EP 2005-5186 Heat Exchangers

Restricted EP 2005-5186

EP Heat Exchanger Selection Guideline by

T&OE Process Engineering Discipline Standards & Guidelines Working Group

Sponsor: SIEP Rijswijk (EPT-OE-FL)

Approved by: J. Marshall (EPT-OE-FL)

Date of issue: October 2005

Revision: 3

Account code: S-000049-400

ECCN number: Not subject to EAR-No US content

This document is classified as Restricted. Access is allowed to Shell personnel, designated Associate Companies and Contractors working on Shell projects who have signed a confidentiality agreement with a Shell Group Company. 'Shell Personnel' includes all staff with a personal contract with a Shell Group Company. Issuance of this document is restricted to staff employed by a Shell Group Company. Neither the whole nor any part of this document may be disclosed to Non-Shell Personnel without the prior written consent of the copyright owners.

Copyright 2005 SIEP B.V.

SHELL INTERNATIONAL EXPLORATION AND PRODUCTION B.V., RIJSWIJK

Further electronic copies can be obtained from the Global EP Library, Rijswijk

EP 2005-5186 - II - Restricted

SUMMARY

This new EP guideline on the selection of heat exchanger types has been developed by the Process Engineering Discipline Leadership Team.

The guideline provides an overview of typical applications and gives examples of what heat exchangers have often been selected. It also provides a description of the most common heat exchanger types available: shell and tube, plate and printed circuit. The design envelope of each type has been defined and a procedure has been developed to select a fit for purpose heat exchanger with the lowest life cycle costs.

The design envelopes are summarised in the table below:

Type Design pressure Pressure drop Design temperature Leakage

Shell & Tube

(standard)

< 350 bar(g) Low -100 to 600 C Low risk

Shell & Tube

hair pin

< 350 bar(g) Low -100 to 600 C Low risk

Shell & Tube

with

turbulators

< 350 bar(g) Medium -100 to 600 C Low risk

Plate (gasket) < 25 bar(g) Medium -30 to 160 C Medium risk

Plate (semi-

welded)

< 25 bar(g) Medium -30 to 160 C Medium risk on

gasket side. Low

risk on welded

side.

Plate (welded) < 40 bar(g) Medium -30 to 300 C Low risk

Printed Circuit < 600 bar(g) Medium -100 to 200 C Avoid

rapid cycling greater

than 50 C.

Low risk

Air cooler < 350 bar(g) Low -100 to 400 C Low risk

KEYWORDS

Process Engineering, heat exchangers

EP 2005-5186 - III - Restricted

TABLE OF CONTENTS

SUMMARY II

1. INTRODUCTION 1 1.1. Background and objectives 1 1.2. Guideline structure 1 1.3. Review and improvements 1

2. HEAT EXCHANGER TYPES 2 2.1. General 2 2.2. Shell and tube heat exchangers 2 2.3. Plate heat exchangers 4 2.4. Printed circuit heat exchangers 6 2.5. Air cooled heat exchangers 6 2.6. Special heat exchangers 8

3. TYPE SELECTION GUIDELINE 10 3.1. Key design envelope parameters 10 3.2. Design envelope heat exchanger types 11 3.3. Type selection procedure 12 3.4. Selection cooling or heating medium 13 3.5. Heat exchangers not normally operating 14

4. TYPICAL APPLICATIONS 15 4.1. Well stream cooling 15 4.2. Gas/gas heat exchanger in LTS plant 15 4.3. Compressor gas cooling 15 4.4. Wet oil heating 15 4.5. Glycol regeneration skid 16 4.6. Direct versus indirect seawater cooling 16

5. ABBREVIATIONS USED 17

REFERENCES 18

EP 2005-5186 - IV - Restricted

LIST OF FIGURES

Figure 2.1: Shell & Tube Heat Exchanger (from Southern Heat Exchanger Website) 2

Figure 2.2: Schematic hair pin Shell & Tube Heat Exchanger (from Brown Fintube Website) 3

Figure 2.3: Schematic of twisted tubes (from Brown Fintube Website) 3

Figure 2.4: EMBaffle arrangement 4

Figure 2.5: Schematic turbulator (from Cal Galvin Web site) 4

Figure 2.6: Schematic of Plate Heat Exchanger (from ISO-15547) 5

Figure 2.7: Schematic of fully welded Plate Heat Exchanger (from Alfa Laval website) 5

Figure 2.8: Schematic Printed Circuit Heat Exchanger (from DEP 31.21.01.11-Gen) 6

Figure 2.9: Schematic of air cooled heat exchanger (from ISO-13706) 7

Figure 2.10: Schematic spiral flow heat exchanger (from Alfa Laval Website) 8

Figure 2.11: Schematic plate fin heat exchanger (from Chart Heat Exchangers Website) 9

Figure 2.12: Plate and shell heat exchanger (from Vahterus Website) 9

Figure 3.1: Heat exchanger type selection flow chart 12

Figure 4.1: Schematic LTS plants (from Heatric Website) 15

Figure 4.2: Schematic glycol regeneration system 16

LIST OF TABLES

Table 3.1: Design envelope heat exchanger types 11

EP 2005-5186 - 1 - Restricted

1. INTRODUCTION

1.1. Background and objectives

In 2003, the Process Engineering Discipline Leadership Team (DLT) identified the need for an EP guideline on the selection of heat exchangers. The existing Design Engineering Practices (DEPs) define how to design a heat exchanger, but provide little guidance on what type to select. The Shell Expro heat exchanger selection guide (EA-105) essentially covers this area and served as the starting point for this new EP guideline. Another important source of information has been the Surface Global Network (SGN).

1.2. Guideline structure

The guideline starts with a general discussion on the types of heat exchangers available (section 2). This section should be skipped by those familiar with the types. The selection is driven by the design envelope of each heat exchanger and ultimately the life cycle costs (section 3). Typical applications are described in section 4.

Mandatory requirements are defined in DEPs, procedures, specifications and standards.

For process safeguarding aspects, the reader is referred to section 3 of the EP Process Safeguarding guideline (EP 2004-5042).

1.3. Review and improvements

This guideline has been prepared by the working group on standards and guidelines and approved by the Process Engineering DLT. The guideline was posted on the Surface Global Network to obtain feedback from the surface facilities community.

The document will be revalidated on a 5 yearly basis by the Process Engineering working group on standards and guidelines. The next revalidation is due in December 2009. In the event any significant changes are required, the document will be updated earlier.


2. HEAT EXCHANGER TYPES

2.1. General

The heat exchanger type classification is aligned to the DEP and ISO standards:

Shell & Tube Heat Exchangers (STHE)

Plate Heat Exchangers (PHE)

Printed Circuit Heat Exchangers (PCHE)

Air Cooled Heat Exchangers (ACHE)

These types of exchangers are described in this section. Special heat exchangers are mentioned, but not further considered, as they are not commonly applied in EP or are not yet proven technology.

2.2. Shell and tube heat exchangers

Shell and Tube Heat Exchangers (STHE) are the most widely used type of heat exchangers. They are robust and the thermal, hydraulic and mechanical design is well established. The design details are provided in DEP 31.21.01.30-Gen. A typical schematic is shown in Figure 2.1 below.

Figure 2.1: Shell & Tube Heat Exchanger (from Southern Heat Exchanger Website)

Double pipe and multi-tube, hair pin heat exchangers are a variation to the shell and tube heat exchanger type. The double pipe heat exchanger is particularly suited for dirty services on the shell side. The multi-tube heat exchanger is designed for counter current flow and thus allows temperature cross-over, i.e. the hot fluid outlet temperature is below the cold fluid outlet temperature. A schematic is shown in Figure 2.2.


Figure 2.2: Schematic hair pin Shell & Tube Heat Exchanger (from Brown Fintube

Website)

The twisted tube, shell and tube heat exchanger, is another novel variation, which can improve the heat transfer, particularly on the tube side. It is used for both new installations and retrofitting in existing shells. The exchanger is more expensive per unit surface area, but does reduce space and is therefore suitable for offshore facility applications. Whilst retrofitting twisted tubes, the 2 additional circumferential welds to fit the U bend, needs attention. Figure 2.3 below shows a twisted tube schematic.

Figure 2.3: Schematic of twisted tubes (from Brown Fintube Website)

Other heat transfer improvements include the installation of helix baffles/vanes on the shell side and/or turbulators in the tubes. The helix baffles may improve the performance on the shell side. Shell Global Solutions developed the Expanded Metal baffle arrangement (EMBaffle), which supports the tubes and guides the flow in predominantly axial direction (see Figure 2.4). There are no stagnant zones and the expanded metal causes disturbances that enhance the heat transfer.


Figure 2.4: EMBaffle arrangement

Turbulators increase the turbulence in the tubes, at the expense of a higher pressure drop. The increased turbulence can reduce the fouling propensity on the one hand, but the inserts create more obstructions on the other hand. Figure 2.5 shows a schematic of the HiTran turbulator.

Figure 2.5: Schematic turbulator (from Cal Galvin Web site)

2.3. Plate heat exchangers

Plate and Frame Heat Exchangers (PHE) consists of an arrangement of pressed metal plates, aligned on two bars and secured between two covers by compression bolts (see Figure 2.6). Plates can be added and removed in the field, should service requirements change.

The plate pack can be assembled with:

Gaskets

Semi welded plates (one side welded only)

Fully welded plates

Low pressure designs (< 25 bar) consist of the gasket type. They are often cheaper than shell and tube heat exchangers and allow access to the heat exchange surface for mechanical cleaning. Medium pressure services (< 40 bar) can be achieved with welded plates. A schematic of a fully welded heat exchanger is shown in Figure 2.7.


The Plate Heat Exchangers are compact and therefore have a high heat exchange surface to volume ratio (< 300 m2/m3), compared to shell and tube heat exchangers (~ 50 m2/m3). Further details are provided in DEP 31.21.01.32-Gen.

Figure 2.6: Schematic of Plate Heat Exchanger (from ISO-15547)

Figure 2.7: Schematic of fully welded Plate Heat Exchanger (from Alfa Laval website)


2.4. Printed circuit heat exchangers

Printed Circuit Heat Exchanger (PCHE) consists of a pack of stainless steel plates with 2 mm flow channels chemically milled on one side (see Figure 2.8). The pack is diffusion bonded in a furnace to form a solid heat exchanger core. The fluid manifold headers and nozzles are welded to the outside of the core. For small units a ported design is used with internal headers provided by holes inside the core block.

PCHEs are very compact and light weight and therefore particularly suited to offshore applications. The effective heat area over volume ratio can be as high as 2500 m2/m3. PCHEs are primarily recommended for clean service. Chemical and pressure pulse techniques are available for cleaning. Rapid temperature cycling has caused fatigue failure in the past. Temperature cycles exceeding 50 C should therefore be avoided. PCHEs are only available from a single source, Heatric.

For further details consults DEP 31.21.01.11-Gen and DEP 31.21.01.33-Gen.

Figure 2.8: Schematic Printed Circuit Heat Exchanger (from DEP 31.21.01.11-Gen)

2.5. Air cooled heat exchangers

Air Cooled Heat Exchangers (ACHE) consist of finned tube bundles mounted over electric motor driven fans rejecting heat to ambient air (see Figure 2.9).


Figure 2.9: Schematic of air cooled heat exchanger (from ISO-13706)

The normal design has forced draft fans which are mounted below the tube bundle for easier maintenance. If induced draft units are selected, motor drivers should be mounted under the bundles for ease of maintenance. The advantages of forced draft are:

Lower power consumption of the fan drives.

Fan blades are not exposed to hot air.

Better accessibility to fan and drive.

More suitable to install a warm air re-circulation arrangement.

The advantages of induced draft are:

Better distribution of air across the section

Less re-circulation of hot air.

If control of the process outlet temperature is required within close limits, there are three basic methods of control including auto louvers, variable pitch fans, variable speed and on/off motors. Louver control is not preferred since louvers are a high maintenance item being subject to corrosion and linkage failure. Variable pitch fans are an option but can require high maintenance on actuators. Variable speed motors involve higher costs but are very reliable and are therefore usually preferred.

If it is possible to over cool gas streams and operate in hydrate formation regions during low ambient temperatures, a method of control is required to prevent low process temperatures, for example by a split range control on louvers and variable speed fans. Temperature control with a bypass gas stream is not feasible in this case.

The design ambient air temperature should be carefully selected. The design value is usually the temperature not exceeded for more than 2% of the operating time. A probabilistic approach can be adopted to trade-off increased air cooler costs against the expected production deferment.


The performance of (existing) air coolers can be increased by water spraying, but this practice is not recommended. The application is generally restricted to regions with limiting dry bulb temperatures and low service temperature requirements.

2.6. Special heat exchangers

Kettle re-boilers

Kettle re-boilers are commonly applied in the refinery industry. It is essentially a tube bundle fitted into a kettle vessel. They are not further addressed in this guideline.

Spiral heat exchangers

A spiral heat exchanger is a circular heat exchanger with two concentric spiral channels, one for each fluid (see Figure 2.10). It is a welded plate heat exchanger type. The experience in the EP industry is limited.

Figure 2.10: Schematic spiral flow heat exchanger (from Alfa Laval Website)

Plate fin heat exchangers

Plate fin heat exchangers are assembled from a series of flat sheets and fins in a sandwich construction. Parting sheets are positioned alternatively with the layers of fins in a stack to form the containment between individual layers. These elements are built into a complete core and then brazed to form an integral unit (see Figure 2.11). The exchangers can be made from brazed aluminium or stainless steel. The stainless steel versions are available only in small block sizes and with reduced design pressures. Aluminium brazed heat exchangers have long experience in cryogenic service, where fluids are very clean. The exchanger is susceptible to mechanical damage, corrosion from chlorides/mercury and fire.


Figure 2.11: Schematic plate fin heat exchanger (from Chart Heat Exchangers Website)

Plate and shell heat exchangers

Plate and shell heat exchangers consist of a fully welded plate pack of circular plates housed within an outer pressure vessel. It is a compact design and allows for pressures up to 100 bar(g) and temperature up to 400 C. Figure 2.12 shows a schematic.

Figure 2.12: Plate and shell heat exchanger (from Vahterus Website)


3. TYPE SELECTION GUIDELINE

3.1. Key design envelope parameters

Design pressure

Design pressure is an important parameter and several heat exchanger types, e.g. gasket plate heat exchangers, have limited design pressures due to the relatively large flat surface areas exposed to process pressure. High pressure shell and tube exchangers can also be extremely heavy due to the required wall thickness. The high pressure fluid should therefore generally be on the tube side.

Design temperature

For most applications design temperatures are not particularly high (< 200 C) and most heat exchanger types can be selected, apart from gasket plate heat exchanger designs which have limitations due to the gasket material.

Pressure drop

The pressure drop across the heat exchanger (both sides) can be a critical parameter in selecting the type. For example, the pressure drop in a gas plant often needs to be compensated by additional compression capacity, which increases the life cycle costs.

Materials

Materials of construction and gasket material should be selected to ensure an adequate design life for the equipment. The options are discussed in reasonable detail in section 3.2.8 of DEP 39.01.10.11-Gen for all types of heat exchangers. Shell and tube heat exchanger materials are discussed in detail in DEP 31.21.01.31-Gen.

Leakage

The risk of leakage from one stream to another stream and/or ambient, should be evaluated and the consequence of leakage should be considered in the overall system to ensure a safe design. Certain types of exchanger e.g. shell and tube exchangers have higher integrity when considering leakage. Plate heat exchangers are not particularly robust requiring either total re-gasketing or a new plate pack.

Fouling, blockage and cleaning

The fouling and blockage nature of the fluid is also an important parameter. The need to obtain access to the surface for inspection and mechanical cleaning is also an important consideration in heat exchanger selection. The type of fouling should be identified as either particulate type (risk of blockage) or precipitation/deposition type (risk of scaling or wax fouling, etc.). Hydrate formation can also cause blockage and might need continuous inhibition. For further details consult DEP 20.21.00.31-Gen.


3.2. Design envelope heat exchanger types

The design envelope of heat exchanger types is listed in table 3.1 below. These limits might be relaxed with special designs the manufacturers can offer.

Table 3.1: Design envelope heat exchanger types

Type Designpressure

Pressure drop

Design temperature Leakage Fouling, cleaning and inspection Robustness Repair ease

Shell & Tube (standard)

< 350 bar(g)

Low -100 to 600 C Low risk Tube side is tolerant to fouling. Bundle with straight tubes can be removed for cleaning and inspection.

High High

Shell & Tube hair pin

< 350 bar(g)

Low -100 to 600 C Low risk Tolerant to fouling and easy to clean and inspect.

High Medium

Shell & Tube with turbulators

< 350 bar(g)

Medium -100 to 600 C Low risk Increased turbulence can reduce the fouling propensity, but the inserts are an obstruction. Bundle can be removed for cleaning and inspection.

Medium High

Plate (gasket)

< 25 bar(g)

Medium -30 to 160 C Medium risk Sensitive to fouling. Can be taken apart, but re-assembly can be difficult.

Low Medium

Plate (semi-welded)

< 25 bar(g)

Medium -30 to 160 C Medium risk on gasket side. Low risk on welded side.

Sensitive to fouling. Chemical cleaning only option on welded side. Difficult to inspect.

Low Medium

Plate (welded)

< 40 bar(g)

Medium -30 to 300 C Low risk Sensitive to fouling. Chemical cleaning only. Difficult to inspect.

Low Low

Printed Circuit

< 600 bar(g)

Medium -100 to 200 C Avoid rapid cycling greater than 50 C.

Low risk Very sensitive to fouling. Chemical or pressure pulse cleaning only option. Difficult to inspect.

Low Low

Air cooler < 350 bar(g)

Low -100 to 400 C Low risk Tube side tolerant to fouling. Cleaning and inspection ease depends on header type.

Medium Depends onheader type


3.3. Type selection procedure

The type selection procedure is shown in the flow chart below:

Define heating and

cooling medium.

Determine operating

envelope.

Eliminate types that can not

meet envelope (table 3.1).

Size heat exchanger and

ancillary equipment (filters).

Eliminate types that do not fit

any space & weight

restrictions.

Estimate Capex, Opex and

potential deferments for each

remaining type.

Select type with the required

availability and lowest life

cycle costs.

Figure 3.1: Heat exchanger type selection flow chart

Space and weight

In general shell and tube heat exchangers are the largest and heaviest exchanger type and removable bundle types require space for bundle withdrawal. Space savings can be made by considering the use of a special tube bundle withdrawing device. This device is a frame supported by a crane which can pull bundles into open space at the side of modules removing the requirement for bundle withdrawal floor areas in the module.

Plate and printed circuit heat exchangers can offer significant benefits in terms of weight and space. Some units can give over 50% reduced plot area compared with shell and tube type, although space savings can be reduced by the requirement for upstream filters, etc.


Capex

The materials need to be selected at this stage, as they have a significant impact on the Capex. The estimates should be based on historical costs (if available) or by seeking vendor quotations. The Capex should include the costs of any upstream filters, installation costs and the support costs. The support cost in an offshore environment is the platform costs assigned to the heat exchanger and in an onshore environment is the foundation costs.

Opex

The Opex is driven by cleaning, inspection, maintenance, repair and energy costs. What level of mechanical and/or chemical cleaning will be required? How often does the heat exchanger need to be inspected? What is the energy efficiency?

Potential deferment

When failure of the heat exchanger will cause (partial) shutdown of the process and production loss, the likelihood and time to repair will have to be assessed for each heat exchanger type. Can the heat exchanger be repaired in-situ? The potential deferment might justify installing spare heat exchangers.

3.4. Selection cooling or heating medium

The selection of an external cooling medium is largely driven by the location of the facilities. For offshore and coastal facilities both air and seawater are available. For in-land facilities air would essentially be the only choice. In general seawater cooling would allow the process stream to be cooled further, relative to air coolers. This can have positive effects on the downstream equipment (e.g. smaller glycol dehydration units). As a rule of thumb, air coolers are more cost effective if the process fluid is 40 C above the air ambient temperature.

Process streams within the plant can provide a suitable cooling medium. For example the cold condensate from a Low Temperature Separation (LTS) plant. In other applications a dedicated refrigerant loop will be required to achieve low temperatures.

External heat is usually provided by (gas) fired equipment or electric heaters and generates hot water, dedicated oil or steam. The application of water is limited to temperatures below 200 C. Hot oil systems can normally run up to 300 C. Steam is not commonly used in EP.

Process streams can also be a useful source of heat. For example heat recovery from turbines, glycol from the bottom of the regenerator still, crude from a stabiliser column. Heat recovery can either be direct or via an indirect closed circuit system. Heat integration across a plant is important to reduce the energy consumption. For example the hot water from a water cooler to heat-up a process stream elsewhere in the plant. The number of system interlinks should be limited, otherwise the plant will become inoperable. A formal pinch analysis could be carried-out to optimise the heat integration across a complex plant. In EP this technique is not often applied, as the plants are relatively simple.


3.5. Heat exchangers not normally operating

Heat exchangers can be required during start-up or shutdown, but not during normal operation. For example the well stream to a gas plant might have to be heated during start-up to avoid hydrates. These heat exchangers need special attention with respect to:

Materials need to be suitable for stagnant flow.

The duty might not have to cater for full flow.

Consider keeping the heat exchanger on-line by not providing a bypass.

Protection needs to consider the low and no flow situations.


4. TYPICAL APPLICATIONS

4.1. Well stream cooling

Well streams are either cooled with air or seawater. The service is two-phase and erosive in nature due to the velocities and potential sand production. The heat exchanger type would typically be shell and tube, in view of the high design pressures. Double pipe heat exchangers are particularly robust in seawater cooling applications, since the inner, well stream pipe is usually the same wall thickness and diameter as the flowline, whereas the shell and tube heat exchanger uses thin walled, small diameter tubes, more susceptible to fatigue and erosion. The flow direction in a double pipe heat exchanger hardly changes flow direction, whereas the fluid tends to slam into the tube sheet of a shell and tube heat exchanger and can lead to water hammer.

4.2. Gas/gas heat exchanger in LTS plant

The most common gas/gas heat exchanger type is shell and tube.

The use of printed circuit heat exchangers is nowadays a well accepted alternative, provided the service is clean. It allows the exchange of heat from more than 2 fluids in one heat exchanger (see Figure 4.1). The condensate stream from the cold separator is often added. Applications with glycol injection in printed circuit heat exchangers are rare in the Shell group (1 in Oman).

Figure 4.1: Schematic LTS plants (from Heatric Website)

4.3. Compressor gas cooling

The most common type of compressor inter-stage and outlet cooling is air coolers. Offshore, direct or indirect seawater cooling can be used with shell & tube heat exchangers. Plate heat exchangers are not normally used in view of the pressure limitations and pressure pulsations.

4.4. Wet oil heating

To dehydrate heavy oil it is often required to heat the wet oil to 70 to 80 C. The wet oil is typically heated directly by a fired heater (e.g. PDO Marmul station) or indirectly with plate heat exchangers (e.g. PDO Nimr station).


4.5. Glycol regeneration skid

Glycol regeneration skids have a number of heat exchangers (see Figure 4.2). The glycol/glycol heat exchangers are usually of the plate type. The condenser is normally an air cooler.

Figure 4.2: Schematic glycol regeneration system

4.6. Direct versus indirect seawater cooling

Seawater cooling can be applied directly or indirectly via a closed (water) cooling loop. The advantages of an indirect cooling system are:

The seawater/water heat exchanger is of low pressure and allows for the selection of a plate heat exchanger.

The water/process fluid heat exchanger experiences a clean medium on the cold side and enables the selection of low cost materials (carbon steel).

The disadvantages of an indirect cooling system are:

The number of equipment items is higher.

The overall approach temperature is increased.

In any case, the seawater bulk temperature should be kept below 60C, to minimise scaling and fouling risks. Detailed consideration of the wall temperature and scaling tendency of the specific application, might allow a higher temperature. Local regulations might also limit the temperature of the seawater returned to the sea. The seawater should be treated to avoid marine growth. Further details are provided in DEP 37.05.10.10-Gen.


5. ABBREVIATIONS USED

ACHE Air Cooled Heat Exchanger

DEP Design Engineering Practice

DLT Discipline Leadership Team

EP Exploration & Production

ISO International Standards Organisation

LTS Low Temperature Separation

PCHE Printed Circuit Heat Exchanger

PHE Plate Heat Exchanger

SGN Surface Global Network

STHE Shell and Tube Heat Exchanger


REFERENCES

Shell Design Engineering Practices:

Fouling resistances for heat transfer equipment

DEP 20.21.00.31-Gen, December 1998

Printed circuit heat exchangers selection and application

DEP 31.21.01.11-Gen, January 2005

Shell and tube heat exchangers (amendments/supplements to ISO 16812)

DEP 31.21.01.30-Gen, May 2004

Selected construction materials for shell and tube heat exchangers

DEP 31.21.01.31-Gen, December 2004

Plate and frame heat exchangers (amendments/supplements to ISO 15547)

DEP 31.21.01.32-Gen, September 2002

Printed circuit heat exchangers design and fabrication

DEP 31.21.01.33-Gen, January 2005

Air-cooled heat exchangers (amendments/supplements to ISO 13706)

DEP 31.21.70.31-Gen, March 2001

Design of seawater systems and utility heat transfer systems for offshore installations

DEP 37.05.10.10-Gen., September 2002

Selection of materials for life cycle performance (EP)

DEP 39.01.10.11-Gen., January 2005

Shell guidelines:

EP Guideline on Process Safeguarding, EP 2004-5042, 2004

International standards:

Petroleum and natural gas industries Air-cooled heat exchangers

ISO-13706, 2000

Petroleum and natural gas industries Plate heat exchangers

ISO-15547, 2000

Petroleum and natural gas industries Shell-and-tube heat exchangers

ISO-16812, 2003


The copyright of this document is vested in Shell International Exploration and Production B.V., The Hague, The Netherlands. All rights reserved. Neither the whole nor any part of this document may be reproduced, stored in any retrieval system or transmitted in any form or by any means (electronic, mechanical, reprographic, recording or otherwise) without the prior written consent of the copyright owner.

SUMMARYTABLE OF CONTENTSINTRODUCTIONBackground and objectivesGuideline structureReview and improvements

HEAT EXCHANGER TYPESGeneralShell and tube heat exchangersPlate heat exchangersPrinted circuit heat exchangersAir cooled heat exchangersSpecial heat exchangers

TYPE SELECTION GUIDELINEKey design envelope parametersDesign envelope heat exchanger typesType selection procedureSelection cooling or heating mediumHeat exchangers not normally operating

TYPICAL APPLICATIONSWell stream coolingGas/gas heat exchanger in LTS plantCompressor gas coolingWet oil heatingGlycol regeneration skidDirect versus indirect seawater cooling

ABBREVIATIONS USEDREFERENCES

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EP 2005-5186 Heat Exchangers

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