external sprays, covers, collection pan, and solids discharge chute. The screen shall be capable of treating a wastewater flow of up to 0.150 mgd at a maximum suspended solids concentration of 400 mg/L. Screens shall be as manufactured by Waste-Tech div of Kusters Zima Corporation, Spartanburg, S.C. or approved equal. The supplier (equipment manufacturer) shall furnish the equipment described above.

2. SELECTION OF EQUIPMENT

All equipment furnished shall be subject to the approval of the Owner. Proposals shall include delivery of equipment, freight allowed to the job site, and services of the manufacturer’s representative to assist the Contractor in the installation, adjustment, and testing the installed equipment, and to instruct the Owner’s operating personnel in the proper operation and maintenance of the equipment.

3. FIELD SERVICE AND ACCEPTANCE TESTING Each supplier shall include in his proposal, their services of a field service technician for one (1) trip totaling two (2) working days. This service shall be for the purpose of checkout, initial startup, certification of the equipment, and training the Owner’s operating personnel. A written report covering the technician’s findings and installation approval shall be submitted to the Owner. Voltage, current, and other significant parameters shall be recorded. The supplier shall provide all formal test procedures, forms for recording data, and any special test apparatus required. All labor and common materials necessary for conducting the tests shall be furnished by the Owner.

ROTOSIEVE PERFORATED DRUM SCREEN – MODEL RDS-OF-30 PAGE 2 SPECIFICATION

4. INFORMATION REQUIRED WITH SUBMITTAL The equipment manufacturer shall include descriptive literature, dimensional prints of all components described herein, and performance data in sufficient detail to fully describe the equipment being offered. Failure to supply sufficient information to evaluate the bid will be cause for rejection of equipment.

5. CORROSION CONTROL The fine screens may be subjected to corrosive conditions. The main concern involves continuous exposure to anaerobic wastewater, containing significant concentrations of dissolved sulfides. Various forms of chlorine and chlorides may also be present, both in the main flow and in the screen spray water. In order to reduce the potential for corrosion, the screens shall be fabricated from 304 stainless steel. The only non-stainless components allowed shall be those so described later. Two (2) possible concerns remain regarding fabrication procedures: 1. Possible contamination of stainless steel through use of mild steel cleaning

brushes; to this end, no wire brushing shall be allowed during fabrication; and 2. Potential corrosion at welds; to this end, all welds shall be passivated.

Passivation shall consist of the following:

1. Removal of oil, grease and other foreign matter from the weld and heat affected zone.

2. Bathing in ten molar (10 M) nitric acid until the area is cleansed. 3. Flushing with clear water and inspection to verify that the passivated surface is

clean and has a dulled or slightly roughed appearance. “Paste passivation” will not be acceptable.

In the event the Owner does not observe fabrication, the manufacturer shall certify that these measures have been followed without exception.


6. SCREEN ASSEMBLY The screening element shall be a perforated cylinder, constructed of type 304 stainless steel. Each end of the screen elements shall be fitted with a type 304 stainless steel end ring welded to the screen element substructure throughout the circumference. End rings shall be 10 gauge with a minimum thickness of 0.135" and have stiffening flanges welded around their circumference. One (1) end ring shall be at the discharge end and be designed with an extended bellmouth to provide effective discharge of dewatered solids away from the base of the unit. Each end ring shall also include a steel track area specifically designed to be supported by the trunnion wheel assemblies. The drum is directly driven by a gear motor coupled to the drum via a flexible coupling. The screening element perforations shall be a nominal 0.80 mm (0.031 inches). The screen element shall be equipped with type 304 stainless steel flights. Flights arranged in a helical pattern throughout the length of the screen causing the solids to continually move towards the discharge end. The diverter height shall be a minimum of 0.50". The flights shall be designed to structurally strengthen the perforated cylinder and make it suitable for the intended duty.

7. BASE FRAME AND LOWER COLLECTION PAN

The base frame shall be constructed of type 304 stainless steel sections, and shall be accurately fabricated to provide a mounting surface for the screen assembly. The frame shall be designed to withstand all loads imposed by the screen components plus wastewater passing through the unit. The base shall also be designed in such a way to allow for four-point support without the linear deflection exceeding 0.0014. Four (4) anchor bolt holes ad four (4) lifting lugs shall be incorporated in the base. Anchor bolt assemblies shall be 304 stainless steel and shall be furnished by the Contractor. If required a method of changing the perforated screen cylinder angle of inclination shall be provided to raise the screenings discharge end of the screen from 00 to a max of 60. Standard installation angle will be 60. The increase or decrease of the screen cylinder slope shall be made possible without dismantling or disassembling the piping to and from the screen.


8. TRUNNION The trunnion wheel assembly shall be designed such that the wheel and/or sleeve bearing may be replaced independently of the other wheel parts. Cantilevered trunnions are not acceptable. The trunnions must be supported on each side. a. The screen assembly shall be provided with two (2) trunnion wheels and trunnion

wheel mounting assemblies. The trunnion wheel assemblies shall be accurately mounted to the base frame to provide positive horizontal placement of the screen assembly.

b. Trunnion wheels shall be constructed of solid polyethylene or solid phenolic resin mounted on stainless steel axles. Each wheel shall have a maximum outside diameter of 10". Each wheel shall be supported by two (2) deep groove, lubricated and sealed bearings. The wheel bearing assembly shall be an anti-friction ball with inner race.

c. Support shafts shall be of type 304 stainless steel. Each shaft shall be accurately positioned and secured by the trunnion mounting bracket.

d. Trunnion support brackets shall be fabricated of type 304 stainless steel plates.

Each bracket assembly shall be of type 304 stainless steel construction accurately fabricated to interface with the support base. The bracket assembly shall be designed to locate the trunnion support shafts and support the loads imposed by the cylinder assembly.

9. INLET PIPE AND FLOW DISTRIBUTION BOX ASSEMBLY

All components of the piped inlet shall be fabricated of minimum 12 gauge type 304 stainless steel. The piped inlet and flow distribution assembly shall be sized for a peak design flow of 0.150 mgd, as shown on the Waste-Tech div Kusters Zima Corporation general arrangement drawing. Flow shall be controlled to provide smooth, uniform distribution.

An integral overflow shall be provided to detect an overflow condition during flow periods exceeding the design flow, or if the screen should be inoperative for any reason during flow to the screen. Overflow detection will be monitored conductivity probes. A separate overflow pipe will be provided to separate overflow from the drum screen effluent flow.


10. SPLASH GUARDS The screen shall be equipped with external splash guards constructed of minimum 12 gauge type 304 stainless steel. These guards shall be located on each side of the screening element and attached to the base. The splash guards shall be designed to contain and direct the entire flow through the screen base discharge opening. The splash guards shall have internal guided flow vanes. The use of rubber or rivets on the splash guards shall not be allowed. The guards shall be designed to be easily removed for maintenance or access purposes. The splash guards shall be self-supporting throughout their entire length and shall also support the weight of the external covers/hoods which mount on them.

11. COVER HOODS

A cover hood assembly shall be provided for each screen. Each cover hood will consist of multiple sections each sized to facilitate handling by the operator or maintenance personnel. Each section shall be sufficiently durable to withstand visual damage from 1" hailstones, and designed for a live load of 40 psf on horizontal projection plus 30 psf wind load. Each cover section shall be capable of being removed completely from the machine by one operator. Each cover section shall be capable of being removed by a maximum of one (1) operator. Each section of the cover hood shall consist of a panel, plus support members, lift-off hinge and locking assemblies. Cover panels shall be fiberglass construction, with 0.125" minimum thickness. All resin shall be chemical-resistant and shall contain light stabilizers such as UV-9, or equal. Resin shall be suitable for service in temperatures ranging from 300F to 1400F. Fiberglass reinforcement shall consist of a combination of shopped strand mat and woven roving, shall be equal to PPG 526, and shall be treated with a finish compatible to the resin being used.

Cover panels shall be formed on suitable molds to insure constant and accurate dimensions of the finished units. Molds shall be designed so each panel can be cast in one (1) piece without jointing members by bonding or bolting. All layers shall contain pigment to produce a translucent panel. Standard color shall be pigmented blue.


Stiffening angles, base brackets, inspection bars, and all assembly hardware shall be type 18-8 stainless steel, and shall be die formed to insure accurate dimensions of the finished units. Cover hood assemblies shall fasten to and be supported by the splash guards located below them. The 304 stainless steel fasteners shall be coordinated and furnished by the screen manufacturer, who will also make the final assembly.

12. SOLIDS DISCHARGE CHUTE AND SCREEN END COVER.

Each screen shall include a heavy-duty type 304 stainless steel solids discharge chute. The lower part of the chute shall fit closely beneath the screen discharge, so that all solids are captured. The hopper chute shall extend downward. The chute shall converge to a nominal 20 inches by 8 inches discharge opening and the converging sides shall be not less than 600 from horizontal. Bottom of the discharge chute is a reinforced with matching companion mounting holes; stainless steel fasteners shall be provided for attaching a rubber extension chute; the rubber extension chute shall be furnished by others.

13. SCREEN DRIVE Each screen shall have a drive system consisting of an electric motor, gear reducer, flexible drive coupling, and mating flexible drive coupling located and fixed externally onto the drive end of the screen cylinder. The motor shall be as manufactured by Reliance, NORD, or Baldor, rated for severe duty, TEFC, 0.5 HP, 460V/3Ph/60Hz, with a minimum service factor of 1.15.

The motor shall be directly coupled to a flange mounted, parallel helical, double reduction gear reducer. The reducer shall be as manufactured by NORD. The reducer shaft shall be keyed to a drive shaft.

The drive assembly shall be mounted onto the 304 stainless steel screen frame and will be equipped with an adjustment means to provide vibration free operation and minimum wear.


Drive assemblies which include chains, belts, pinions, sprockets, chain tensioners, or chain oilers, will not be accepted.

14. SCREEN CLEANING SYSTEM Each screen shall be provided with an external spray system and rotating horizontal cleaner brush. As available, portable or plant water shall be supplied to the spray systems at the required volume and pressure. The removable external spray system shall consist of a 304 stainless steel spray header provided with 304 stainless steel spray nozzles. The nozzles shall be easily accessible for cleaning. The nozzles shall operate on plant water (treated plant effluent or portable water) at 60 psi. Maximum simultaneous flow, at 60 psi shall be.15 gpm. Inlet connections to spray header shall be 1” NPT. The cleaner brush shall consist of a rotary nylon bristle mounted on a 304 stainless steel shaft with pillow block bearings at each end. The brush located above the perforated cylinder rotates in contact with the cylinder as it turns. The angular contact generated by the unique shape of the brush cleans the perforations. The joint cleaning action of the brush and the washwater sprays effectively maintains the open area of the screen cylinder and prevents blinding.

Control Panel The system shall be equipped with controls to provide both manual and automatic operation. Controls shall be housed in a NEMA 4X enclosure complete with HOA Switch for screen and Compactor, Screen and Compactor ON/OFF Lights, Screen and Compactor Fail Lights, Overflow Alarm Light, Main Disconnect with panel mounted disconnect lockable in the off position. All necessary starters, breakers, fuses, timers and relays for Automatic and Manual Control.

15. EQUIPMENT STORAGE AND INSTALLATION

The supplier shall furnish, as part of shop drawing submittals, detailed instructions on storage and installation of the fine screens. The concrete screen structure shown on the plans is based on the Waste-Tech div of Kusters Zima Corporation ROTOSIEVE Perforated Drum Screen..


16. SPARE PARTS ) (available ex stock Spartanburg, SC) The supplier shall furnish, boxed for storage and clearly marked, the following spare parts: two (2) complete trunnion wheel assemblies.

17. ACCEPTANCE TESTING

The screen shall be fully assembled and run “dry” for a minimum of six (6) consecutive hours at the manufacturer’s factory. Any mechanical defects or problems shall be corrected prior to shipment. A certified report of compliance and of any corrective actions shall be submitted to the Owner. In addition, prior to shipment, the screens shall be thoroughly inspected to insure trouble-free operation, proper interface, and adjustment of all components. The manufacturer shall provide the Owner with a certified inspection report. Finally, the screen shall be field tested prior to final acceptance; this shall entail operation for several hours at the average wastewater flows. Then tested for operation at the peak wastewater flow over a period of approximately 15 minutes.



APPENDIX D

Equipment Sizing Calculations and BioWin Modeling Results

EQUIPMENT SIZING CALCS

1 Internal Recycle Pump2 Selected turnover flow 241.28 gpm3 Nominal Pipe Diameter 8 in4 Pipe Velocity 1.54 ft/s 1-2 ft/s5 Piping distance 76 ft6 Multiplication Factor for Clean Water 17 Nominal losses per 100-ft of piping 0.280 ft/100 ft8 Piping losses 0.21 ft9 Loss for 90 degree elbow 0.45

10 Number of Elbows 2.0011 Loss for Tee 0.3012 Number of Tees 113 Total K 1.2014 Fitting losses 0.0442 ft15 Elevation of Downstream water surface 34 ft16 Elevation of Upstream water surface 15 ft 2 ft f/b17 Change in water surface elevation 19 ft18 System Head 15.00 ft19 Mixing Pump Drive Motor 1.44 Hp20 Selected Nominal Pump Motor 2.00 Hp2122 Membrane Feed Pump23 Selected turnover flow 1,025.42 gpm24 Nominal Pipe Diameter 12 in25 Pipe Velocity 2.91 ft/s 1-2 ft/s26 Piping distance 77 ft27 Multiplication Factor for Clean Water 128 Nominal losses per 100-ft of piping 0.750 ft/100 ft29 Piping losses 0.58 ft30 Loss for 90 degree elbow 0.3931 Number of Elbows 4.0032 Loss for Tee 0.2633 Number of Tees 134 Loss of Cross 1.7135 Number of Crosses 536 Total K 10.3737 Fitting losses 1.3626 ft38 Elevation of Downstream water surface 34 ft39 Elevation of Upstream water surface 15 ft 2 ft f/b40 Change in water surface elevation 19 ft41 System Head 20.94 ft42 Mixing Pump Drive Motor 8.52 Hp43 Selected Nominal Pump Motor 10.00 Hp

444546 Membrane Permeate Pump47 Selected turnover flow 60.32 gpm48 Nominal Pipe Diameter 2 in49 Pipe Velocity 6.16 ft/s 3-6 ft/s50 Piping distance 83 ft51 Multiplication Factor for Clean Water 152 Nominal losses per 100-ft of piping 5.000 ft/100 ft53 Piping losses 4.15 ft54 Loss for 90 degree elbow 0.5755 Number of Elbows 4.0056 Loss for Tee 0.3857 Number of Tees 258 Total K 3.0459 Fitting losses 1.7914 ft60 Elevation of Downstream water surface 22 ft61 Elevation of Upstream water surface (4.62) ft62 Change in water surface elevation 27 ft63 System Head 32.56 ft64 Mixing Pump Drive Motor 0.78 Hp65 Selected Nominal Pump Motor 1.0 Hp6667 Backwash Pump 68 Selected turnover flow 616.32 gpm69 Nominal Pipe Diameter 3 in70 Pipe Velocity 27.97 ft/s 3-6 ft/s71 Piping distance 76 ft72 Multiplication Factor for Clean Water 173 Nominal losses per 100-ft of piping 2.300 ft/100 ft74 Piping losses 1.75 ft75 Loss for 90 degree elbow 0.5476 Number of Elbows 3.0077 Loss for Tee 0.3678 Number of Tees 379 Total K 2.7080 Fitting losses 32.8106 ft81 Elevation of Downstream water surface 69 ft82 Elevation of Upstream water surface 8.50 ft83 Change in water surface elevation 60 ft84 System Head 94.71 ft85 Mixing Pump Drive Motor 23.15 Hp86 Selected Nominal Pump Motor 25 Hp8788

89 MIXER SIZING CALCS

90

91 Train A - Anoxic Tank Submersible Mixer92 Wetted Volume (gal) 13,400 gallons93 Wetted Volume (ft3) 1,791 ft394 Mixer Design Power Input 1 hp/1000ft395 Mixer Shaft Power 1.79 hp96 Motor Efficiency 0.9097 Motor Safety Factor 1.2098 Mixer Motor 2.39 hp99 Selected Motor Size 3.00 hp

100101102 Train A - Post Anoxic Tank Submersible Mixer103 Wetted Volume (gal) 8,800 gallons104 Wetted Volume (ft3) 1,176 ft3105 Mixer Design Power Input 1 hp/1000ft3106 Mixer Shaft Power 1.18 hp107 Motor Efficiency 0.90108 Motor Safety Factor 1.20109 Mixer Motor 1.57 hp110 Selected Motor Size 2.00 hp111112113 Train B - Anoxic Tank Submersible Mixer114 Wetted Volume (gal) 13,400 gallons115 Wetted Volume (ft3) 1,791 ft3116 Mixer Design Power Input 1 hp/1000ft3117 Mixer Shaft Power 1.79 hp118 Motor Efficiency 0.90119 Motor Safety Factor 1.20120 Mixer Motor 2.39 hp121 Selected Motor Size 3.00 hp122123124 Train B - Post Anoxic Tank Submersible Mixer125 Wetted Volume (gal) 8,800 gallons126 Wetted Volume (ft3) 1,176 ft3127 Mixer Design Power Input 1 hp/1000ft3128 Mixer Shaft Power 1.18 hp129 Motor Efficiency 0.90130 Motor Safety Factor 1.20131 Mixer Motor 1.57 hp132 Selected Motor Size 2.00 hp

133

134 Blower Calcs135136 Process Blower Calc137 k 1.40138 p1 14.70 psi139 p1 2,116.22 psf140 p2 21.51 psi

141 p2 3,098.04 psf142 Constant 550.00 ft‐lbf/hp‐sec143 V1 175.00 ft3/min

144 V1 2.92 ft3/sec

145 Pideal,hp ‐4.52

146 Efficiency 0.70147 Pactual,hp ‐6.46

148 Selected Motor Size 7.50 hp149150 Membrane Blower Calc151 k 1.40152 p1 14.70 psi153 p1 2,116.22 psf154 p2 21.51 psi

155 p2 3,098.04 psf156 Constant 550.00 ft‐lbf/hp‐sec157 V1 60.00 ft3/min

158 V1 1.00 ft3/sec

159 Pideal,hp ‐1.55

160 Efficiency 0.70161 Pactual,hp ‐2.21

162 Selected Motor Size 3.00 hp

File D:\Zakir's Stuff\City of Anaheim\BioWin Model\Anaheim MBR Single Recycle 08072009.bwc 1

BioWin user and configuration data Project details Project name: Anaheim - Water Recycling Demonstration Project Plant name: Anaheim Demo Plant 8/7/2009 Steady state solution Target SRT: 20 SRT: 20.03 Temperature: 15.0 Flowsheet

Configuration information for all Bioreactor units Physical data Element name Volume [Mil. Gal] Area [ft2] Depth [ft] # of diffusers Membrane Tank 0.0009 10.0260 12.0 3 Post-Anoxic 0.0179 159.5255 15.0 Un-aerated Pre-Anoxic 0.0260 231.7130 15.0 Un-aerated Aerobic 0.0439 391.2384 15.0 89 Operating data Average (flow/time weighted as required) Element name Average DO Setpoint [mg/L] Post-Anoxic 0 Pre-Anoxic 0 Aerobic 2.0 Element name Average Air supply rate [ft3/min (20C, 1 atm)] Membrane Tank 130.0

Membrane Tank MBR EfflueInfluent Post-AnoxicPre-Anoxic Aerobic

Waste Sludge


Aeration equipment parameters Element name k1 in C =

k1(PC)^0.25 + k2 k2 in C = k1(PC)^0.25 + k2

Y in Kla = C Usg ^ Y - Usg in [m3/(m2 d)]

Area of one diffuser

% of tank area covered by diffusers [%]

Membrane Tank 1.0000 0.0432 0.6250 0.0410 15.0000 Post-Anoxic 2.5656 0.0432 0.7965 0.0410 20.0000 Pre-Anoxic 2.5656 0.0432 0.8200 0.0410 10.0000 Aerobic 2.5656 0.0432 0.8200 0.0410 10.0000 Operating data Average (flow/time weighted as required) Element name Influent Time 0 Flow 0.13 Total COD mgCOD/L 972.00 Total Kjeldahl Nitrogen mgN/L 75.00 Total P mgP/L 8.60 Nitrate N mgN/L 0 pH 7.90 Alkalinity mmol/L 10.40 Inorganic S.S. mgTSS/L 54.00 Calcium mg/L 63.00 Magnesium mg/L 20.00 Dissolved oxygen mg/L 0 Element name Influent Fbs - Readily biodegradable (including Acetate) [gCOD/g of total COD] 0.1190 Fac - Acetate [gCOD/g of readily biodegradable COD] 0.1900 Fxsp - Non-colloidal slowly biodegradable [gCOD/g of slowly degradable COD] 0.6500 Fus - Unbiodegradable soluble [gCOD/g of total COD] 0.0300 Fup - Unbiodegradable particulate [gCOD/g of total COD] 0.1000 Fna - Ammonia [gNH3-N/gTKN] 0.4800 Fnox - Particulate organic nitrogen [gN/g Organic N] 0.5000 Fnus - Soluble unbiodegradable TKN [gN/gTKN] 0.0200 FupN - N:COD ratio for unbiodegradable part. COD [gN/gCOD] 0.0350 Fpo4 - Phosphate [gPO4-P/gTP] 0.5470 FupP - P:COD ratio for influent unbiodegradable part. COD [gP/gCOD] 0.0110 FZbh - Non-poly-P heterotrophs [gCOD/g of total COD] 0.0151 FZbm - Anoxic methanol utilizers [gCOD/g of total COD] 0.0001 FZaob - Ammonia oxidizers [gCOD/g of total COD] 0.0001 FZnob - Nitrite oxidizers [gCOD/g of total COD] 0.0001 FZamob - Anaerobic ammonia oxidizers [gCOD/g of total COD] 0.0001 FZbp - PAOs [gCOD/g of total COD] 0.0001 FZbpa - Propionic acetogens [gCOD/g of total COD] 0.0001 FZbam - Acetoclastic methanogens [gCOD/g of total COD] 0.0001 FZbhm - H2-utilizing methanogens [gCOD/g of total COD] 0.0001 Album page - Table Elements Total

suspended solids [mgTSS/L]

Volatile suspended solids [mgVSS/L]

Total COD [mg/L]

Total Kjeldahl Nitrogen [mgN/L]

Total P [mgP/L]

Ammonia N [mgN/L]

Nitrate N [mgN/L]

pH []

Influent 491.34 436.37 972.00 75.00 8.60 36.00 0 7.90 Pre-Anoxic 8815.32 6618.94 9212.09 541.81 249.33 5.16 0.03 7.21 Aerobic 8812.70 6598.24 9177.40 537.88 249.33 0.80 3.56 7.18 Post-Anoxic

8809.04 6593.96 9171.18 537.79 249.33 1.08 2.01 7.17

Membrane 9576.74 7168.35 9966.91 584.31 271.07 1.03 2.01 7.17


Tank MBR Effluent

0.00 0.00 38.17 3.72 0.10 1.03 2.01 7.17

Waste Sludge

9576.74 7168.35 9966.91 584.31 271.07 1.03 2.01 7.17

Album page - Distributions

Album page - Distributions

Volume Distribution

Pre-Anoxic 29 %

Aerobic 49 %

Post-Anoxic 20 %

Membrane Tank 1 %

Mass Distribution

Pre-Anoxic 29 %

Aerobic 49 %

Post-Anoxic 20 %

Membrane Tank 1 %


Album page - Nutrient profiles

Album page - MLSS profile

NH3-NNO3-N

PO4-P Profile

NO3-N and NH3-N ProfilesPre-Anoxic Aerobic Post-Anoxic Membrane Tank MBR Effluent

N C

ON

CS

(mg/

L)

20

18

16

14

12

10

8

6

4

2

0

SOL.

PO

4-P

(mg/

L) 25

20

15

10

5

Pre-Anoxic 6.10

Aerobic 0.36 Post-Anoxic 0.15 Membrane Tank 0.10MBR Effluent 0.10

TSS Profile

Pre-Anoxic Aerobic Post-Anoxic Membrane Tank

CO

NC

(mg/

L)

12,000

10,000

8,000

6,000

4,000

2,000

0

8,815 8,813 8,809

9,577


Global Parameters AOB Name Default Value Max. spec. growth rate [1/d] 0.90000 0.90000 1.0720 Substrate (NH4) half sat. [mgN/L] 0.70000 0.70000 1.0000 Aerobic decay rate [1/d] 0.17000 0.17000 1.0290 Anoxic/anaerobic decay rate [1/d] 0.08000 0.08000 1.0290 KiHNO2 [mmol/L] 0.00500 0.00500 1.0000 NOB Name Default Value Max. spec. growth rate [1/d] 0.70000 0.70000 1.0600 Substrate (NO2) half sat. [mgN/L] 0.10000 0.10000 1.0000 Aerobic decay rate [1/d] 0.17000 0.17000 1.0290 Anoxic/anaerobic decay rate [1/d] 0.08000 0.08000 1.0290 KiNH3 [mmol/L] 0.07500 0.07500 1.0000 ANAMMOX Name Default Value Max. spec. growth rate [1/d] 0.10000 0.10000 1.1000 Substrate (NH4) half sat. [mgN/L] 2.00000 2.00000 1.0000 Substrate (NO2) half sat. [mgN/L] 1.00000 1.00000 1.0000 Aerobic decay rate [1/d] 0.01900 0.01900 1.0290 Anoxic/anaerobic decay rate [1/d] 0.00950 0.00950 1.0290 Ki Nitrite [mgN/L] 1000.00000 1000.00000 1.0000 Nitrite sensitivity constant [L / (d mgN) ] 0.01600 0.01600 1.0000 OHOs Name Default Value Max. spec. growth rate [1/d] 3.20000 3.20000 1.0290 Substrate half sat. [mgCOD/L] 5.00000 5.00000 1.0000 Anoxic growth factor [-] 0.50000 0.50000 1.0000 Aerobic decay [1/d] 0.62000 0.62000 1.0290 Anoxic/anaerobic decay [1/d] 0.30000 0.30000 1.0290 Hydrolysis rate (AS) [1/d] 2.10000 2.10000 1.0290 Hydrolysis half sat. (AS) [-] 0.06000 0.06000 1.0000 Anoxic hydrolysis factor [-] 0.28000 0.28000 1.0000 Anaerobic hydrolysis factor [-] 0.50000 0.50000 1.0000 Adsorption rate of colloids [L/(mgCOD d)] 0.80000 0.80000 1.0290 Ammonification rate [L/(mgN d)] 0.04000 0.04000 1.0290 Assimilative nitrate/nitrite reduction rate [1/d] 0.50000 0.50000 1.0000 Fermentation rate [1/d] 3.20000 3.20000 1.0290 Fermentation half sat. [mgCOD/L] 5.00000 5.00000 1.0000 Anaerobic growth factor (AS) [-] 0.12500 0.12500 1.0000 Hydrolysis rate (AD) [1/d] 0.10000 0.10000 1.0500 Hydrolysis half sat. (AD) [mgCOD/L] 0.15000 0.15000 1.0000 Methylotrophs Name Default Value


Max. spec. growth rate of methanol utilizers [1/d] 1.30000 1.30000 1.0720 Methanol half sat. [mgCOD/L] 0.50000 0.50000 1.0000 Aerobic decay rate of methanol utilizers [1/d] 0.04000 0.04000 1.0290 Anoxic/anaerobic decay rate of methanol utilizers [1/d] 0.03000 0.03000 1.0290 PAOs Name Default Value Max. spec. growth rate [1/d] 0.95000 0.95000 1.0000 Max. spec. growth rate, P-limited [1/d] 0.42000 0.42000 1.0000 Substrate half sat. [mgCOD(PHB)/mgCOD(Zbp)] 0.10000 0.10000 1.0000 Substrate half sat., P-limited [mgCOD(PHB)/mgCOD(Zbp)] 0.05000 0.05000 1.0000 Magnesium half sat. [mgMg/L] 0.10000 0.10000 1.0000 Cation half sat. [mmol/L] 0.10000 0.10000 1.0000 Calcium half sat. [mgCa/L] 0.10000 0.10000 1.0000 Aerobic decay rate [1/d] 0.10000 0.10000 1.0000 Anaerobic decay rate [1/d] 0.04000 0.04000 1.0000 Sequestration rate [1/d] 6.00000 6.00000 1.0000 Anoxic growth factor NO3 [-] 0.33000 0.33000 1.0000 Anoxic growth factor NO2 [-] 0.33000 0.33000 1.0000 Acetogens Name Default Value Max. spec. growth rate [1/d] 0.25000 0.25000 1.0290 Substrate half sat. [mgCOD/L] 10.00000 10.00000 1.0000 Acetate inhibition [mgCOD/L] 10000.00000 10000.00000 1.0000 Decay rate [1/d] 0.05000 0.05000 1.0290 Aerobic decay rate [1/d] 0.52000 0.52000 1.0290 Methanogens Name Default Value Acetoclastic Mu Max [1/d] 0.30000 0.30000 1.0290 H2-utilizing Mu Max [1/d] 1.40000 1.40000 1.0290 Acetoclastic Ks [mgCOD/L] 100.00000 100.00000 1.0000 Acetoclastic methanol Ks [mgCOD/L] 0.50000 0.50000 1.0000 H2-utilizing CO2 half sat. [mmol/L] 0.10000 0.10000 1.0000 H2-utilizing Ks [mgCOD/L] 0.10000 0.10000 1.0000 H2-utilizing methanol Ks [mgCOD/L] 0.50000 0.50000 1.0000 Acetoclastic propionic inhibition [mgCOD/L] 10000.00000 10000.00000 1.0000 Acetoclastic decay rate [1/d] 0.13000 0.13000 1.0290 Acetoclastic aerobic decay rate [1/d] 0.60000 0.60000 1.0290 H2-utilizing decay rate [1/d] 0.13000 0.13000 1.0290 H2-utilizing aerobic decay rate [1/d] 0.60000 0.60000 1.0290 pH Name Default Value Heterotrophs low pH limit [-] 4.00000 4.00000 Heterotrophs high pH limit [-] 10.00000 10.00000 Methanol utilizers low pH limit [-] 4.00000 4.00000 Methanol utilizers high pH limit [-] 10.00000 10.00000 Autotrophs low pH limit [-] 5.50000 5.50000 Autotrophs high pH limit [-] 9.50000 9.50000 PolyP heterotrophs low pH limit [-] 4.00000 4.00000 Poly P heterotrophs high pH limit [-] 10.00000 10.00000 Heterotrophs low pH limit (anaerobic) [-] 5.50000 5.50000 Heterotrophs high pH limit (anaerobic) [-] 8.50000 8.50000


Propionic acetogens low pH limit [-] 4.00000 4.00000 Propionic acetogens high pH limit [-] 10.00000 10.00000 Acetoclastic methanogens low pH limit [-] 5.00000 5.00000 Acetoclastic methanogens high pH limit [-] 9.00000 9.00000 H2-utilizing methanogens low pH limit [-] 5.00000 5.00000 H2-utilizing methanogens high pH limit [-] 9.00000 9.00000 Switches Name Default Value Heterotrophic DO half sat. [mgO2/L] 0.05000 0.05000 Aerobic denit. DO half sat. [mgO2/L] 0.05000 0.05000 Ammonia oxidizer DO half sat. [mgO2/L] 0.25000 0.25000 Nitrite oxidizer DO half sat. [mgO2/L] 0.50000 0.50000 Anaerobic ammonia oxidizer DO half sat. [mgO2/L] 0.01000 0.01000 Anoxic NO3 half sat. [mgN/L] 0.10000 0.10000 Anoxic NO2 half sat. (mgN/L) 0.05000 0.05000 NH3 nutrient half sat. [mgN/L] 1.0000E-4 1.0000E-4 PolyP half sat. [mgP/L] 0.01000 0.01000 VFA sequestration half sat. [mgCOD/L] 5.00000 5.00000 P uptake half sat. [mgP/L] 0.15000 0.15000 P nutrient half sat. [mgP/L] 0.00100 0.00100 Autotroph CO2 half sat. [mmol/L] 0.10000 0.10000 Heterotrophic Hydrogen half sat. [mgCOD/L] 1.00000 1.00000 Propionic acetogens Hydrogen half sat. [mgCOD/L] 5.00000 5.00000 Synthesis anion/cation half sat. [meq/L] 0.01000 0.01000 AOB Name Default Value Yield [mgCOD/mgN] 0.15000 0.15000 N in biomass [mgN/mgCOD] 0.07000 0.07000 N in inert [mgN/mgCOD] 0.07000 0.07000 P in biomass [mgP/mgCOD] 0.02200 0.02200 P in inert [mgP/mgCOD] 0.02200 0.02200 Fraction to endogenous residue [-] 0.08000 0.08000 COD:VSS ratio [mgCOD/mgVSS] 1.42000 1.42000 NOB Name Default Value Yield [mgCOD/mgN] 0.09000 0.09000 N in biomass [mgN/mgCOD] 0.07000 0.07000 N in inert [mgN/mgCOD] 0.07000 0.07000 P in biomass [mgP/mgCOD] 0.02200 0.02200 P in inert [mgP/mgCOD] 0.02200 0.02200 Fraction to endogenous residue [-] 0.08000 0.08000 COD:VSS ratio [mgCOD/mgVSS] 1.42000 1.42000 ANAMMOX Name Default Value Yield [mgCOD/mgN] 0.11400 0.11400 Nitrate production [mgN/mgBiomassCOD] 2.28000 2.28000 N in biomass [mgN/mgCOD] 0.07000 0.07000 N in inert [mgN/mgCOD] 0.07000 0.07000 P in biomass [mgP/mgCOD] 0.02200 0.02200 P in inert [mgP/mgCOD] 0.02200 0.02200 Fraction to endogenous residue [-] 0.08000 0.08000


COD:VSS ratio [mgCOD/mgVSS] 1.42000 1.42000 OHOs Name Default Value Yield (aerobic) [-] 0.66600 0.66600 Yield (fermentation, low H2) [-] 0.10000 0.10000 Yield (fermentation, high H2) [-] 0.10000 0.10000 H2 yield (fermentation low H2) [-] 0.35000 0.35000 H2 yield (fermentation high H2) [-] 0 0 Propionate yield (fermentation, low H2) [-] 0 0 Propionate yield (fermentation, high H2) [-] 0.70000 0.70000 CO2 yield (fermentation, low H2) [-] 0.70000 0.70000 CO2 yield (fermentation, high H2) [-] 0 0 N in biomass [mgN/mgCOD] 0.07000 0.07000 N in inert [mgN/mgCOD] 0.07000 0.07000 P in biomass [mgP/mgCOD] 0.02200 0.02200 P in inert [mgP/mgCOD] 0.02200 0.02200 Endogenous Residue [-] 0.08000 0.08000 COD:VSS ratio [mgCOD/mgVSS] 1.42000 1.42000 Yield (anoxic) [-] 0.54000 0.54000 Yield propionic (aerobic) [-] 0.50000 0.50000 Yield propionic (anoxic) [-] 0.41000 0.41000 Yield acetic (aerobic) [-] 0.40000 0.40000 Yield acetic (anoxic) [-] 0.32000 0.32000 Yield methanol (aerobic) [-] 0.50000 0.50000 Adsorp. max. [-] 1.00000 1.00000 Methylotrophs Name Default Value Yield (anoxic) [-] 0.40000 0.40000 N in biomass [mgN/mgCOD] 0.07000 0.07000 N in inert [mgN/mgCOD] 0.07000 0.07000 P in biomass [mgP/mgCOD] 0.02200 0.02200 P in inert [mgP/mgCOD] 0.02200 0.02200 Endogenous Residue [-] 0.08000 0.08000 COD:VSS ratio [mgCOD/mgVSS] 1.42000 1.42000 PAOs Name Default Value Yield (aerobic) [-] 0.63900 0.63900 Yield (anoxic) [-] 0.52000 0.52000 Aerobic P/PHA uptake [mgP/mgCOD] 0.95000 0.95000 Anoxic P/PHA uptake [mgP/mgCOD] 0.35000 0.35000 Yield of PHA on sequestration [-] 0.88900 0.88900 N in biomass [mgN/mgCOD] 0.07000 0.07000 N in part. inert [mgN/mgCOD] 0.07000 0.07000 N in sol. inert [mgN/mgCOD] 0.07000 0.07000 P in biomass [mgP/mgCOD] 0.02200 0.02200 P in part. inert [mgP/mgCOD] 0.02200 0.02200 Fraction to endogenous part. [-] 0.25000 0.25000 Inert fraction of endogenous sol. [-] 0.20000 0.20000 P/Ac release ratio [mgP/mgCOD] 0.49000 0.49000 COD:VSS ratio [mgCOD/mgVSS] 1.42000 1.42000 Yield of low PP [-] 0.94000 0.94000 Acetogens


Name Default Value Yield [-] 0.10000 0.10000 H2 yield [-] 0.40000 0.40000 CO2 yield [-] 1.00000 1.00000 N in biomass [mgN/mgCOD] 0.07000 0.07000 N in endogenous residue [mgN/mgCOD] 0.07000 0.07000 P in biomass [mgP/mgCOD] 0.02200 0.02200 P in endogenous residue [mgP/mgCOD] 0.02200 0.02200 Fraction to endogenous residue [-] 0.08000 0.08000 COD:VSS ratio [mgCOD/mgVSS] 1.42000 1.42000 Methanogens Name Default Value Acetoclastic yield [-] 0.10000 0.10000 Methanol acetoclastic yield [-] 0.10000 0.10000 H2-utilizing yield [-] 0.10000 0.10000 Methanol H2-utilizing yield [-] 0.10000 0.10000 N in acetoclastic biomass [mgN/mgCOD] 0.07000 0.07000 N in H2-utilizing biomass [mgN/mgCOD] 0.07000 0.07000 N in acetoclastic endog. residue [mgN/mgCOD] 0.07000 0.07000 N in H2-utilizing endog. residue [mgN/mgCOD] 0.07000 0.07000 P in acetoclastic biomass [mgP/mgCOD] 0.02200 0.02200 P in H2-utilizing biomass [mgP/mgCOD] 0.02200 0.02200 P in acetoclastic endog. residue [mgP/mgCOD] 0.02200 0.02200 P in H2-utilizing endog. residue [mgP/mgCOD] 0.02200 0.02200 Acetoclastic fraction to endog. residue [-] 0.08000 0.08000 H2-utilizing fraction to endog. residue [-] 0.08000 0.08000 Acetoclastic COD:VSS ratio [mgCOD/mgVSS] 1.42000 1.42000 H2-utilizing COD:VSS ratio [mgCOD/mgVSS] 1.42000 1.42000 General Name Default Value Particulate substrate COD:VSS ratio [mgCOD/mgVSS] 1.60000 1.32000 Particulate inert COD:VSS ratio [mgCOD/mgVSS] 1.60000 1.32000 Ash content of biomass (synthesis ISS) [%] 8.00000 8.00000 Molecular weight of other anions [mg/mmol] 35.50000 35.50000 Molecular weight of other cations [mg/mmol] 39.10000 39.10000 Mg to P mole ratio in polyphosphate [mmolMg/mmolP] 0.30000 0.30000 Cation to P mole ratio in polyphosphate [meq/mmolP] 0.30000 0.30000 Ca to P mole ratio in polyphosphate [mmolCa/mmolP] 0.05000 0.05000 Cation to P mole ratio in organic phosphate [meq/mmolP] 0.01000 0.01000 Bubble rise velocity (anaerobic digester) [cm/s] 23.90000 23.90000 Bubble Sauter mean diameter (anaerobic digester) [cm] 0.35000 0.35000 Anaerobic digester gas hold-up factor [] 1.00000 1.00000 Tank head loss per metre of length (from flow) [m/m] 0.00250 0.00250 Minimum air flow (per unit volume) without mixing [ m3/(m3 d) ] 1.00000 1.00000 Mass transfer Name Default Value Kl for H2 [m/d] 17.00000 17.00000 1.0240 Kl for CO2 [m/d] 10.00000 10.00000 1.0240 Kl for NH3 [m/d] 1.00000 1.00000 1.0240 Kl for CH4 [m/d] 8.00000 8.00000 1.0240 Kl for N2 [m/d] 15.00000 15.00000 1.0240 Kl for O2 [m/d] 13.00000 13.00000 1.0240


Physico-chemical rates Name Default Value Struvite precipitation rate [1/d] 3.0000E+10 3.0000E+10 1.0240 Struvite redissolution rate [1/d] 3.0000E+11 3.0000E+11 1.0240 Struvite half sat. [mgTSS/L] 1.00000 1.00000 1.0000 HDP precipitation rate [L/(molP d)] 1.0000E+8 1.0000E+8 1.0000 HDP redissolution rate [L/(mol P d)] 1.0000E+8 1.0000E+8 1.0000 HAP precipitation rate [molHDP/(L d)] 5.0000E-4 5.0000E-4 1.0000 Physico-chemical constants Name Default Value Struvite solubility constant [mol/L] 6.9180E-14 6.9180E-14 HDP solubility product [mol/L] 2.7500E-22 2.7500E-22 HDP half sat. [mgTSS/L] 1.00000 1.00000 Equilibrium soluble PO4 with Al dosing at pH 7 [mgP/L] 0.01000 0.01000 Al to P ratio [molAl/molP] 0.80000 0.80000 Al(OH)3 solubility product [mol/L] 1.2590E+9 1.2590E+9 AlHPO4+ dissociation constant [mol/L] 7.9430E-13 7.9430E-13 Equilibrium soluble PO4 with Fe dosing at pH 7 [mgP/L] 0.01000 0.01000 Fe to P ratio [molFe/molP] 1.60000 1.60000 Fe(OH)3 solubility product [mol/L] 0.05000 0.05000 FeH2PO4++ dissociation constant [mol/L] 5.0120E-22 5.0120E-22 Aeration Name Default Value Alpha (surf) OR Alpha F (diff) [-] 0.50000 0.40000 Beta [-] 0.95000 0.95000 Surface pressure [kPa] 101.32500 101.32500 Fractional effective saturation depth (Fed) [-] 0.32500 0.32500 Supply gas CO2 content [vol. %] 0.03500 0.03500 Supply gas O2 [vol. %] 20.95000 20.95000 Off-gas CO2 [vol. %] 2.00000 2.00000 Off-gas O2 [vol. %] 18.80000 18.80000 Off-gas H2 [vol. %] 0 0 Off-gas NH3 [vol. %] 0 0 Off-gas CH4 [vol. %] 0 0 Surface turbulence factor [-] 2.00000 2.00000 Set point controller gain [] 1.00000 1.00000 Modified Vesilind Name Default Value Maximum Vesilind settling velocity (Vo) [ft/min] 0.3873 0.3873 Vesilind hindered zone settling parameter (K) [L/g] 0.3700 0.3700 Clarification switching function [mg/L] 100.0000 100.0000 Specified TSS conc.for height calc. [mg/L] 2500.0000 2500.0000 Maximum compactability constant [mg/L] 15000.0000 15000.0000 Double exponential Name Default Value Maximum Vesilind settling velocity (Vo) [ft/min] 0.9341 0.9341 Maximum (practical) settling velocity (Vo') [ft/min] 0.6152 0.6152 Hindered zone settling parameter (Kh) [L/g] 0.4000 0.4000 Flocculent zone settling parameter (Kf) [L/g] 2.5000 2.5000


Maximum non-settleable TSS [mg/L] 20.0000 20.0000 Non-settleable fraction [-] 0.0010 0.0010 Specified TSS conc. for height calc. [mg/L] 2500.0000 2500.0000 Biofilm general Name Default Value Attachment rate [ g / (m2 d) ] 80.00000 80.00000 Attachment TSS half sat. [mg/L] 100.00000 100.00000 Detachment rate [g/(m3 d)] 8.0000E+4 8.0000E+4 Solids movement factor [] 10.00000 10.00000 Diffusion neta [] 0.80000 0.80000 Thin film limit [mm] 0.50000 0.50000 Thick film limit [mm] 3.00000 3.00000 Assumed Film thickness for tank volume correction [mm] 0.75000 0.75000 Film surface area to media area ratio - Max.[ ] 1.00000 1.00000 Minimum biofilm conc. for streamer formation [gTSS/m2] 4.00000 4.00000 Maximum biofilm concentrations [mg/L] Name Default Value Non-polyP heterotrophs 5.0000E+4 5.0000E+4 1.0000 Anoxic methanol utilizers 5.0000E+4 5.0000E+4 1.0000 Ammonia oxidizing biomass 1.0000E+5 1.0000E+5 1.0000 Nitrite oxidizing biomass 1.0000E+5 1.0000E+5 1.0000 Anaerobic ammonia oxidizers 5.0000E+4 5.0000E+4 1.0000 PolyP heterotrophs 5.0000E+4 5.0000E+4 1.0000 Propionic acetogens 5.0000E+4 5.0000E+4 1.0000 Acetoclastic methanogens 5.0000E+4 5.0000E+4 1.0000 Hydrogenotrophic methanogens 5.0000E+4 5.0000E+4 1.0000 Endogenous products 3.0000E+4 3.0000E+4 1.0000 Slowly bio. COD (part.) 5000.00000 5000.00000 1.0000 Slowly bio. COD (colloid.) 0 0 1.0000 Part. inert. COD 5000.00000 5000.00000 1.0000 Part. bio. org. N 0 0 1.0000 Part. bio. org. P 0 0 1.0000 Part. inert N 0 0 1.0000 Part. inert P 0 0 1.0000 Stored PHA 5000.00000 5000.00000 1.0000 Releasable stored polyP 1.1500E+6 1.1500E+6 1.0000 Fixed stored polyP 1.1500E+6 1.1500E+6 1.0000 PolyP bound cations 1.1500E+6 1.1500E+6 1.0000 Readily bio. COD (complex) 0 0 1.0000 Acetate 0 0 1.0000 Propionate 0 0 1.0000 Methanol 0 0 1.0000 Dissolved H2 0 0 1.0000 Dissolved methane 0 0 1.0000 Ammonia N 0 0 1.0000 Sol. bio. org. N 0 0 1.0000 Nitrite N 0 0 1.0000 Nitrate N 0 0 1.0000 Dissolved nitrogen gas 0 0 1.0000 PO4-P (Sol. & Me Complexed) 1.0000E+10 1.0000E+10 1.0000 Sol. inert COD 0 0 1.0000 Sol. inert TKN 0 0 1.0000 Inorganic S.S. 1.3000E+6 1.3000E+6 1.0000 Struvite 8.5000E+5 8.5000E+5 1.0000 Hydroxy-dicalcium-phosphate 1.1500E+6 1.1500E+6 1.0000 Hydroxy-apatite 1.6000E+6 1.6000E+6 1.0000 Magnesium 0 0 1.0000 Calcium 0 0 1.0000 Metal 1.0000E+10 1.0000E+10 1.0000 Other Cations (strong bases) 0 0 1.0000


Other Anions (strong acids) 0 0 1.0000 Total CO2 0 0 1.0000 User defined 1 0 0 1.0000 User defined 2 0 0 1.0000 User defined 3 5.0000E+4 5.0000E+4 1.0000 User defined 4 5.0000E+4 5.0000E+4 1.0000 Dissolved oxygen 0 0 1.0000 Effective diffusivities [m2/s] Name Default Value Non-polyP heterotrophs 5.0000E-14 5.0000E-14 1.0290 Anoxic methanol utilizers 5.0000E-14 5.0000E-14 1.0290 Ammonia oxidizing biomass 5.0000E-14 5.0000E-14 1.0290 Nitrite oxidizing biomass 5.0000E-14 5.0000E-14 1.0290 Anaerobic ammonia oxidizers 5.0000E-14 5.0000E-14 1.0290 PolyP heterotrophs 5.0000E-14 5.0000E-14 1.0290 Propionic acetogens 5.0000E-14 5.0000E-14 1.0290 Acetoclastic methanogens 5.0000E-14 5.0000E-14 1.0290 Hydrogenotrophic methanogens 5.0000E-14 5.0000E-14 1.0290 Endogenous products 5.0000E-14 5.0000E-14 1.0290 Slowly bio. COD (part.) 5.0000E-14 5.0000E-14 1.0290 Slowly bio. COD (colloid.) 6.9000E-11 6.9000E-11 1.0290 Part. inert. COD 5.0000E-14 5.0000E-14 1.0290 Part. bio. org. N 5.0000E-14 5.0000E-14 1.0290 Part. bio. org. P 5.0000E-14 5.0000E-14 1.0290 Part. inert N 5.0000E-14 5.0000E-14 1.0290 Part. inert P 5.0000E-14 5.0000E-14 1.0290 Stored PHA 5.0000E-14 5.0000E-14 1.0290 Releasable stored polyP 5.0000E-14 5.0000E-14 1.0290 Fixed stored polyP 5.0000E-14 5.0000E-14 1.0290 PolyP bound cations 5.0000E-14 5.0000E-14 1.0290 Readily bio. COD (complex) 6.9000E-10 6.9000E-10 1.0290 Acetate 1.2400E-9 1.2400E-9 1.0290 Propionate 8.3000E-10 8.3000E-10 1.0290 Methanol 1.6000E-9 1.6000E-9 1.0290 Dissolved H2 5.8500E-9 5.8500E-9 1.0290 Dissolved methane 1.9625E-9 1.9625E-9 1.0290 Ammonia N 2.0000E-9 2.0000E-9 1.0290 Sol. bio. org. N 1.3700E-9 1.3700E-9 1.0290 Nitrite N 2.9800E-9 2.9800E-9 1.0290 Nitrate N 2.9800E-9 2.9800E-9 1.0290 Dissolved nitrogen gas 1.9000E-9 1.9000E-9 1.0290 PO4-P (Sol. & Me Complexed) 2.0000E-9 2.0000E-9 1.0290 Sol. inert COD 6.9000E-10 6.9000E-10 1.0290 Sol. inert TKN 6.8500E-10 6.8500E-10 1.0290 Inorganic S.S. 5.0000E-14 5.0000E-14 1.0290 Struvite 5.0000E-14 5.0000E-14 1.0290 Hydroxy-dicalcium-phosphate 5.0000E-14 5.0000E-14 1.0290 Hydroxy-apatite 5.0000E-14 5.0000E-14 1.0290 Magnesium 7.2000E-10 7.2000E-10 1.0290 Calcium 7.2000E-10 7.2000E-10 1.0290 Metal 4.8000E-10 4.8000E-10 1.0290 Other Cations (strong bases) 1.4400E-9 1.4400E-9 1.0290 Other Anions (strong acids) 1.4400E-9 1.4400E-9 1.0290 Total CO2 1.9600E-9 1.9600E-9 1.0290 User defined 1 6.9000E-10 6.9000E-10 1.0290 User defined 2 6.9000E-10 6.9000E-10 1.0290 User defined 3 5.0000E-14 5.0000E-14 1.0290 User defined 4 5.0000E-14 5.0000E-14 1.0290 Dissolved oxygen 2.5000E-9 2.5000E-9 1.0290 EPS Strength coefficients [ ]


Name Default Value Non-polyP heterotrophs 1.00000 1.00000 1.0000 Anoxic methanol utilizers 1.00000 1.00000 1.0000 Ammonia oxidizing biomass 1.00000 1.00000 1.0000 Nitrite oxidizing biomass 1.00000 1.00000 1.0000 Anaerobic ammonia oxidizers 1.00000 1.00000 1.0000 PolyP heterotrophs 1.00000 1.00000 1.0000 Propionic acetogens 1.00000 1.00000 1.0000 Acetoclastic methanogens 1.00000 1.00000 1.0000 Hydrogenotrophic methanogens 1.00000 1.00000 1.0000 Endogenous products 1.00000 1.00000 1.0000 Slowly bio. COD (part.) 1.00000 1.00000 1.0000 Slowly bio. COD (colloid.) 0 0 1.0000 Part. inert. COD 1.00000 1.00000 1.0000 Part. bio. org. N 1.00000 1.00000 1.0000 Part. bio. org. P 1.00000 1.00000 1.0000 Part. inert N 1.00000 1.00000 1.0000 Part. inert P 1.00000 1.00000 1.0000 Stored PHA 1.00000 1.00000 1.0000 Releasable stored polyP 1.00000 1.00000 1.0000 Fixed stored polyP 1.00000 1.00000 1.0000 PolyP bound cations 1.00000 1.00000 1.0000 Readily bio. COD (complex) 0 0 1.0000 Acetate 0 0 1.0000 Propionate 0 0 1.0000 Methanol 0 0 1.0000 Dissolved H2 0 0 1.0000 Dissolved methane 0 0 1.0000 Ammonia N 0 0 1.0000 Sol. bio. org. N 0 0 1.0000 Nitrite N 0 0 1.0000 Nitrate N 0 0 1.0000 Dissolved nitrogen gas 0 0 1.0000 PO4-P (Sol. & Me Complexed) 1.00000 1.00000 1.0000 Sol. inert COD 0 0 1.0000 Sol. inert TKN 0 0 1.0000 Inorganic S.S. 0.33000 0.33000 1.0000 Struvite 1.00000 1.00000 1.0000 Hydroxy-dicalcium-phosphate 1.00000 1.00000 1.0000 Hydroxy-apatite 1.00000 1.00000 1.0000 Magnesium 0 0 1.0000 Calcium 0 0 1.0000 Metal 1.00000 1.00000 1.0000 Other Cations (strong bases) 0 0 1.0000 Other Anions (strong acids) 0 0 1.0000 Total CO2 0 0 1.0000 User defined 1 0 0 1.0000 User defined 2 0 0 1.0000 User defined 3 1.00000 1.00000 1.0000 User defined 4 1.00000 1.00000 1.0000 Dissolved oxygen 0 0 1.0000



APPENDIX E

Information and Specifications/Warranty for Norit/Dynatec Membrane System

Municipal Waste WaterChallengeMunicipal waste water needs to be treated as it originates exactly

there where people live. The treatment should be done as close as

possible to the source. With growing cities the footprint of these

plants and the quality of effluent needed have given more and more

interest in compact waste water treatment plants.

In a growing number of plants submerged membranes are applied to

improve them to Membrane Bioreactors (MBR). However cleanability

and maintenance are not ideal in these plants, as the membranes are

difficult to reach. Uniform distribution of membranes and the ability

to reach every square meter of the membrane area are essential for

optimal operation and keeping a plant running satisfactory.

SolutionThe X-Flow’s AirLiftTM configuration offers a membrane solution out-

side the reactor allowing the maintenance of the plant to be simple

and clean. Due to the inside out configuration of membrane filtration

all membrane area is subject to the same process conditions.

Energy consumption is at the same level of submerged membranes

or even less, due to the efficient usage of process conditions for

flux enhancement.

X-Flow’s tubular 5 mm UF membrane will allow a bioreactor to

run up to 15 g/l MLSS biomass.

X-Flow’s 5 mm tubes found their way in MBR applications in the

municipal and industrial market in areas such as:

• Municipal WWTP

• Food industry

The X-Flow tubular membrane modules are being produced with

ISO 9000 certification.

AirliftTM MBR

AirliftTM MBR

Features and benefitsTight UF membrane Turbidity < 0.1 NTU

Silt Density Index < 3

AirLift filtration Very low energy consumption

Simple lay out

High flux rates

Low trans membrane pressure

Cleaning In Place Fully automated cleanings

Use of low cost chemicals

Fully automatic operation Logging of operating parameters

Atmospheric system Fully enclosed

No operator exposure to fumes or aerosols

Small footprint

ExamplesX-Flow has provided membranes for MBRs for a growing number of plants world

wide. Capacity ranges from less than 10 m3/hr (44 gpm) to more than 150 m3/hr

(440 gpm).

WWTP Grand Traverse - USA

Capacity 100.000 gpd

Year of start up 2004

Technology X-Flow AirLiftTM MBR

WWTP Ootmarsum - Holland

Capacity 150 m3/h

Year of start up 2006/2007


Cigarette factory Xuzhou - China

Capacity 2000 m3/day


Technology X-Flow AirLiftTM

WWTP Millsborough - USA

Capacity 175 m3/h (1,1 MGD)



X-Flow BV reserves the right to make changes in the technical specifications at any time.

X-Flow BV

P.O. Box 739 • 7500 AS Enschede • The Netherlands

T +31 (0)53 42 87 350 • F +31 (0)53 42 87 351

E [email protected] www.x-flow.com

References membrane bioreactors X-FLOW Membranes

MBR membranes and their application REF-MBR-0806daytot

OVEROVEROVEROVER 77775555.000.000.000.000 M M M M3/3/3/3/DAY DAY DAY DAY MBRMBRMBRMBR CAPACITYCAPACITYCAPACITYCAPACITY

Page 1 of 6

Capacity [m3/day]

Year Customer/OEM Location Membrane and Module Application

17000 2007/8 Veolia Palm Jumeira 38PRV F4385 Municipal 4200 2006/7 Parkson Millsborough, US 38PRV F4385 Municipal 4000 2007 UEM Valyampet 38PRV F4385 Industrial 3600 2005/6 NMT Ootmarsum 38PRV F4385 Municipal 3600 2003 ATM NL 38GRV, F5385 Cleaning waste water

3000 + 2000 2006 DMT/NORIT Istanbul 38GRH F5385 Leachate (2 units) 2400 2007 NMT Obolon 38GRH F5385 Brewery MBR 2400 2008 NMT Venezuela 38PRV F4385 Brewery AL MBR 2400 2007 UEM Thuthipet 38PRV F4385 Industrial 2160 2006 Dynatec Singapore 38GRH F5385 Thermophilic MBR 2040 2000 Wehrle Werk AG Dairy Gold, Irel. 38GRH, F5385 Dairy waste water 2000 2007 Tsinghua Xuzhou China 38PRV, F4385 Cigarette factory 2000 2004 Septo/NMT Bavaria 38GRH, F5385 Maltery water

~2000 2006/7 Dynatec US 38PRV F4385 Chicken factory / municipal 1680 2006 Fumatech Sachsenmilch 38GRH F5385 Dairy waste water; recycle

(RO) 1750 2008 Ternois Riec sur Belon 38PRV F4385 Municipal 1560 2003 Wehrle Werk AG Kellogs, UK 38GRH, F5385 Food waste water 1560 2005 Dynatec/Aquabio Food appl. USA 38GRH, F5385 Food waste water 1440 2006 Aquabio / NMT Glasgow, UK 38GRH F5385 Waste water carbon factory




Page 2 of 6

Capacity [m3/day]


1320 2006 White Martins Brasil 38GRH F5385 Textile factory 1200 2005 Cruise ship Germany Marine style, F5385 Municipal 1200 2006 Cruise ship Germany Marine style, F5385 Municipal 1200 2004 Aquabio Geest Bourn S. 38GRH, F5385 Food waste water (veg.) 1080 2003 Aquabio Eden Vale 38GRH, F5385 Dairy waste water 1000 1999 SEAB Munkedal, S *) 38PRH, F4385 Paper mill 960 2001 Cruise ship Italy Marine style, F5385 Municipal 960 2001 Cruise ship UK Marine style, F5385 Municipal 960 2002 Cruise ship UK Marine style, F5385 Municipal 900 2007 NMT/Strix E Europe 38GRH, F5385 Industrial 900 2007 Baradero Argentina 38GRH, F5385 textile 840 2000 WNWB Cargill, NL 38GRH, B5125 Food processing waste w. 800 2007 UEM Malligaithope 38PRV F4385 Industrial 720 2007 NMT Belgium 38 GRH F5385 Brewery MBR 720 1993 Otto AWG, D 33PE, B4125 Leachate 720 2002 Cruise ship UK Marine style, F5385 Municipal 720 2003 Cruise ship UK Marine style, F5385 Municipal 640 2002 Cruise ship UK Marine style, F5385 Municipal 640 2002 Cruise ship Italy Marine style, F5385 Municipal 620 2003 Cruise ship Italy Marine style, F5385 Municipal




Page 3 of 6

Capacity [m3/day]


600 2007 Pilar Argentina 38GRH, F5385 textile 600 2006 Aquatech Pakistan 38GRH F5385 Textile wastewater 500 2006 Parkson Port of the Island 38PRV F4385 Municipal 500 2003 ATM NL 38GRV, F5385 Industrial 480 2002 Grontmij Hooge Maey, B 38GRH, F5385 Leachate 490 2006 Dayen Munic. Oman 38GRH F5385 Municipal waste water crflow. 480 1994 Otto ART, D 7P, S0220 Leachate 480 2003 Cruise ship UK Marine style, F5385 Municipal 480 2003 Aquabio Golden West, UK 38GRH, F5385 Dairy waste water 480 2005 MFT China 38GRH F5385 Leachate 420 2002 Dynatec Engine factory 38GRH F5385 Factory waste water 400 2005 Dynatec Grand Traverse 38PRV F4385 Municipal 400 2004 Cruise ship UK Marine style, F5385 Municipal 400 2003 Cruise ship UK Marine style, F5385 Municipal 400 2008 Zhong China Gaoantun 2 38GRH F5385 Leachate 400 2008 Yihuan Huashan 38GRH F5385 Leachate 360 2001 Dynatec Michigan, USA 38GRH, F5385 Car factory waste 360 2001 Triqua Weert, NL 38GRH, F5385 Tankcleaning 360 2002 Aquabio Kanes Food UK 38GRH, F5385 Foodprocessing 360 2004 Aquabio Ledbury Preserves 38GRH, F5385 Foodprocessing




Page 4 of 6

Capacity [m3/day]


360 2001 Wehrle Werk AG Lanarkshire, Scotl. 38PRH, F5385 Dairy waste water 360 2001 Wehrle Werk AG Lanarkshire, Scotl. 38PRH, F5385 Dairy waste water 350 1997 Wehrle Werk AG Lorrach, D 7P, A0220 Leachate 320 2003 Cruise ship UK Marine style, F5385 Municipal 300 2004 Cruise ship UK Marine style, F5385 Municipal 250 2004 Wehrle Werk AG China Gaoantun 38GRH F5385 Leachate 250 2004 Wehrle Werk AG China, Beishanshu 38GRH, F5385 Leachate 250 2003 Wehrle Werk AG China, Zhongshan 38GRH, F5385 Leachate 250 2004 ATM NL 38PRV F4385 Industrial 250 2003 RMT Leeuwarden 38PRV, F4385 Municipal 250 2004 Dynatec Glen Meadows 38PRV, F4385 Municipal 250 2002 Dynatec Bahama’s 38GRH F5385 Wastewater 240 2004 Cruise ship Germany Marine style, F5385 Municipal 225 2000 Triqua Apeldoorn, NL 33GE, F5385 Paper mill 200 2004 Proserpol France 38GRH, F5385 Wastewater candy 200 2002 Septo Zaandam, NL 38GRH, F5385 Tank cleaning 200 2002 Septo Maastricht, NL 38GRH, F5385 Tank cleaning 200 2000 Ecotechnica Italy 38PRH, A4125 Chemical plant 200 1998 Wehrle Werk AG Piesberg, D 7P, A0220 Leachate 200 2001 White Martins Manaus, (Brasil) 38PRH, F4385 Municipal wastewater




Page 5 of 6

Capacity [m3/day]


180 1998 Grontmij VBM, NL 38PRH, A4125 Leachate chemical site 180 2003 K-Pack Rotterdam, NL 38GRH, F5385 Tankcleaning 175 2006 PWT India pilot 38GRH F5385 Tannery effluent 175 2001 DHV Pernis, NL 38PRV, F4385 Tankcleaning 175 2005 BekkerLagram Waalwijk NL 38GRH F5385 Roadcleaning, mobile 175 2006 BekkerLagram Waalwijk NL 38GRH F5385 Roadcleaning, mobile 175 2003 Seghers Cova, Portugal 38GRH, F5385 Leachate 175 1996 Wehrle Werk AG CAW, NL 7P, A0220 Leachate 175 2000 Ecotechnica Milan, Italy 38PRH, F5172 Waste water 175 2001 ATM NL 38GRV, F4385 Cleaning waste water 175 2001 MG Italy 38PRV, F4385 Waste water 175 1999 VA Tech Wabag Vienna, Austria 38PRV, F4385 Municipal waste water 175 2003 Yanmar Japan 38GRH, F4385 Municipal waste water 175 2002 G&C Eng. S.Korea 33PEF4385 Wastewater 175 2002 Enercon Italy 38PRH, F5172 Food waste water 150 1997 Wedeco Biberach, D 38PE, F4385 Leachate 125 2003 Dynatec Saddle Ridge, US 38PRV F4385 Municipal 120 2000 Wehrle Freiburg, Germany 38PRV F4385 leachate 120 1999 VA Tech Vienna, Austria 38PRV F4385 Municipal 100 2002 Marine UK Marine style, F5385 Municipal




Page 6 of 6

Capacity [m3/day]


100 2003 Marine UK Marine style, F5385 Municipal 100 2003 Marine UK Marine style, F5385 Municipal 100 2004 Marine UK Marine style, F5385 Municipal 100 2005 Marine UK Marine style, F5385 Municipal 100 2006 Marine UK Marine style, F5385 Municipal

X-Flow B.V. P.O. Box 739 – 7500 AS ENSCHEDE – The Netherlands

Tel: +31 (0)53 4287350 Fax: +31 (0)53 4287351 E-mail: [email protected] Internet: www.x-flow.com

Appendix A2 Compact, Pro-rated Lifetime Warranty Conditions

Page 1 of 2 2008 rev7

1. Membrane Element warranty

There is no other warranty express or implied as provided for herein.

X-Flow warrants that its membrane elements supplied shall be free from defects in materials and workmanship. The membrane element warranty for lifetime will commence upon

installation of the membrane elements in the UF system or three months after the date of membrane element ready for shipment ex works Enschede, The Netherlands, whichever comes first. X-Flow’s sole liability and the Purchaser and/or Owner exclusive remedy under this warranty shall be to provide replacement membrane elements

and is limited to the initial membrane element contract value. Any membrane element found to be defective under the terms of this warranty during the first 12 months of the warranty period will be replaced at no cost to the Purchaser and/or Owner, excluding shipping and handling

charges

Any membrane element found to be defective under the terms of this warranty after the initial 12 months of the warranty period will be replaced

based on the pro-rata membrane element value as calculated below, excluding shipping and handling charges.

Pro-rata membrane element value:

Membrane element Replacement Price* X Months Beneficial Use Total membrane element Warranty Period (months)

The Membrane Replacement Price is based on the actual list price at the time of replacement or otherwise agreed upon.

The months of beneficial use will be calculated based on the calendar month of the warranty claim relative to the commencement of the warranty period.

The membrane element warranty period is 36 months or otherwise agreed upon.

2. Membrane Element Failure Criteria A membrane element shall be considered defective if it meets one or more of the following criteria:

An individual membrane element shall be considered defective;

• if more than 5 of the total number of membrane tubes in the

element have required repair (i.e.: by plugging, pinning and/or gluing) during any consecutive period of 12 months

• if more than 10 of the total number of membrane tubes in the element have required repair (i.e.: by plugging, pinning and/or gluing) over the total course of the warranty period.

Note: Tubes repaired during production and testing are excluded from the failure count. Tube repair on site is the responsibility of the purchaser and or owner. 3. General Warranty Conditions

All warrantees shall be null and void if any of the following conditions are not met:

a) Accidental and/or external caused damages and damages caused by

improper use are excluded from this warranty. Accidental and/or external caused damages and damages caused by improper use are damages

caused by but not limited to operation and/or exposure of membranes modules to conditions, outside the instructions and conditions listed in the X-Flow Product Datasheets or misuse, abuse or improper installation,

operation, maintenance, or repair, alteration, accidents. Also, damages caused by uncontrolled and/or defective operation of the overall water

treatment process in which the membrane elements are used or parts thereof are excluded from this warranty. This warranty is strictly limited to

membrane failure due to X-Flow’s fault in manufacturing; all other

causes are excluded. If there is any dispute with respect to the above, the Purchaser should provide evidence to X-Flow.

b) The Purchaser and/or Owner of the membrane elements will immediately notify X-Flow in writing of any potential issues or claims relating to the membrane element warranties.

c) The feed and/or backwash stream to the element(s) shall contain neither organic nor inorganic matter or solutions harmful to the membrane elements as listed on the X-Flow Product Datasheets and/or X-Flow Chemical Resistance Datasheet (see appendix B). Also fiber damage due to foreign debris is excluded from this warranty. d) Membrane elements shall be handled and stored according the instructions on the X-Flow data and instruction sheets. e) During normal operation the membrane element(s) shall be protected against the introduction or intrusion of any and all gasses

(i.e.: air) unless the entering of gas is required and/or allowed during certain controlled process steps / sequences, such as but not limited to air-flush, airlift or integrity tests. f) The membrane element shall be operationally protected against

hydraulic and pneumatic shock loading such as, but not limited to water hammer, etc. g) X-Flow understands that the membrane elements will be used as a part of a larger water treatment process. X-Flow must be given the opportunity, with a reasonable notice, to review engineering

documents and attend testing and commissioning activities of all aspects of the water treatment process which may affect membrane

lifetime. Note: That neither a review of the engineering documents nor attendance of testing or commissioning nor the declining of the opportunity does constitute any responsibility for any aspect of the

system. h) The purchaser and/or Owner will calculate and record the temperature-normalized clean membrane permeability after each membrane element cleaning for the duration of the membrane

element warranty period and any subsequent extensions. The Purchaser and/or Owner will immediately notify X-Flow in writing of any recorded drop in temperature-normalized clean membrane permeability of greater than 10% of reference permeability value. The notification shall include all pertinent treatment process and

operating parameters at the time of the reading. Purchaser and/or Owner should avoid scaling or fouling of membranes at all times. i) The Purchaser and/or Owner of the membrane elements will maintain for the duration of the warrantees complete and accurate

daily records of all relevant process settings and data (see Appendix C, “Trending and Logging”). Copies of these data shall be made

available to X-Flow upon request. j) Any defects or faults caused by any alterations to the membrane elements, or improper use or mishandling of consumable items used in the operation of the membrane elements, by the Purchaser and/or

Owner or his authorized representative are specifically excluded from this warranty. Furthermore any replacement of X-Flow membranes by

membranes not produced and/or supplied by X-Flow will render this warranty null and void.

k) In the case where the Purchaser and Owner are separate parties, the Purchaser has sole and exclusive responsibility for making the Owner aware of his responsibilities under the conditions of this warranty. Failure of the Purchaser and/or Owner to meet their respective obligations under this agreement will render this warranty

null and void.

X-Flow B.V. P.O. Box 739 – 7500 AS ENSCHEDE – The Netherlands

Tel: +31 (0)53 4287350 Fax: +31 (0)53 4287351 E-mail: [email protected] Internet: www.x-flow.com

Appendix A2 Compact, Pro-rated Lifetime Warranty Conditions

Page 2 of 2 2008 rev7

4. Conditions for Testing and Shipment

a) X-Flow reserves the right to test and verify the failure of any membrane element for which a warranty claim is made. b) Membrane elements shipped to X-Flow for warranty examination must

be shipped freight, tax and custom duties prepaid.

c) Before returning any membrane element(s) to X-Flow for warranty

examination, X-Flow must be contacted to obtain return authorization. For that purpose, follow X-Flow’s return procedure which can be found on our website (www.x-flow.com). Any element(s) shipped to X-Flow without

return documentation will be returned to shipper unopened, freight collect.

d) If after the testing the failure of the membrane element is determined to be caused by the Purchaser, the Purchaser shall pay X-

Flow all damages and expenses such as but not limited to: costs for testing, reports, site visits, etc.. e) Membrane elements examined as part of a warranty claim, which

are found to be performing as warranted will be returned to the Purchaser freight collect and a handling charge will be levied against the Purchaser.

ALL MEMBRANE ELEMENT WARRANTEES ARE SUBJECT TO THE

WARRANTY CONDITIONS AS DEFINED IN THIS DOCUMENT UNLESS AGREED OTHERWISE. LIABILITY FOR DIRECT, INDIRECT, CONSEQUENTIAL, INCIDENTAL,

SPECIAL, EXEMPLARY, AND PUNITIVE DAMAGES ARE EXCLUDED

(C) Norit Printed 7/29/2009 @ 5:08 PM

V 2.5

Projection AirLift UF installationCustomerProjectnamePr.NumberRevisionSubjectDateDesigned byChecked by

Design requirements (based on biological treatment inlet conditions):Nominal flow gpm 70.0 15.9 m3/h Assistance regarding peak (and nominal) flow durationPeak flow not applicable gpm 80.0 18.2 m3/hAverage flow equals Nominal flow 2 Advise 2 What is the duration of the peak flow? 2 hours 24

22 Advise 22 How often does the peak flow occur per day? 1 time(s) a dayRequired daily throughput: m3/d 382Required average net capacity m3/h 15.9

UF skid mass balance based on 14 modules installed, without safety margins!Buffer capacity:Buffer required to continously run at average capacitym3 Not aplicable PER SECTION

0 Dosing set 1: 115 l/hNo buffercapacity is available within treatment Dosing set 2: 1117 l/h

Design requirements (based on biological treatment outlet conditions, including buffer capacity)Maximum capacity required: m3/h 15.9Maximum capacity with current design m3/h 16.0 Overdesign: 0.8% Backwash flow: 138.6 m3/hNominal capacity required: m3/h 15.9

UF configuration Maximum gross perm flow: 19 m3/hSkid type - 20 Maximum nett perm flow: 16 m3/hNumber of sections - 1Number skids per section (max = 14) - 1Number of installed UF modules per skid - 14 Airlift: 140 nm3/hMembrane area per module m2 33Spare modules per skid - 6 30% spare positions Sludge recirculation: 319.2 m3/hTotal number of skids - 1Total number of modules - 14 Drain volume 2.4 m3Membrane area per skid m2 462Membrane area total installation m2 462 UF SKID lay-out based on 14 modules installed!!, total number skids = 1

UF design settings Resulting plant operationDesign constraint flux lmh 50Design constraint filtration time min 10 Calculated daily throughput:Maximum gross flux lmh 42.0 Nominal operation @ 16.0 m3/h during 24.0 h/d (34.7 lmh net flux)Filtration time min 9 Maximum operation @ 16.0 m3/h during 2.0 h/d (34.692 lmh net flux)Drain Sequence frequency per skid hr/DS 4 Daily thoughput 384 m3/dCEB frequency per skid days/CEB 31Recovery during maximum flux - 83.4%Total maximal net permeate production m3/h 16 This document is provided for information only. Membrane or system performance warrantees are neither expressed nor implied by this design.

Rev 1: 50 Kgpd to start, expandable to 100 Kgpd.

Comments:40 lmh is conservative. Higher flux rates can be tested as needed for peak design considerations. Pump and blower capacities will be the only issue since supply and discharge capacities are essentially unlimited due to direct draw and discharge to the sewer.

100 kgpd

TBroad7/29/2009

City of Anaheom, CAAL-MBR DemoX09-0027/SF#09-01-1932 1

Bio reactor

X09-0027_XBV_AnaheimCA_Demo_AL-MBR_100Kgpd rev1.xls Fill in sheet Page 1 of 1



APPENDIX F

Information, Specifications and Calculations for Ozonation System

MWHClient: City of Anaheim

234567891011121314151617181920212223242526272829303132333435363738394041424344454647484950515253545556575859606162636465666768697071

B C D E FTITLE: Ozone Disinfection System Design

OBJECTIVE To provide calculations for the Ozone Disinfection System and related facilites

denotes entered value

DESIGN ASSUMPTIONS & INFORMATION1 Applied Process Technologies's (APT) HiPOx® will be utilized for this application2 System will be designed for 0.1 mgd maximum flow (70 mgd)3 Reactor mode will be for disinfection (ozone feed only; hydrogen peroxide feed may be added later for advanced oxidation - emerging contaminants removal)4 Reactor has CADPH conditional approval for Title 22 Disinfection using CT= 1.0 mg*min/L 5 Lower CT may be required, but calculations will assume 1.0 to be conservative. High quality from MBR effluent may require lower CT for disinfection6 Ozone system to operate 24/7

DESCRIPTION UNIT CALCULATIONS COMMENT

OZONATION EQUIPMENTOzone Requirements

Design Flow - max mgd 0.13gpm 90

Ozone demand mg/L 4.0 Expected from MBR effluent (6 to 8 mg/L for raw wastewater)Ozone residual mg/L 0.5 Sufficient for detectionTotal Ozone Dose - Dissolved mg/L 4.5 Transfer efficiency % 90 Estimated for tubular reactors with multiple injection pointsTotal Ozone Dose - Transferred mg/L 5.0 Total Ozone Requirements - daily ppd 5.4 Contingency % 30.0 Total Ozone Requirements - daily (loaded) ppd 8.0

Ozone GeneratorsOperating unit 1Stand-by unit 1Total Number of Generators unit 2

Equipment factor % 100.0 Ozone Concentration in oxygen feed % 8 Capacity, each unit ppd 8

Oxygen/Air Requirements GOX density kg/m3 1.331 1 atm and 68 deg F

pcf 0.0831 1 atm and 68 deg FGOX demand ppd 100 GOX flow, total scfm 0.8 GOX % in air % 21 Air flow, total scfm 4.0

Liquid Oxygen Requirements (optional) GOX demand ppd 100 GOX flow, total scfd 1,203 LOX density kg/m3 1,140 at boiling point

pcf 71.2 at boiling pointVGOX/VLOX ratio ratio 856.50Equivalent LOX volume cfd 1.40LOX mass ppd 100.0 ok - must match GOX mass (E45)

LOX volume in dewar vessel L 240 Based on standard LOX dewar 53" height, 26" diametercf 8.5

Dewars on site unit 2 Total LOX capacity onsite cf 17 Days of storage days 12.1

Power RequirementsOzone generator + Pumps + Instruments Kwh 15.0 Provided by APTEnergy cost $/Kwh 0.10Annual Energy Cost $/year 13,140.00$

Page 1

PRELIMINARY DESIGN

PRELIMINARY DESIGN



APPENDIX G

Information and Specifications for UV System

WASTEWATER DISINFECTION FILTERED IN-PIPE TREATMENT

Around the globe, wastewater treatment plants of all sizes are responding to the water quality and quantity demands of the communities they serve. As more municipalities adopt wastewater reuse policies and practices, wastewater treatment plants are required to treat effluent to higher levels –essentially eliminating all pathogens prior to reuse or discharge. Depending on site and design conditions, wastewater treatment plants producing

filtered effluent sometimes prefer a disinfection solution using closed-vessel or pressurized UV reactors. The TrojanUVFit™ offers an effective and energy-efficient closed-vessel UV solution. This compact reactor is available in multiple configurations to treat a wide range of flow rates. The streamlined hydraulic profile of closed-vessel systems disinfect filtered effluent without breaking head in the treatment process. These benefits along with UV’s ability to provide environmentally-friendly, chemical-free treatment for chlorine resistant microorganisms (such as Cryptosporidium and Giardia) make the

TrojanUVFit™ closed-vessel solution an attractive option for wastewater disinfection.

Trojan Technologies is an ISO 9001:2000 registered company that has been leading the UV disinfection market with open-channel solutions for wastewater disinfection (e.g. TrojanUV3000Plus™) in over 5,000 municipal installations worldwide – the largest UV installation base. The TrojanUVFit™, the latest addition to the Trojan product line, rounds out a complete portfolio of products for wastewater disinfection and reuse applications.

Proven Trojan products. A new application.Validated, chemical-free disinfection from the industry leader

Key Benefits TrojanUVFit™

Fully Validated Performance. System sizing is based on actual dose delivery

verified through bioassay validation. Real-world, field performance data eliminates sizing

assumptions and risks associated with theoretical dose calculations.

Compact Design. The small reactor footprint simplifies indoor retrofit installations and

reduces construction costs.

Reliable, Proven Components. UV lamps, quartz sleeves, electronic ballasts, sensors

and sleeve wiping system have been tested, proven reliable and are operating

in hundreds of installations.

Design Flexibility. Reactors can be installed in parallel or in series, making it simple to

incorporate redundancy or future expansion needs.

Wide Range of Flow Rates. Peak flow rates per reactor are suitable for either

individual post-filter or manifold installation. Flows up to 7 MGD per reactor – the largest

validated low-pressure lamp in-pipe wastewater system in the industry.

Validated Lamp Performance. Lamp output and aging characteristics validated

through industry protocols and proven through years of operating experience.

Automatic Wiping. Automatic sleeve wiping saves operator’s time and money. Ensures

the maximum UV output is available for disinfection and minimizes energy consumption.

Global support. Local service. Trojan’s comprehensive network of certified service

providers offers fast response for service and spare parts.

Guaranteed Performance and Comprehensive Warranty. Trojan systems

include a Lifetime Disinfection Performance Guarantee. Ask for details.

Amalgam Lamps High-output amalgam lamps are energy-efficient and save operating costs due to reduced electrical consumption. Lamps are located within protective quartz sleeves with easy access from the service entrance.

Sleeve Wiping System Automatic sleeve wiping system operates on-line without interrupting disinfection. The wiping sequence occurs automatically at preset intervals without operator involvement.

UV Intensity Sensor Highly accurate, photodiode sensor monitors UV output within the reactor. The sensor ensures UV light is fully penetrating the water for complete disinfection.

System Control Center The microprocessor or PLC-based controller continuously monitors and controls UV system functions. SCADA communication via ModBus for remote monitoring, control and dose pacing is available. Programmable digital and analog I/O capabilities can generate unique alarms for individual applications and send signals to operate valves and pumps.

Compact reactors designed for high flow rates also available. This reactor contains lamps in both ends of the reactor. Multiple inlet and outlet flange orientations are available.

Designed for efficient, reliable performance

UV Reactor Electropolished 316L stainless steel chamber available in multiple configurations for a wide range of flow rates. Optional flange orientations allow reactors to fit into existing piping galleries or tight spaces.

Power Distribution Center (PDC) The PDC panel distributes power to the reactor, UV intensity sensor and sleeve wiping system. The panel also houses high-efficiency, variable-output (60 – 100% power) or constant-output ballasts with proven performance in hundreds of installations around the world.

End Cap The end cap protects and isolates connections for components such as lamps, sleeves and wiping system. Power is automatically disconnected if end cap is removed thereby ensuring a safe working environment for operators.

Benefits:• Validated in accordance with industry protocols established by National Water Research Institute (NWRI)

• Performance data is generated from actual field testing over a wide range of flow rates and water quality (UV transmission)

• Bioassay testing offers peace of mind and improved public and environmental safety due to verified dose delivery – not theoretical calculations

Benefits:• Compact footprint simplifies

installation and minimizes related capital costs – ideal for retrofit and new construction applications

• Lamps and sleeves are fully serviceable from the reactor end – allowing the system to be installed against walls, other equipment or piping

• Low headloss design simplifies integration into existing process, and avoids additional pumping and associated capital and operational costs

• Multiple flange orientations available – increasing design flexibility Benefits:• Each lamp draws 250 Watts

• Trojan’s amalgam lamps maintain 98% output during entire lamp life – 20% less decline than competitive UV lamps

• Validated performance provides assurance of reliable dose delivery and prolonged lamp life

• Deliver consistent and stable UV output over a wide range of water temperatures

Regulatory-Endorsed Bioassay ValidationField testing ensures accurate dose delivery

Compact Reactor for Installation FlexibilityEfficient, cost-saving design enables retrofit or new construction

Amalgam Lamps Require Less EnergyMaintain maximum output and reduce O&M costs

Reactors can be installed in parallel or in series for increased design and installation flexibility.

Benefits:• Routine procedures, including lamp changeouts are simple and require minimal time – reducing maintenance costs

• Access to internal components (lamps, sleeves, cleaning system) through service entrance at one end.

• Service entrance and connections isolated and protected by end cap

• Intensity sensor continuously monitors UV output to ensure dose delivery

Robust Sleeve Wiping SystemAutomatic wiping system maintains consistent dose delivery

Built for Reliable Performance and Easy MaintenanceDesigned for trouble-free operation and minimal service

User-Friendly Operator InterfaceTouch-screen display allows easy operation and monitoring

The TrojanUVFit™ lamps are easily replaced in minutes without the need for tools.

Benefits:• Wiping system minimizes fouling of quartz sleeves

• Ensures consistent UV dose delivery and optimum performance

• Automatic wiping occurs while the lamps are disinfecting, reducing downtime

• Optional off-line chemical cleaning to reduce maintenance associated with manual cleaning

Benefits:• Microprocessor or PLC-based system controls all functions and dose pacing to minimize energy use while maintaining required UV dose

• Controller features intuitive, graphical display for at-a-glance system status

• Controller communicates with plant SCADA systems for centralized monitoring of performance, lamp status, power levels, hours of operation and alarm status

The PLC-based controller combines sophisticated system operation and reporting with an operator-friendly, touch screen display.

Head Office (Canada)3020 Gore RoadLondon, Ontario, Canada N5V 4T7Telephone: (519) 457-3400 Fax: (519) 457-3030 www.trojanuv.com

Printed in Canada. Copyright 2008. Trojan Technologies London, Ontario, Canada.No part of this publication may be reproduced, stored in a retrieval system, or transmitted in any form or by any means without the written permission of Trojan Technologies.

Products in this publication may be covered by one or more of the following patents: Can. 2,117,004; Can. 2,239,925; US 5,418,370; US RE36,896; US 6,342,188; US 6,564,157; US 6,773,604; US 6,646,269; US 6,659,431; US 6,500,346. Other patents pending.OA-E-M&S-5.2-BR-CA0003-0908

Trojan UV Technologies UK Limited (UK): +44 1905 77 11 17Trojan Technologies (The Netherlands): +31 70 391 3020Trojan Technologies (France): +33 1 6081 0516Trojan Technologies Espana (Spain): +34 91 564 5757Trojan Technologies Deutschland GmbH (Germany): +49 6024 634 75 80Hach/Trojan Technologies (China): 86-10-65150290

System SpecificationsModel 04AL20 08AL30 18AL40 32AL50 72AL75 D72AL75

Number of Lamps 4 8 18 32 72 144

Lamp Type High-efficiency, High-output, Low-Pressure Amalgam

Sleeve WipingAutomatic Wiping System

(Optional Off-line Chemical Cleaning)

Ballast Electronic, constant output (100% power) Electronic, variable output (60 to 100% power)

Reactor Chamber

Materials of Construction 316L Stainless Steel

Standard Flange Size (ANSI/DIN), inches (mm) 6 (150) 8 (200) 10 (250) 12 (300) 20 (500) 20 (500)

Outlet Flange OrientationMultiple orientations available 3, 6, 9, or 12 o’clock position

Approx. Reactor Length, inches (mm) 80 (2032) 80 (2032) 80 (2032) 90 (2286) 90 (2286) 152 (3861)

Max. Operating Pressure, PSI (bar) 150 (10) 150 (10) 150 (10) 100 (6.8) 65 (4.5) 65 (4.5)

Dry Reactor Weight, lbs (kg) 107 (49) 210 (95) 400 (181) 1600 (726) 2100 (953) 3700 (1678)

Wet Reactor Weight, lbs (kg) 232 (105) 480 (218) 877 (398) 2200 (998) 3700 (1678) 7200 (3265)

Power Distribution Center

Electrical Supply 240 VAC, 1 phase, 2 wire + GND, 50/60 Hz 480Y/277 V, 3 phase, 4 wire + GND, 60 Hz

Dimensions, inches 24 x 24 x 10 30 x 24 x 10 36 x 48 x 10 40 x 78 x 18 48 x 86 x 24 96 x 86 x 24

Dimensions, mm 610 x 610 x 254 762 x 610 x 254 914 x 1219 x 254 1016 x 1981 x 457 1219 x 2184 x 610 2438 x 2184 x 610

Available Materials of ConstructionMild Painted Steel

304 Stainless Steel

Panel Rating NEMA 3R or 4X NEMA 12 or 4X

System Control Center

Controller Microprocessor PLC-based

Location Built into Power Distribution Center (PDC) Stand-alone Panel

Electrical Supply N/A (see PDC) 120 V, 1 phase, 2 wire + GND, 60Hz

Panel Rating N/A (see PDC) NEMA 12 or 4X

Typical Outputs Provided Reactor status, common alarms and SCADA communication

Find out how your wastewater treatment plant can benefit from proven TrojanUVFIT™ solutions. Contact us today.



APPENDIX H

Calculations for Odor Control System

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B C D E F

TITLE: Ventialtion Requirments

Prepared by: C. Alix Date: 7/24/2009Date:

Revision: 0

OBJECTIVE To determine ventialtion form WW processes excluding rooms

denotes calculated value

DESIGN ASSUMPTIONS & INFORMATIONInlet Screen

1 NFPA requires 12 ACH 2 H2S Concentration could govern vent rate

For Anoxic Zones1 No NFPA requirement2 Provide capture velocity of 100 ft/min across one hatch per zone

For Aeration Basins1 No NFPA requirement2 Provide capture velocity of 100 ft/min across one hatch per zone3 Collect input process air in addition to hactch capture air 150 cfm per basin

For Post Aeration Zone 1 No NFPA requirement2 Provide capture velocity of 100 ft/min across one of two hatches per zone

MBR1 Collect scour air 130 cfm2 No NFPA requirement

Odor Control Area1 NFPA requires 6 ACH within 3 ft of equipment

Rooms1 All process air will be drawn from the rooms

DESCRIPTION UNIT CALCULATION COMMENT

Ventilation CalculationInlet Screen

Space Volume ft3 54 Air change Rate ACH 12 Min per air change minutes 5 Airflow ft3/min 11

Anoxic ZonesNumber of zones 2 Hatch size ft2 9 Capture velocity ft/min 100 Open hatches per zone 1 Airflow ft3/min 1,800

Aeration BasinsNumber of basins 2 Hatch size ft2 9 Capture velocity ft/min 100 Open hatches per zone 1 Airflow ft3/min 1,800

Post Anoxic ZoneNumber of zones 2 Hatch size ft2 9 Capture velocity ft/min 100 Open hatches per zone 1 Airflow ft3/min 1,800

Odor Control AreaAssumed footprint area 15 x 15 ft2 225 Area Height around possible leak areas ft 10 Required air changes ACH 6 minutes per air change minutes 10 Airflow ft3/min 225 Total process air collection rate ft3/min 5,636

Room area 1Length ft 18 Width ft 30 Height ft 19 Volume ft3 10,278 Rate ACH 12 Minutes per air change minutes 5 Airflow ft3/min 2,056

Room area 2Length ft 30 Width ft 30 Height ft 15 Volume ft3 14,095 Rate ACH 12 Minutes per air change minutes 5 Airflow ft3/min 2,819 Total room air collection rate ft3/min 4,875 Process air governs ventilation thus 100% fresh air in rooms

Total ventilation in rooms ft3/min 5,636 Constant fresh air supply ft3/min 5,636 Recirculation air ft3/min None

CALC_Odor Control_Rev 0.xlsx Ventilation Page 1

TITLE: Carbon Filter Sizing

Inlet Air Properties ReferenceAbsorption Capacity

(lbs/lbs carbon)General Carbon Carbtrol Purafil TIGG Virgin

Caustic Impregna

ted CatalyticAir flow 7,000 cfm Hydrogen Sulfide 0.20 0.05 0.30 0.04 0.29 0.20 Temperature 70 oF siloxaneRelative Humidity 70 % Methyl MercaptanSpecific Volume 13.5863 ft3/lbs ASHRAE Handbook adjusted for temp and RH VOC 0.24 0.21 0.20 Molewcular Weight 28.97 lbs/lbs mole Dimethyl SulfideMolar Volume 393.6 ft3/lbs mole Carbon Disulfide

Carbonyl SulfideCarbon Type Virgin Dimethyl DisulfideRequired Media Life 8760 hoursPropertiesDensity 28.09 lbs/ft3 Media specificationsMax face Velocity 50.0 ft/minResidence Time 3.0 sec

Compound Concentration Molecular

WeightAdsoption Capacity

Compound Loading

Carbon Required

Carbon Required

Carbon Usage

(ppm)(lbs/lbs mole) (lbs/lbs carbon) (lbs/hr) (lbs) (ft3) (lbs/day)

Hydrogen Sulfide 1.00 34 0.04 0.04 7,946 282.8 21.8 siloxane - 371 1 0.000 - - Methyl Mercaptan - 48 1 0.00 - - VOC 1.00 92 0.21 0.10 4,095 145.8 11.2 Dimethyl Sulfide - 62 1.00 0.00 - - Carbon Disulfide - 94 1 0.00 - - Carbonyl Sulfide - 1Dimethyl Disulfide - 1Total 12,041 429

Vessel Sizing

Bed type DualCarbon Volume Req'd 428.61 ft3

Number of vessels 1.00 Req'd Vessel Diamter 9.44 ftVessel Diameter 10.00 ftTotal Bed Depth 5.46 ftTotal Bed Depth 6.00 ftResidence time 3.67 secondsFace Velocity 44.56 ft/minHeadloss through bed 1.00 in w.c./ft bed depthActual bed headloss 3.00 in w.c.

Bed type RadialCarbon Volume Req'd 428.61 ft3

Number of vessels 3.00 2.00 1.00 Req'd Vessel Diamter 7.00 8.00 10.00 ftBed Height 13.00 13.00 15.00 ftPlenum Diameter 2.17 2.50 3.00 ftTotal Bed Dia. 4.23 4.90 6.40 ftTotal Bed volume 405.14 362.67 376.52 ft3

Residence time 3.47 3.11 3.23 secFace Velocity 40.49 34.98 23.21 ft/minHeadloss through bed 0.50 0.50 0.50 in w.c./ft bed depthActual bed headloss 1.06 1.23 1.60 in w.c.

Vendor WEF MOP 8 Reference Table 13.

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