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Page 1: Hextran Keyword v9

HEXTRAN 9.0Keyword Manual

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HEXTRAN Keyword Manual The software described in this guide is furnished under a licenseagreement and may be used only in accordance with the terms ofthat agreement. Information in this document is subject tochange without notice. Invensys Systems, Inc. assumes noliability for any damage to any hardware or software componentor any loss of data that may occur as a result of the use of theinformation contained in this manual.

Copyright Notice © 2002 Invensys Systems, Inc. All rights reserved. No part ofthe material protected by this copyright may be reproduced orutilized in any form or by any means, electronic or mechanical,including photocopying, recording, broadcasting, or by anyinformation storage and retrieval system, without permission inwriting from Invensys Systems, Inc.

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Table of Contents

Chapter 1 Introduction . . . . . . . . . . . . . . . . . . . . . . 1-1About This Manual . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 1-1

About HEXTRAN . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 1-2

Compatibility with Earlier Versions of HEXTRAN . . . . . . . . . . . . . . 1-2

About SIMSCI . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 1-4

Chapter 2 Overview . . . . . . . . . . . . . . . . . . . . . . . 2-1About This Chapter . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 2-1

Scope and Objectives of HEXTRAN. . . . . . . . . . . . . . . . . . . . . . 2-1

Chapter 3 Using HEXTRAN . . . . . . . . . . . . . . . . . . . . 3-1About This Chapter . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 3-1

What HEXTRAN Does . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 3-1

Global Settings . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 3-1

Defining Components. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 3-3

Stream Data . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 3-10

Flowsheet Calculations . . . . . . . . . . . . . . . . . . . . . . . . . . . . 3-11

Targeting Calculations. . . . . . . . . . . . . . . . . . . . . . . . . . . . . 3-13

Unit Operations . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 3-15

Building an Input File . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 3-22

Chapter 4 Input Reference . . . . . . . . . . . . . . . . . . . . 4-1About This Chapter . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 4-1

Categories of Input . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 4-1

Keywords . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 4-2

HEXTRAN Keyword ManualJune 2002 i

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Qualifiers . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 4-3

Multiple Entries . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 4-3

Commenting Input . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 4-3

Defaulting . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 4-3

Units of Measure . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 4-4

Continuing Statements . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 4-5

Layout of Input . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 4-5

Key to Description of Input Statements . . . . . . . . . . . . . . . . . . . . 4-6

General Data Category of Input . . . . . . . . . . . . . . . . . . . . . . . . 4-7

Component Data Category of Input . . . . . . . . . . . . . . . . . . . . . . 4-21

Thermodynamic Data Category of Input . . . . . . . . . . . . . . . . . . . 4-30

Stream Data Category of Input . . . . . . . . . . . . . . . . . . . . . . . . 4-38

Internal Property Data Category of Input . . . . . . . . . . . . . . . . . . . 4-64

External Property Data Category of Input . . . . . . . . . . . . . . . . . . 4-67

Flowsheet Calculations Category of Input . . . . . . . . . . . . . . . . . . 4-75

Simulation Category of Input . . . . . . . . . . . . . . . . . . . . . . . . . 4-83

Regression Category of Input . . . . . . . . . . . . . . . . . . . . . . . . . 4-90

Cleaning Casestudy Category of Input . . . . . . . . . . . . . . . . . . . 4-101

Split Flow Optimization Category of Input . . . . . . . . . . . . . . . . . 4-112

Area Optimization Category of Input . . . . . . . . . . . . . . . . . . . . 4-121

Targeting Category of Input . . . . . . . . . . . . . . . . . . . . . . . . . 4-131

Synthesis Category of Input . . . . . . . . . . . . . . . . . . . . . . . . . 4-141

Unit Operations Category of Input . . . . . . . . . . . . . . . . . . . . . 4-148

Chapter 5 Technical Reference . . . . . . . . . . . . . . . . . 5-1General Information . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 5-1

Pipes . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 5-3

Rigorous Heat Exchanger. . . . . . . . . . . . . . . . . . . . . . . . . . . . 5-6

Index. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . I-1

HEXTRAN Keyword Manualii June 2002

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HEXTRAN Keyword ManualJune 2002 iii

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Chapter 1IntroductionAbout This Manual

The HEXTRAN Keyword Manual describes the capabilities and use of theHEXTRAN program and is designed to help you get the best out of theprogram. It can be used with all mainframe and PC versions of HEXTRAN.

See... Which... If you are a ...

Chapter 1Introduction

Introduces the manual, theprogram, and the company.

New User

Chapter 2Overview

Explains the main concepts ofheat exchangers.

New User

Chapter 3Using HEXTRAN

Describes the data needed torun HEXTRAN, the way it usesthe data, and how to use theprogram.

New or Occasional User

Chapter 4Input Reference

Provides statement-by-statement descriptions of theHEXTRAN input.

New, Occasional, orExperienced User

Chapter 5Technical Reference

Provides detailed backgroundinformation to models used inHEXTRAN.

New or Occasional orExperienced User

New UsersNote: If you read nothing else, read Chapter 3, Using HEXTRAN.

If you are an engineer new to HEXTRAN, this manual tells you what theprogram does and how to use it. Chapter 2, Overview, describes the scopeof the program and the concepts involved in heat exchange.

Chapter 3, Using HEXTRAN, describes the data that the program needs, theconventions to follow in entering the data into the program, and what theprogram will produce as output. It then describes all the capabilities of theprogram and how to invoke them, with signposts given to guide youthrough Chapter 4, Input Reference.

Finally, Chapter 5, Technical Reference, gives more detailed information onmethodologies used in the program calculations.

HEXTRAN Keyword Manual Chapter 1, IntroductionJune 2002 1-1

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Occasional UsersIf you are an occasional user revisiting HEXTRAN after an absence, takesome time to skim through Chapter 3, Using HEXTRAN, to remind yourselfof the program’s capabilities and conventions. Then go on to Chapter 4,Input Reference.

Experienced UsersIf you use HEXTRAN regularly, you will be able to find everything youneed in Chapter 4, Input Reference, and Chapter 5, Technical Reference.

About HEXTRANThe HEXTRAN simulation program is a comprehensive simulation systemdesigned to assist process engineers analyze and design all types of heattransfer systems. The complete spectrum of heat transfer design is included,from conceptual design with pinch analysis through the rating and design ofexchangers and networks of exchangers. HEXTRAN versions 8.0 and laterinclude the full capabilities of the PRO/II® Simulation Program forrepresenting process streams and generating the associated thermodynamicand transport properties. Steam and water phase behavior and theassociated properties can be retrieved from the steam tables. TheHEXTRAN standard version is the basic HEXTRAN calculations engine,and is required for Typical, Custom and Network installations. This basicpackage offers a keyword driven interface.The GUI provides a Microsoft®Windows®-based graphical interface for the standard program.

Only HTRI and HTFS members can install and use the HTRI and HTFSadd-ons, respectively.

Compatibility with Earlier Versions of HEXTRANThe keyword input files for HEXTRAN versions 7.x and earlier are notcompatible with the current release. These changes are the result of theincorporation of the powerful PRO/II thermophysical process package andPRO/II’s stream-specific point access feature. Most of the keyword changesare therefore related to the PRO/II syntax. This section enumerates thechanges that have been made.

Unit of Measure KeywordsHEXTRAN now supports syntax for dimensional units as used in PRO/II.In cases where the HEXTRAN syntax is inconsistent with the PRO/IIsyntax, both forms of syntax are supported (Table 1-1).

Note: This change impacts input processing only. There is no impact oneither calculations or reports.

Chapter 1, Introduction HEXTRAN Keyword Manual1-2 June 2002

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Table 1-1: Dimensional Unit Keyword Changes

Category HEXTRAN Syntax PRO/II Syntax

PressureKGCM KG/CM2

WeightSTLTMT

TONTONLTONM

U-value, Film CoefficientBTUHKCH

BTU/HKC/H

DensityLBFTKGM3

LB/FT3KG/M3

Viscosity LBFSLBSFLBFH

LB/FSLBS/FLB/FH

PRINT StatementThe PRINT statement in the General Data section has been expanded tosupport the stream reports that are now available with point access.

Note: This change impacts processing and report formats only. There is noimpact on existing report formats; input files are upwardly compatible.

The old syntax is:

PRINT ALL, NONE, GENERAL, PROPERTY, STREAM, UNIT

The new syntax is:

PRINT ALL, NONE, GENERAL, PROPERTY, STREAM, UNIT, *SFORMAT=ALL or COMPONENT or SUMMARY, *RATE=M, WT, LV, GV, *PERCENT=M, WT, LV, GV, *TBP

Note: The new keyword functionality is explained in detail in Chapter 5,Input Reference.

Stream/Unit ID LengthStream and unit IDs now support a 12 character format rather than theformer 4 character format. This applies to all streams and unit operations.Unit, stream, and data sheet reports support the new 12 character format.

HEXTRAN Keyword Manual Chapter 1, IntroductionJune 2002 1-3

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Stream DataThe following changes have been made to Stream Data statements:

■ The PROC keyword has been changed to PROP.

■ The STRM keyword has been changed to STREAM.

■ The SET keyword now specifies the thermodynamic property set asso-ciated with a stream. One of the main reasons old keyword input filesmay not run unless they are converted to version 8 syntax.

■ SETNO now specifies a set number for HEXTRAN’s internal propertygrid. If a SETNO is not specified, HEXTRAN will use point access.

■ BLEND and XBLEND keywords are supported.

Note: The new keyword functionality is explained in detail in Chapter 4,Input Reference.

File ConversionsIf you are using the keyword version of HEXTRAN, please see theHEXTRAN PC/LAN Installation Guide for more information.

Note: You cannot upgrade HEXTRAN files earlier than version 7.0 directlyto version 9.0 format. You must first use the HEXTRAN version 7.0conversion file, HXDBUPDT, to update the old files to version 7.0 format,and then convert the files to 9.0 format. See the HEXTRAN PC/LANInstallation Guide for more information.

About SIMSCIHEXTRAN is backed by the full resources of Simulation Sciences a leaderin process simulation since 1967. SIMSCI provides the most thoroughservice capabilities and advanced process modeling technologies availableto the process industries. SIMSCI’s comprehensive support around theworld, allied with its training seminars for every user level, is aimed atmaking your use of these products as efficient, effective and profitable aspossible.

Simulation Sciences (SIMSCI) is an operating unit of the InvensysProduction Management Division and a worldwide supplier of commercialsimulation and optimization software and related services to the petroleum,petrochemical and industrial chemical process industries and engineeringand construction firms. SIMSCI’s products are designed to increaseprofitability by reducing capital investment costs, improving yields, andenhancing management decision-making. SIMSCI, as part of Invensys plc.,maintains offices in Brazil, Venezuela, Germany, Japan, Singapore, theUnited Arab Emirates, the United Kingdom, and the United States andprovides support and services to more than 750 customers in over 70countries. For more information about SIMSCI, visit the SIMSCI Web site

Chapter 1, Introduction HEXTRAN Keyword Manual1-4 June 2002

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at http://www.simsci.com. About Invensys plc:Invensys plc, theinternational production technology and energy management group,specializes in helping companies to improve efficiency, performance andprofitability. With close to 76,000 employees, Invensys is headquartered inLondon, England.

Our Production Management businesses work closely with customers inorder to drive up performance of their production assets and maximize thereturn on investments in product technologies. The division businessesinclude APV, Baan, Esscor, Eurotherm, Foxboro, PacSim, SimulationSciences, Triconex, and Wonderware, and it addresses the oil, gas, andchemicals; food beverage and personal healthcare; and discrete and hybridmanufacturing sectors.

Our Energy Management businesses actively work with clients involved inboth the supply and consumption of energy and water, developing systemsusing innovative technologies that improve the management of energy andwater costs and the reliability and security of power supplies. The divisionincludes Energy Solutions, Metering Systems, Home, Appliance andClimate Controls and Powerware and focuses on markets connected withpower and energy infrastructure and commercial and residential buildings.For more information, visit the Invensys home page atttp://www.invensys.com .

HEXTRAN Keyword Manual Chapter 1, IntroductionJune 2002 1-5

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Chapter 1, Introduction HEXTRAN Keyword Manual1-6 June 2002

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Chapter 2OverviewAbout This Chapter

This chapter describes the scope and capabilities of HEXTRAN and itsapplication in heat exchanger system design. This chapter should be readby anyone new to HEXTRAN.

Scope and Objectives of HEXTRANHEXTRAN is a simulation program that calculates the heat exchangedbetween two fluids. HEXTRAN can also calculate the utility requirements(such as steam, cooling water, or air).

HEXTRAN allows you to determine the optimal configuration for heatexchanger networks. Optional interfaces allow you to transfer data to morerigorous heat transfer programs (for example, HTFS and HTRI).HEXTRAN includes PRO/II’s rigorous thermodynamic and componentphysical property calculation methods.

HEXTRAN’s functionality is summarized in Figure 2-1.

HEXTRAN Keyword Manual Chapter 2, OverviewJune 2002 2-1

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Figure 2-1: Scope of HEXTRAN

StreamsHEXTRAN uses six main stream types:

■ Compositional

■ Assay

■ Bulk property

■ Water/steam

■ Mix/flash

■ Utility

Chapter 3, Using HEXTRAN, provides an overview of the streaminformation.

Property DataHEXTRAN can simulate fluids defined either by composition or by assay(ASTM, TBP) data. All component, thermodynamic, and transport propertydata are stored in, or created from, HEXTRAN’s data and calculation

Chapter 2, Overview HEXTRAN Keyword Manual2-2 June 2002

Online HelpPC Windows Version

Technical SupportFull Documentation

CompositionalComponent Data

Thermodynamic DataTransport Data

UnitOperations

Rigorous

Shortcut

Shell-and-Tube ExchangerRod-and-Baffle Exchanger

Double Tube ExchangerMulti-Tube Exchanger

Finned Tube ExchangerAir-Cooled Exchanger

Plate and Frame ExchangerMulti-Variable Controller

MixerSplitterPipeValve

DesalterDecanter

Flash DrumHeat Exchanger

HeaterCooler

Fired HeaterCompressor

Pump

Streams

CompositionalAssay

Bulk PropertyMix/Flash

Water/SteamUtility

Intermediate/Product

TargetingSynthesisSimulationRegression

Split Flow OptimizationArea Optimization

Cleaning Casestudy

HEXTRAN

CalculationMethods

PropertyData

UserConvenience

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libraries. Details of defining components are in Chapter 3, UsingHEXTRAN.

Calculation ModesHEXTRAN supports the following calculation methods:

■ Pinch technology:

Targeting: Provides the upper and lower bounds of exchanger networkheat recovery.

Synthesis: Generates optimal networks which contain the minimumnumber of exchangers for a specified heat recovery.

■ Network and heat exchanger rating/design:

Simulation: Designs and rates heat exchanger networks.

■ Data reconciliation:

Regression: Use to improve questionable plant data measurements.

■ Optimization:

Area optimization: Use to balance capital cost of exchangers againstutility savings.

Split flow optimization: Use to modify split fractions to minimize util-ity costs.

Cleaning casestudy: Use to track fouling and optimize exchangercleaning cycles.

User ConvenienceHEXTRAN is fully supported by SIMSCI’s experienced staff, who cansupply advice on using the program and offer assistance if you encounterproblems. Simply call the nearest of the offices listed in Chapter 1,Introduction. Full documentation is also available from your SIMSCIoffice.

In addition to the easy-to-use keyword version of HEXTRAN, SIMSCIoffers a version with a graphical user interface (GUI) to run underWindows 3.1, Windows 95, or Windows NT. Contact your SIMSCIrepresentative for information.

HEXTRAN Keyword Manual Chapter 2, OverviewJune 2002 2-3

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Chapter 2, Overview HEXTRAN Keyword Manual2-4 June 2002

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Chapter 3Using HEXTRANAbout This Chapter

This chapter contains information about the way HEXTRAN works, thedata you need, and the correlations used. In addition, it includesinstructions on building an input file.

For each of the capabilities of HEXTRAN, this chapter explains which datayou must provide and which data are optional. Throughout the tables in thischapter, the right-hand column contains a pointer to a STATEMENTpertinent to the specific type of heat exchanger where you will find detailson how to format the data.

Before you start running HEXTRAN, you should decide what type ofcalculation you will be performing.

What HEXTRAN DoesHEXTRAN calculates the heat exchanged between two fluids. HEXTRANcan also calculate the utility requirements (such as steam or cooling air).

HEXTRAN allows you to determine the optimal configuration for heatexchanger networks. Optional interfaces allow you to transfer data to morerigorous heat transfer programs (for example, HTFS and HTRI).HEXTRAN includes PRO/II’s rigorous thermodynamic and componentphysical property calculation methods.

Rating and Design ModesHEXTRAN works in both rating and design modes. In rating mode, yousupply data about the exchangers and streams, and HEXTRAN rigorouslycomputes the pressure drop and heat transfer coefficients from yourmechanical and process data. In design mode, you supply ranges ofexchanger data, and HEXTRAN designs a new STE from processrequirements and your design and operating constraints. You can specifynetworks of exchangers that use both modes.

Global SettingsBefore you provide HEXTRAN with information about the units andstreams in your problem, you must set global parameters and define theproblem. You can choose how to control the simulation, define the inputunits, and specify what type of output reports you want to produce (Table3-1).

HEXTRAN Keyword Manual Chapter 3, Using HEXTRANJune 2002 3-1

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Table 3-1: Global Settings

To provide… See…

Descriptive text You must use a TITLE statement thatdenotes that the input has started. At aminimum, the word TITL must appear.Mandatory statement.

4-8 TITLE

You can supply text in the TITLE statement;this text will appear at the top of every pageof output, and will make the run easier toidentify. Optional statement.

4-8 TITLE

You can further describe the problem usingup to four lines of 60 characters each. Thisdescription appears once at the top of eachpage. Optional statement.

4-9 DESCRIPTION

Input data checking You can use HEXTRAN to check your inputsyntax and topology without performingany calculations. Optional statement.

4-19 CALCULATION

Units of MeasureHEXTRAN allows you to construct a group of units of measure (or“dimensions”) that will be used throughout the simulation input (Table3-2). However, you can override individual units of measure if necessary.The output is always in the units you specify in the Input Dimensionsdialog box, unless you specify specific output overrides in the OutputDimensions dialog box.

Table 3-2: Units of Measure

To provide… See…

Input units Global units of measure are defined at thebeginning of the input. HEXTRAN hasthree pre-selected dimension sets:English, Metric, and SI. Select the set thatmost closely matches your requirements.If you do not specify a set, HEXTRANdefaults to the English set. Optionalstatement.

4-9 DIMENSION

Printout OptionsHEXTRAN generates a lot of data during its calculations. The defaultprintout is usually sufficient for most engineering applications. You canincrease or decrease the amount of output depending on your requirements(Table 3-3).

Chapter 3, Using HEXTRAN HEXTRAN Keyword Manual3-2 June 2002

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Table 3-3: Printout Options

To set the… See…

Output units The default units of measure for outputare the same as those defined globallyfor input in the DIMENSION statement.Using the OUTDIMENSION statement,you can define a separate set of unitsfor the output. Optional statement.

4-15 OUTDIMENSION

Input reprint HEXTRAN always produces a reprint ofyour input file. You can optionally selectto print HEXTRAN’s interpretation of theinput. Optional statement.

4-17 PRINT

Intermediate results During regression, area optimization,split flow optimization, and cleaningcasestudy calculations, HEXTRAN pro-duces intermediate calculation resultsthat you can select to print. Optionalstatement.

4-17 PRINT

Printing optionsfor synthesiscalculations

For synthesis calculations, you can setprint options separately for the split andunsplit networks. You can print abbrevi-ated or complete reports for each net-work type. Optional statement.

4-17 PRINT

Printing optionsfor targetingcalculations

For targeting calculations, you can se-lect to print duty tables, composite ta-bles and curves, grand composites, allcases, and a summary of results.Optional statement.

4-17 PRINT

Defining ComponentsHEXTRAN requires you to select the components in your simulations. Youcan define properties for the components if the library data is incomplete orunsatisfactory.

Library ComponentsThe SIMSCI library contains over 1700 components. A complete list isavailable in the SIMSCI Component and Thermodynamic Data InputManual, Vol I & II. For all components, the databank contains data for allthe fixed properties and temperature-dependent properties necessary tocarry out phase-equilibrium calculations. For all common components, thedatabank also contains a full set of transport properties necessary to carryout pressure drop and heat transfer calculations (Table 3-4). You maysupplement and/or override the library data.

HEXTRAN Keyword Manual Chapter 3, Using HEXTRANJune 2002 3-3

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Non-Library ComponentsYou can use components that are not included in the component library(Table 3-4). In order to simulate components that are not in the componentlibrary, you must input all the necessary data for thermodynamic andtransport properties. If you need help in determining data for suchcomponents, you can use SIMSCI’s DATAPREP program.

Table 3-4: Library and Non-Library Components

To specify… See…

Library components You can access all fixed property datafrom the SIMSCI databank. Mandatorystatement.

4-23 COMPONENT

Library ID Identify the components for which theproperties will be taken from the SIM-SCI databank. Optional statement.

4-23 LIBID

Constants You can override the SIMSCI constantproperties for any component. See theSIMSCI Component and Thermody-namic Data Input Manual for keywordsyntax. Optional statement.

4-26

4-26

4-26

4-26

4-26

4-27

4-27

4-27

4-27

4-27

MW

SPGR

API

ACENTRIC

ZC

TC

PC

VC

NBP

STDDENSITY

Variables You can override the SIMSCI variable(temperature-dependent) propertiesfor any of the components. See theSIMSCI Component and Thermody-namic Data Input Manual, Vol I & II forkeyword syntax. Optional statement.

4-28

4-28

4-28

4-28

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4-28

VP

ENTHALPY

CP

LATENT

DENSITY

VISCOSITY

CONDUCTIVITY

SURFACE TENSION

Non-librarycomponents

If you want to use a component that isnot in the component databank, youmust supply its name and all therequired properties in the text box. Seethe SIMSCI Component and Thermo-dynamic Data Input Manual, Vol. I & IIfor keyword syntax. Optionalstatement.

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Petroleum PseudocomponentsTo define hydrocarbon pseudocomponents, you must supply at least two ofthe following three parameters:

■ Molecular weight (MW)

■ API or Specific Gravity

■ Normal boiling point (NBP)

HEXTRAN predicts the third parameter if you omit it. HEXTRAN usesindustry-standard characterization methods to predict all fixed andtemperature-dependent property data for each pseudocomponent. You canselect the method most suitable for your pseudocomponents (Table 3-5).

Table 3-5: Petroleum Pseudocomponents

To define… See…

Pseudocomponents Define petroleum pseudocomponentsby supplying at least two of the follow-ing: molecular weight, gravity, and nor-mal boiling point. Optional statement.

4-24 PETROLEUM

Property-calculationMethods

You can select the method HEXTRANuses to calculate the properties of yourpseudocomponents. Optionalstatement.

4-24 ASSAY

Fixed Property Data You can supply your own fixedproperty data to override the data thatHEXTRAN predicts. Optional statement.

4-26

4-26

4-26

4-26

4-26

4-26

4-27

4-27

4-27

4-27

MW

SPGR

API

ACENTRIC

ZC

TC

PC

VC

NBP

STDDENSITY

Variable PropertyData

You can supply your owntemperature-dependent property datato override the data that HEXTRANpredicts. Optional statement.

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4-28

4-28

4-28

4-28

4-28

VP

ENTHALPY

CP

LATENT

DENSITY

VISCOSITY

CONDUCTIVITY

SURFACETENSION

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Assay CurveFor a stream defined by an assay curve (TBP, D86, D2887, or D1160),HEXTRAN divides the curve into a number of cuts. You can control thenumber of cuts and the ranges they cover. Each of the cuts is then treated asa pseudocomponent. You can also define a lightends analysis to go with theassay curve (Table 3-6).

Table 3-6: Assay Curve

To supply… See…

Assay Data You supply an assay curve, andHEXTRAN divides it into petroleum cuts.You can specify a D86, D1160, D2887,or TBP curve type. Optional statement.

4-46 D86, D1160,D2887, TBP

You must also supply gravity as API orspecific gravity, or UOP K-factor.Optional statement.

4-50 API, SPGR,UOPK, DATA

HEXTRAN calculates molecular weightdata, or you can enter average molecu-lar weight or enter molecular weights atvarious petroleum cut points. Optionalstatement.

4-51 MW

You can define the number of petroleumfractions to be generated and their tem-perature ranges. Optional statement.

4-26 CUTPOINTS

You can select the method HEXTRANuses to calculate the properties of thegenerated petroleum fractions. Optionalstatement.

4-24 ASSAY

LIGHTENDS You can mix defined components andpseudocomponents with assay data bydefining a lightends composition andrate for each source. Optionalstatement.

4-52 LIGHTENDS

Defining Thermodynamic MethodsHEXTRAN can use a generalized correlation, an equation of state, or aliquid activity method to calculate thermodynamic properties at the flowingconditions, and hence to predict the split between the liquid and vaporphases. The choice of the thermodynamic property calculation methoddepends on the components in the fluid and the prevailing temperatures andpressures. HEXTRAN also provides several methods that can rigorouslycalculate vapor-liquid-liquid equilibrium and solid-liquid equilibrium.

Table 3-7 provides recommendations for thermodynamic properties. Table3-8 shows the HEXTRAN options for defining thermodynamic methods.

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Table 3-7: Recommended Methods for Thermodynamic Properties

Method

PropertyHeavy HydrocarbonSystems

Light HydrocarbonSystems

Natural GasSystems

K-value Braun K10 (<100 psia)

Grayson-Streed

Peng-Robinson

Soave-Redlich-Kwong

Peng-Robinson

Soave-Redlich-Kwong

Benedict-Webb-Rubin-Starling

Chao-Seader

Peng-Robinson

Soave-Redlich-Kwong

Enthalpy Curl-Pitzer

Johnson-Grayson

Lee-Kesler

Peng-Robinson

Soave-Redlich-Kwong

Peng-Robinson

Soave-Redlich-Kwong

Lee-Kesler-Plöcker

Benedict-Webb-Rubin-Starling

Curl-Pitzer

Lee-Kesler

Peng-Robinson

Soave-Redlich-Kwong

LiquidDensity

API

Lee-Kesler

API

Lee-Kesler

API

Lee-Kesler

Vapor Density Peng-Robinson

Soave-Redlich-Kwong

Peng-Robinson

Soave-Redlich-Kwong

Peng-Robinson

Soave-Redlich-Kwong

Table 3-8: Defining Thermodynamic Methods

To specify… See…

K-values, enthalpy,density

You must select a thermodynamic methodfor calculating the vapor-liquid equilibriumand mixture properties from componentproperties. Select either a system with apredefined method for each property, or anindividual method for each property.Optional statement.

4-32 METHOD

Vapor-liquid-liquidequilibria

You can specify a VLLE thermodynamicsystem, a K-value method, or a second LLEK-value method.

4-32 METHOD

Different enthalpymethods for liquidand vapor

You must include two enthalpy methods,one for the liquid and one for the vapor.

4-32 METHOD

Different densitymethods for liquidand vapor

You must include two density methods,one for the liquid and one for the vapor.

4-32 METHOD

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Table 3-8: Defining Thermodynamic Methods

To specify… See…

Aqueous phaseenthalpy

If you have water in a hydrocarbon system,you can select a method for calculatingaqueous liquid and vapor enthalpies eitherby a simplified method that assumes thestream is at its saturation point, or by a rig-orous method that takes into account thedegree of superheat of the vapor, if any.

4-32 METHOD

Transport PropertiesThe SIMSCI databank contains pure component data for the thermalconductivity, surface tension, and viscosity of liquids and vapors asfunctions of temperature (Table 3-9). You can use these data and simplemixing rules to predict the flowing properties of the fluid.

Alternatively, you can use the API Data Book property prediction methodsand mixing rules for mixed hydrocarbons.

Approximately 60 of the bank components have data for viscosity andthermal conductivity from the GPA TRAPP program. If you choose to usethe TRAPP properties, all of your components must be TRAPP componentsand you cannot have any pseudocomponents or assay data.

Table 3-9: Transport Properties

To specify… See…

Prediction Methods Select a method for calculating bulktransport properties from componentproperties. Select a system with pre-defined methods for each property, orselect an individual method for eachproperty.

4-32 METHOD

Overriding Predictions You can override individual predic-tions by entering your own data.Optional statement.

4-33 SET

Using Multiple MethodsIn most cases, a single set of thermodynamic and transport methods isadequate for calculating properties of all sources. However, your flowsheetmay contain sources with widely varying compositions, or it may includeconditions that cannot be simulated accurately using just one set ofmethods. To account for this, you can define more than one set of methods(there is no limit) and apply different sets to different streams (Table 3-10).

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Table 3-10: Using Multiple Methods

To specify… See…

More than onethermodynamic set

You can assign a different thermodynamicdata set to each stream.

4-32 METHOD

Additional Thermodynamic CapabilitiesAll of SIMSCI’s industry-standard thermophysical property calculationmethods have been incorporated into HEXTRAN (Table 3-11). For detailsof these methods and their applicability, see Section 2 in the SIMSCIComponent and Thermodynamic Data Input Manual, Vol. I & II.

Table 3-11: Summary of Other Thermodynamic Options

GeneralizedCorrelations

Grayson-Streed

Improved-Grayson-Streed

Grayson-Streed-Erbar

Braun-K10

Chao-Seader

Chao-Seader-Erbar

Ideal

Equations ofState

Soave-Redlich-Kwong

SRK-Kabadi-Danner

SRK-Huron-Vidal

SRK-Panagiotopoulos-Reid

SRK-Modified

SRK-SIMSCI

SRK-Hexamer

Panagiotopoulos-Reid

Peng-Robinson

PR-Huron-Vidal

PR-Panagiotopoulos-Reid

BWRS

Uniwaals

Liquid ActivityMethods

Nonrandom Two-liquidEquation

Universal Quasi-chemical(UNIQUAC)

van Laar

Wilson

Margules

Regular Solution Theory

Flory-Huggins Theory

Universal Functional ActivityCoefficient (UNIFAC)

Lyngby-modified UNIFAC

Dortmund-modified UNIFAC

Modified UNIFAC method

Free volume modification to UNIFAC

Ideal

SpecialPackages

Glycol

Sour

GPA Sour Water

Amine

Alcohol

Other Features Heat of Mixing

Poynting Correction

Henry’s Law

Amine Residence Time Correction

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Generating and Using Tables of PropertiesFor large-scale simulations, you can build a table of fluid properties (Table3-12). This reduces the amount of computation time taken by phaseseparation calculations during the solution procedure.

Table 3-12: Tables of Properties

To … See…

Build and use a table You can have HEXTRAN build the tableand use it in the same run.

4-64 PGEN

Retrieve a table You can have HEXTRAN build the table,store it in a file, and then use it in a sub-sequent run.

4-64

4-71

PGEN

FILE

Stream DataHEXTRAN uses six main stream types:

■ Compositional

■ Assay

■ Bulk property

■ Water/steam

■ Mix/flash

■ Utility

Table 3-13 provides information about entering stream data.

Table 3-13: Entering Stream Data

To … See…

Enter compositionalstream data

Mandatory statement. 4-41 PROPERTY

Enter assay streamdata

All statements are mandatory exceptMW and LIGHTEND.

4-44 PROPERTY

D86, TBP, D1160, orD2887

API, SPGR, orWATSONK

MW

LIGHTENDS

Enter mix/flashstream data

Mandatory statement. 4-53 PROPERTY

Enter referencestream data

Mandatory statement. 4-53 PROPERTY

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Table 3-13: Entering Stream Data

To … See…

Enter petroleumliquids and vaporsstream data

Mandatory statement. 4-56 PROPERTY

Enter water andsteam stream data

Mandatory statement. 4-58 PROPERTY

Enter utility streamsfor pinchcalculations data

Mandatory statement. 4-60 UTILITY

Enter networksynthesis data

Optional statement. 4-62 PROPERTY

Flowsheet CalculationsFlowsheet calculations specify the type of defined network calculations tobe performed and the associated general parameters and options.

Simulation CalculationsSimulation calculations are performed on exchanger networks that consistof any combination of rigorous and shortcut unit operation models.Rigorous STE models can be both old exchangers to be rated and newexchangers to be designed. Heat transfer coefficients and pressure drops arecalculated for all rigorous unit operations. Complete mass, pressure, andenergy balances are performed for the entire network. Outlet temperatures,temperature approaches, outlet liquid quality, or duty specifications can beplaced on any old exchanger and are required on any new exchanger to bedesigned. Temperature, pressure, or duty specifications can also beimplemented using a multivariable controller (MVC).

Regression CalculationsRegression is HEXTRAN's data reconciliation tool. It works like an MVCexcept that it is overconstrained with more specifications than variables.Regression verifies plant data by attempting to minimize the differencesbetween the calculated and desired values of the specifications bymanipulating the allowed variables within specified limits.

Cleaning Casestudy CalculationsThe cleaning casestudy option provides the ability to evaluate the economicimpact when you clean one, several, or all of the exchangers in a flowsheet.A cleaning casestudy calculation first prepares a base case and thenperforms the specified cleaning casestudies.

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Area Optimization CalculationsIn area optimization calculations, the objective is to design all newexchangers to meet a specified payback criteria.

Split Flow Optimization CalculationsThe objective of split flow optimization is to minimize the total utility costsfor the network, including the costs of pumping, air cooling, furnace firing,and so on. Costs and/or savings can be assigned to selected streamsdepending on whether the streams are heated or cooled. HEXTRANprepares multiple simulation runs that shift the duty loads between parallelexchangers. The objective function is calculated from utility costs and anypenalty assessments for violating plant operating constraints. The variablein this case is the stream split fractions.

Table 3-14: Flowsheet Calculation Statements

To specify… See…

Property Mandatory statement. 4-764-764-764-76

SIMULATION,REGRESSION,OPTIMIZATION,or CASESTUDY

Tolerances Optional statement. 4-76 TOLERANCE

Limits Optional statement. 4-77 LIMITS

Calculation methods forindividual exchangerson a global basis

Optional statement. 4-78 CALCULATIONS

Print options Optional statement. 4-79 PRINT

Economic factors Optional statement. 4-80 ECONOMICS

Utility costs Optional statement. 4-80 UTCOST

Global exchangercosting data

Optional statement. 4-81 HXCOST

Specifications for re-gression calculations,payout period for allnew heat exchangersfor area optimizationcalculations, or ex-changer fouling factorsfor cleaning casestudycalculations

Mandatory statement forREGRESSION, AREAOPTIMIZATION, and CASESTUDYcalculations. Not available forSIMULATION and SPLITFLOWOPTIMIZATION calculations.

4-82 SPECIFICATION

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Table 3-14: Flowsheet Calculation Statements

To specify… See…

Variables for regressioncalculations, or thevariable stream splitfractions for split flowoptimizationcalculations

Mandatory statement forREGRESSION and SPLITFLOWOPTIMIZATION calculations. Notavailable for SIMULATION, AREAOPTIMIZATION, and CASESTUDYcalculations.

4-82 VARIABLE

Minimum or maximumtemperature constraintson selected streams, ormaximum pressuredrop constraints on anyexchanger in theflowsheet

Mandatory statement forOPTIMIZATION calculations. Notavailable for REGRESSION,SIMULATION, or CASESTUDYcalculations.

4-82 CONSTRAINT

The exchangers that areto have fouling factoradjustments for eachcase

Mandatory statement forCASESTUDY calculations. Notavailable for REGRESSION,SIMULATION, or OPTIMIZATIONcalculations.

4-82 CASE

Estimates of the splitfraction “incrementalstepsize” and “range”values

Mandatory statement forOPTIMIZATION calculations. Notavailable for REGRESSION,SIMULATION, or CASESTUDYcalculations.

4-82 PARAMETER

Targeting CalculationsTargeting uses pinch technology to provide numerical and graphicalanalyses of the upper and lower bounds for heat recovery problems.

Table 3-15 provides the statements used in a targeting calculation.

Table 3-15: Targeting Calculation Statements

To … See…

Specify a targetingcalculation

Mandatory statement. 4-131 TARGETING

Specify the heat re-covery of the processstreams as a functionof temperatures,duties, and areas

Optional statement. 4-133 SPEC

Define heat transfercoefficients and areaefficiencies

Optional statement. 4-134 PARAMETER

Specify print options Optional statement. 4-137 PRINT

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Table 3-15: Targeting Calculation Statements

To … See…

Enter plot options Optional statement. 4-137 PLOT

Specify global ex-changer costing data

Optional statement. 4-138 HXCOST

Specify economicfactors

Optional statement. 4-139 ECONOMICS

Modify an individualstream’s HRAT

Optional statement. 4-140 PROCESS(STREAM datasection)

Using SynthesisSynthesis generates optimal heat exchanger networks from processconditions and constraints that you specify. The objective of the synthesiscalculation mode is to design the network with the fewest possible numberof exchanger services. This results in a heat exchanger network in theoptimum cost region.

Table 3-16 provides the statements used in a synthesis calculation.

Table 3-16: Synthesis Calculation Statements

To … See…

Specify a synthesiscalculation

Mandatory statement. 4-142 SYNTHESIS

Specify the heatrecovery of the processstreams and theexchanger minimumapproach temperature

Optional statement. 4-142 SPEC

Define the film coeffi-cients for each stream

Optional statement. 4-143 PARAMETER

Specify print options Optional statement. 4-144 PRINT

Request network plotsthat show the connec-tivity of the synthesizednetworks

Optional statement. 4-144 PLOT

Specify global ex-changer costing data

Optional statement. 4-145 HXCOST

Specify economicfactors

Optional statement. 4-146 ECONOMICS

Impose limits on theexchanger design

Optional statement. 4-147 LIMITS

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Unit OperationsAll rigorous heat exchangers rigorously compute the film coefficients andthe pressure drops based on the fluid properties and the mechanical data forthe exchanger.

Tables 3-17 through 3-37 describe the available statements for the heatexchangers HEXTRAN supports.

Table 3-17: Shell-and-Tube Exchanger Specifications

To define… See…

Shell-and-tubeexchanger (STE)

Mandatory statement. 4-165 STE

Basic characteristics Mandatory statement. 4-165 TYPE

Tubesidecharacteristics

Mandatory statement. 4-170 TUBESIDE

Finned tubes Optional statement. 4-174 FINS

Shellsidecharacteristics

Mandatory statement. 4-177 SHELLSIDE

Baffles and tube sheet Optional statement. 4-181 BAFFLE

Tubeside nozzles Optional statement. 4-188 TNOZZLE

Shellside nozzles Optional statement. 4-188 SNOZZLE

Shellside intermediateliquid nozzles

Optional statement. 4-189 INOZZLE

Shellside liquidnozzles

Optional statement. 4-190 LNOZZLE

HTRI modules Optional statement. 4-190 HTRI

HTFS module Optional statement. 4-190 HTFS

Calculation methods Optional statement. 4-191 CALCULATION

Exchanger performancecriteria

Optional statement for rating and areaoptimization. Mandatory statement fordesign.

4-192 SPECIFICATION

Printing options Optional statement. 4-193 PRINT

Special costing data Optional statement. 4-193 COST

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Table 3-18: Rod Baffle Exchanger Specifications

To define… See…

Rod baffle exchanger(RBE)

Mandatory statement. 4-195 RBE

Basic characteristics Mandatory statement. 4-196 TYPE

Tubeside characteristics Mandatory statement. 4-197 TUBESIDE

Shellside characteristics Mandatory statement. 4-199 SHELLSIDE

Baffles and tube sheet Mandatory statement. 4-201 BAFFLE

Tubeside nozzles Optional statement. 4-201 TNOZZLE

Shellside nozzles Optional statement. 4-202 SNOZZLE

Calculation methods Optional statement. 4-202 CALCULATION

Exchanger performancecriteria

Optional statement. 4-203 SPECIFICATION

Printing options Optional statement. 4-204 PRINT

Special costing data Optional statement. 4-204 COST

Table 3-19: Double Pipe Exchanger Specifications

To define… See…

Double pipe (DPE) Mandatory statement. 4-206 DPE

Basic characteristics Mandatory statement. 4-207 TYPE

Tubesidecharacteristics

Mandatory statement. 4-208 TUBESIDE

Finned tubes Optional statement. 4-210 FINS

Shellsidecharacteristics

Mandatory statement. 4-211 SHELLSIDE

Tubeside nozzles Optional statement. 4-212 TNOZZLE

Shellside nozzles Optional statement. 4-213 SNOZZLE

Calculation methods Optional statement. 4-213 CALCULATION

Exchangerperformance criteria

Optional statement. 4-214 SPECIFICATION

Printing options Optional statement. 4-215 PRINT

Special costing data Optional statement. 4-215 COST

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Table 3-20: Multi-Tube Exchanger Specifications

To define… See…

Multitube exchanger(MTE)

Mandatory statement. 4-217 MTE

Basic characteristics Mandatory statement. 4-218 TYPE

Tubeside characteristics Mandatory statement. 4-219 TUBESIDE

Finned tubes Optional statement. 4-221 FINS

Shellside characteristics Mandatory statement. 4-222 SHELLSIDE

Tubeside nozzles Optional statement. 4-223 TNOZZLE

Shellside nozzles Optional statement. 4-224 SNOZZLE

Calculation methods Optional statement. 4-224 CALCULATION

Printing options Optional statement. 4-226 PRINT

Exchanger performancecriteria

Optional statement. 4-225 SPECIFICATION

Special costing data Optional statement. 4-227 COST

Table 3-21: Finned-Tube Exchanger Specifications

To define… See…

Finned-tube exchanger(FTE)

Mandatory statement. 4- FTE

Basic characteristics Mandatory statement. 4-228 TYPE

Tubeside characteristics Mandatory statement. 4-232 TUBESIDE

Finned tubes Optional statement. 4-235 FINS

Ductside characteristics Mandatory statement. 4-236 DUCTSIDE

Tubeside nozzles Optional statement. 4-238 TNOZZLE

Exchanger performancecriteria

Optional statement for rating.Mandatory statement for design.

4-238 SPECIFICATION

Calculation methods Optional statement. 4-239 CALCULATION

Printing options Optional statement. 4-240 PRINT

Special costing data Optional statement. 4-240 COST

HTRI module Optional statement. 4-241 HTRI

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Table 3-22: Air-Cooled Exchanger Specifications

To define… See…

Air-cooled exchanger(ACE)

Mandatory statement. 4-242 ACE

Basic characteristics Mandatory statement. 4-244 TYPE

Tubeside characteristics Mandatory statement. 4-245 TUBESIDE

Finned tubes Optional statement. 4-248 FINS

Airside characteristics Mandatory statement. 4-249 AIRSIDE

Fan information Optional statement. 4-251 FAN

Tubeside nozzles Optional statement. 4-252 TNOZZLE

Exchanger performancecriteria

Optional statement for rating.Mandatory statement for design.

4-252 SPECIFICATION

Calculation methods Optional statement. 4-253 CALCULATION

Special costing data Optional statement. 4-254 COST

Report printing options Optional statement. 4-254 PRINT

HTRI module Optional statement. 4-255 HTRI

Table 3-23: Plate-and-Frame Exchanger Specifications

To define… See…

Plate-and-frameexchanger (PHE)

Mandatory statement. 4- PHE

Basic characteristics Mandatory statement. 4-256 TYPE

Hotside characteristics Mandatory statement. 4-25 HOTSIDE

Coldsidecharacteristics

Mandatory statement. 4-259 COLDSIDE

Plate pack Mandatory statement. 4-260 PACK

Plate information Optional statement for design. 4-26 PLATE

Pack arrangement Mandatory statement (rating only). 4-264 ARRANGEMENT

Channel f-factor Optional statement. 4-26 FPLATE

Channel JN-factor Optional statement. 4-266 JPLATE

Hotside nozzle data Optional statement. 4-267 HNOZZLE

Coldside nozzle data Optional statement. 4-26 CNOZZLE

Calculation methods Optional statement. 4-267 CALCULATION

Exchanger performancecriteria

Optional statement for rating.Mandatory statement for design.

4-268 SPECIFICATION

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Table 3-23: Plate-and-Frame Exchanger Specifications

To define… See…

Printing options Optional statement. 4-269 PRINT

Special costing data Optional statement. 4-269 COST

Table 3-24: Mixer Unit

To define… See…

Mixer Mandatory statement. 4-271 MIXER

Feed and productstreams

Mandatory statement. 4-271 STREAM

Table 3-25: Splitter Unit

To define… See…

Splitter Mandatory statement. 4-273 SPLITTER

Feed and productstreams

Mandatory statement. 4-273 STREAM

Performancespecifications

Mandatory statement. 4-274 OPERATION

Table 3-26: Pipe Unit

To define… See…

Pipe Mandatory statement. 4-276 PIPE

Feed and product streams Mandatory statement. 4-277 STRMS

Dimensions and character-istics for the pipe

Optional statements. 4-277

4-280

LINE

FITTINGS

Performance specifications Mandatory statement. 4-281 OPERATION

Table 3-27: Valve Unit

To define… See…

Valve Mandatory statement. 4-283 VALVE

Feed and product streams Mandatory statement. 4-283 STRMS

Performance specifications Optional statement. 4-284 OPERATION

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Table 3-28: Desalter Unit

To define… See…

Desalter Mandatory statement. 4-285 DESALTER

Feed, product, and brineproduct streams

Mandatory statement. 4-285 STRMS

Performance specifications Optional statement. 4-286 OPERATION

Table 3-29: Decanter Unit

To define… See…

Decanter Mandatory statement. 4-288 DECANTER

Feed, product, and waterproduct streams

Mandatory statement. 4-288 STRMS

Performance specifications Optional statement. 4-289 OPERATION

Table 3-30: Flash Drum Unit

To define… See…

Flash drum Mandatory statement. 4-291 FLASH

Feed, vapor, and liquidproduct streams

Mandatory statement. 4-291 STRMS

Performance specifications Optional statement. 4-292 OPERATION

Table 3-31: Shortcut Heat Exchanger

To define… See…

Shortcut heat exchanger Mandatory statement. 4-294 HX

Basic characteristics Mandatory statement. 4-294 TYPE

Tubeside characteristics Mandatory statement. 4-296 TUBESIDE

Shellside characteristics Mandatory statement. 4-297 SHELLSIDE

Calculation methods forindividual exchangers on aglobal basis

Optional statement. 4-298 CALCULATION

Exchanger performancecriteria

Optional statement for rating.Mandatory statement for design.

4-298 SPECIFICATION

Report printing options Optional statement. 4-299 PRINT

Special costing data Optional statement. 4-299 COST

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Table 3-32: Shortcut Heater Unit

To define… See…

Heater Mandatory statement. 4-301 HEATER

Feed or product streams Mandatory statement. 4-301 STREAM

Performance specifications Optional statement. 4-302 OPERATION

Special costing data Optional statement. 4-303 COST

Table 3-33: Shortcut Cooler Unit

To define… See…

Cooler Mandatory statement. 4-305 COOLER

Feed or product streams Mandatory statement. 4-305 STRMS

Performance specifications Optional statement. 4-306 OPERATION

Special costing data Optional statement. 4-307 COST

Table 3-34: Fired Heater Unit

To define… See…

Fired heater Mandatory statement. 4-309 FIREDHEATER

Feed or product streams Mandatory statement. 4-309 STRMS

Performance specifications Optional statement. 4-310 OPERATION

Special costing data Optional statement. 4-311 COST

Table 3-35: Compressor Unit

To define… See…

Compressor Mandatory statement. 4-313 COMPRESSOR

Feed or product streams Mandatory statement. 4-313 STRMS

Performance specifications Optional statement. 4-314 OPERATION

Special costing data Optional statement. 4-316 COST

Table 3-36: Pump Unit

To define… See…

Pump Mandatory statement. 4-318 PUMP

Feed or product streams Mandatory statement. 4-318 STRMS

Performancespecifications

Optional statement. 4-319 OPERATION

Special costing data Optional statement. 4-320 COST

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Table 3-37: Multi-Variable Controller

To define… See…

Multi-variable controller(MVC)

Mandatory statement. 4-322 MVC

Exchanger performancecriteria

Mandatory statement. 4-322 SPECIFICATION

Stream and unitparameters

Mandatory statement. 4-323 VARIABLE

Control options Optional statement. 4-325 PARAMETER

Building an Input FileYou can start an input file in one of two ways: By creating a file fromscratch, or by taking an existing input file and changing it as needed tomeet the new requirements. This section provides a sample input file anddescribes each of its data categories. The data categories are described indetail in Chapter 4, Input Reference. If you create a simulation in the GUI,you can export to an input file. Note however, that input files cannot beimported into the GUI.

Where applicable, abbreviated forms of statements are shown inparentheses. You can use either form in your input files.

A line that begins with a dollar sign ($) is a remark. You can use a remarkline to insert a note or to create blank spaces between lines for easierreading. HEXTRAN ignores everything on a remark line.

To continue a statement that does not fit on one line, insert an asterisk (*)or an ampersand (&) at the end of the line being continued. For easierreading, you can indent the continuation line.

Sample Input File$$ General Data Section$TITLE PROJECT=SAMPLES, PROBLEM=TUTORIAL, USER=SIMSCI,*

DATE=AUGUST11997, SITE=BREA$DESC SHELL AND TUBE EXCHANGER DESIGNDESC INTERNAL PROPERTY CALCULATION$DIME ENGLISH, AREA=FT2, CONDUCTIVITY=BTUH, DENSITY=LBFT3,*

ENERGY=BTU, FILM=BTUH, LIQVOLUME=FT3, POWER=HP,*PRESSURE=PSIA, SURFACE=DYNE, TIME=HR, TEMPERATURE=F,*UVALUE=BTUH, VAPVOLUME=FT3, VISCOSITY=CP, WT=LB,*XDENSITY=API, STDVAPOR=379.490

$OUTD ENGLISH,AREA=FT2, CONDUCTIVITY=BTUH, DENSITY=LBFT3,*

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ENERGY=BTU, FILM=BTUH, LIQVOLUME=FT3, POWER=HP,*PRESSURE=PSIA, SURFACE=DYNE, TIME=HR, TEMPERATURE=F,*UVALUE=BTUH, VAPVOLUME=FT3, VISCOSITY=CP, WT=LB,*XDENSITY=API, STDVAPOR=379.490, ADD

$PRINT GENERAL, PROPERTY, STREAM, UNIT, NEWS, RATE=M$CALC PGEN=NEW, WATER=KEENAN$$ Component Data Section$COMPONENT DATA$LBID 1,H2O /*

2,EBZN /*3,STYR ,*BANK=PROCESS, SIMSCI

$$ Thermodynamic Data Section$THERMODYNAMIC DATA$METHOD SET=SET1, SYSTEM=SRK, KVALUE=SRK,*

ENTHALPY(L)=SRK, ENTHALPY(V)=SRK, ENTROPY(L)=SRK,*ENTROPY(V)=SRK, DENSITY(L)=API, DENSITY(V)=SRK,*TRANSPORT=PURE, VISCOS(L)=PURE, VISCOS(V)=PURE,*CONDUCT(L)=PURE, CONDUCT(V)=PURE, SURFACE=PURE

$$ Stream Data Section$STREAM DATA$PROP STRM=1, NAME=HC+STEAM, TEMP=1000.00, PRES=12.000*

TOUT=1500.00, POUT=8.000, SET=SET1, SETN=1,*RATE(W)=350000.000, COMP(M)=1,55.00/2,25.000/*3,20.000

$PROP STRM=3, NAME=SH STEAM, TEMP=1500.00, PRES=35.000,*

STEAM=160000.000$$ Internal Property Data Section$INTERNAL PROPERTY DATA$PGEN STRM=1, SET=1, TEMP=1000.00,1055.56,1111.11,*

1166.67,1222.22,1277.78,1333.33,1388.89,*1444.44,1500.00, PRES=8.000,12.000,*PETRO, PXTR

$$ Calculation Type Section$

SIMULATION

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$TOLERANCE TTRIAL=0.01

$LIMITS AREA=200.00,60000.00, SERIES=1,10, PDAMP=0.00,*

TTRIAL=50$

CALC TWOPHASE=NEW, DPSMETHOD=STREAM, MINFT=0.80$

PRINT UNITS, ECONOMICS, STREAM, STANDARD,*EXTENDED, ZONES

$ECONOMICS DAYS=350, EXCHANGERATE=1.00, CURRENCY=USDOLLAR

$UTCOST OIL=3.50, GAS=3.50, ELECTRICITY=0.10,*

WATER=0.03, HPSTEAM=4.10, MPSTEAM=3.90,*LPSTEAM=3.60, REFRIGERANT=0.00, HEATINGMEDIUM=0.00

$HXCOST BSIZE=1000.00, BCOST=0.00, LINEAR=50.00,*

EXPONENT=0.60, CONSTANT=0.00, UNIT$$ Unit Operations Data$UNIT OPERATIONS$STE UID=1,NAME=E-101

TYPE NEW, TEMA=NEN, HOTSIDE=SHELL, ORIENTATION=VERTICAL,*FLOW=COUNTERCURRENT, AREA=5000.00,12000.00,*UESTIMATE=50.00, USCALER=1.00

$TUBE FEED=1, PRODUCT=2,*

LENGTH=25.00,25.00,0.00, OD=1.750,*BWG=10, PASS=1,1,1, PATTERN=30,*PITCH=2.188, MATERIAL=9,*FOUL=0.0015, LAYER=0,*DPSHELL=2.000,10.000

$SHELL FEED=3, PRODUCT=4.*

ID=60.00,80.00, SERIES=1,2,*SEALS=0, MATERIAL=INCOLOGY, DENSITY=501.0,*FOUL=0.004, LAYER=0,*DPSHELL=10.000,20.000

$BAFF NTIW, SEGMENTAL=SINGLE

$SPEC DUTY=28.06

$

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General Data CategoryThe first statement in the General Data category must be a TITLEstatement. The TITLE statement includes the following optional keywords,which appear at the top of each page of the output report:

■ PROJECT

■ PRODUCT

■ USER

■ DATE

TITLE PROJECT=SAMPLES, PROBLEM=TUTORIAL, USER=SIMSCI,*DATE=AUGUST11997,SITE=BREA

The next statement is the DESCRIPTION (DESC) statement. You caninclude up to four DESCRIPTION statements in an input file.

DESC SHELL AND TUBE EXCHANGER DESIGNDESC INTERNAL PROPERTY CALCULATION

The following statement is the DIMENSION (DIME) statement. If you donot include the statement, ENGLISH is the default dimension unit. You canspecify a global dimension unit set and then specify different dimensionunits for specific measurements.

DIME ENGLISH, AREA=FT2, CONDUCTIVITY=BTUH, DENSITY=LBFT3,*ENERGY=BTU, FILM=BTUH, LIQVOLUME=FT3, POWER=HP,*PRESSURE=PSIA, SURFACE=DYNE, TIME=HR, TEMPERATURE=F,*UVALUE=BTUH, VAPVOLUME=FT3, VISCOSITY=CP, WT=LB,*XDENSITY=API, STDVAPOR=379.490

The next statement, OUTDIMENSION (OUTD), lets you specify adifferent dimension unit set than the set you specified in the DIMENSIONstatement. You can also specify whether you want the output to include

■ One report that uses the output dimensions (REPLACE)

■ Two reports, one that uses the output dimensions and one that uses theinput dimensions (ADD).

OUTD ENGLISH, AREA=FT2, CONDUCTIVITY=BTUH, DENSITY=LBFT3,*ENERGY=BTU, FILM=BTUH, LIQVOLUME=FT3, POWER=HP,*PRESSURE=PSIA, SURFACE=DYNE, TIME=HR, TEMPERATURE=F,*UVALUE=BTUH, VAPVOLUME=FT3, VISCOSITY=CP, WT=LB,*XDENSITY=API, STDVAPOR=379.490, ADD

The PRINT statement specifies the input report options.

PRINT GENERAL, PROPERTY, STREAM, UNIT, NEWS, RATE=M

The CALCULATION (CALC) statement lets you specify input datachecking options, stream and property data limits, internally generatedproperty data file options, and water and steam calculation methods.

CALC PGEN=NEW, WATER=KEENAN

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Component Data SectionThe Component Data section allows you to define the components in thesimulation.

The COMPONENT DATA statement identifies the section.

COMPONENT DATA

The LIBID statement identifies the library IDs of the components used inthe simulation.

LBID 1,H2O /*2,EBZN /*3,STYR ,*BANK=PROCESS, SIMSCI

Thermodynamic Data SectionThe Thermodynamic Data section defines the methods that HEXTRANuses to determine phase separation, enthalpy calculation, and transportproperties.

The THERMODYNAMIC DATA statement identifies the section.

THERMODYNAMIC DATA

The METHOD statement defines the method used in calculatingthermodynamic and transport properties of the flowing fluid.

METHOD SET=SET1, SYSTEM=SRK, KVALUE=SRK,*ENTHALPY(L)=SRK, ENTHALPY(V)=SRK, ENTROPY(L)=SRK,*ENTROPY(V)=SRK, DENSITY(L)=API, DENSITY(V)=SRK,*TRANSPORT=PURE, VISCOS(L)=PURE, VISCOS(V)=PURE,*CONDUCT(L)=PURE, CONDUCT(V)=PURE, SURFACE=PURE

Stream Data SectionThe Stream Data section defines the process streams.

The STREAM DATA statement identifies the section.

STREAM DATA

The PROPERTY statement (PROP) specifies the properties of a stream.The keywords you use depend on the type of stream you are defining.

PROP STREAM=1, NAME=HC+STEAM, TEMP=1000.00, PRES=12.000*TOUT=1500.00, POUT=8.000, SET=SET1, SETN=1,*RATE(W)=350000.000, COMP(M)=1,55.00/2,25.000/*3,20.000

PROP STREAM=3, NAME=SH STEAM, TEMP=1500.00, PRES=35.000,*STEAM=160000.000

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Internal Property Data SectionThe Internal Property Data section supplements the default internalproperty calculations for streams.

The INTERNAL PROPERTY DATA statement identifies the section.

INTERNAL PROPERTY DATA

The PGEN statement overrides the default generation of thethermodynamic and transport property data for compositional or assaystreams.

PGEN STRM=1, SET=1, TEMP=1000.00,1055.56,1111.11,*1166.67,1222.22,1277.78,1333.33,1388.89,*1444.44,1500.00, PRES=8.000,12.000,*PETRO, PXTR

Calculation Type SectionThe Calculation Type section specifies the type of calculations to beperformed and allows you to specify general parameters and options.

The keyword that follows the Calculation Type section heading indicatesthe type of calculation.

SIMULATION

The TOLERANCE statement modifies the default tolerance values.

TOLERANCE TTRIAL=0.01

The LIMITS statement defines limits on the design of STE exchangers andlimits on flowsheet calculations.

LIMITS AREA=200.00,60000.00, SERIES=1,10, PDAMP=0.00,*TTRIAL=50

The CALCULATION (CALC) statement sets the calculation methods forindividual exchangers on a global basis.

CALC TWOPHASE=NEW, DPSMETHOD=STREAM, MINFT=0.80

The PRINT statement sets print options on a global basis.

PRINT UNITS, ECONOMICS, STREAM, STANDARD,*EXTENDED, ZONES

The ECONOMICS statement defines economic factors affecting utility costcalculations.

ECONOMICS DAYS=350, EXCHANGERATE=1.00, CURRENCY=USDOLLAR

The UTCOST statement specifies the cost of utilities.

UTCOST OIL=3.50, GAS=3.50, ELECTRICITY=0.10,*WATER=0.03, HPSTEAM=4.10, MPSTEAM=3.90,*LPSTEAM=3.60, REFRIGERANT=0.00, HEATINGMEDIUM=0.00

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The HXCOST statement sets exchanger costing data on a global basis.

HXCOST BSIZE=1000.00, BCOST=0.00, LINEAR=50.00,*EXPONENT=0.60, CONSTANT=0.00, UNIT

Unit Operations SectionThe Unit Operations Data section allows you to enter information about theunit operations that are used in the simulation.

The UNIT OPERATIONS DATA statement identifies the section.

UNIT OPERATIONS

The unit keyword specifies the unit model.

STE

The TYPE statement defines the basic characteristics of the unit.

TYPE NEW, TEMA=NEN, HOTSIDE=SHELL, ORIENTATION=VERTICAL,*FLOW=COUNTERCURRENT, AREA=5000.00,12000.00,*UESTIMATE=50.00, USCALER=1.00

The TUBESIDE (TUBE) statement specifies the details for the exchangertubeside.

TUBE FEED=1, PRODUCT=2,*LENGTH=25.00,25.00,0.00, OD=1.750,*BWG=10, PASS=1,1,1, PATTERN=30,*PITCH=2.188, MATERIAL=9,*FOUL=0.0015, LAYER=0,*DPSHELL=2.000,10.000

The SHELLSIDE (SHELL) statement specifies the details for theexchanger shellside.

SHELL FEED=3, PRODUCT=4.*ID=60.00,80.00, SERIES=1,2,*SEALS=0, MATERIAL=INCOLOGY, DENSITY=501.0,*FOUL=0.004, LAYER=0,*DPSHELL=10.000,20.000

The BAFFLE (BAFF) statement provides details about the baffles and tubesheet.

BAFF NTIW, SEGMENTAL=SINGLE

The SPECIFICATION (SPEC) statement defines exchanger performancecriteria.

SPEC DUTY=28.06

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Chapter 4Input Reference

About This ChapterThis chapter contains information about the data that HEXTRAN needs toperform different types of simulation. These data are input in a free formatstyle ascii file, and the file is divided into categories; for example,Component Data, Thermodynamic Data, etc.

This chapter explains the general rules for input, which categories aremandatory, and which are optional. It defines all the terms used in the inputdescriptions and the conventions used throughout this chapter.

Each data category, the statements contained in it, and the keywords oneach statement are then described. For an explanation of how the programuses this data, please refer to Chapter 3, Using HEXTRAN, and Chapter 5,Technical Reference.

Categories of InputThe data that are required by HEXTRAN are input to the program in eightmain categories:

■ General Data Category Define general problem administration, and globalsettings that control the whole flowsheet.

■ Component Data Category Define all components present in the simulation.

■ Thermodynamic Data Category Define calculational and thermodynamic methods.

■ Stream Data Category Define all the streams present in the flowsheet.

■ Internal Property Data Category Define the default internal property calculations forthe streams.

■ External Property Data Category Define the user-specified properties that will overrideany property calculations made by HEXTRAN.

■ Flowsheet Calculations, Simulation,Regression, Cleaning Casestudy, SplitFlow Optimization Area Optimization,Targeting, and Synthesis DataCategory

Define the type of calculations to be performed.

■ Unit Operations Data Category Define the process units present in the flowsheet.This category is required when either of the Simula-tion, Regression, Cleaning Casestudy, Split FlowOptimization, or Optimization Area calculation cate-gories is used.

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Order of CategoriesThe only restriction on order of data input is that the General Data categoryof input must be first. However, it is always good practice to maintain aconsistent order. The order of the categories above, which is followed inthis chapter, is recommended.

KeywordsHEXTRAN’s primary mode for entering input is in the form ofkeyword-controlled, free format statements. The keyword entries on astatement are separated by commas. For example:

SETNO=5, STREAM=S1, TEMP=150

For ease of interpretation, each keyword is an engineering word. To makethe input easier to enter, any keyword with more than four characters can betruncated to a minimum of four characters. Keywords with fewer than fourcharacters cannot be lengthened. For example:

The keyword TEMPERATURE may be written TEMPThe keyword DPOINTS may be written DPOIThe keyword ID cannot be written IDIA

Keywords can stand alone, indicating that they are acting as a switch, orthey can be associated with a value or another keyword by the use of anequals sign (=). This value can be entered in integer, decimal, or scientificformat. For example:

ENGLISH English units set will be usedLENGTH=FT Units of length are feetTEMP=50 Temperature set to 50 unitsPRES=2.0E2 Pressure is 200 units

In the instructions presented in this chapter, the presence of an equals sign(=) after a keyword means that HEXTRAN expects a value or anotherkeyword. In some cases, however, a less simplistic form of input isrequired. When this situation arises, the instructions will include theformat for the data input. For example:

TEMP= indicates that a single value of temperature isrequired.

VISC= temp1, indicates that the program requires two data values withvalue1/temp2, their associated temperatures.value2

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QualifiersMany keywords can be qualified by entering a keyword in brackets afterthem. The most common use of a qualifier is for defining a unit of measureto override the set of units declared globally in the General Data categoryof input. Other qualifiers include the basis of a composition or flowrate.Some qualifiers are optional and some are mandatory. The inputinstructions explain which qualifiers are available for each keyword.Examples are:

PRES(BAR)=2 pressure is 2 bars absoluteRATE(W)=1000 rate is 1000 weight units

Multiple EntriesSome statements or keywords require more than one data item or group ofdata items to be input. In this case, the data items are separated by theslash (/) character. For example:

LIBID C1/C2/C3

is equivalent to:

LIBID C1

LIBID C2

LIBID C3

The input instructions specify where this is required. If an indeterminatenumber of data items is allowed, the input instruction will indicate this byadding three dots (...) to the end of the instruction.

Commenting InputFor clarity, you may add comments to your input. If a dollar sign ($) isplaced in a statement, any text on that statement that appears after the $ isignored by HEXTRAN. For example:

PRES=3.54 $ Pressure data, taken 0800 10/6/94

DefaultingMany of HEXTRAN’s data items are given default values. Therefore, ifyou do not explicitly specify such an item, the program will assign a value.These values have been selected to be reasonable for normal engineeringpurposes. Most methods also have defaults associated with them.

These defaults are for your convenience. They have not been selectedspecifically for your application and are not intended to replace engineeringjudgment. You should check that invalid output does not result due toinadvertent use of inappropriate defaults.

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The input instructions indicate the defaults that the program will use in theabsence of user input. All the numerical defaults in the input instructionsare expressed in terms of the units of measurement of the English set.

When you specify a value or override a default in the General Datacategory of input your value becomes the default for the entire simulation.You can then override your own default value later in the input.

Units of MeasureAlmost every item of data that you input to HEXTRAN has a unit ofmeasure associated with it. Most have alternatives: for example, length canbe measured in feet, meters, miles, or kilometers, and temperature in °F, °C,°R, or K. It is also possible to specify the unit of measure individually forevery item of data, but to avoid this, you may define at the beginning of theinput the units that are to be used for each quantity - temperature, duty,power etc. - throughout the whole simulation input. This is done on theDIMENSION statement in the General Data category of input. Individualdata items may be expressed in different units by using qualifiers asdescribed above.

For the user’s convenience, HEXTRAN has three sets of units of measure:English, Metric, and SI. Each set has predefined units for each data item.By selecting a set of units, then globally overriding some of the predefinedunits and then more specifically overriding those units for any individualdata item, the user is afforded a great deal of input flexibility.

For example, if you wanted to use the SI predefined unit set but withtemperature in F, and pressure in psia, your General Data category of inputwould contain the statement:

DIMENSION SI, TEMP=F, PRES=PSIA

If the temperature of one of your streams is measured in Kelvin you wouldhave in the Stream Data category of input:

PROP STREAM=S1, TEMP=300

Basis of MeasurementsWith some quantities – for example flow and composition – you can alsochoose a basis of measurement. The basis may be weight, liquid volume orgas volume, or molar, and you may use a qualifier to define it.

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The input instructions explain which bases are allowed. If a basis isspecified, HEXTRAN will then assume the unit to be the defaultappropriate to the basis you have defined.

Multiple Units of MeasureSome input items – for example a curve of viscosity against temperature –have more than one unit of measure. You can specify one or both units asqualifiers:

VISC(C,CP)=100,1.0/200,0.7

The order in which the qualifiers are entered is not important.

Continuing StatementsAn input statement may be too long to fit on one line. It may be continuedonto a second line or further by using the asterisk, *, or the & sign as thecontinuation character.

DIMENSION SI, LENGTH=FT, TEMP=C

is the same as

DIMENSION SI, LENGTH=FT, *TEMP=C

Layout of InputYou may indent any line of input to make the data more readable, and youmay have any number of spaces between data entries. For example:

DIMENSION SI, LENGTH=FT, *TEMP=C

is equivalent to

DIMENSION SI , LENGTH = FT, *TEMP= C

However, you may not embed any blanks within your keywords or dataentries. (The only exceptions are on the DESCription statement and on theNAME keyword.)

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Key to Description of Input StatementsEach data category is described in this chapter. At the start of each datacategory, there is a full listing of statements with all of their associatedkeywords. Each statement and each keyword are then explained in detail.

Throughout the input descriptions, the following conventions apply:

BOLD Bold capitals are used for keywords.For example: ENGLISH

You must use this word exactly as it is printed (or truncate it to four ormore characters). If a keyword has an equals sign (=) after it, you mustenter a value or another keyword after it.

If the keyword is underlined, this indicates that the keyword is the default.For example: PETROLEUM

If you omit the entry or statement altogether, the program will use thiskeyword as the default.

LIGHT Light capitals are used for values, methods, and entries.For example: SET=sid

Default entries are underlined.If you omit the entry altogether the program will use the default.

A number indicates a numerical default value.For example: DT=20

If you omit the entry altogether, the program will use this value as the default.

or A number of alternative entries are separated by the word or.For example: {PETROLEUM or NOPETRO}

You may select only one of the options contained within the { } bracketsand separated by the word or.

{ } This symbol indicates that a statement, keyword, or group of keywordsis/are optional.

For example: {TEMP=value}Your input will work without this entry. There is usually a default invokedif an entry is omitted.

( ) Indicate that qualifiers are allowed.For example: RATE(M)=

Unless otherwise noted, qualifiers are units of measurement.

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General Data Category of InputThe General Data input category allows you to enter required and optionalinformation about the particular HEXTRAN problem, define the input andoutput dimensional units, and select various input printout and calculationoptions.

Table 4-1: General Data Category of Input

Statement Keywords See ...

GENERAL DATA None Page 4-7

TITLE PROJECT=, PROBLEM=, USER=, DATE=, SITE= Page 4-8

{DESCRIPTION} Any text Page 4-9

DIMENSION {ENGLISH, METRIC, SI, AREA=, CONDUCTIVITY=, DENSITY=,ENERGY=, FILM=, LIQVOLUME=, POWER=, PRESSURE=, SURFACE=,TIME=, TEMPERATURE=, UVALUE=, VAPVOLUME=, VISCOSITY=,WT=, XDENSITY=, PBASIS =14.695, STDVAPOR=379.49}

Page 4-9

{OUTDIMEN-SION}

{ENGLISH, METRIC, SI, AREA=, CONDUCTIVITY=, DENSITY=,ENERGY=, FILM=, LIQVOLUME=, POWER=, PRESSURE=, SURFACE=,TIME=, TEMPERATURE=, UVALUE=, VAPVOLUME=, VISCOSITY=,WT=, XDENSITY=, PBASIS =14.695, STDVAPOR=379.49, ADD, -REPLACE}

Page 4-15

{PRINT} {ALL, NONE, GENERAL, PROPERTY, STREAM, UNIT, NEWS} Page 4-17

{CALCULATION} INCHECK, PGEN=NEW, WATER=SATURATED Page 4-19

GENERALDATA

GENERAL Data Category of Input

Optional statement. This statement identifies the GENERAL DATA input category for reference.If used, it must be the first statement in the General Data category.

Optional entries:

None

Example:

GENERAL DATA

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TITLE GENERAL Data Category of Input

Mandatory statement. This statement must be the first statement following the GENERALDATA statement (if given), or it can be used alone as the initial input statement. All entries onthis statement are optional and will be printed in the page headings in the output reports.

Mandatory entries:

None

Optional entries:

PROJECT= Identifies the project. Enter up to 12 alphanumeric characters.There is no default.

PROBLEM= Identifies the problem. Enter up to 12 alphanumeric characters.There is no default.

USER= Identifies the user. Enter up to 12 alphanumeric characters.There is no default.

DATE= Identifies the date. Enter up to 12 alphanumeric characters.There is no default.

SITE= Specifies the site code. Enter up to 12 alphanumeric characters.This entry is optional. If problems occur with the use of the SITEkeyword, check with your Systems Administrator to determine ifthe SITE keyword is required.

Examples:

GENERAL DATATITLE PROJECT=MANUAL,*

PROBLEM=EXAMPLE2, DATE=07-01-97...TITLE PROJECT=MANUAL,*

PROBLEM=EXAMPLE3, DATE=JULY 97...

In the first example, the GENERAL DATA statement is given and is followed by the TITLE state-ment (required).

In the second example, there is no GENERAL DATA statement. As a result, the TITLE statementis the first statement in the HEXTRAN program input file.

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DESCRIP-TION

GENERAL Data Category of Input

Optional statement. This statement is used to enter descriptive text about the HEXTRAN inputfile. Enter up to 60 alphanumeric characters, excluding the asterisk (*). Up to 4 DESCRIPTIONstatements can be entered in the General Data input category. The DESCRIPTION statementsdo not have to be grouped together in the input file, however, they must all be in the GeneralData input category.

Example:

TITLE PROJECT=MANUAL,*PROBLEM=EXAMPLE, USER=SIMSCI

DESCRIPTION THIS IS ONLY A TEST.DESCRIPTION IF THIS WASDESCRIPTION A REAL FILE...PRINT ALLDESCRIPTION WOULD COMPLETE IT....CALCULATION PGEN=SAVE...

DIMENSION GENERAL Data Category of Input

Optional statement. This statement defines the input and output dimensional units for aHEXTRAN problem. Various individual dimensional units may be selected to override thosedefined by the global set. Acceptable keyword entries for the various individual dimensionalunits are given in Table 4-3. The output dimensions may be supplemented or replaced bythose defined by the OUTDIMENSION statement (see page 4-15). Special optional dimensionkeywords are provided to define atmospheric pressure and standard vapor volume for compo-sitional and/or assay streams. The keywords are PBASIS and STDVAP, respectively (see page4-11).

Mandatory entries:

None

Optional entries:

ENGLISH or Specifies that the set of English dimensions will be used. Thestandard sets of units is given in Table 4-2. ENGLISH is thedefault.

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METRIC or Specifies that the set of Metric dimensions will be used. Thestandard sets of unit is given in Table 4-2. ENGLISH is thedefault.

SI Specifies that the set of SI dimensions will be used. The stan-dard sets of units is given in Table 4-2. ENGLISH is the default.

AREA= Overrides the set units for AREA values specified by theENGLISH, METRIC, or SI keywords. Acceptable values are listedunder AREA in Table 4-2. There is no default.

CONDUCTIVITY= Overrides the set units for CONDUCTIVITY values specified bythe ENGLISH, METRIC, or SI keywords. Acceptable values arelisted under CONDUCTIVITY in Table 4-2. There is no default.

DENSITY= Overrides the set units for DENSITY values specified by theENGLISH, METRIC, or SI keywords. Acceptable values are listedunder DENSITY in Table 4-2. There is no default.

ENERGY= Overrides the set units for ENERGY values specified by theENGLISH, METRIC, or SI keywords. Acceptable values are listedunder ENERGY in Table 4-2. There is no default.

FILM= Overrides the set units for FILM values specified by theENGLISH, METRIC, or SI keywords. Acceptable values are listedunder FILM in Table 4-2. There is no default.

LIQVOLUME= Overrides the set units for LIQVOLUME values specified by theENGLISH, METRIC, or SI keywords. Acceptable values are listedunder LIQVOLUME in Table 4-2. There is no default.

POWER= Overrides the set units for POWER values specified by theENGLISH, METRIC, or SI keywords. Acceptable values are listedunder POWER in Table 4-2. There is no default.

PRESSURE= Overrides the set units for PRESSURE values specified by theENGLISH, METRIC, or SI keywords. Acceptable values are listedunder PRESSURE in Table 4-2. There is no default.

SURFACE= Overrides the set units for SURFACE values specified by theENGLISH, METRIC, or SI keywords. Acceptable values are listedunder SURFACE in Table 4-2. There is no default.

TIME= Overrides the set units for TIME values specified by theENGLISH, METRIC, or SI keywords. Acceptable values are listedunder TIME in Table 4-2. There is no default.

TEMPERATURE= Overrides the set units for TEMPERATURE values specified bythe ENGLISH, METRIC, or SI keywords. Acceptable values arelisted under TEMPERATURE in Table 4-2. There is no default.

UVALUE= Overrides the set units for UVALUE values specified by theENGLISH, METRIC, or SI keywords. Acceptable values are listedunder UVALUE in Table 4-2. There is no default.

VAPVOLUME= Overrides the set units for VAPVOLUME values specified by theENGLISH, METRIC, or SI keywords. Acceptable values are listedunder VAPVOLUME in Table 4-2. There is no default.

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VISCOSITY= Overrides the set units for VISCOSITY values specified by theENGLISH, METRIC, or SI keywords. Acceptable values are listedunder VISCOSITY in Table 4-2. There is no default.

WT= Overrides the set units for WT values specified by the ENGLISH,METRIC, or SI keywords. Acceptable values are listed under WTin Table 4-2. There is no default.

XDENSITY= Overrides the standard petroleum density unit for supplied pe-troleum and synthetic fuel data as described in the COMPONENTDATA input category (page 4-21). Enter API, DENSITY, or SPGR(see Table 4-2). There is no default.

Note: When “XDENSITY=DENSITY” is given, the density mustbe given in the units of WT and LIQVOL selected; e.g., lb/ft3 orkg/m3.

PBASIS=14.696 Defines atmospheric pressure. The default is 14.696 psia (Eng-lish), 1.033kg/cm 2 (metric), or 101.642 kPa (SI).

STDVAPOR=379.49 Overrides the standard vapor volume basis. Enter a real value.The default is 379.49 ft3 /lbmole @ 60 °F and 14.696 PSIA (Eng-lish), or 22.414 m3 /kgmole @ 0 °C and 1 atmosphere (metricand SI).

Examples:

DIMENSION ENGLISHDIMENSION PRESSURE=PSIGDIMENSION SI, PRESSURE=ATE, PBASIS=0.987

� The first example selects the standard English set of dimensional units, which is alsothe default when the line is omitted.

� In the second example, the standard English pressure units (PSIA) are replaced withPSIG units.

The third example utilizes the PBASIS entry to redefine the pressure basis for ATE.

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Table 4-2: Standard Dimensional UnitsDimension Type Keyword English Metric SI

Area AREA ft 2 m 2 m 2

Density DENSITY lbm/ft 3 kg/m 3 kg/m 3

Duty MMBtu/time MMkcal/time MMkJ/time

Energy ENERGY Btu kcal kJ

Enthalpy Btu/lbm kcal/kg kJ/kg

Film coefficient FILM Btu/hr-ft 2 -F kcal/hr-m 2 -C W/m 2 -K

Foulingresistance

ft 2 -hr-F/Btu m 2 -hr-C/kcal m 2 -K/W

Latent heat Btu/lbm kcal/kg kJ/k

Length ft (or in) m (or mm) m (or mm)

Liquid volume LIQVOLUME ft 3 m3 m3

Petroleumdensity

XDENSITY API gravity density, kg/m 3 density, kg/m 3

Power POWER hp kW kW

Pressure PRESSURE psia kg/cm2 kPa

Specific heat Btu/lbm-F kcal/kg-C kJ/kg-K

Surface tension SURFACE dyne/cm dyne/cm N/m

Temperature TEMPERATURE F C K

Thermalconductivity

CONDUCTIVITY Btu/hr-ft-F kcal/hr-m-C W/m-K

Time TIME hr hr hr

U-value UVALUE Btu/hr-ft 2 -F kcal/hr-m 2 -C W/m 2 -K

Vapor volume VAPVOLUME ft 3 m 3 m 3

Velocity ft/sec m/s m/s

Viscosity VISCOSITY cP cP Pa-s

Weight WT lbm kg kg

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Table 4-3: Allowable Dimensional Units for DIMENSION and OUTDIMENSION StatementsDimension Type Keyword Entry Units

Area AREA = FT2M2

ft2 (square foot)m2 (square meter)

Thermal conductivity CONDUCTIVITY = BTUHKCHCALSWMCWMK

Btu/hr-ft-Fkcal/hr-m-Ccal/scm-CW/m-CW/m-K

Density DENSITY = LBFT, LBM/FT3

KGM3, KG/M3lbm/ft3

kg/m3

Energy ENERGY = BTUKCALKJPCUCHU

Btu (British thermal units)kcal (kilocalorie)kJ (kilojoule)pcu (pound-centigrade unit)chu (centigrade heat unit)

Film coefficient FILM = BTUH, BTU/HKCH, KC/HCALSWMCWMK

Btu/hr-ft2-Fkcal/hr-m2-Ccal/s-cm2-CW/m2-CW/m2-K

Liquid volume LIQVOLUME = FT3GALIGALBBLM3LITERDM3

ft3 (cubic foot)U.S. gal (U.S. liquid gallon)imp gal (Imperial gallon)bbl (U.S. petroleum barrel)m3 (cubic meter)L (liter)dm3 (cubic decimeter)

Power POWER = HPKW

hp (British horsepower)kW (kilowatts)

Pressure PRESSURE = PSIAPSIGKGCM, KG/CM2

TORRMMHGPAKPAMPABARATMATEATA

INH2FTH2

psia (lbf/in2-absolute)psig (lbf/in2-gauge)kg/cm2 (absolute)torr (1 mmHg at O C)mmHg (mm of mercury at O C)Pa (pascal, N/m2)kPa (kilopascal)MPa (megapascal)bar (absolute)atm (standard atmosphere)at (technical atmosphere-gauge)at (technical atmosphere absolute,kg/cm2)in H2O (inches H2O at 39.2 F)ft H2O (feet H2O at 39.2 F)

Surface tension SURFACE = NMDYNE

N/m (newton per meter)dyne/cm (dyne per centimeter)

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Table 4-3: Allowable Dimensional Units for DIMENSION and OUTDIMENSION Statements, continued

Dimension Type Keyword Entry Units

Time TIME = DAYHRMINSEC

dayhr (hour)min (minute)s (second)

Temperature TEMPERATURE = FRCK

F (degrees Fahrenheit)R (degrees Rankine)C (degrees Celsius)K (kelvin)

U-value(heat transfer coefficient)

UVALUE = BTUHKCHCALSWMCWMK

Btu/hr-ft2-Fkcal/hr-m2-Ccal/s-cm2-CW/m2-CW/m2-K

Vapor volume VAPVOLUME = FT3M3

ft3 (cubic foot)m3 (cubic meter)

Viscosity(dynamic, absolute)

VISCOSITY = CPPASLBFS, LB/FSLBFH, LB/FHLBSF, LBS/F

cP (centipoise, mPas)Pas (pascal-second)lbm/ft-slbm/ft-hrlbf-s/ft2

Weight WT = LBKGST, TONLT, TONLMT, TONM

lbm (pound avoirdupois)kg (kilogram)ton (short ton, 2000 lbm)ton (long ton, 2240 lbm)t (metric ton, 1000 kg, tonne)

Petroleum density XDENSITY = APIDENSSPGR

API gravityDensity unitsSpecific gravity

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OUT-DIMENSION

GENERAL Data Category of Input

Optional statement. This statement specifies different output dimensional units from those in-dicated on the DIMENSION statement. You can also use this statement to print two sets ofoutput; one based on DIMENSION statement units and one based on the OUTDIMENSIONstatement units.

Mandatory entries:

None

Optional entries:

ENGLISH or Specifies that the set of English dimensions will be used. Thestandard sets of units for is given in Table 4-2. ENGLISH is thedefault. Various individual dimensional units may be selected tooverride those defined by the standard set. Acceptable keywordentries for the various individual dimensional units are given inTable 4-3.

METRIC or Specifies that the set of Metric dimensions will be used. Thestandard sets of units is given in Table 4-2. ENGLISH is thedefault.

SI Specifies that the set of SI dimensions will be used. The stan-dard sets of units is given in Table 4-2. ENGLISH is the default.

AREA Overrides the set units for AREA values specified by theENGLISH, METRIC, or SI keywords for output purposes only.Acceptable values are listed under AREA in Table 4-2. There isno default.

CONDUCTIVITY Overrides the set units for CONDUCTIVITY values specified bythe ENGLISH, METRIC, or SI keywords for output purposes only.Acceptable values are listed under CONDUCTIVITY in Table 4-2.There is no default.

DENSITY Overrides the set units for DENSITY values specified by theENGLISH, METRIC, or SI keywords for output purposes only.Acceptable values are listed under DENSITY in Table 4-2. Thereis no default.

ENERGY Overrides the set units for ENERGY values specified by theENGLISH, METRIC, or SI keywords for output purposes only.Acceptable values are listed under ENERGY in Table 4-2. Thereis no default.

FILM Overrides the set units for FILM values specified by theENGLISH, METRIC, or SI keywords for output purposes only.Acceptable values are listed under FILM in Table 4-2. There is nodefault.

LIQVOLUME Overrides the set units for LIQVOLUME values specified by theENGLISH, METRIC, or SI keywords for output purposes only.Acceptable values are listed under LIQVOLUME in Table 4-2.There is no default.

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POWER Overrides the set units for POWER values specified by theENGLISH, METRIC, or SI keywords for output purposes only.Acceptable values are listed under POWER in Table 4-2. There isno default.

PRESSURE Overrides the set units for PRESSURE values specified by theENGLISH, METRIC, or SI keywords for output purposes only.Acceptable values are listed under PRESSURE in Table 4-2.There is no default.

SURFACE Overrides the set units for SURFACE values specified by theENGLISH, METRIC, or SI keywords for output purposes only.Acceptable values are listed under SURFACE in Table 4-2. Thereis no default.

TIME Overrides the set units for TIME values specified by theENGLISH, METRIC, or SI keywords for output purposes only.Acceptable values are listed under TIME in Table 4-2. There is nodefault.

TEMPERATURE Overrides the set units for TEMPERATURE values specified bythe ENGLISH, METRIC, or SI keywords for output purposes only.Acceptable values are listed under TEMPERATURE in Table 4-2There is no default.

UVALUE Overrides the set units for UVALUE values specified by theENGLISH, METRIC, or SI keywords for output purposes only.Acceptable values are listed under UVALUE in Table 4-2 There isno default.

VAPVOLUME Overrides the set units for VAPVOLUME values specified by theENGLISH, METRIC, or SI keywords for output purposes only.Acceptable values are listed under VAPVOLUME in Table 4-2.There is no default.

VISCOSITY Overrides the set units for VISCOSITY values specified by theENGLISH, METRIC, or SI keywords for output purposes only.Acceptable values are listed under VISCOSITY in Table 4-2.There is no default.

WT Overrides the set units for WT values specified by the ENGLISH,METRIC, or SI keywords for output purposes only. Acceptablevalues are listed under WT in Table 4-2. There is no default.

XDENSITY= Overrides the standard petroleum density unit for supplied pe-troleum and synthetic fuel data as described in the COMPONENTDATA input category (page 4-21) for output purposes only. EnterAPI, DENSITY, or SPGR (see Table 4-3). There is no default.

Note: When “XDENSITY=DENSITY” is given, the density must begiven in the units of WT and LIQVOL selected; e.g., lb/ft3 orkg/m3.

PBASIS=14.696 Specifies atmospheric pressure for output only. The default is14.696 psia (English), 1.033kg/cm2 (metric), or 101.642 kPa(SI).

STDVAPOR=379.49 Overrides the standard vapor volume basis for output only. Entera real value. The default is 379.49 ft3 /lbmole @ 60 °F and

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14.696 PSIA (English), or 22.414 m3 /kgmole @ 0 °C and 1 at-mosphere (metric and SI).

ADD Specifies two outputs; one using the DIMENSION statement set-tings, and one using the OUTDIMENSION statement settings.The ADD and REPLACE keywords are mutually exclusive. ADD isthe default.

REPLACE Specifies a single output using the OUTDIMENSION statementsettings. The ADD and REPLACE keywords are mutually exclu-sive. ADD is the default.

Examples:

DIMENSION ENGLISHOUTDIMENSION ADD, SIDIMENSION METRIC OUTDIMENSION REPLACE, TIME=DAY

� In the first example, two sets of output are requested. The first will be in English units,the second in SI units.

� In the second example, the default metric output is replaced with output in Englishunits. The standard time unit of hours (HR) is replaced by days with the TIME=DAYentry.

PRINT GENERAL Data Category of Input

Optional statement. This statement specifies the input reprint options. The printout options aredivided into two categories: global (ALL,NONE), or selective (GENERAL,PROPERTY,STREAM,UNIT, and NEWS). The selective keywords may be used individually or grouped to-gether, separated by commas. Regardless of the PRINT options selected, an echo of the inputdata statement is always printed.

Mandatory entries:

None

Optional entries:

ALL Specifies the full input data reprint. The only other keyword al-lowed on the PRINT statement with ALL is NEWS. ALL is thedefault.

NONE Suppresses the entire input data reprint.

GENERAL Specifies the general data section input reprint. All other inputreprint is suppressed.

PROPERTY Specifies the property section input reprint. All other input re-print is suppressed.

STREAM Specifies the stream section input reprint. All other input reprintis suppressed.

TBP Specifies the TBP and ASTM distillation reports for all appropri-ate streams in the flowsheet.

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SFORMAT=ALL Specifies sections of the stream results printout.

COMPONENT prints stream component reports.

ALL prints all standard stream component rates and the streamsummary report.

SUMMARY prints only the stream summary report.

RATE=M Specifies the basis for the stream component flow rates. Mspecifies a molar basis, WT specifies a weight basis, LV speci-fies a liquid volume basis, and GV specifies a gas volume basis.You can specify more than one basis.

FRACTION=M Specifies the basis for the stream component fractions. M speci-fies a molar basis, WT specifies a weight basis, LV specifies aliquid volume basis, and GV specifies a gas volume basis. Youcan specify more than one basis.

PERCENT=M Specifies the basis for the stream component percentage. Mspecifies a molar basis, WT specifies a weight basis, LV speci-fies a liquid volume basis, and GV specifies a gas volume basis.You can specify more than one basis.

UNIT Specifies the unit operations section input reprint. All other inputreprint is suppressed.

Examples:

PRINT NONEPRINT STREAM, UNITPRINT SFORMAT=COMPONENT

RATE=M, WT

� In the first example the input data reprint has been turned off.

� In the second example, only the STREAM and UNIT data input reprint will be printed.All other input data reprint has been suppressed.

� In the third example, the stream component report is printed, with flow rates reportedon a molar basis and a weight basis.

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CALC-ULATION

GENERAL Data Category of Input

Optional statement. This statement controls calculation options related to:

� input data checking

� stream and property data limits

� compositional and assay stream property data file control

� water and steam calculation methods

Mandatory entries:

None.

Optional entries:

INCHECK Specifies input data checking only. This option allows for com-plete processing and printing of all input data and any associ-ated error messages. INCHECK suppresses all calculations andassociated output. There is no default.

PGEN=NEW Specifies the use of the internally generated property data file forcompositional and/or assay streams. Enter either NEW, SAVE, orOLD. The PGEN option refers only to compositional and/or assaystreams given in the STREAM DATA input category. Propertycalculations for all other streams are unaffected by this option.The default is NEW.

NEW specifies internal property calculations for each composi-tional and/or assay stream. New property data values are com-puted for each HEXTRAN run. The internal property data file isnot saved for future use, and there is no royalty charge.

SAVE specifies internal property calculations for each composi-tional and/or assay stream, and saves the file to disk. The royaltycharge for the run will include a charge for the internal propertycalculations.

OLD specifies that internal property data will be taken from apreviously generated file. New property calculations will not beperformed for any of the compositional or assay streams. Thisoption is recommended to save computer time when the prop-erty data values (compositional and assay streams only) do notchange from run to run.

WATER=SATURATED Specifies the method used to calculate water and steam thermalproperties. Enter SATURATED, KEENAN, or SENSIBLE. The de-fault is SATURATED.

SATURATED specifies calculation based on saturated conditions.The enthalpy of superheated steam will be identical to that ofsaturated steam at the same conditions.

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KEENAN specifies calculation based on the 1969 Keenan &Keyes Steam Tables. The stream inlet temperature and pressureare used to determine if the stream is a compressed liquid, satu-rated, or superheated.

Note: The SATURATED method is accurate for most problems,and results in considerably less (up to one half) computing timethan the more accurate KEENAN method. The KEENAN methodis recommended for compositional or assay streams where wa-ter is a major component, (or non-compositional and non-assaystreams where the stream flow rate is given with the WATER= orSTEAM= entries (Stream Data section)) and accurate subcooledand superheated thermal data values are needed.

SENSIBLE specifies that the specific heats of water and steamare to be used for the heat balance calculations. This entry isonly applicable to non-compositional and non-assay streamswhen the stream flow rate is given with the WATER= or STEAM=entries (Stream Data section).

Note: With the SENSIBLE option, once the water or steam phaseis defined, phase changes will not be detected. Thus, this optionis useful (and quicker) for streams such as cooling water, or fora superheated steam that does not condense.

Examples:

CALCULATION INCHECKCALCULATION PGEN=SAVE, WATER=KEENAN

� In the first example, the INCHECK option is used to request input data checking only.This option results in complete processing and printing of all input data and any asso-ciated error messages. However, all calculations and the associated output are sup-pressed.

� In the second example, the SAVE option is used to retain the property data file createdby HEXTRAN for the compositional and/or assay streams given in the STREAM DATAinput category. The saved property data file can then be used in another HEXTRANproblem, if desired. The KEENAN entry specifies the use of the 1969 Keenan & Keyessteam tables for calculation of water and steam properties.

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Component Data Category of InputThe Component Data category defines the pure and pseudocomponents inthe simulation and, if necessary, defines or modifies component properties.All components encountered in a problem, except for assay streamcomponents, must be defined in this category. Streams defined bydistillation assay curves in the Stream Data category are broken intopseudocomponents based on the rules defined in the Component Datacategory of input.

Using keyword input, HEXTRAN accepts up to 250 components.

The SIMSCI Component and Thermodynamic Data Input Manual, Vol. Iand II, describes all the features of the SIMSCI Component Data system.Only the commonly used features are described here in detail. Refer to theSIMSCI Component and Thermodynamic Data Input Manual, Vol. I and IIfor details on additional component data options.

Table 4-4: Component Data Category of InputStatement Keywords See...

COMPONENT None Page 4-23

LIBID number, name {, , alias}/ ..., {BANK=, FILL=} Page 4-23

{PETROLEUM()} number, name, mol wt, gravity, normal boilingpoint/...

Page 4-24

{ASSAY} CHARACTERIZE= CAVETT, MW=SIMSCI, GRAV-ITY=WATSONK, {FIT=SPLINE,CONVERSION=API187, TBPIP=1, TBPEP=98, NBP=}

Page 4-24

{CUTPOINTS} TBPCUTS() = 100,800,28/1200,8/1600,4 Page 4-26

{Constants}MWSPGRAPIACENTRICZCTC()PC()VC()NBP()STDDENSITY()

component number, value/...Page 4-26Page 4-26Page 4-26Page 4-26Page 4-26Page 4-27Page 4-27Page 4-27Page 4-27Page 4-27

{Variables}VP()ENTHALPY()CP()LATENT()DENSITY()VISCOSITY()CONDUC-TIVITY()SURFACE

CORR = , {LN or LOG or EXPFAC = }, DATA =orTABULAR =

Page 4-28Page 4-28Page 4-28Page 4-28Page 4-28Page 4-28Page 4-28

Page 4-28

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Table 4-4: Component Data Category of InputStatement Keywords See...

Otherstatements:

For details, refer to the SIMSCI Component and Thermodynamic DataInput Manual, Vol. I and II.

NONLIBRARY Components that are not in the SIMSCI bank and forwhich you have to supply a full set of properties.

PHASE Identifies solid components

SYNCOMP Data for a synfuel component of a specific type.

SYNLIQ Data for a synfuel component that is a mixture ofdifferent petroleum types.

RACKETT Rackett parameter required for the Rackett methodfor liquid densities.

DIPOLE Dipole moment required for the Hayden-O’Connellmethod for vapor properties.

RADIUS Radius of gyration required for the Hayden-O’Connellmethod for vapor properties.

SOLUPARA Hildebrand solubility parameter required for variousgeneralized and liquid activity thermodynamiccorrelations.

MOLVOL Liquid molar volume required for various generalizedand liquid activity thermodynamic correlations.

VANDERWAAL Van der Waals area and volume required for UNIFACand UNIQUAC liquid activity thermodynamiccorrelations.

STRUCTURE,GROUP

Data for non-library components for use with theUNIFAC thermodynamic method.

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COMPONENT COMPONENT Data Category of Input

Mandatory statement for compositional fluids. Introduces the category.

Mandatory entries:

None

Optional Entries:

None

LIBID COMPONENT Data Category of Input

Optional statement. Identifies the components whose properties are to be taken from theSIMSCI databank.

Mandatory entries:

number, name{, , alias} / ... For each component, its number in the component list for thissimulation followed by its library name (not the full name).Separate one components entry from the next using the /character.

Select components from the list in the SIMSCI Component andThermodynamic Data Input Manual, Vol. I and II. For conven-ience, some components have more than one allowable name.

Optionally, you may also enter an alias (up to 16 characters) fora component, which will be used in the output reports. If youenter an alias, you must have two commas before it.

You may enter the components in any order but there must be nogaps in the component number sequence and each componentnumber must be used only once. This rule applies to all definedcomponents, including Petroleum pseudocomponents entered us-ing the PETROLEUM statement below, but does not apply to pe-troleum fractions generated by the program from ASTM curves.

Other entries: (For details, refer to the SIMSCI Component and Thermody-namic Data Input Manual, Vol. I and II.)

BANK Selects order of component databanks which are searched forpure components.

FILL Specifies that SIMSCI property prediction methods be used forcomponents missing library or user-supplied data.

Examples:

LIBID 1, C1/2, C2/3, C3LIBID 1, C1,, METHANE/3, C3/2, ETHN,, PURE ETHANE

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PETROLEUM COMPONENT Data Category of Input

Optional statement. Defines petroleum fraction pseudocomponents. Component propertiesare calculated using the characterization method selected on the ASSAY statement below.

Mandatory entries:

number, name, MW,std liquid density, NBP/...

You may supply a name of up to 16 characters for each compo-nent. The name is used in the output reports. You must supplyat least two of the three quantities: molecular weight, gravity andnormal boiling point. The remaining value is calculated. You mayuse qualifiers to define units of measurement for gravity and/ornormal boiling point.

The number must follow the rules described above under LIBID.

If a name is not given, PRO/II will assign a name based on thenormal boiling point.

If you omit any data item, you must retain the embeddedcomma.

Example:

PETRO 5, CUT11, 91,64,180/6, CUT12,100,,210/ &7, CUT13,120,55,280/8, CUT14,150,,370/ &9, CUT15,200,40,495/10, CUT16,245,,590/ &11, CUT17,300,30,687/12, CUT18,360,,770

ASSAY COMPONENT Data Category of Input

Optional statement. Used to specify the method by which PIPEPHASE calculates the proper-ties of defined pseudocomponents or those generated from assay data.

Mandatory entries:

CHARACTERIZE = CAVETT Define the method to be used for calculating critical propertiesand enthalpies of pseudocomponents. Options are described inTable 4-5.

MW = SIMSCI Define the method to be used for calculating molecular weightsof pseudocomponents. Options are described in Table 4-6.

GRAVITY = WATSONK Define the method to be used for calculating gravities for pseu-docomponents when only the average gravity of a curve isgiven. Options are described in Table 4-7.

Other entries: (For details, refer to the SIMSCI Component and Thermody-namic Data Input Manual, Vol. I and II.)

FIT = SPLINE Selects the curve fitting procedure for user supplied assay data.

CONVERSION = API187 Selects the method for inter-conversion between ASTM-D86 andTBP distillation curves.

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TBPIP = 1,TBPEP = 98

Define the volume percents for determining the initial point andend point (EP) temperatures when specifying streams and re-porting assay curves at output time.

NBP = Designates the method used for calculating the normal boilingpoint of narrow cuts.

Example:

ASSAY CHAR = SIMSCI, MW = CAVETT, GRAV = WATSONK

Table 4-5: HEXTRAN Characterization Methods

Method Description

CAVETT CAVETT is used for critical constants and ideal gas enthalpies.Yen-Alexander is used for vapor pressures.Edmister is used for acentric factors.

SIMSCI SIMSCI’s extension of the CAVETT method is used for all prop-erties. Also known as the Twu method.

LK Lee-Kesler is used for all properties.

Table 4-6: HEXTRAN Molecular Weight Methods

Method Description

SIMSCI Method developed by SIMSCI to match the APITechnical Data Book method for 300 to 800° F boil-ing components and to provide a better match tothe available field data both above and below thattemperature range.

EXTAPI 1980 API Technical Data Book method with adjust-ment for components boiling below 300° F to matchknown pure component data better. Also known asthe CAVETT80 method.

CAVETT Old (pre-1980) API Technical Data Book method.

Table 4-7: HEXTRAN Gravity Methods

Method Description

WATSONK Assumes constant Watson K for all componentsbased on TBP temperatures.

PRE301 Assumes constant Watson K for all componentsbased on ASTM temperatures.

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CUTPOINTS COMPONENT Data Category of Input

Optional statement. Used to define the TBP cut points for components defined by assaycurve.

Mandatory entries:

TBPCUTS()=t0, t1, n1{/t2, n2/..}

t0 is the start temperature for the whole assay, t1 is the end tem-perature for the first group and n1 is the number of cuts in thefirst group. Then, for each subsequent group of cuts, enter theend temperature for the group and the number of cuts in thatgroup.

The default is 100, 800, 28/1200, 8/1600, 4

Examples:

CUTPOINTS TBPCUTS(F)=100,800,20/ 1000, 10/ 1200,8CUTPOINTS TBPCUTS(F)=100,1200,38

MW, SPGRAPI

ACENTRICZC

COMPONENT Data Category of Input

Optional statements. Define constant properties of pure components.

Mandatory entries:

number, value/ ... The number corresponds to the components number on theLIBID statement.

Example:

MW 1, 59.3/4, 76.5

The molecular weight of component 1 is 59.3 gm/gmmole or 59.3 lb/lbmole. The molecularweight of component 4 is 76.5.

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TC(), PC()NBP()

STDDENSITY()

COMPONENT Data Category of Input

Optional statements. Define constant properties of pure components. A qualifier may be usedto specify units of measurement.

Mandatory entries:

number, value/ ... The number corresponds to the components number on theLIBID statement.

Example:

STDD(LBFT3) 4,45/7,50

The standard density of component 4 is 45 lb/ft3 and the standard density of component 7 is50 lb/ft3.

VC COMPONENT Data Category of Input

Optional statement. Defines critical volume of pure components. Qualifiers may be used tospecify units of measurement and basis.

Mandatory entries:

number, value/ ... The number corresponds to the components number on theLIBID statement.

Example:

VC(CC,M) 1, .09 (Note: This is equivalent to 90 cc/gm mole.)

The critical volume of component 1 is 0.09 cc/kgmole.

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VP()ENTHALPY()

CP()LATENT()

DENSITY()VISCOSITY()

CONDUC-TIVITY()

SURFACE()

COMPONENT Data Category of Input

Optional statements. Define pure component properties that vary with temperature. Whereappropriate, qualifiers may be used to specify phase, temperature unit, property units and ba-sis. Properties are listed in Table 4-8.

Table 4-8: HEXTRAN Pure Component Variable Properties

Property Keyword Phase* Property Units Basis

Density DENSITY() L or S density M or WT

Enthalpy ENTHALPY() I, L or S energy M or WT

Solid specific heat CP() heat capacity M or WT

Latent heat ofvaporization

LATENT() energy M or WT

Vapor pressure VP() L or S pressure

Viscosity VISCOSITY() V or L viscosity

Thermal conductivity COND() V, L or S conductivity

Liquid surface tension SURFACE() surface tension

*Phases are: IVLS

ideal gasvaporliquidsolid

You may enter either coefficients of an equation or tabular data.

Coefficient form:

Mandatory entries:

CORRELATION The correlation form for equation based data. See the SIMSCIComponent and Thermodynamic Data Input Manual, Vol. I andII, for equation forms. Note: Only equation 1 may be used forCP.

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DATA = Data entry for equation based correlations. The format is:DATA = i, tmax, tmin, C1, ..., C8/...

i corresponds to the components number on the LIBIDstatement.

tmax, tmin are temperature limits for the data. They must be en-tered for Chebychev equations, and are optional for others. Ifomitted, the embedded commas must be retained.

C1,...,C8 are equation coefficients.

EXPFAC = Exponential factor. Only used in equations 3 and 4.

Optional entries:

LN or LOG Select the logarithmic base e (LN) or 10 (LOG). Only used inequations with logarithmic terms.

Tabular form:

Mandatory entries:

TABULAR = Data entry for tabular data. The format is:TABULAR = t1, t2, .../i, p1, p2, .../...

t1, t2,... are temperatures at which tabular data are entered.

i corresponds to the components number on the LIBIDstatement.

p1, p2,... are data values at temperatures t1, t2,... . A minimum ofone value must be given. You need not provide a value for everytemperature point but if you skip a value you must retain theembedded comma.

Examples:

DENSITY(L,C,LBFT3) TABULAR = 60, 80, 100/1,55.5,43.7/ &2,45.8,,40.2

ENTHALPY(I,C,KCAL/KG,M) TABULAR=100,140,180/&1,700000,825000,910000/ 2,410000, ,470000

VP(C,MMHG) CORR=21, LN, DATA= 1,,, 14.321, -1068, 60.3/ &2,,, 16.15, -1372, 1.7

The liquid density of component 1 is 55.5 lb/ft3 at 60°C, 43.7 lb/ft3 at 80°C, and the liquid den-sity of component 2 is 45.8 lb/ft3 at 100°C.

The ideal density of component 1 is 700000 kcal/kgmol at 100°C, 825000 kcal/kgmol at140°C, 910000 kcal/kgmol at 180°C, and the ideal enthalpy of component 2 is 410000kcal/kgmol at 100 °C, 470000 kcal/kgmol at 180°C.

The vapor pressure of components 1 and 2 in mmhg is given by correlation #21.

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Thermodynamic Data Category of InputThe Thermodynamic Data Category of input defines the methods thatHEXTRAN uses to determine phase separation and transport properties incompositional runs. This category is required only if you have specified thatthe fluid is compositional on the Calculation statement in the General Datacategory.

Only the commonly used features are described here in detail. Refer to theSIMSCI Component and Thermodynamic Data Input Manual, Vol. I and IIfor details on additional thermodynamic data options.

Table 4-9: Thermodynamic Data Category of Input

Statement Keywords See ...

THERMODYNAMIC None Page 4-31

METHOD {SYSTEM() =, KVALUE() =, ENTHALPY() =, DENSITY() =,TRANSPORT = PURE, VISCOSITY() =, CONDUCTIVITY() =,SURFACE =, SET = , DEFAULT}

Page 4-32

WATER DECANT = , {GPSA, SOLUBILITY = SIMSCI,PROPERTY = SATURATED}

Page 4-35

BWRS i, j, kij/ ... Page 4-36

LKP i, j, kij/ ... Page 4-36

PR i, j, kija, kijb, kijc/ ... Page 4-36

SRK i, j, kija, kijb, kijc/ ... Page 4-36

Other statements: For details, refer to the SIMSCI Component and Thermodynamic Data Input Manual.

KVALUEENTHALPYDENSITY

Used to identify non-default databanks and methods of calcu-lating missing data.

KDATA Allows user-supplied K-value data.

HEXAMER, HOCV,TVIRIAL, IDIMER,RK1, RK2, SRKKD,SRKM, SRKH, PRP,PRM

Allows user-supplied binary interaction data for equations ofstate and generalized correlations.

Other statements For details, refer to the SIMSCI Component and Thermodynamic Data Input Manual,Vol. I and II.

NRTL, UNIQUAC,WILSON, VAN-LAAR, MAR-GULES, FLORY,IDEAL, AZEO-TROPE, INFINITE,MUTUAL,

Allows user-supplied binary interaction data for liquid activitymethods.

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Table 4-9: Thermodynamic Data Category of Input

Statement Keywords See ...

PHI Used to identify vapor fugacity databanks.

HENRY, SOLUTE,HENDATA

Used to identify Henry’s Law databanks.

SOLUTE, SOLDATA Used to supply data for solid-liquid equilibrium.

UNIFAC, UNIFTn,UNFV

Group contribution data for UNIFAC and/or UNIWAALS.

PAnn, SAnn, VAnn Supplies pure component alpha formulations for PR, SRKand UNIWAAL.

TC, PC, VC, ZC,ACENTRIC, NBP,MOLVOL, DIPOLE,RADIUS,SOLUPARA,RACKETT, WDELT

Used to specify pure component data for use with a specificthermodynamic method in place of the data input in the Com-ponent Category.

THERMO-DYNAMIC

THERMODYNAMIC Data Category of Input

Mandatory statement for compositional fluids. Introduces the category.

Mandatory entries:

None

Optional entries:

None

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METHOD THERMODYNAMIC Data Category of Input

Optional statement. Defines the methods to be used for calculating thermodynamic propertiesand transport properties of the flowing fluid. Choose systems with predefined methods for allproperties or choose individual methods for each property.

If you want to use different methods to calculate properties of different sources, use multipleMETHOD statements. Identify each METHOD statement using a SET keyword and refer to thatidentifier with the SET keyword on the SOURCE statement in the Structure Category.

Mandatory entries: You must specify either SYSTEM or KVALUE, ENTHALPY andDENSITY.

All other entries are optional.

Optional Entries:

SYSTEM() = Select a thermodynamic system from Table 4-10. The SYSTEMwill allocate methods for calculating K-values, enthalpies anddensities. If you select a SYSTEM, you can still override one ormore of the individual methods by using the other keywords onthis statement.

Use a qualifier to denote which type of equilibrium calculationsare to be performed. Allowable qualifiers are:

SYSTEM VLE vapor-liquidVLLE vapor-liquid-liquid

KVALUE() =ENTHALPY() =DENSITY() =

Select methods from Table 4-11 for calculating K-values, enthalpiesand densities. If you have selected a SYSTEM, you do not needthese keywords; use them if you want to override the individualmethods automatically selected as part of the predefined SYSTEM.

Use qualifiers to denote which type of equilibrium calculationsare to be performed and the phases to which the methods apply.Allowable qualifiers are:

KVALUE VLE (or none) vapor-liquidLLE liquid-liquidVLLE vapor-liquid-liquidSLE solid-liquid

ENTHLPY VL (or none) both vapor and liquidV vapor onlyL liquid only

DENSITY VL (or none) both vapor and liquidV vapor onlyL liquid only

If you want to specify a different method for different phases, you may have more than oneKVALUE entry. However it is done, whether with SYSTEM or KVALUE or a combination, youmust include all phases present in the simulation.

For ENTHALPY and DENSITY you must specify methods for both vapor and liquid either byspecifying a method for VL or a method for V and a method for L.

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TRANSPORT = Select a transport system from Table 4-12 TRANSPORT will al-locate methods for calculating viscosity, conductivity and sur-face tension. If you select TRANSPORT, you can still overrideone or more of the individual methods by using other keywordson this statement.

VISCOSITY() =CONDUCTIVITY() =SURFACE =

Select methods from Table 4-13 for calculating conductivity,surface tension and viscosity. If you have selected aTRANSPORT system, you do not need these keywords; usethem if you want to override the individual methods automati-cally selected as part of the predefined TRANSPORT system.

Use qualifiers to denote the phases to which the methods apply.Allowable qualifiers are:

VISCOSITY VL (or none) both vapor and liquidV vapor onlyL liquid only

CONDUCTIVITY VL (or none) both vapor and liquidV vapor onlyL liquid only

SURFACE none liquid only

For VISCOSITY and CONDUCTIVITY you must specify methodsfor both vapor and liquid either by specifying a method for VL ora method for V and a method for L.

SET = Up to 12 alphanumeric characters. Identifies this METHOD state-ment. Needed only when multiple METHOD statements are used.Referenced using the SET keyword on the SOURCE statement inthe Structure category of input.

DEFAULT Identifies the default method set. When a SOURCE statement inthe Structure Category does not explicitly specify a SET, thedefault method set is used. If no METHOD statement has theDEFAULT keyword, the first METHOD statement in the input isused as the default set. Only one METHOD statement may havethe DEFAULT keyword.

Other entries: (For further information, refer to the SIMSCI Component andThermodynamic Data Input Manual, Vol. I and II.)

PHI Method to be used to compute pure component and mixturevapor fugacity coefficients for liquid activity methods.

HENRY Used to model dissolved gases in a liquid solution for liquidactivity methods.

Examples:

METHOD SYSTEM=SRK, TRANS=HCMIX, SET=MYSET1METHOD KVALUE=SRK, ENTHALPY=SRK, DENS(L)=API, DENS(V)=SRK, &

VISC(V)=PETRO, VISC(L)= PURE, COND=PETRO, SURFACE=PURE, &DEFAULT, SET=MYSET2

METHOD SYSTEM=SRK, KVALUE(LLE)= NRTL, KVALUE(SLE) = VANTHOFF

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Table 4-10: Methods Used by Predefined Thermodynamic Systems

System K-value Enthalpy Density (V) Density (L)

BK10 BK10 JG IDEAL API

BWRST BWRST BWRST BWRST BWRST

CS CS CP SRK API

GS GS CP SRK API

LKP LKP LKP LKP API

PR PR PR PR API

SRK SRK SRK SRK API

For other systems, refer to Appendix B, SIMSCI Thermodynamic Data InputManual, Vol. I, Table B20.4-1.

Table 4-11: Thermodynamic Property Calculation MethodsMethod Keyword K-value Enthalpy Density (L) Density(V)

API Method API Yes

BWRS-Twu BWRST Yes Yes Yes Yes

Braun K-10 BK10 Yes

Chao-Seader CS Yes*

Curl-Pitzer CP Yes

Grayson-Streed GS Yes*

Johnson-Grayson JG Yes

Lee-Kesler LK Yes Yes Yes

Lee-Kesler-Plöcker LKP Yes Yes Yes Yes

Peng-Robinson PR Yes Yes Yes

Redlich-Kwong RK Yes

Soave-Redlich-Kwong

SRK Yes Yes Yes

For other methods, refer to Appendix B, SIMSCI Thermodynamic Data Input Manual, Vol. I,Table B20.3-1.

*Not to be used for systems with more than a total of 5% molar carbon dioxide and hydrogensulfide or for fluids above their critical points.

Table 4-12: Methods Used by Predefined TRANSPORT SystemsSystem Viscosity Conductivity Surface Tension

PURE PURE PURE PURE

PETRO PETRO PETRO PETRO

TRAPP TRAPP TRAPP PETRO

TACITE LBC TRAPP PARACHOR

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Table 4-13: Transport Property Calculation Methods

Method Keyword Viscosity Conductivity SurfaceTension

Library Data PURE Yes Yes Yes

Hydrocarbon predictions PETRO Yes Yes Yes

TRAPP Method TRAPP Yes Yes

API Technical Data Book API Liquidonly

Woelfin Method (Tight correlation usingPURE or PETRO method)

TWOELF orTSWOELF

Liquidonly

Woelfin Method (Medium correlationusing PURE or PETRO method)

MWOELForMSWOELF

Liquidonly

Woelfin Method (Loose correlationusing PURE or PETRO method)

LWOELF orLSWOELF

Liquidonly

Lohrenz-Bray-Clark LBC Liquidonly

Parachor Method PARACHOR Yes

WATER THERMODYNAMIC Data Category of Input

Optional statement. Defines the method to be used for calculating water and steamproperties.

Mandatory entries:

DECANT = When ON, water is treated as a special component, its solubilityin the hydrocarbon phase is calculated and the non-dissolvedwater put into a separate phase. When OFF, water is treated asbeing fully soluble in the rest of the stream. When SRK, PR, GS,CS, GSE, CSE, IGS, LKP, BK10 or BWRS methods are used,DECANT is optional and defaults to ON.

Optional Entries:

GPSA Used with DECANT = ON to specify that water partial pressuresare calculate using the GPSA Data Book Figure 20-3. If this key-word is not present, steam tables are used.

SOLUBILITY = SIMSCI Used to specify the method of computing the solubility of waterin the hydrocarbon phase. Options are in Table 4-14.

PROPERTY = SATURATED The calculation basis of pure water properties. Options are inTable 4-15.

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Example:

WATER DECANT=ON, GPSA, SOLU=KERO, PROP=STEAM

Table 4-14: Water Solubility Calculation Options

SIMSCI Calculations are based on the solubility of water in a number of commoncomponents, including hydrocarbons and non-hydrocarbon gases. See Ap-pendix B, SIMSCI Thermodynamic Data Input Manual, Vol. I, for details.

KEROSENE Calculations are based on the solubility of water in kerosene, as presented inthe API Technical Data Book, Figure 9A1.4.

EOS Solubility is calculated from equation of state water K-values using water-hydrocarbon interaction parameters.

Table 4-15: Water Property Calculation Options

SATURATED Properties are based on vapor/liquid curves. Adequate for most simulations.

STEAM Properties are calculated using the Keenan and Keyes equation of state forwater. Use this method when water is present as a superheated vapor.

BWRS THERMODYNAMIC Data Category of InputLKP

Optional statements. Define the interaction parameters for the BWRS and LKP equation ofstate.

Mandatory entries:

i, j, kij /... Enter component pair numbers followed by the numerical valueof the binary interaction coefficient for the pair. Multiple entriesare separated by the “/” character.

Example:

BWRS 2,3,0.055/3,4,0.008

PR THERMODYNAMIC Data Category of InputSRK

Optional statements. Define the interaction parameters for the Peng-Robinson and Soave-Redlich-Kwong equation of state.

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Mandatory entries:

i, j, kija, kijb, kijc / ... Enter component pair numbers followed by the numerical valueof the binary interaction coefficients for the pair. Multiple en-tries are separated by the “/” character.

Example:

PR 2,3,0.001, 0.054, 3.8/3,4,0.0089, 0.0006, 0.5601

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Stream Data Category of InputThe Stream Data Section defines the process streams for HEXTRAN. Itsets the stream identification, component flowrate, and thermal condition ofeach external stream that feeds into the flowsheet. Optionally, the user maysupply initial estimates for recycle streams or assign a name to any streamin the flowsheet.

For streams with defined compositions and/or assay data, thethermodynamic and transport data are computed with the methods fromPRO/II v4.15. For petroleum liquids and vapors, the properties arecomputed from bulk stream properties (UOPK and gravity). For purewater/steam, the steam table properties are used. Note that any of thecomputed properties may be replaced with average property or a tabular setof properties defined in an External Property Data category of input. Atleast one PROPERTY statement must be included in every simulation.

Hextran utilizes two methods of generating physical property data ofcompositional streams during calculations, referred to as database andpoint access methods. The database method has been available inHEXTRAN for many years, and is further described in the InternalProperty Data section, page 4-64. The point access method, available inVersion 9.0 and subsequent releases, can provide enhanced accuracy insome situations and makes the problem input easier to configure and use.These methods can be mixed within a given simulation problem, permittingthe user to use point access for increased accuracy on some streams anddata base methods on others for improved solution speed.

The database method relies on the user to estimate prior to the simulationthe temperature and pressure range that a stream will use. A grid ofproperties covering this temperature and pressure range is generated beforesimulation calculations begin. Properties are generated during simulationby using table lookup and interpolation methods. The advantage of thismethod is that it reduces computational effort associated with propertygeneration and speeds overall execution of the program, in some casessignificantly. The disadvantage is that it does require the user to estimateand specify the operating range of the stream prior to simulation. Ifproperties are required during simulation that are outside the range of theT/P grid, the values are not extrapolated.

The point access method relies on a more rigorous approach to propertygeneration and calculates required physical properties based on streamconditions and composition during simulation whenever required, similar tothe operation of PRO/II and other flowsheet simulators. No estimate of theoperation range of the stream is required. An additional advantage of thismethod is that estimates of stream compositions for mixed and flashed

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streams do not need to be specified at input time since the composition ofthese streams is determined during the calculations.

Problem Type Recommended Method

Single Exchanger - Single Phase Either

Single Exchanger - Two Phase Point Access

Exchanger Network w/o Mixers or Flashes Data Base

Flashes or Mixers Point Access

Plate-Frame Exchangers Data Base

Table 4-16: Stream Data Category of InputStatement Keywords See…

S T R E A M S D E F I N E D W I T H P U R E C O M P O N E N T S

PROPERTY STREAM=, {NAME=}, COMPOSITION()=, {RATE( )=,NORMALIZE, SET=, SETNO=, TOUT=, POUT= ,FLUSH, pname(AVG)}

(Temperature and pressure fixed)

TEMP=, PRES=, {PHASE=M},or(Phase fixed)TEMP=or PRES=, PHASE= or LFRAC()=,

Page 4-41

S T R E A M S W I T H A S S A Y D A T A

PROPERTY STREAM=, RATE(WT)=, ASSAY= LV, {BLEND= orXBLEND=, NAME= , SET=, SETNO=, TOUT=, POUT=,pname(AVG)=, FLUSH, NOBLEND}

(Temperature and pressure fixed)

TEMP=, PRES=, {PHASE= M},or(Phase fixed)TEMP= or PRES=, PHASE= or LFRAC()=

Page 4-44

D86 DATA= {TEMP=, STREAM=, PRES(MMHG)=760.0,CRACKING}

Page 4-46

orTBP or D1160

DATA= {TEMP=, STREAM=, PRES(MMHG)=760.0}, Page 4-47

orD2887

DATA= {TEMP=, STREAM=} Page 4-48

API or SPGR orWATSONK

AVERAGE=, {STREAM=}, {DATA=} Page 4-50

{MW} DATA= {AVERAGE=, STREAM=} Page 4-51

{LIGHTENDS } COMPOSITION(M)= {RATE(M)= or FRACTION()= orPERCENT()= or MATCH or NOMATCH, STREAM=,NORMALIZE}

Page 4-52

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Table 4-16: Stream Data Category of InputStatement Keywords See…

S T R E A M S C R E A T E D B Y M I X I N G O R F L A S H I N GC O M P O S I T I O N A L A N D / O R A S S A Y S T R E A M S

PROPERTY STREAM=, {TEMP=}, PRES=, {PHASE=}, SET=,SETNO=, TOUT=, {POUT=, pname(SETNO)=, NAME=},REFSTREAM, {REFPHASE}, {SET=}

Page 4-53

P E T R O L E U M L I Q U I D S A N D V A P O R S

PROPERTY STREAM=,TEMP=,PRES=,VAPOR=, LIQUID(W or V)=,NONCONDENSIBLE=, WATER= or STEAM=, SPGR= orAPI=, UOPK=, {pname(AVG)=} ,{TOUT, POUT, NAME=}

Page 4-56

W A T E R A N D S T E A M

PROPERTY STREAM=, TEMP=, PRES=, WATER= or STEAM=,{TOUT=, POUT=, NAME=}

Page 4-58

U T I L I T Y S T R E A M S F O R P I N C H C A L C U L A T I O N S

UTILITY STREAM=,TEMP=,TOUT=,{COST= ,FILM= ,BSIZE=1000, BCOST= ,LINEAR =50, CONSTANT=,EXPONENT=.60, UNIT or SHELL, NAME=, DUTY= }

Page 4-60

N E T W O R K S Y N T H E S I S

PROPERTY {TADDITIONAL=,TSPLIT=, CSCALER= , NOSPLIT,NOUTILITY, SINGLE, DHRAT=, DEMAT= }

Page 4-62

STREAM STREAM Data Category of Input

Mandatory statement. Introduces the category. The mandatory and optional statements in theSTREAM Data category of Input depend on the type of stream(s) being defined. At least onePROPERTY statement must be included.

Mandatory entries: None.

Optional entries: None.

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STREAMS DEFINED WITH PURE COMPONENTS

PROPERTY STREAM Data Category of Input

Conditional statement. The PROPERTY statement is required for all compositionally-definedstreams. It assigns an identification label, defines the initial thermal conditions, and specifiesthe rate and initial composition of the overall fluid (vapor and liquid) phases of the stream.

Mandatory entries for all pure component streams:

STREAM= Supplies the identification label required by each stream in theproblem. The label must be unique among all streams in theproblem. The label may contain up to 12 alphanumeric char-acterss Embedded blanks and delimiters are not allowed.

COMPOSITION The COMPOSITION entry is required for compositional streams.Components not identified here are not included in the streamfluid fraction. COMPOSITION may be given on a mole(M-default), weight (WT), liquid volume (LV), or gas volume(GV) basis and need not match the RATE basis.

Optional entries for all pure component streams:

NAME= Gives a descriptive name optionally assigned to the stream. Itmay contain up to 12 alphanumeric characters including embed-ded blanks. It serves only as an aid to the user in identifying thestream in the results printout, and does not have to be unique.

RATE(M)= The RATE entry sets the initial overall rate of the stream fluidfraction. It is allowed as an option only when the COMPOSITIONentry is present. If RATE is missing, values entered on the COM-POSITION entry represent actual component flow rates. RATEmay be supplied on a mole (M - default), weight (WT), liquidvolume (LV), or gas volume (GV) basis.

NORMALIZE Instructs the program to normalize the component flowrate tothe specified RATE. This option is ignored unless both the COM-POSITION and RATE entries appear on the PROPERTY state-ment. By default, NORMALIZE is inactive.

SET= Assigns a thermodynamic method set to the individual stream. Ifthis entry is missing, the program will use the default thermody-namic method set.

SETNO= A unique integer used to distinguish generated properties fromother property sets used in the problem. SETNO may also beused to refer to properties generated by a PGEN operation as de-scribed in the Internal Property Data section. Point access willbe used if SETNO is not specified. Valid range for SETNO is1..97.

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TOUT= Temperature bound for a generated grid of properties. By de-fault, the grid of properties is generated at ten (10) equallyspaced temperatures between TEMP and TOUT at pressures ofPRES and POUT. If POUT is not given, the table will be at PRESonly.

POUT= Pressure bound for generated property grid. If POUT is notgiven, the table will be at PRES only.

FLUSH This keyword is used to delete a stream and its associated prop-erty data from HEXTRAN’s inlet stream data storage once thedata is no longer needed. Use this feature to delete the streamsreferenced with REFSTREAM, where the feed streams that areMIXed or FLASHed will not be used anywhere else in the flow-sheet. Once HEXTRAN finishes generating property data for theMIXed or FLASHed stream, the inlet streams and their propertiescan be deleted with FLUSH. FLUSHing increases the availablestorage for stream property data points and can speed programexecution.

Note: This keyword is only useful in conjunction with generatedproperty grids, i.e., with the SETNO keyword. When point accessthermodynamics are being used (the default) this keyword doesnot improve performance.

pname(AVG)= Used to specify an average value for a property. Choose a prop-erty name from Table 4-17, page 4-59.

pname(SETNO)= Used to replace generated properties with tabular data sets asexplained in the Stream Data category of input. Choose a prop-erty name from Table 4-17, page 4-5.

Mandatory entries for temperature and pressure-fixed compositional streams:

TEMP= Stream temperature.

PRES= Stream pressure.

Optional entries for temperature and pressure-fixed compositional streams:

PHASE= This declares the initial phase condition of the stream. Phasemay be declared as mixed (M), vapor only (V), or liquid only (L).When only one of TEMP or PRES is given, PHASE=L sets thestream at its bubble point and PHASE=V sets the stream at itsdew point. If TEMP and PRES are both given, the program cal-culates the resulting phase and overrides the user providedPHASE.

Mandatory entries for phase-fixed compositional streams:

TEMP= orPRES=

Stream temperature.Stream pressure.

PHASE= or

LFRAC(M)=

See above.

The initial liquid fraction of the stream. Normally, it serves as analternative for the PHASE entry. May be given on a mole (M -default), weight (WT), or liquid volume (LV) basis.

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The COMPOSITION and (optional) RATE entries define the composition and rate of the fluidphase components (vapor and liquid). When the RATE entry is missing, the total fluid rate iscalculated as the sum of the values supplied on the COMPOSITION entry.

Examples:

PROPERTY STREAM=LIQ7, PHASE=L, PRES=200,*RATE=3000, COMP=2,50/4,50

PROPERTY STREAM =HXFD, TEMP=300,PRES=50,*COMP=70/200/50/150/7/0.2, TOUT=400, SETNO=1, FLUSH

PROPERTY STREAM =R1, TEMP=100, PRES=40,*RATE(V)=1500, COMP(W)=1,10/70/3,147,*NORMALIZE, TOUT=200, POUT=35, SETNO=2

PROPERTY STREAM =MXAL, REFSTREAM=LIQ7, HXFD, R1, *REFPHASE=L, TEMP=225, PRES=40, *TOUT=300, SETNO=4

In the first example, components 2 and 4 each comprises 50 percent of the total rate, 3000;components 1 and 3 comprise 0.0 percent. This stream uses point access, because it does notinclude a SETN entry.

In the second example, component 1 is 70 moles, component 2 is 200, etc. After the stream ismixed in the fourth example, it is FLUSHed from HEXTRAN’s data storage area.

In the third example, the stream component weight flows given are normalized by the programto give a total stream flow of 1500 standard liquid volume units.

The fourth example creates a new stream with properties derived from the liquid phase of amixture of streams LIQ7, HXFD, and R1.

Note: For the third example, 10 equally spaced sets of properties will be generated at pres-sures of 40 and 35 between the temperatures 100 and 200 degrees. The properties will be as-signed a set number of 2.

Examples using multiple thermodynamic methods:

THERMODYNAMIC DATAMETHOD SYST=SRK,TRANS=PURE, SET=SET1METHOD SYST=GS, TRANS=PETRO, SET=SET2...PROP STREA=1, PRES=35, TEMP=100,*

COMP=1,50/2,50, RATE=1000,*SET=SET2, SETNO=1

PROP STREA=2, PRES=35, TEMP=100,*COMP=1,50/2,50, RATE=1000,*SETNO=2 (no SET entry specified)

PROP STREA=3, PRES=35, TEMP=100,*COMP=1,50/2,50, RATE=1000,*SET=SET1 (no SETNO entry specified)

In the first example, the second thermodynamic method is selected.

In the second example, there is no SET entry. Therefore, the first (default) thermodynamicmethod will be used.

In the third example, the first thermodynamic method is selected. No SETNO entry is speci-fied, so HEXTRAN will use point access for property generation.

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PROPERTY STREAM Data Category of Input

Conditional statement. Mandatory for assay streams. The PROPERTY statement assigns anidentification label, defines the initial thermal conditions, and specifies the rate and initial com-position of the overall fluid (vapor and liquid) phases of the stream.

Mandatory entries for all assay streams:

STREAM= Supplies the identification label required by each stream in theproblem. The label must be unique among all streams in theproblem. The label may contain up to 12 alphanumeric charac-ters, excluding embedded blanks and delimiters.

RATE(WT)= Sets the initial overall rate of the stream fluid fraction. It is re-quired for assay streams. RATE may be supplied on a weight(WT) or liquid volume (LV) basis.

Optional entries for all assay streams:

ASSAY=LV Declares the basis used by the supplied assay data. Either liquidvolume (LV) or weight (WT) basis is allowed. LV is the defaultbasis if the ASSAY option is omitted, except if D2887 data areprovided, in which case WT is the default (and only) option.

BLEND= Creates a blend of components from this assay stream. When theBLEND keyword is not given, the default blend as indicated on aCUTPOINTS statement is used. If there is no default cutpointsblend, a ‘‘noname’’ blend will be used. The blend name can have amaximum of 12 characters, with no embedded blanks.

XBLEND=name Excludes the pseudocomponents that could have been createdwith this assay from the components created in blend ‘‘name’’.The stream designated on this PROPERTY statement will be syn-thesized from pseudocomponents present in blend ‘‘name’’. Ifthere are no components created for blend ‘‘name’’, an errormessage will be issued. When ‘‘name’’ is not given on theXBLEND keyword, the default blend as indicated on a CUT-POINTS statement will be used. If there is no default blend, the‘‘noname’’ blend will be used. If there is no ‘‘noname’’ blend, anerror message will be issued.

NAME= Gives a descriptive name optionally assigned to the stream. Itmay contain up to 12 alphanumeric characters including embed-ded blanks, but excluding delimiters. It serves only as an aid tothe user in identifying the stream in the results printout, anddoes not have to be unique. If this entry is used, a name shouldnot be assigned to this stream on the NAME statement.

SET= Assigns a thermodynamic method set to the individual stream.

SETNO= A unique integer used to distinguish generated properties fromother property sets used in the problem. SETNO may also be

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used to refer to properties generated by a PGEN operation asdescribed in the Internal Property Data category of input. Pointaccess will be used if SETNO is not specified.

TOUT= Temperature bound for a generated grid of properties The grid ofproperties is generated at ten (10) equally spaced temperaturesbetween TEMP and TOUT at pressures of PRES and POUT. IfPOUT is not given, the table will be at PRES only.

POUT= Second pressure for generated property table. If POUT is notgiven, the table will be at PRES only.

pname(AVG)= Used to specify an average value for a property. Choose a prop-erty name from Table 4-17.

pname(SETNO)= Used to replace generated properties with tabular data sets asexplained in the Stream Data category of input. Choose a prop-erty name from Table 4-17.

FLUSH This keyword is used to delete a stream and its associated prop-erty data from HEXTRAN’s inlet stream data storage once thedata is no longer needed. Use this feature to delete the streamsreferenced with REFSTREAM, where the feed streams that areMIXed or FLASHed will not be used anywhere else in the flow-sheet. Once HEXTRAN finishes generating property data for theMIXed or FLASHed stream, the inlet streams and their propertiescan be deleted with FLUSH. FLUSHing increases the availablestorage for stream property data points and can speed programexecution.

Note: This keyword is only useful in conjunction with generatedproperty grids, i.e., with the SETNO keyword. When point accessthermodynamics are being used (the default) this keyword doesnot improve performance.

NOBLEND This keyword is used to exclude a stream with assay data fromthe assay blend which is used by HEXTRAN to characterize pe-troleum components. For a stream defined with the NOBLENDoption, there must exist a stream (or streams) that define petro-leum components that cover the same TBP range.

Note: Rate bases of M or G are not allowed. If no rate basis isspecified, weight (W) is assumed.

Mandatory entries for temperature and pressure-fixed assay streams:

TEMP= Stream temperature.

PRES= Stream pressure.

Optional entry for temperature and pressure-fixed assay streams:

PHASE= Declares the initial phase condition of the stream. Phase may bedeclared as mixed (M), vapor only (V), or liquid only (L). Whenonly one of TEMP or PRES is given, PHASE=L sets the stream atits bubble point and PHASE=V sets the stream at its dew point.If TEMP and PRES are both given, the program calculates the re-sulting phase and overrides the user provided PHASE.

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Mandatory entries for phase-fixed assay streams:

TEMP= orPRES=

Stream temperature.Stream pressure.

PHASE= orLFRAC=

See above.Fixes the initial liquid fraction of the stream. Normally, it servesas an alternative for the PHASE entry. It may be given on aweight (WT) or liquid volume (LV) basis.

Distillation Data

D86 STREAM Data Category of Input

Conditional statement. This statement supplies ASTM D86 distillation data, normally taken atatmospheric pressure (760 mm Hg). Use the PRES entry to correct for data measured at an-other pressure. Use the CRACKING entry (below) to correct for thermal cracking. Either theD86, TBP, D1160 or D2887 distillation data statement is required for streams with assay data.The chosen distillation data statement must appear immediately after the correspondingPROPERTY statement and prior to the next PROPERTY statement or THERMO statement.

Mandatory entry:

DATA= Supplies the actual distillation data points. Each data point con-sists of two pieces of information: (1) the cutpoint, expressed asa percentage of the cumulative distillates (pct) and (2) the tem-perature of the cut (value). Data must appear with the cut per-centages in ascending order, consistent with the basis declaredon the ASSAY entry of the PROPERTY statement. The statementformat is DATA= pct,value / pct,value... Any data supplied on theLIGHTENDS statement override the corresponding portion of thedistillation data.

Optional entries:

TEMP= Identifies the dimensional unit used to supply temperature data. Ifomitted, the temperature unit declared on the DIMENSION state-ment in the General Data Category serves as the default. Availablearguments include C (Celsius), K (Kelvin), F (Fahrenheit), or R(Rankine).

STREAM= This supplies a stream label. It is optional, but when used, itmust agree with the stream label declared on the PROPERTYstatement, or an input error occurs.

PRES(MMHG)=760.0 The PRES entry allows specifying the pressure at which the dis-tillation data were measured, or to which the data are corrected.The default pressure is 760 mm Hg. The default dimensionalunit is the problem pressure unit.

CRACKING Corrects D86 data for the effects of thermal cracking. It is avail-able only on the D86 statement.

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Note: The D86 correlation was removed from the API Data Bookin 1987, but remains available as an option to provide consis-tency for older data.

TBP STREAM Data Category of Input

Conditional statement. This statement supplies true boiling point distillation data. Either theD86, TBP, D1160 or D2887 distillation data statement is required for streams with assay data.The chosen distillation data statement must appear immediately after the correspondingPROPERTY statement and prior to the next PROPERTY statement or THERMO statement.

Mandatory entry:

DATA= Supplies the actual distillation data points. Each data point con-sists of two pieces of information: (1) the cutpoint, expressed asa percentage of the cumulative distillates(pct) and (2) the tem-perature of the cut (value). Data must appear with the cut per-centages in ascending order, consistent with the basis declaredon the ASSAY entry of the PROPERTY statement. The statementformat is “DATA= pct,value / pct,value...”. Any data supplied onthe LIGHTENDS statement override the corresponding portion ofthe distillation data.

Optional entries:

TEMP= Identifies the dimensional unit used to supply temperature data.If omitted, the temperature unit declared on the DIMENSIONstatement in the General Data category serves as the default.Available arguments include C (Celsius), K (Kelvin), F (Fahren-heit), or R (Rankine).

STREAM= Supplies a stream label. It is optional, but when used, it mustagree with the stream label declared on the PROPERTY state-ment, or an input error occurs.

PRES(MMHG)=760.0, Specifies the pressure at which the distillation data were meas-ured, or to which the data are corrected. The default pressure is760 mm Hg. The default dimensional unit is the problem pres-sure unit.

D1160 STREAM Data Category of Input

Conditional statement. This statement supplies ASTM D1160 distillation data, normally meas-ured in partial vacuum conditions. By default, data is corrected to 1 atmosphere (760 torr).Use the PRES entry to correct data to another pressure. Either the D86, TBP, D1160 or D2887distillation data statement is required for streams with assay data. The chosen distillation datastatement must appear immediately after the corresponding PROPERTY statement and prior tothe next PROPERTY statement or THERMO statement.

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Mandatory entry:

DATA= Supplies the actual distillation data points. Each data point con-sists of two pieces of information: (1) the cutpoint, expressed asa percentage of the cumulative distillates(pct) and (2) the tem-perature of the cut (value). Data must appear with the cut per-centages in ascending order, consistent with the basis declaredon the ASSAY entry of the PROPERTY statement. The statementformat is “DATA= pct,value / pct,value...”. Any data supplied onthe LIGHTENDS statement override the corresponding portion ofthe distillation data.

Optional entries:

TEMP= Identifies the dimensional unit used to supply temperature data.If omitted, the temperature unit declared on the DIMENSIONstatement in the General Data Category serves as the default.Available arguments include C (Celsius), K (Kelvin), F (Fahren-heit), or R (Rankine).

STREAM= This supplies a stream label. It is optional, but when used, itmust agree with the stream label declared on the PROPERTYstatement, or an input error occurs.

PRES(MMHG)=760.0, The PRES entry allows specifying the pressure at which the dis-tillation data were measured, or to which the data are corrected.The default pressure is 760 mm Hg. The default dimensionalunit is the problem pressure unit.

D2887 STREAM Data Category of Input

Conditional statement. Allows entry of data that describes a distillation curve simulated in ac-cordance with the ASTM D2887 procedure. Note: No pressure entry appears on this state-ment. Either the D86, TBP, D1160 or D2887 distillation data statement is required for streamswith assay data. The chosen distillation data statement must appear immediately after the cor-responding PROPERTY statement and prior to the next PROPERTY statement or THERMOstatement.

Mandatory entry:

DATA= Supplies the actual distillation data points. Each data point con-sists of two pieces of information: (1) the cutpoint, expressed asa percentage of the cumulative distillates (pct) and (2) the tem-perature of the cut (value). Data must appear with the cut per-centages in ascending order, consistent with the basis declaredon the ASSAY entry of the PROPERTY statement. The statementformat is “DATA= pct,value / pct,value...”. Any data supplied onthe LIGHTENDS statement override the corresponding portion ofthe distillation data.

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Optional entries:

TEMP= Identifies the dimensional unit used to supply temperature data.If omitted, the temperature unit declared on the DIMENSIONstatement in the General Data Category serves as the default.Available arguments include C (Celsius), K (Kelvin), F (Fahren-heit), or R (Rankine).

STREAM= This supplies a stream label. It is optional, but when used, itmust agree with the stream label declared on the PROPERTYstatement, or an input error occurs.

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Gravity Data

For streams with assay data, one of the three gravity statements must follow the distillationdata statement after the PROPERTY statement. These statements offer alternative forms fordefining the liquid density of the assay at 60 F (15.5 C). The AVERAGE entry is required; allother entries are optional. When the DATA entry is not supplied, PRO/II generates a gravitycurve based on the distillation data and the average gravity value.

API STREAM Data Category of Input

Conditional statement. Indicates that gravity data is to be supplied in the form of API gravity.

Mandatory entry:

AVERAGE= This entry defines the average gravity value for the stream, in-cluding any lightends.

Optional entries:

STREAM= Stream label. It is optional, but when used, it must agree withthe stream label declared on the PROPERTY statement, or an in-put error occurs.

DATA= This option allows entry of user-supplied data points that replacethe program generated gravity curve. If used, at least 3 data pointsmust be provided, consistent with the basis declared on the ASSAYentry of the PROPERTY statement. The statement format is DATA=pct, value / pct, value / pct, value / ... where pct is the mid-volumepercent or mid-weight percent of the data point and value is the APIgravity of the point associated with the ‘‘pct’’ argument.

SPGR STREAM Data Category of Input

Conditional statement. Indicates that gravity data is to be supplied in the form of specific gravity.

Mandatory entry:

AVERAGE= This entry defines the average gravity value for the stream, in-cluding any lightends.

Optional entries:

STREAM= Stream label. It is optional, but when used, must agree with thestream label declared on the PROPERTY statement, or an inputerror occurs.

DATA= This option allows entry of user-supplied data points that replacethe program generated gravity curve. If used, at least 3 datapoints must be provided, consistent with the basis declared onthe ASSAY entry of the PROPERTY statement. The statement for-mat is DATA= pct, value / pct, value / pct, value / ... where pct isthe mid-volume percent or mid-weight percent of the data point

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and value is the specific gravity of the point associated with the‘‘pct’’ argument.and value is the specific gravity of the point associated with the‘‘pct’’ argument.

WATSONK STREAM Data Category of Input

Conditional statement. Indicates that gravity data is to be supplied in the form of Watson (orUOP) characterization factor data.

Mandatory entry:

AVERAGE= This entry defines the average value for the stream, includingany lightends.

Optional entries:

STREAM= Stream label. It is optional, but when used, must agree with thestream label declared on the PROPERTY statement, or an inputerror occurs.

DATA= This option allows entry of user-supplied data points that re-place the program generated gravity curve. If used, at least 3data points must be provided, consistent with the basis declaredon the ASSAY entry of the PROPERTY statement. The statementformat is DATA= pct, value / pct, value / pct, value / ... where pctis the mid-volume percent or mid-weight percent of the datapoint and value is the Watson characterization value of the pointassociated with the ‘‘pct’’ argument.

MW STREAM Data Category of Input

Optional statement. Defines the molecular weight curve for the assay stream.

If the MW statement is not given, the program estimates the molecular weights for all assaycuts, using the method chosen by the MW entry on the ASSAY statement, in the ComponentData category of input.

Mandatory entry:

DATA= The data entry must define at least 3 points that appear in the or-der of ascending weight percentages. An unlimited number ofpoints may be supplied. The statement format is DATA= pct, value/ pct, value / pct, value / ... where pct is the mid-volume percentor mid-weight percent of the data point and value is the molecularweight of the point associated with the ‘‘pct’’ argument.

Optional entries:

AVERAGE= Defines the average molecular weight of the stream. If AVERAGEis given, the program normalizes or extrapolates the molecularweight curve, as required to satisfy the average molecularweight of the stream. If omitted, the program uses quadratic ex-trapolation of the molecular weight curve, as needed, to com-pute an average molecular weight.

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STREAM= Stream label. It is optional, but when used, it must agree withthe stream label declared on the PROPERTY statement, or an in-put error occurs.

LIGHTENDS STREAM Data Category of Input

Optional statement. Defines the light hydrocarbon components in the assay analysis. All com-ponents appearing on this statement must be defined in the Component Data category. TheCOMPOSITION entry is required, but all other entries are optional.

Mandatory entry:

COMPOSITION= Identifies the components that constitute the lightends of thestream. The flow of each component in the lightends may besupplied as an actual flowrate or as a fraction or percentage ofthe total stream fluid rate. The basis may be mole (M), weight(WT), liquid volume (LV), or gas volume (GV) and may be differ-ent from the basis used on the RATE, FRACTION, or PERCENTentry.

The statement format is “COMPOSITION i, value / ...”

If ‘‘i’’ is omitted, it defaults to the next component number in se-quence. If none of the ‘‘i’’ arguments are given, then the first‘‘value’’ is associated with component 1. If RATE, PERCENT, orFRACTION is given: ‘‘value’’ is the composition for each compo-nent ‘‘i’’. The sum of the values must equal 1.0 ± 0.01, 100 ± 1or the desired rate ± 1%. Alternatively, the NORMALIZE keywordmay be used to adjust the values to the desired rate.

If MATCH is given:The values are adjusted by a constant factor so that the light-ends flowrate matches the low-boiling portion of the TBP curve.

If NOMATCH is given:The values are the actual flowing amounts.

Optional entries:

RATE= Defines the total lightends rate on a mole (M), weight (WT), liq-uid volume (LV), or gas volume (GV) basis. The basis may bedifferent from the COMPOSITION basis.

FRACTION or PERCENT Defines the total lightends rate as a fraction or percent of the to-tal stream fluid rate. The basis may be either weight (WT) or liq-uid volume (LV). The basis may be different from theCOMPOSITION basis. The default basis is set by the ASSAY en-try on the PROPERTY statement.

MATCH or NOMATCH The MATCH option adjusts the lightends flow rate to match theTBP curve. The adjustment ensures the mid-volume percentageof the highest boiling lightend component (that is available insignificant quantity) and intercepts the TBP temperature curve atthe specified volume percent. This is the default. The NOMATCHoption does not adjust the lightends flowrate to match the TBPcurve.

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STREAM Stream label. It is optional, but when used, it must agree withthe stream label declared on the PROPERTY statement, or an in-put error occurs.

NORMALIZE When RATE, FRACTION, or PERCENT is present, the NORMAL-IZE option normalizes the total rate of the lightends to obtain therequired rate, regardless of the sum of the values supplied forthe COMPOSITION entry.

Example:

PROPERTY STREAM=1,TEMP=150,PRES=50,*RATE(V)=1200,PHASE=L,ASSAY=LVD86 STREAM=1,DATA=0,100/10,210/30,240/50,*

260/70,275/90,290/100,310API AVG=60,STREAM=1LIGHTENDS STREAM=1,RATE=50,*COMPOSITION=1,2/2,10/3,28/4,7/5,3

PROPERTY STREAM =2,TEMP=100,PRES=50,*RATE(V)=1500,PHASE=L,ASSAY=LVD1160 STREAM=2,DATA=0,310/10,360/30,385/50,*

410/70,560UOPK AVG=12.5,STREAM=2

PROPERTY STREAM =V6,TEMP=200,PRES=75,*RATE(W)=2700,PHASE=M,ASSAY=WTTBP STREAM=V6,DATA=0,201/30,370/50,390/90,450SPGR STREAM=V6,AVG=.76,DATA=25,.31/37,*

.42/52,.65LIGHTENDS STREAM=V6,PERCENT=11,*COMP(W)=1,8/2,12/3,31/4,42/5,7

STREAMS CREATED BY MIXING OR FLASHING COMPOSITIONALAND/OR ASSAY STREAMS

PROPERTY STREAM Data Category of Input

Conditional statement. This statement is used to define a new flowsheet inlet stream createdby mixing or flashing one or more compositional and/or assay streams at specified conditions.

Mandatory entries:

STREAM= Supplies the identification label required by each stream in theproblem. The label must be unique among all streams in theproblem. The label may contain up to 12 alphanumericcharacters.

REFSTREAM= This keyword is used to identify the compositional and/or assaystreams to be MIXed or FLASHed to rigorously calculate theproperties of a new stream. HEXTRAN will perform a rigorous iso-thermal, bubble, or dew point flash to determine the properties ofthe new stream, depending on the keywords provided by the user.

Limitations:

1) Up to twenty (20) compositional and/or assay input streams are allowed.

2) Input streams used with REFSTREAM can not be the product of another REFSTREAM.

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Sample Assay Data

1 2 v6

Assay Basis LV LV WT

Distillation type ASTM D86 ASTM D1160 TBP

IBP 100 310 201

10% 210 360 —-

30% 240 385 370

50% 260 410 390

70% 275 560 —-

90% 290 —- 450

Gravity Type API UOPK SPGR

Stream average 60 12.5 .76

Mid % : 25 —- —- .31

37 —- —- .42

52 —- —- .65

LIGHTENDS

Total flow 50 moles —- 11%

Comp. no. by wt.

1 2 —- 8

2 10 —- 12

3 28 —- 31

4 7 —- 42

5 3 —- 7

Temperature 150 100 200

Pressure 50 50 75

Total rate, basis 1200,V 1500,V 2700,W

Phase Liquid Mixed

PRES= Stream pressure.

Optional entries:

TEMP= Stream temperature.

PHASE= This declares the initial phase condition of the stream. Phase maybe declared as mixed (M), vapor only (V), or liquid only (L).When only one of TEMP or PRES is given, PHASE=L sets thestream at its bubble point and PHASE=V sets the stream at itsdew point. If TEMP and PRES are both given, the program calcu-lates the resulting phase and overrides the user provided PHASE.

SET= Assigns a thermodynamic method set to the individual stream.

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SETNO= A unique integer used to distinguish generated properties fromother property sets used in the problem. SETNO may also beused to refer to properties generated by a PGEN operation as de-scribed in the Internal Property Data category of input. Point ac-cess thermodynamics will be used if SETNO is not specified.

TOUT= Temperature bound for a generated grid of properties The grid ofproperties is generated at ten (10) equally spaced temperaturesbetween TEMP and TOUT at pressures of PRES and POUT. IfPOUT is not given, the table will be at PRES only.

POUT= Second pressure for generated property table. If POUT is notgiven, the table will be at PRES only.

pname(SETNO)= Used to replace generated properties with tabular data sets asexplained in the Stream Data category of input. Choose a prop-erty name from Table 4-17.

NAME= Gives a descriptive name optionally assigned to the stream. Itmay contain up to 12 alphanumeric characters including embed-ded blanks, but excluding delimiters. It serves only as an aid tothe user in identifying the stream in the results printout, anddoes not have to be unique. If this entry is used, a name shouldnot be assigned to this stream on the NAME statement.

REFPHASE= This keyword is used to FLASH one or more compositional andassay streams defined with REFSTREAM. REFPHASE creates anew stream from the specified flash fraction of one or more in-put streams. The stream fraction options are:

V Vapor product from the isothermal or dew pointflash

L Liquid product from the isothermal or bubble pointflash

W Decanted water from the isothermal flash

LMIX Combined liquid and decanted water (if it exists)from the isothermal or bubble point flash

Limitations:

1) When used with PHASE, the only allowable entries for REFPHASE are:PHASE = L, REFPHASE = L, or LMIXPHASE = V, REFPHASE = V

Example:

PROPERTY STREAM=LIQ7, PHASE=L, PRES=200,*RATE=3000,COMP=2,50/4,50

PROPERTY STREAM =HXFD, TEMP=300, PRES=50,*COMP=70/200/50/150/7/0.2

PROPERTY STREAM =R1,TEMP=100,PRES=40,*RATE(V)=1500,COMP(W)=1,10/70/3,147,*NORMALIZE

PROPERTY STREAM =MXAL, REFSTREAM=LIQ7,HXFD, R1, *REFPHASE=L,TEMP=225,PRES=40, *

The fourth PROPERTY statement above creates a new stream, MXAL, with properties derivedfrom the liquid phase of a mixture of streams LIQ7, HXFD, and R1.

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STREAMS WITH PETROLEUM LIQUIDS AND VAPORS

PROPERTY STREAM Data Category of Input

Conditional statement. Defines petroleum streams. The statement is mandatory for petroleumstreams. HEXTRAN has built-in property generation methods specific for petroleum streamswhich correlate the properties with gravity and UOPK (Watson characterization factor). Thegravity may be specific gravity or ºAPI at 60º F.

Mandatory entries:

STREAM= Stream label.

TEMP= Stream temperature.

PRES= Stream pressure.

VAPOR= For vapor streams, the flowrate in weight units.

LIQUID(W)= The flowrate for liquid streams where the qualifier (W) or (V)may be given to designate weight units or liquid volume units. Ifno qualifier is given, W is assumed.

NONCONDENSIBLE= Noncondensible flow in weight flow units. This material is addedto the vapor flow

WATER= or STEAM= Water or stream flow in weight units to add to the liquid orSTEAM vapor flow respectively.

SPGR= or API= The average gravity for the stream

UOPK= Watson characterization factor for the stream defined as:

360

NBPSPGR F( )�

where: NBP= normal boiling pointSPGR= specific gravity

Optional entries:

pname(SETNO)= Used to replace generated properties with tabular data sets asexplained in Stream Data category of input. Choose a propertyname from Table 4-17.

pname(AVG)= Used to specify an average value for a property. Choose a prop-erty name from Table 4-17.

Note that petroleum streams are considered to be single phaseunless a pname entry is used to enter condensate liquid fraction(CFRAC) data. Water or steam may also be flowing with the pe-troleum stream, however, no phase change will be consideredunless a pname entry for water fraction (WFRAC) is entered.When condensate or water fraction data are given, the associ-ated combined stream enthalpy must be given with a pname en-try for proper duty calculations.

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Stream bubble and dew points and liquid/vapor water split aredetermined by interpolation of the condensate and water fractiontables supplied via pname entries. When condensate fractiondata are supplied, average values or tabular sets of UOPK valuesand gravities may be furnished via pname entries for the liquidand vapor portions of the petroleum stream to improve the indi-vidual phase property characterizations.

TOUT= Stream exit temperature for pinch calculations.

POUT= Stream exit pressure for pinch calculations.

NAME= Stream name.

Examples:

PROP STREAM=F1,TEMP=100,PRES=500,*LIQUID=1000,UOPK=12,API=34,*NAME=DIESEL

PROP STREAM=V1,TEMP=200,PRES=50,*VAPOR=5000,UOPK=11.6,API=58.8,*NAME=GASOLINE

PROP STREAM=CR1,TEMP=120,PRES=300,*LIQUID=100000,WATER=1000,UOPK=11.8,*API=34

PROP STREAM=CR2,TEMP=120,PRES=300,*LIQUID=100000,VAPI(SETNO)=1,WATER=1000,*LUOPK(SETNO)=1,LAPI(SETNO)=1,*VUOPK(SETNO)=1,CFRAC(SETNO)=1,*WFRAC(SETNO)=1,ENTH(SETNO)=1

In the first example, a liquid diesel stream is supplied. The properties are computed frombuilt-in correlations for petroleum liquids. Note that no phase change will be predicted, re-gardless of how much heat is added.

The second example is a gasoline vapor in which all properties are generated from petroleumcorrelations. Similar to example 1, no phase change will be predicted, regardless of how muchcooling is supplied.

In the third example, liquid crude oil and liquid water are flowing together. The crude oil prop-erties are computed for a petroleum liquid with the supplied UOPK and API.

In the fourth example, the liquid/vapor split, water fraction and corresponding enthalpies are givenin an External Property Data category of input. External sets corresponding to a temperature/pres-sure grid are also given for the liquid and vapor UOPK’s and API gravities. These sets are used tocompute the other needed properties for the petroleum vapor and liquid. The water/steam proper-ties are computed with the steam tables, based on the water/steam ratio given in the WFRAC dataset.

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WATER AND STEAM

PROPERTY STREAM Data Category of Input

Conditional statement. Defines water and stream streams. The steam tables for water andsteam are used to determine the proper phase and properties for the streams entered usingthis statement. Default steam/water data are used for saturated streams. The full steam tablesmay be requested with the WATER entry on the CALCULATION statement in the General Datacategory of input.

Mandatory entries:

STREAM= Stream label.

PRES= Stream pressure.

WATER= orSTEAM=

The flow in weight units of water or steam. If temperature isgiven, phase is corrected.

Optional entries:

TEMP= Stream temperature. If temperature is not specified, it will be setto the saturation temperature.

TOUT= Outlet temperature. This entry only applies to pinch calculations.

POUT= Outlet pressure. This entry only applies to pinch calculations.

NAME= Optional stream name.

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Table 4-17: Property Keywords

pname Description

ENTHALPY Total stream enthalpy in energy units/weight unit.

DUTY Total stream duty in millions of energy units per time.

LATENT Latent heat.

LCP Liquid specific heat.

VCP Vapor specific heat.

CFRACTION Liquid condensate weight fraction on a water-free basis.

WFRACTION Liquid water weight fraction on a hydrocarbon-free basis.

BUBBLE Bubble point enthalpy.

DEWP Dew point enthalpy.

ADEW Aqueous dew point enthalpy.

LCOND Liquid thermal conductivity

VCOND Vapor thermal conductivity.

LVISC Liquid viscosity.

VVISC Vapor viscosity.

SURFACE Liquid surface tension.

LDENS Liquid density.

VDENS Vapor density.

LAPI or LSPGR Liquid API or specific gravity for petroleum stream.

VAPI or VSPGR Vapor API or specific gravity for petroleum stream.

LUOPK Liquid UOPK values for petroleum stream.

VUOPK Vapor UOPK values for petroleum stream.

FILM Film coefficients for PINCH calculations.

COST Cost of a stream in currency units per million energy units for FLOWSHEETcalculations only. A negative entry indicates a cost savings. Only an averagevalue may be supplied.

Examples:

PROP STREAM=ST1,NAME=STEAM,STEAM=1000,*TEMP=300,PRES=28

PROP STREAM=WT1,NAME=COOL H2O,*WATER=10000,PRES=300

In the first example, 1000 weight units of steam are supplied at a temperature of 300 and a pres-sure of 28. Note that the correct phase will be determined by checking the steam tables. There-fore, care must be exercised to ensure that the temperature and pressure supplied define thedesired phase. As the steam is cooled, condensation will be determined from the steam tables.

The second example supplies 10000 weight units of cooling water at a pressure of 300 and atemperature corresponding to saturation. As the water is heated, the proper phase conditionwill be determined from the steam tables.

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UTILITY STREAMS FOR PINCH CALCULATIONS

UTILITY STREAM Data Category of Input

Conditional statement. Utility streams are restricted to pinch calculations only. They provide ameans to calculate utility usage costs and utility exchanger costs. In general, all entries maybe applied to both TARGETING and SYNTHESIS calculations except the UNIT or SHELL entrywhich is only applicable to SYNTHESIS calculations.

Mandatory entries:

STREAM= Stream label.

TEMP= Inlet temperature.

TOUT= Exit temperature. This is considered the battery limittemperature.

Optional entries:

COST= Cost of the utility stream in currency units per million energy units.

FILM= Film coefficient for the utility. When this entry is given, the costingfor the utility exchanger is on an area basis using the costing pa-rameters supplied on this statement or on the HXCOST statementin the Targeting/Synthesis category of Input. If this entry is notsupplied, costing of utility exchanger surface is on a duty basis.

BSIZE= The base area used in the costing equation.

=1000.0 ft2 (English)=93.0 m2 (metric and SI)

BCOST= The base cost used in the costing equation.

=0.00 USDOLLAR/ft2 (English)=0.00 USDOLLAR/m2 (metric and SI)

LINEAR=50 The linear cost factor in the costing equation.=50.00 USDOLLAR/ft2 (English)=538.20 USDOLLAR/m2 (metric and SI)

CONSTANT= The constant cost factor in the costing equation. This entry canbe used to define fixed costs associated with installation of anexchanger and is not a function of exchanger size.

EXPONENT=0.60 The exponential cost factor in the costing equation.

UNIT or SHELL Defines the basis for exchanger CONSTANT cost factor. The de-fault is UNIT. UNIT results in the constant cost factor being ap-plied once to each unit regardless of the number of shells in theunit. SHELL results in the constant cost factor being applied toeach shell in the unit.

RESTRICTION: This entry has no effect in TARGETING calcula-tions since individual exchangers and shells are not calculated.

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Figure 4-1: Additional Temperature Points

DUTY= The availability of the utility in energy units/time units fortargeting Calculations Only. Note that this value will be exceededas needed to satisfy the system heating/cooling requirements.

NAME= Stream name.

Examples:

UTILITY STREAM=CU1,TEMP=60,TOUT=120,*FILM=100,LINEAR=60,DUTY=28

UTILITY STREAM=HOT,TEMP=1000,TOUT=999,*COST=3.50,DUTY=100,LINEAR=1000.0

UTILITY STREAM=COLD,TEMP=20,TOUT=90,*FILM=120

In the first example a cold utility is supplied with a film coefficient of 100. The exchangers willbe costed, based on a linear cost of 60 currency units per area unit. Up to 28 million units ofenergy per time are available. Note that the supplied duty will be exceeded as necessary toheat balance the problem and the required additional cooling duty will be reported. Utilitycosts will not be calculated since no cost has been specified.

The second example uses a hot utility to represent a furnace. Since no film coefficient is sup-plied, the exchanger cost will be calculated on the basis of $1000 per MMBTU/hr of requiredutility duty. The cost of the utility stream will be based on energy required with the suppliedcost of 3.50 currency units per million energy units. As in Example 1, additional duty will beused as required. Note that TOUT must be less than TEMP for the stream to be treated as ahot utility.

In the third example, the FILM entry requests costing the utility ‘‘COLD’’ on an area basis usingthe costing information supplied on the HXCOST statement see the Synthesis Data category ofinput.

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ENTHALPY

TEMP

H

D G'

G

C

C'

F'

F

B

B'

A

E

w/o TADDITIONAL

Points A, D, E and Hrepresent the inlet andoutlet streamtemperatures. If no ad-ditional temperaturepoints are given, onlyTAE and TDH will bechecked against EMATfor possible violation. Ifpoints B, C, F and G aresupplied as additionaltemperature points,T'BB, T'FF, T'CC and T'GGwill also be checked.

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������ ��������

PROPERTY STREAM Data Category of Input

Optional statement. These keywords can be used on any PROPERTY statement when usingSYNTHESIS calculations.

Mandatory entries: None

Optional entries:

TADDITIONAL= This feature allows HEXTRAN to calculate accurate HRAT andEMATs for streams which change phase. For HRAT/EMAT calcu-lations, HEXTRAN normally assumes a linear heat release be-tween the stream inlet and outlet temperature. For two phasestreams, enter the bubble, and dew point temperatures and upto 8 other temperatures which will help HEXTRAN find the non-linearities on the heat release curve. As shown in Figure 4-1,page 4-61, HEXTRAN uses the additional temperatures as break-points for ensuring the EMAT is not violated in the two phaseexchangers.

TSPLIT= Split stream temperature limitation. This entry limits the tem-perature a stream may be heated or cooled to in the split sec-tion. This is very useful in split flow networks where the splitstream outlet temperatures are very different from each other. Astream can have only one TSPLIT limitation.

CSCALER=1.0 CSCALER is a multiplier for the HXCOST heat exchanger costingequation in the Synthesis category of input section.

NOSPLIT Prevents HEXTRAN from splitting the stream.

NOUTILITY Avoids exchanging the stream with a utility. HEXTRAN will makeevery effort to avoid matching the stream with a utility, but thiscannot be guaranteed.

SINGLE Limits the stream to heat exchange with one other stream.Thiscannot be guaranteed.

DHRAT=0 Adjusts network minimum approach temperature, HRAT, on astream selective basis.

HRATstream = HRATnetwork + DHRATstream

Positive DHRAT values are useful for modeling the additional ap-proach temperature required by streams which exchange heatthrough a heating medium or third party stream. NegativeDHRAT values are useful for specifying a preference betweentwo streams which have a common temperature range. A nega-tive DHRAT makes one of the streams appear hotter and biasesHEXTRAN’s matching of streams.

RESTRICTION: DHRAT + HRAT must be greater than 0.

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DEMAT=0 Adjust the network’s exchanger minimum approach tempera-ture, EMAT, on a stream selective basis.

EMATstream = EMATnetwork + DEMATstream

A negative DEMAT will generally result in fewer exchangers withlarger areas for the designated stream.

RESTRICTION: EMAT + DEMAT must be less than HRAT +DHRAT

��������� ������� �������� ������ ��� ������� ����������It is possible to selectively replace any internally generated stream property with a single value(designated as AVG) or a table of values at designated temperatures and pressures (desig-nated as a SETNO). Property sets are supplied in an External Property Data category of inputas described in the External Property Data section.

The property is identified with the appropriate keyword as shown in Table 4-17. In the discus-sion of stream input in the Streams Defined with Pure Components, and Streams with AssayData sections, these keywords were designated symbolically as the ‘‘pname’’ entry. Multiplepname entries are permissible per stream. The keywords LAPI, LSPGR, LUOPK and VUOPKapply to petroleum streams only. All other keywords in Table 4-17 may be supplied for anystream defined with a PROPERTY statement.

The concept of selective override of properties is best illustrated with several examples:PROP STREAM=1,TEMP=50,TOUT=120,PRES=100,*

SETNO=2,RATE(W)=10000,COMP=3,20/80,*LVIS(SETNO)=3,VVIS(SETNO)=3

PROP STREAM=PET1,TEMP=800,PRES=300,*LIQUID=10500,API=28,UOPK=10.8,*LCOND(AVG)=.3

PROP STREAM=PET2,TEMP=20,PRES=35,*VAPOR=80000,API=55,UOPK=11.5,*CFRAC(SETNO)=2,ENTH(SETNO)=2,VCP=0.6

In the first example, the viscosities generated automatically by property generation are re-placed by values supplied in External Property data sets LVIS=3, VVIS=3.

In the second example, an average value of liquid thermal conductivity is used for all calcula-tions. All other properties are generated with petroleum correlations for liquids.

In the third example, condensate fraction and the corresponding enthalpy are provided in Ex-ternal Property data sets. As defined in CFRAC, the stream may reflect two phase behaviorwith both liquid and vapor properties computed to correspond to an API of 55 and a UOPK of11.5. All values of vapor heat capacity (VCP) are replaced by the single value supplied. Notethat (AVG) is the default.

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Internal Property Data Category of InputThe Internal Property Data category of input supplements the defaultinternal property calculations for streams (PGEN). PGEN data entries arerequired for all streams that use PHASE or LFRAC entries for specifyingstream temperature.

Table 4-18: Internal Property Data Category of Input

Statement Keywords See ...

INTERNALPROPERTY

None Page 4-64

PGEN STREAM=sid, {SETNO=n,} TEMPERATURE=T1, ...,T20, DT,TPOINTS, PRESSURE=P1,..., P10, DP, PPOINTS,PXTRAPOLATE or TXTRAPOLATE, PETROLEUM or NOPE-TRO. {FIXED}

Page 4-64

INTERNALPROPERTY

INTERNAL PROPERTY Data Category of Input

Mandatory statement. Introduces the category.

Optional entries:

None

Example�

INTERNAL PROPERTY

PGEN INTERNAL PROPERTY Data Category of Input

Optional statement. This statement is used to override the default generation of the necessarythermodynamic and transport property data for streams defined with either composition or as-say data in the STREAM DATA category of input. The primary advantage of this option versusthe automatic property generation (using the default TEMPERATURE, TOUT, PRESSURE andPOUT given on the PROCESS statement in the STREAM DATA section) is the user can selectthe temperature/ pressure grid values in a variety of fashions. Note that both PGENstatementss and the automatic property generation will include bubble, dew point, and aque-ous dew point data if they are found to exist in the region of interest.

Optional entries:

SETNO= n The property data set number, any integer from 1-97. This entryis required if it is not supplied on the PROCESS statement in theSTREAM DATA catagory of input.

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Example:INTERNAL PROPERTY

PGEN STREAM=S1, SETNO=2 ...orSTREAM DATA

PROCESS STREAM=S1, SETNO=2 ...

Mandatory entries:

STREAM= sid The stream label for which property tables are to be generated.This is an alphanumeric string up to 12 characters long.

TEMPERATURE = T1,...,T20orTEMPERATURE = T1,DT=TPOINTS=orDT=TPOINTS=

Temperatures for the properties tables where up to 20 entriesare allowed. TPOINTS is the number of temperature points,while DT is the temperature increment between adjacent points.The maximum number allowed for TPOINTS is 20. DT can bepositive or negative, but it must have an absolute value of atleast 0.01. If one entry is given, entries must also be given forDT and TPOINTS and the TEMPERATURE entry will be assumedas the first point and TOUT, supplied on the PROCESS statementin the STREAM DATA category of input will be used as the sec-ond entry for TEMPERATURE. If no TEMPERATURE values areinput, the current temperature for STRM will be assumed to bethe first point and entries for DT and TPOINTS must be given.

Example:

PGEN STREAM=V1, DT=20, TPOINTS=5, SET=5

Five total temperature points beginning with the PROCESS statement TEMPERATURE entry forstream V1 are requested. A 20 degree temperature delta is used to determine the last fourpoints and a SET number of 5 is assigned to the grid of calculated properties. All propertiesare at the pressure(s) supplied on the PROCESS statement for stream V1.PGEN STREAM=10, TEMP=100, DT=0.5,* TPOINTS=20, SET=2

In this example, a twenty temperature point grid of properties is developed at equal tempera-ture intervals of 0.5 degrees. The pressure(s) for the grid of properties is taken from thestream PROCESS statement for stream 10.

PRESSURE = P1,...,P10orPRESSURE = P1,DP=PPOINTS=orDP=PPOINTS=

Pressures for the properties tables where up to 10 entries are al-lowed. PPOINTS is the number of pressure points, while DP isthe pressure increment between adjacent points. The maximumnumber allowed for TPOINTS is 20. DT can be positive or nega-tive, but it must have an absolute value of at least 0.01. If noPRESSURE values are input, the current pressure for STRM willbe assumed to be the first point and POUT, supplied on thePROCESS statement in the STREAM DATA category of input willbe used as the second entry for PRESSURE.

PXTRAPOLATEorTXTRAPOLATE

The method for filling a grid of temperature and pressure pointswhen a property disappears as the temperature increases or de-creases, e.g., liquid properties disappear as the dew point isreached. The default is PXTRAPOLATE which means that themissing grid points will be filled by copying the closest tempera-ture value at the same pressure. Properties which fail to appearfor all temperatures at a given pressure or all pressures at agiven temperature will be eliminated altogether from the particu-lar row or column.

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PETROLEUMorNOPETRO

By default, the PETROLEUM option generates LAPI, VAPI,LUOPK, VUOPK, LSPGR, and VSPGR property values in additionto the standard propterties. These properties will be assignedthe set number SET. The NOPETRO option suppresses genera-tion of the above PETROLEUM properties.

FIXED FIXED is an option for HTRI runs. In this case the T-P grid whichis supplied to HTRI is specified by the user. With this option theuser cannot enter more than 10 temperature and three pressurelevels.

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External Property Data Category of Input

The External Property Data category of input may be used to entertemperature and pressure dependent property sets for streams. Eachexternal property set must be assigned a unique set number in the range1-97, with the further restriction that any given set number only be usedonce for a given type of property data. (Note that it is permissible to use thesame set number for different property data types.)

This data section is optional and may be used as needed to supplementand/or replace stream properties generated automatically from STREAMdata entries as described in the Stream Data category of input, or generatedin the Internal Property Data category of input, page 4-64.

The External Property Data category of input, when present, must followthe Internal Property Data category of input when this section is present, orthe Stream Data category of inputwhen no Internal Property Data categoryof input is present.

HEXTRAN has a limit of 4000 property points, including both internal andexternal property data. The limiting values for each property will not beextrapolated except for enthalpy data sets. For all other properties, thelimiting value will be used and an appropriate warning message given inthe printed results.

An External Property Data category of input may also reference apreviously stored property data file. These data may have been generatedby HEXTRAN and saved as described in the General Data category ofinput, or may have been previously created via the PGEN option inSIMSCI's PROCESS Simulation Program.

Note: All necessary properties for COMPOSITIONAL and ASSAY streamswill be calculated internally by HEXTRAN, unless the PGEN=OLD entry isgiven on the CALCULATION statement (see page 4-19).

Table 4-19: External Property Data Category of Input

Statement Keywords See ...

EXTERNALPROPERTY

None Page 4-68

PNAME SETNO, TEMPERATURE=T1,...,T20, Page 4-68

DATA PRESSURE=P1,VALUES=V1,...V20/,...PRESSURE=P10,VALUES=V1,...V20/...

Page 4-68

FILE (no entries) Page 4-71

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EXTERNALPROPERTY

EXTERNAL PROPERTY Data Category of Input

Optional statement. This statement identifies the External Property Data section.

This category, if specified, must follow the STREAM DATA category, or the optional INTERNALPROPERTY DATA section, if specified.

Optional entries:

None

Example:

EXTERNAL PROPERTY

PNAME EXTERNAL PROPERTY Data Category of Input

Mandatory statement. This statement specifies the external property data type for a propertytable. Possible values for PNAME , and their descriptions, are given in Table 4-20, EXTERNALPROPERTY DATA TYPES. Default dimensional units are given in Table 4-21.

Mandatory entries:

SETNO Specifies the property data set number, any integer from 1-97.This entry is required if it is not supplied on the PROCESS state-ment in the STREAM DATA category of input.

TEMPERATURE= Specifies temperature points for the property table. Enter up to20 temperature points, separated by commas. For the propertytypes BUBBLE, DEWP, and ADEW, a maximum of ten (10) tem-peratures may be entered. There are no defaults.

DATA EXTERNAL PROPERTY Data Category of Input

Mandatory statement. This statement specifies the external property data for a property table.Default dimensional units are given in Table 4-21.

Mandatory entries:

None

Optional entries:

PRESSURE= Specifies pressure for up to ten (10) property points. If omitted,the property points will be assumed independent of pressure.There are no defaults. Pressure entries are required for theseproperties.

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VALUE= Specifies corresponding property values for up to ten (10) pres-sure levels. Only one property value may be given for each pres-sure level. There are no defaults.

Example:

.

.

.STREAM DATA...INTERNAL PROPERTY DATA...EXTERNAL PROPERTY DATABUBBLE SETNO=5,TEMP=105.3,109.8,119.8

DATA PRES=100,VALUES=131.5/*PRES=105,VALUES=137.8/*PRES=110,VALUES=141.4

VVISC SETNO=5,TEMP=80,100,120DATA VALUES=.015,.013,.010

CFRAC SETNO=1,TEMP=10,20,30,40,50DATA PRES=50,VALUES=1.0,1.0,0.9,0.8,0.7/*DATA PRES=70,VALUES=1.0,1.0,1.0,0.85,0.81

ENTH SETNO=1,TEMP=10,20,30,40,50DATA PRES=50,VALUES=101,105,108,111,115/*DATA PRES=70,VALUES=103,107,109,113,119

.

.

.

In this example, a three temperature, three pressure set of bubble point enthalpies are sup-plied as SETNO=5. To use this data set, a compositional or assay stream must have been de-fined in STREAM Data with a SETNO entry of 5.

Vapor viscosity set number 5 is supplied at three temperatures. Since no pressure entries arefurnished, the data are assumed to be independent of pressure.

CFRAC and ENTH data sets are defined as SETNO=1 at five temperatures for each of threepressure levels. The ENTHALPY data are the total stream enthalpy values on a unit basis whichcorrespond to the CFRAC values. Note that the stream bubble point occurs at a temperaturelevel between 20 and 30 degrees at a pressure of 50 units and between 30 and 40 degrees at apressure of 70 units. Unless a supplemental BUBBLE data set is supplied, HEXTRAN will line-arly interpolate the data to define the bubble point.

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Table 4-20: External Property Data Types

PNAME Notes

ENTHALPY Stream enthalpy, needed for all types of calculations.

LATENT Latent heat. This entry is only applicable to Kettle reboilers.

LCP, VCP Liquid and vapor heat capacities. For single phase petroleumstreams, these data are used instead of enthalpy.

CFRACTION Weight fraction liquid condensate on a water-free basis.

WFRACTION Weight fraction of water that is condensed on a hydrocarbon-free basis.

BUBBLE, DEWP, ADEW Stream bubble point, dewpoint, aqueous dewpoint, and en-thalpy values.

LCONDUCTIVITY,VCONDUCTIVITY

Liquid and vapor thermal conductivities.

LVISCOSITY,VVISCOSITY

Liquid and vapor viscosities.

SURFACE Liquid surface tension. This entry is only applicable to Kettlereboilers.

LDENSITY,VDENSITY

Liquid and vapor densities.

Petroleum Streams only

LAPI, VAPI, orLSPGRAVITY,VSPGRAVITY

Liquid and vapor API gravities or specific gravities.

LUOPK, VUOPK Liquid and vapor Watson characterization factors.

Pinch Calculations only

DUTY Stream heating/cooling duty. May be used as an alternate tostream enthalpy.

FILM Stream film coefficient for sizing and costing exchangers.

CSCALER Cost scaler for SYNTHESIS calculations only.

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FILE EXTERNAL PROPERTY Data Category of Input

Optional statement. This statement specifies that a previously prepared external property datafile will be included in this section. This file may have been previously prepared by HEXTRANor PROCESS, or typed in by the user. In any case, the format of the PROPERTY data sets mustcorrespond to the PGEN format described on page 4-68. The SET numbers in the stored fileand other property data sets used in the problem on STRM, PGEN, or PNAME input state-ments must be consistent.

Mandatory entries:

None

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Table 4-21: Default Dimensional Units For External Property Data Dimensions

DIMENSIONS

PROPERTY KEYWORD ENGLISH METRIC SI

+Stream Enthalpy ENTHALPY Btu/lbm kcal/kg kJ/kg

+Stream Duty DUTY MMBtu/time MMkcal/time MMkJ/time

+Stream Latent Heat LATENT Btu/lbm kcal/kg kJ/kg

+Liquid Specific Heat LCP Btu/lbm-F kcal/kg-C kJ/kg-K

+Vapor Specific Heat VCP Btu/lbm-F kcal/kg-C kJ/kg-K

Water Weight Fraction WFRACTION - - -

Condensate Weight Fraction CFRACTION - - -

+Bubble Point Enthalpy BUBBLE Btu/lbm kcal/kg kJ/kg

+Hydrocarbon Dew Point Enthalpy DEWP Btu/lbm kcal/kg kJ/kg

+Aqueous Dew Point Enthalpy ADEW Btu/lbm kcal/kg kJ/kg

*Liquid Thermal Conductivity LCONDUCTIVITY Btu/hr-ft-F kcal/hr-m-C W/m-K

*Vapor Thermal Conductivity VCONDUCTIVITY Btu/hr-ft-F kcal/hr-m-C W/m-K

*Liquid Viscosity LVISCOSITY cP cP Pa-s

*Vapor Viscosity VVISCOSITY cP cP Pa-s

*Liquid Surface Tension SURFACE dyne/cm dyne/cm N/m

Liquid Density LDENSITY lbm/ft3 kg/m3 kg/m3

Vapor Density VDENSITY lbm/ft3 kg/m3 kg/m3

Liquid API Gravity LAPI - - -

Vapor API Gravity VAPI - —

Liquid Specific Gravity LSPGRAVITY

Vapor Specific Gravity VSPGRAVITY

Liquid UOPK LUOPK - - -

Vapor UOPK VUOPK - - -

*Film Heat Transfer Coeff. FILM Btu/hr-ft2-F kcal/hr-m2-C W/m2-K

Constant Stream Cost Factor CSCALER - - -

* Additional allowable units for these properties are given in Table 4-22.+ Changing the dimensional units for ENERGY, WT, and TIME requires that these property data values be adjusted

accordingly.

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Table 4-22: Additional Units For External Data

Property Type Keyword Entry Units

Thermal Conductivity LCONDUCTIVITYVCONDUCTIVITY

=BTUH=KCHCALSWMCWMK

Btu/hr-ft-Fkcal/hr-m-Ccal/s-cm-CW/m-CW/m-K

Film coefficient FILM =BTUHKCHCALSWMCWMK

Btu/hr-ft2-Fkcal/hr-m2-Ccal/s-cm2-CW/m2-CW/m2-K

Surface tension SURFACE =NMDYNE

N/mdyne/cm

Viscosity(dynamic, absolute)

LVISCOSITYVVISCOSITY

=CP=PASLBFSLBFHLBSF

cPPa-slbm/ft-slbm/ft-hrlbf-s/ft2

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Table 4-23: External Property Data Types

Calculation TypeProperty Type Targeting Synthesis Flowsheet

Thermodynamic

ENTHALPY X X X

DUTY X X

LATENT X

LCP X

VCP X

CFRACTION X

WFRACTION X

BUBBLE X

DEWP X

ADEW XTransport

LCONDUCTIVITY X

VCONDUCTIVITY X

LVISCOSITY X

VVISCOSITY X

SURFACE XDensity

LDENSITY X

VDENSITY XPetroleum

LAPI X

VAPI X

LSPGRAVITY X

VSPGRAVITY X

LUOPK X

VUOPK XMiscellaneous

FILM X X

CSCALER X X

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Flowsheet Calculations Category of InputThis data category specifies the type of defined network calculations to beperformed, and the associated general parameters and options.

Table 4-24: Flowsheet Calculation Category of Input

Statement Keywords See ...

Calculation Type SIMULATION or REGRESSION or OPTIMIZATION or CASESTUDY Page 4-76

{TOLERANCE} {TTRIAL=0.01, STRIAL=0.10 UTRIAL=0.04} Page 4-76

{LIMITS} {AREA=200,6000, SERIES=1,10, PARALLEL=1,10, TDAMP=0.00,PDAMP=0.00, TTRIAL=30, STRIAL, UTRIAL=5}

Page 4-77

{CALCULATION} {MINFT=0.80, NOCHECK, DPSMETHOD=STREAM, INCREMENTAL,TWOPHASE=NEW}

Page 4-78

{PRINT} {ALL, UNITS, ECONOMICS, STREAM, STANDARD, EXTENDED,ZONES, MONITOR, INTERMEDIATE}

Page 4-79

{ECONOMICS} {DAYS=350, EXCHANGERATE=1.0, CURRENCY=USDOLLAR} Page 4-80

{UTCOST} {OIL=3.50, GAS=3.50, ELECTRICITY=0.10, WATER=0.03,HPSTEAM=4.10, MPSTEAM=3.90, LPSTEAM=3.60,REFRIGERANT=0.00, HEATINGMEDIUM=0.00}

Page 4-80

{HXCOST} {BSIZE=1000, BCOST=0.00, LINEAR=50.00, EXPONENT=0.60,CONSTANT=0.00, UNIT or SHELL}

Page 4-81

{SPECIFICATION} {PAYOUT=2.0, STRM, TEMPERATURE, UNIT, DUTY, FOUL} Page 4-82

{VARIABLE} {STRM, FRACTION, RATE, TEMPERATURE, UNIT, DUTY} Page 4-119

{CONSTRAINT} STRM, TEMPERATURE, UNIT, DPTMAX, DPSMAX Page 4-82

{CASE} UNIT Page 4-82

{PARAMETER} {AREA=400,4000, FRACTION=0.01,0.50} Page 4-82

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PROPERTY FLOWSHEET CALCULATION Data Category of Input

This entry must be specified. Only one entry is allowed. Each calculation type is described indetail in the following sections.

Mandatory entries:

SIMULATION or Rating of all rigorous exchanger models and design of shell andtube exchangers. See Shell-and-Tube Heat Exchangers later onin this chapter.

REGRESSION or Solution of flowsheets with more specifications than variables.Rating of all rigorous exchanger models. Useful for reconcilingplant data.

OPTIMIZATION AREA or Design of new shell and tube exchangers to meet a specifiedpayout period. Networks can consist of both OLD (Rating) andNEW (Design) exchangers.

OPTIMIZATIONSPLITFLOW or

Solution of flowsheets to minimize utility costs by varying split-ter fractions. Rating of all rigorous exchanger models. Use tomaximize performance of existing networks.

CLEANING CASESTUDY Multiple flowsheet solutions for specified exchanger fouling fac-tors. Use to evaluate effect of cleaning exchangers.

TOLERANCE FLOWSHEET CALCULATION Data Category of Input

Optional statement. This statement modifies the default tolerance values. The default toler-ances are suitable for most calculations.

Optional entries:

TTRIAL=0.01 Temperature tolerance for flowsheet heat balance convergence.Flowsheet solution is reached when all stream temperatureschange by less than this amount from one iteration to the next.The default is 0.01 F (English), or 0.006 C (metric and SI).

STRIAL=0.10 Search trial tolerance for optimization and regression conver-gence. Final solution of an optimization or regression problem isreached when the error sum is less than STRIAL. The default is0.10.

UTRIAL=0.04 U-value trial tolerance for area optimization convergence. Thisentry applies only to area optimization. The default is 0.04.

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LIMITS FLOWSHEET CALCULATION Data Category of Input

Optional statement. This statement defines two groups of information relating to limits on thedesign of shell and tube exchangers and limits on flowsheet calculations. Exchanger design lim-its for AREA, SERIES, and PARALLEL are applied on a global basis unless redefined individuallyfor specified STE exchangers (see Shell-and-Tube Heat Exchangers later on in this chapter).

Optional entries:

AREA=200, 6000 Area per shell for “design”. Area is total outside surface for bareand finned tubes. Enter both a minimum and maximum limit for“designing” new exchangers. Entering only one limit is not al-lowed. The default is 200, 6000 ft2 (English), or 19, 557 m2(metric and SI).

Note: For rating shells with an area greater than 6000 ft 2 , theuser must raise the maximum area on the AREA statement. Thiscan also be done on the rigorous exchanger’s TYPE statementwith AREA =.

SERIES=1,10 Number of shells in series per unit. Enter both a minimum andmaximum limit for “designing” new exchangers. This entry hasno effect on old exchangers. The default is 1,10.

RESTRICTION: The SERIES entry may not be used in conjunc-tion with the PARALLEL entry.

PARALLEL=1,10 Number of shells in parallel per unit. Enter both a minimum andmaximum limit for “designing” new exchangers. This entry hasno effect on old exchangers. The default is 1,10.

RESTRICTION: The PARALLEL entry may not be used in con-junction with the SERIES entry.

TDAMP= Fraction of temperature damping. TDAMPING is useful when aflowsheet has difficulties converging and the sum of squares er-ror seems to oscillate between iterations. By default, HEXTRANuses the stream temperature from the previous iteration as anestimate for the next iteration. TDAMP decreases the incre-mental temperature change between iterations by using aweighted average of the current and previous iterationtemperatures.

For example, if TDAMP=0.4, the temperature estimate becomes:

TEMPest = (TEMPprevious) * 0.4 + (TEMPpresent) * 0.6

There are three TDAMP modes:

1. AUTODAMPING By omitting the TDAMP keyword from theinput file, HEXTRAN will automatically use TDAMPINGwhere necessary. Once autodamping starts, HEXTRANadjusts the TDAMP fraction between 0.0 and 0.5 until theflowsheet converges.

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2. FIXED DAMPING By specifying a TDAMP fraction, auto-damping is disabled, and the TDAMP fraction is used forevery flowsheet iteration. This is useful when a flowsheetneeds a damping fraction greater than 0.5.

3. NO DAMPING To disable temperature damping, specifyTDAMP=0.0.

PDAMP=0.00 Fraction of pressure damping. Operation and use of PDAMP issimilar to TDAMP (described above), except there is no auto-matic pressure damping mode. The default is 0.00.

TTRIAL=30 Maximum number of flowsheet iterations. The default value (30)is sufficient for most applications. This number may be in-creased to a maximum of 99.

Application: Increase the maximum number of iterations if themaximum temperature error shows a slow convergence. In-creasing the maximum number of iterations will not help if themaximum temperature error shows oscillatory behavior.

STRIAL= Maximum number of search trial iterations. This entry applies toarea optimization, split flow optimization and regression calcula-tions only. The default number of iterations is listed for eachavailable calculation type in the formulas below.

= 3 * Number of New Exchangers (AREA OPTIMIZATION)

= 10 * number of variable splitters (SPLITFLOW OPTIMIZATION)

= 5 * number of variables, or 10, whichever is greater(REGRESSION)

UTRIAL=5 Maximum number of U-value loop iterations. This entry appliesto area optimization only. The default is 5.

CALCULATION FLOWSHEET CALCULATION Data Category of Input

Optional statement. This statement sets calculation methods for individual exchanges on aglobal basis. Methods can also be selected globally using the CALCULATION statement in theSIMULATION, CASESTUDIES, OPTIMIZATION AREA, OPTIMIZATION SPLIT, or REGRESSIONsections.

Optional entries:

MINFT The minimum log-mean temperature correction factor, Ft, for de-signing NEWS exchangers. If an intermediate exchanger designviolates the minimum Ft, shells are added in series to improvethe Ft.

NOCHECK Suppresses HEXTRAN’s geometry consistency checks and pre-vents HEXTRAN from assigning default values to missing ge-ometry data. The main purpose for NOCHECK is to allow theuser to access HTRI or HTFS defaults.

When using NOCHECK, specify either:

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■ All exchanger data with HEXTRAN keywords, or.■ ST5/CST2/RKH2 or TASC3

WARNING: Using NOCHECK with inconsistent or missing ge-ometry data may result in abnormal program termination (divi-sion by zero, overflow, etc.)

TWOPHASE=NEW Specifies the methods to be used for thermal and hydraulic calcula-tions for all rigorous exchanger. The NEW method utilizes ModifiedChen vaporization for convective boiling and includes predictionsfor sub-cooled and film boiling. Condensation methods account forflow regime and gravity versus shear effects. Pressure drops arecalculated using a stream analysis based method. The NEW methodautomatically sets DPSMETHOD = STREAM.

The OLD method selects algorithms used in versions 5.0x andearlier. Use this method if you wish to make comparison runswith earlier versions of HEXTRAN. The default is NEW.

PRINT FLOWSHEET CALCULATION Data Category of Input

Optional statement. This statement sets print options on a global basis. The default is to printall reports except the design MONITOR. Entry of any keyword other than ALL turns off allother reports.

Optional entries:

ALL Print all output reports. No other entries are allowed.

UNITS Print unit operation summaries including both rigorous and short-cut units. Exchanger data sheets are not printed with this option.

ECONOMICS Print economic summary of flowsheet including equipment capi-tal costs and utility costs.

STREAM Print stream data summary.

INTERMEDIATE Print intermediate results. This print option applies only toREGRESSION, OPTIMIZATION and CLEANING CASESTUDYcalculations.

STANDARD Print standard exchanger data sheets. This produces a TEMA-style data sheet for shell and tube, rodbaffle and double pipe ex-changers. An API-style data sheet is produced for air coolersand finned tube exchangers.

EXTENDED Print extended exchanger data sheets. This produces a datasheet with additional performance and mechanical data not in-cluded on the standard data sheet.

ZONES Print zones analysis for each two phase exchanger.

MONITOR Print design monitor report for each “NEW” exchanger. Prints allintermediate design data.

CAUTION: Use of this option can produce lengthy reports foreach new exchanger.

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Example:

The following statement would cause only exchanger data and extended data sheets to beprinted.PRINT STANDARD, EXTENDED

ECONOMICS FLOWSHEET CALCULATION Data Category of Input

Optional statement. This statement defines economic factors affecting utility cost calculations.

Optional entries:

DAYS=350 The number of days the plant is on stream per year. The defaultis 350.

CURRENCY=USDOLLAR The currency units. This entry is used for printout purposesonly. The default is USDOLLAR.

CAUTION: Do not use the “$” sign in this entry. HEXTRAN willtreat it as a delimiter.

EXCHANGERATE=1.0 The exchange rate expressed as number of currency units perUS dollar. This entry is used for converting any built-in costingdata defaults. The default is 1.0.

UTCOST FLOWSHEET CALCULATION Data Category of Input

Optional statement. This statement defines the cost of utilities.

Optional entries:

OIL=3.50 The cost of fuel oil in currency units per million energy units.This entry applies only to fired heaters. The default is 3.50USDOLLAR/MM Btu (English), or 9.04 USDOLLAR/MM kcal(metric), or 3.32 USDOLLAR/MM kJ (SI).

GAS=3.50 The cost of fuel gas in currency units per million energy units.This entry applies only to fired heaters. The default is 3.50USDOLLAR/MM Btu (English), 9.04 USDOLLAR/MM kcal (met-ric), or 3.32 USDOLLAR/MM kJ (SI).

ELECTRICITY=0.10 The cost of electricity in currency units per kilowatt-hour. Thisentry applies only to pumps and compressors. The default is0.10 USDOLLAR/kW-hr (English, metric, and SI).

WATER=0.03 The cost of cooling water in currency units per thousand US gal-lons. This entry applies only to water coolers. The default is 0.03USDOLLAR/M gallon (English, metric, and SI)

CAUTION: The volume unit of US gallons is not redefined forMetric and SI units.

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HPSTEAM=4.10 The cost of high pressure steam in currency units per thousandweight units. This entry applies only to pumps and compres-sors. The default is 4.10 USDOLLAR/M lb (English), or 9.04USDOLLAR/M kg (metric and SI).

MPSTEAM=3.90 The cost of medium pressure steam in currency units per thou-sand weight units. This entry applies only to pumps and com-pressors. The default is 3.90 USDOLLAR/M lb (English), or 8.60USDOLLAR/M kg (metric and SI).

LPSTEAM=3.60 The cost of low pressure steam in currency units per thousandweight units. This entry applies only to pumps and compres-sors. The default is 3.60 USDOLLAR/M lb (English), or 7.94USDOLLAR/M kg (metric and SI).

REFRIGERANT=0.00 The cost of refrigerant in currency units per million energy units.This entry applies only to coolers. The default is 0.00USDOLLAR/MM Btu (English), 0.00 USDOLLAR/MM kcal (met-ric), or 0.00 USDOLLAR/MM kJ (SI).

HEATINGMEDIUM=0.0 The cost of heating fluid in currency units per million energyunits. This entry applies only to heaters. The default is 0.00USDOLLAR/MM Btu (English), 0.00 USDOLLAR/MM kcal (met-ric), or 0.00 USDOLLAR/MM kJ (SI).

HXCOST FLOWSHEET CALCULATION Data Category of Input

Optional statement.This statement sets exchanger costing data on a global basis. Exchangercosts are calculated using the costing equation described later on in this Chapter. All entriescan be overridden for specific exchangers using the COST statement.

Optional entries:

BSIZE=1000.0 The base area used in the costing equation. The default is1000.0 ft2 (English), or 93.0 m2 (metric and SI).

BCOST=0.00 The base cost used in the costing equation. The default is 0.00USDOLLAR/ft 2 (English), or 0.00 USDOLLAR/m2 (metric and SI).

LINEAR=50.00 The linear cost factor used in the costing equation. The default is50.00 USDOLLAR/ft2 (English), or 538.20 USDOLLAR/m2 (met-ric and SI).

CONSTANT=0.00 The constant cost factor used in the costing equation. This entrycan be used to define fixed costs associated with installation ofan exchanger and is not a function of exchanger size. The de-fault is 0.00 USDOLLAR (English, metric, and SI).

EXPONENT=0.60 The exponential cost factor used in the costing equation. The de-fault is 0.60 (English, metric, and SI).

UNIT orSHELL

Defines the basis for exchanger CONSTANT cost factor. UNIT re-sults in the constant cost factor being applied once to each unitregardless of the number of shells in the unit. SHELL results inthe constant cost factor being applied to each shell in the unit.The default is UNIT.

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SPECIFICATION FLOWSHEET CALCULATION Data Category of Input

The SPECIFICATION statement is applicable to OPTIMIZATION, REGRESSION, and CAS-ESTUDY calculations only. (See Regression--page 4-90, Cleaning Casestudy--page 4-101,Split Flow Optimization--page ,4-112, and Area Optimization--page 4-121, data categories ofinput for complete descriptions.)

VARIABLE FLOWSHEET CALCULATION Data Category of Input

The CONSTRAINT statement is applicable to OPTIMIZATION calculations only. (See theRegression--page 4-90, and the Split Flow Optimization--page ,4-112, data categories of inputfor complete descriptions.)

CONSTRAINT FLOWSHEET CALCULATION Data Category of Input

The CONSTRAINT statement is applicable to OPTIMIZATION calculations only. (See the SplitFlow Optimization--page ,4-112, and the Area Optimization--page 4-121, data categories of in-put for complete descriptions.)

CASE FLOWSHEET CALCULATION Data Category of Input

The CASE statement is applicable to CLEANING CASESTUDY calculations only. (See the Clean-ing Casestudy--page 4-101, data category of input for a complete description.

PARAMETER FLOWSHEET CALCULATION Data Category of Input

The PARAMETER statement is applicable to OPTIMIZATION calculations only. (See the SplitFlow Optimization--page ,4-112, and the Area Optimization--page 4-121, data categories ofinput for complete descriptions.

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Simulation Category of InputSimulation calculations are performed on exchanger networks that consist ofany combination of rigorous and shortcut unit operation models. Rigorousshell and tube exchanger models can be both OLD exchangers to be rated andNEW exchangers to be designed. Heat transfer coefficients and pressuredrops are calculated for all rigorous unit operations. Complete mass, pressureand energy balances are performed for the entire network. Outlettemperatures, temperature approaches, outlet liquid quality or dutyspecifications may be placed on any OLD exchanger and are required on anyNEW exchanger to be designed. Temperature, pressure or duty specificationsmay also be implemented using the Multivariable Controller (MVC).

Table 4-25: Simulation Category of Input

Statement Keywords See ...

Calculation Type SIMULATION Page 4-83

{TOLERANCE} {TTRIAL=0.01} Page 4-84

{LIMITS} {AREA=200,6000, SERIES=1,10, PARALLEL=1,10, TDAMP=0.00,PDAMP=0.00, TTRIAL=30}

Page 4-84

{CALCULATION} {MINFT=0.80, NOCHECK, DPSMETHOD=STREAM, INCREMENTAL,TWOPHASE=NEW}

Page 4-85

{PRINT} {ALL, UNITS, ECONOMICS, STREAM, STANDARD, EXTENDED,ZONES, MONITOR}

Page 4-86

{ECONOMICS} {DAYS=350, EXCHANGERATE=1.0, CURRENCY=USDOLLAR} Page 4-87

{UTCOST} {OIL=3.50, GAS=3.50, ELECTRICITY=0.10, WATER=0.03,HPSTEAM=4.10, MPSTEAM=3.90, LPSTEAM=3.60,REFRIGERANT=0.00, HEATINGMEDIUM=0.00}

Page 4-87

{HXCOST} {BSIZE=1000, BCOST=0.00, LINEAR=50.00, EXPONENT=0.60,CONSTANT=0.00, UNIT or SHELL}

Page 4-88

PROPERTY SIMULATION Data Category of Input

This entry must be specified. Only one entry is allowed. Each calculation type is described indetail in the following sections.

Mandatory entries:

SIMULATION Rating of all rigorous exchanger models and design of shell andtube exchangers. See Shell-and-Tube Heat Exchangers later onin this chapter.

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TOLERANCE SIMULATION Data Category of Input

Optional statement. This statement modifies the default tolerance values. The default toler-ances are suitable for most calculations.

Optional entries:

TTRIAL=0.01 Temperature tolerance for flowsheet heat balance convergence.Flowsheet solution is reached when all stream temperatureschange by less than this amount from one iteration to the next.The default is 0.01 F (English), or 0.006 C (metric and SI).

LIMITS SIMULATION Data Category of Input

Optional statement. This statement defines two groups of information relating to limits on thedesign of shell and tube exchangers and limits on flowsheet calculations. Exchanger design lim-its for AREA, SERIES, and PARALLEL are applied on a global basis unless redefined individuallyfor specified STE exchangers (see Shell-and-Tube Heat Exchangers later on in this chapter).

Optional entries:

AREA=200, 6000 Area per shell for “design”. Area is total outside surface for bareand finned tubes. Enter both a minimum and maximum limit for“designing” new exchangers. Entering only one limit is not al-lowed. The default is 200, 6000 ft2 (English), or 19, 557 m2(metric and SI).

Note: For rating shells with an area greater than 6000 ft 2 , theuser must raise the maximum area on the AREA statement. Thiscan also be done on the rigorous exchanger’s TYPE statementwith AREA =.

SERIES=1,10 Number of shells in series per unit. Enter both a minimum andmaximum limit for “designing” new exchangers. This entry hasno effect on old exchangers. The default is 1,10.

RESTRICTION: The SERIES entry may not be used in conjunc-tion with the PARALLEL entry.

PARALLEL=1,10 Number of shells in parallel per unit. Enter both a minimum andmaximum limit for “designing” new exchangers. This entry hasno effect on old exchangers. The default is 1,10.

RESTRICTION: The PARALLEL entry may not be used in con-junction with the SERIES entry.

TDAMP= Fraction of temperature damping. TDAMPING is useful when aflowsheet has difficulties converging and the sum of squares er-ror seems to oscillate between iterations. By default, HEXTRANuses the stream temperature from the previous iteration as anestimate for the next iteration. TDAMP decreases the incre-mental temperature change between iterations by using a

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weighted average of the current and previous iterationtemperatures.

For example, if TDAMP=0.4, the temperature estimate becomes:

TEMPest = (TEMPprevious) * 0.4 + (TEMPpresent) * 0.6

There are three TDAMP modes:

1. AUTODAMPING By omitting the TDAMP keyword from theinput file, HEXTRAN will automatically use TDAMPINGwhere necessary. Once autodamping starts, HEXTRANadjusts the TDAMP fraction between 0.0 and 0.5 until theflowsheet converges

2. FIXED DAMPING By specifying a TDAMP fraction, auto-damping is disabled, and the TDAMP fraction is used forevery flowsheet iteration. This is useful when a flowsheetneeds a damping fraction greater than 0.5.

3. NO DAMPING To disable temperature damping, specifyTDAMP=0.0.

PDAMP=0.00 Fraction of pressure damping. Operation and use of PDAMP issimilar to TDAMP (described above), except there is no auto-matic pressure damping mode. The default is 0.00.

TTRIAL=30 Maximum number of flowsheet iterations. The default value (30)is sufficient for most applications. This number may be in-creased to a maximum of 99.

Application: Increase the maximum number of iterations if themaximum temperature error shows a slow convergence. In-creasing the maximum number of iterations will not help if themaximum temperature error shows oscillatory behavior.

CALCULATION SIMULATION Data Category of Input

Optional statement. This statement sets calculation methods for individual exchanges on aglobal basis. Methods can also be selected globally using the CALCULATION statement in theSIMULATION, CASESTUDIES, OPTIMIZATION AREA, OPTIMIZATION SPLIT, or REGRESSIONsections.

Optional entries:

MINFT The minimum log-mean temperature correction factor, Ft, for de-signing NEWS exchangers. If an intermediate exchanger designviolates the minimum Ft, shells are added in series to improvethe Ft.

NOCHECK Suppresses HEXTRAN’s geometry consistency checks and pre-vents HEXTRAN from assigning default values to missing ge-ometry data. The main purpose for NOCHECK is to allow theuser to access HTRI or HTFS defaults.

When using NOCHECK, specify either:

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■ All exchanger data with HEXTRAN keywords, or.■ ST5/CST2/RKH2 or TASC3

WARNING: Using NOCHECK with inconsistent or missing ge-ometry data may result in abnormal program termination (divi-sion by zero, overflow, etc.)

DPSMTHOD=keyword The pressure drop method for the shellside calculations. Selecteither STREAM (Will's and Johnston's stream analysis tech-nique) or BELL (Kenneth Bell of Delaware University).

The STREAM method is automatically selected whenTWOPHASE = NEW.

INCREMENTAL Performs incremetnal heat flux calculation. Incremental heat fluxcalculations are preformed by running a series of case studiesafter the initial network is solved. The area is incremented by 5%for each OLD exchanger that does not have a performancespecification (outlet temperature, temperature approach, duty, oroutlet liquid quality). The results of each case study are sum-marized and reported in tabular form. The default is STREAM.

TWOPHASE=NEW Specifies the methods to be used for thermal and hydraulic calcula-tions for all rigorous exchanger. The NEW method utilizes ModifiedChen vaporization for convective boiling and includes predictionsfor sub-cooled and film boiling. Condensation methods account forflow regime and gravity versus shear effects. Pressure drops arecalculated using a stream analysis based method. The NEW methodautomatically sets DPSMETHOD = STREAM.

The OLD method selects algorithms used in versions 5.0x andearlier. Use this method if you wish to make comparison runswith earlier versions of HEXTRAN. The default is NEW.

PRINT SIMULATION Data Category of Input

Optional statement. This statement sets print options on a global basis. The default is to printall reports except the design MONITOR. Entry of any keyword other than ALL turns off allother reports.

Optional entries:

ALL Print all output reports. No other entries are allowed.

UNITS Print unit operation summaries including both rigorous and short-cut units. Exchanger data sheets are not printed with this option.

ECONOMICS Print economic summary of flowsheet including equipment capi-tal costs and utility costs.

STREAM Print stream data summary.

STANDARD Print standard exchanger data sheets. This produces a TEMA-style data sheet for shell and tube, rodbaffle and double pipe ex-changers. An API-style data sheet is produced for air coolersand finned tube exchangers.

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EXTENDED Print extended exchanger data sheets. This produces a datasheet with additional performance and mechanical data not in-cluded on the standard data sheet.

ZONES Print zones analysis for each two phase exchanger.

MONITOR Print design monitor report for each “NEW” exchanger. Prints allintermediate design data.

CAUTION: Use of this option can produce lengthy reports foreach new exchanger.

Example:

The following statement would cause only exchanger data and extended data sheets to beprinted.PRINT STANDARD, EXTENDED

ECONOMICS SIMULATION Data Category of Input

Optional statement. This statement defines economic factors affecting utility cost calculations.

Optional entries:

DAYS=350 The number of days the plant is on stream per year. The defaultis 350.

CURRENCY=USDOLLAR The currency units. This entry is used for printout purposesonly. The default is USDOLLAR.

CAUTION: Do not use the “$” sign in this entry. HEXTRAN willtreat it as a delimiter.

EXCHANGERATE=1.0 The exchange rate expressed as number of currency units perUS dollar. This entry is used for converting any built-in costingdata defaults. The default is 1.0.

UTCOST SIMULATION Data Category of Input

Optional statement. This statement defines the cost of utilities.

Optional entries:

OIL=3.50 The cost of fuel oil in currency units per million energy units.This entry applies only to fired heaters. The default is 3.50USDOLLAR/MM Btu (English), or 9.04 USDOLLAR/MM kcal(metric), or 3.32 USDOLLAR/MM kJ (SI).

GAS=3.50 The cost of fuel gas in currency units per million energy units.This entry applies only to fired heaters. The default is 3.50USDOLLAR/MM Btu (English), 9.04 USDOLLAR/MM kcal (met-ric), or 3.32 USDOLLAR/MM kJ (SI).

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ELECTRICITY=0.10 The cost of electricity in currency units per kilowatt-hour. Thisentry applies only to pumps and compressors. The default is0.10 USDOLLAR/kW-hr (English, metric, and SI).

WATER=0.03 The cost of cooling water in currency units per thousand US gal-lons. This entry applies only to water coolers. The default is 0.03USDOLLAR/M gallon (English, metric, and SI)

CAUTION: The volume unit of US gallons is not redefined forMetric and SI units.

HPSTEAM=4.10 The cost of high pressure steam in currency units per thousandweight units. This entry applies only to pumps and compres-sors. The default is 4.10 USDOLLAR/M lb (English), or 9.04USDOLLAR/M kg (metric and SI).

MPSTEAM=3.90 The cost of medium pressure steam in currency units per thou-sand weight units. This entry applies only to pumps and com-pressors. The default is 3.90 USDOLLAR/M lb (English), or 8.60USDOLLAR/M kg (metric and SI).

LPSTEAM=3.60 The cost of low pressure steam in currency units per thousandweight units. This entry applies only to pumps and compres-sors. The default is 3.60 USDOLLAR/M lb (English), or 7.94USDOLLAR/M kg (metric and SI).

REFRIGERANT=0.00 The cost of refrigerant in currency units per million energy units.This entry applies only to coolers. The default is 0.00USDOLLAR/MM Btu (English), 0.00 USDOLLAR/MM kcal (met-ric), or 0.00 USDOLLAR/MM kJ (SI).

HEATINGMEDIUM=0.0 The cost of heating fluid in currency units per million energyunits. This entry applies only to heaters. The default is 0.00USDOLLAR/MM Btu (English), 0.00 USDOLLAR/MM kcal (met-ric), or 0.00 USDOLLAR/MM kJ (SI).

HXCOST SIMULATION Data Category of Input

Optional statement.This statement sets exchanger costing data on a global basis. Exchangercosts are calculated using the costing equation described later on in this Chapter. All entriescan be overridden for specific exchangers using the COST statement.

Optional entries:

BSIZE=1000.0 The base area used in the costing equation. The default is1000.0 ft2 (English), or 93.0 m2 (metric and SI).

BCOST=0.00 The base cost used in the costing equation. The default is 0.00USDOLLAR/ft 2 (English), or 0.00 USDOLLAR/m2 (metric andSI).

LINEAR=50.00 The linear cost factor used in the costing equation. The default is50.00 USDOLLAR/ft2 (English), or 538.20 USDOLLAR/m2 (met-ric and SI).

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CONSTANT=0.00 The constant cost factor used in the costing equation. This entrycan be used to define fixed costs associated with installation ofan exchanger and is not a function of exchanger size. The de-fault is 0.00 USDOLLAR (English, metric, and SI).

EXPONENT=0.60 The exponential cost factor used in the costing equation. The de-fault is 0.60 (English, metric, and SI).

UNIT orSHELL

Defines the basis for exchanger CONSTANT cost factor. UNIT re-sults in the constant cost factor being applied once to each unitregardless of the number of shells in the unit. SHELL results inthe constant cost factor being applied to each shell in the unit.The default is UNIT.

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Regression Category of InputThis section describes the input data required for REGRESSIONcalculations. REGRESSION calculations are similar to the MVC Controllerunit operation in that specified conditions are met by the simultaneousadjustment of allowed operating variables. However, unlike the MVC,REGRESSION calculations may be performed for cases where the numberof specifications exceeds the number of variables. The REGRESSIONcalculations will attempt to minimize the differences between the currentcalculated and desired values of the specifications by manipulating theallowed variables within specified limits.

Up to 30 conditions may be specified, and up to 29 operating variables maybe allowed. The number of specifications must equal or exceed the numberof variables. Specifications may be placed on stream temperatures orpressures, or an individual exchanger duty, or the sum of several differentexchanger duties. Variables are feed stream rates and temperatures, heatexchanger duties, and the split fractions in simple two-way splitters. Thenumber of specifications may exceed the number of variables.

Table 4-26: Regression Category of Input

Statement Keywords See ...

Calculation Type SIMULATION or REGRESSION or OPTIMIZATION or CASESTUDY Page 4-91

{TOLERANCE} {TTRIAL=0.01, STRIAL=0.10} Page 4-91

{LIMITS} {AREA=200,6000, SERIES=1,10, PARALLEL=1,10, TDAMP=0.00,PDAMP=0.00, TTRIAL=30, STRIAL}

Page 4-92

{CALCULATION} {MINFT=0.80, NOCHECK, DPSMETHOD=STREAM, INCREMENTAL,TWOPHASE=NEW}

Page 4-93

{PRINT} {ALL, UNITS, ECONOMICS, STREAM, STANDARD, EXTENDED,ZONES, MONITOR, INTERMEDIATE}

Page 4-94

{ECONOMICS} {DAYS=350, EXCHANGERATE=1.0, CURRENCY=USDOLLAR} Page 4-95

{UTCOST} {OIL=3.50, GAS=3.50, ELECTRICITY=0.10, WATER=0.03,HPSTEAM=4.10, MPSTEAM=3.90, LPSTEAM=3.60, REFRIGER-ANT=0.00, HEATINGMEDIUM=0.00}

Page 4-95

{HXCOST} {BSIZE=1000, BCOST=0.00, LINEAR=50.00, EXPONENT=0.60, CON-STANT=0.00, UNIT or SHELL}

Page 4-96

{SPECIFICATION} {STRM, TEMPERATURE, UNIT, DUTY} Page 4-97

{VARIABLE} {STRM, FRACTION, RATE, TEMPERATURE, UNIT, DUTY} Page 4-99

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PROPERTY REGRESSION Data Category of Input

This entry must be specified. Only one entry is allowed. Each calculation type is described indetail in the following sections.

Mandatory entries:

SIMULATION or Rating of all rigorous exchanger models and design of shell andtube exchangers. See Shell-and-Tube Heat Exchangers later onin this chapter.

REGRESSION or Solution of flowsheets with more specifications than variables.Rating of all rigorous exchanger models. Useful for reconcilingplant data.

OPTIMIZATION AREA or Design of new shell and tube exchangers to meet a specifiedpayout period. Networks can consist of both OLD (Rating) andNEW (Design) exchangers.

OPTIMIZATIONSPLITFLOW or

Solution of flowsheets to minimize utility costs by varying split-ter fractions. Rating of all rigorous exchanger models. Use tomaximize performance of existing networks.

CLEANING CASESTUDY Multiple flowsheet solutions for specified exchanger fouling fac-tors. Use to evaluate effect of cleaning exchangers.

TOLERANCE REGRESSION Data Category of Input

Optional statement. This statement modifies the default tolerance values. The default toler-ances are suitable for most calculations.

Optional entries:

TTRIAL=0.01 Temperature tolerance for flowsheet heat balance convergence.Flowsheet solution is reached when all stream temperatureschange by less than this amount from one iteration to the next.The default is 0.01 F (English), or 0.006 C (metric and SI).

STRIAL=0.10 Search trial tolerance for optimization and regression conver-gence. Final solution of an optimization or regression problem isreached when the error sum is less than STRIAL. The default is0.10.

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LIMITS REGRESSION Data Category of Input

Optional statement. This statement defines two groups of information relating to limits on thedesign of shell and tube exchangers and limits on flowsheet calculations. Exchanger design lim-its for AREA, SERIES, and PARALLEL are applied on a global basis unless redefined individuallyfor specified STE exchangers (see Shell-and-Tube Heat Exchangers later on in this chapter).

Optional entries:

AREA=200, 6000 Area per shell for “design”. Area is total outside surface for bareand finned tubes. Enter both a minimum and maximum limit for“designing” new exchangers. Entering only one limit is not al-lowed. The default is 200, 6000 ft2 (English), or 19, 557 m2(metric and SI).

Note: For rating shells with an area greater than 6000 ft 2 , theuser must raise the maximum area on the AREA statement. Thiscan also be done on the rigorous exchanger’s TYPE statementwith AREA =.

SERIES=1,10 Number of shells in series per unit. Enter both a minimum andmaximum limit for “designing” new exchangers. This entry hasno effect on old exchangers. The default is 1,10.

RESTRICTION: The SERIES entry may not be used in conjunc-tion with the PARALLEL entry.

PARALLEL=1,10 Number of shells in parallel per unit. Enter both a minimum andmaximum limit for “designing” new exchangers. This entry hasno effect on old exchangers. The default is 1,10.

RESTRICTION: The PARALLEL entry may not be used in con-junction with the SERIES entry.

TDAMP= Fraction of temperature damping. TDAMPING is useful when aflowsheet has difficulties converging and the sum of squares er-ror seems to oscillate between iterations. By default, HEXTRANuses the stream temperature from the previous iteration as anestimate for the next iteration. TDAMP decreases the incre-mental temperature change between iterations by using aweighted average of the current and previous iterationtemperatures.

For example, if TDAMP=0.4, the temperature estimate becomes:

TEMPest = (TEMPprevious) * 0.4 + (TEMPpresent) * 0.6

There are three TDAMP modes:

1. AUTODAMPING By omitting the TDAMP keyword from theinput file, HEXTRAN will automatically use TDAMPINGwhere necessary. Once autodamping starts, HEXTRANadjusts the TDAMP fraction between 0.0 and 0.5 until theflowsheet converges.

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2. FIXED DAMPING By specifying a TDAMP fraction, auto-damping is disabled, and the TDAMP fraction is used forevery flowsheet iteration. This is useful when a flowsheetneeds a damping fraction greater than 0.5.

3. NO DAMPING To disable temperature damping, specifyTDAMP=0.0.

PDAMP=0.00 Fraction of pressure damping. Operation and use of PDAMP issimilar to TDAMP (described above), except there is no auto-matic pressure damping mode. The default is 0.00.

TTRIAL=30 Maximum number of flowsheet iterations. The default value (30)is sufficient for most applications. This number may be in-creased to a maximum of 99.

Application: Increase the maximum number of iterations if themaximum temperature error shows a slow convergence. In-creasing the maximum number of iterations will not help if themaximum temperature error shows oscillatory behavior.

STRIAL= Maximum number of search trial iterations. This entry applies toarea optimization, split flow optimization and regression calcula-tions only. The default number of iterations is listed for eachavailable calculation type in the formulas below.

= 3 * Number of New Exchangers (AREA OPTIMIZATION)

= 10 * number of variable splitters (SPLITFLOW OPTIMIZATION)

= 5 * number of variables, or 10, whichever is greater(REGRESSION)

CALCULATION REGRESSION Data Category of Input

Optional statement. This statement sets calculation methods for individual exchanges on aglobal basis. Methods can also be selected globally using the CALCULATION statement in theSIMULATION, CASESTUDIES, OPTIMIZATION AREA, OPTIMIZATION SPLIT, or REGRESSIONsections.

Optional entries:

MINFT The minimum log-mean temperature correction factor, Ft, for de-signing NEWS exchangers. If an intermediate exchanger design vio-lates the minimum Ft, shells are added in series to improve the Ft.

NOCHECK Suppresses HEXTRAN’s geometry consistency checks and pre-vents HEXTRAN from assigning default values to missing ge-ometry data. The main purpose for NOCHECK is to allow theuser to access HTRI or HTFS defaults.

When using NOCHECK, specify either:

■ All exchanger data with HEXTRAN keywords, or.■ ST5/CST2/RKH2 or TASC3

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WARNING: Using NOCHECK with inconsistent or missing ge-ometry data may result in abnormal program termination (divi-sion by zero, overflow, etc.)

DPSMTHOD=keyword The pressure drop method for the shellside calculations. Selecteither STREAM (Will's and Johnston's stream analysis tech-nique) or BELL (Kenneth Bell of Delaware University).

The STREAM method is automatically selected whenTWOPHASE = NEW.

INCREMENTAL Performs incremetnal heat flux calculation. Incremental heat fluxcalculations are preformed by running a series of case studiesafter the initial network is solved. The area is incremented by 5%for each OLD exchanger that does not have a performancespecification (outlet temperature, temperature approach, duty, oroutlet liquid quality). The results of each case study are sum-marized and reported in tabular form. The default is STREAM.

TWOPHASE=NEW Specifies the methods to be used for thermal and hydraulic cal-culations for all rigorous exchanger. The NEW method utilizesModified Chen vaporization for convective boiling and includespredictions for sub-cooled and film boiling. Condensation meth-ods account for flow regime and gravity versus shear effects.Pressure drops are calculated using a stream analysis basedmethod. The NEW method automatically sets DPSMETHOD =STREAM.

The OLD method selects algorithms used in versions 5.0x andearlier. Use this method if you wish to make comparison runswith earlier versions of HEXTRAN. The default is NEW.

PRINT REGRESSION Data Category of Input

Optional statement. This statement sets print options on a global basis. The default is to printall reports except the design MONITOR. Entry of any keyword other than ALL turns off allother reports.

Optional entries:

ALL Print all output reports. No other entries are allowed.

UNITS Print unit operation summaries including both rigorous and short-cut units. Exchanger data sheets are not printed with this option.

ECONOMICS Print economic summary of flowsheet including equipment capi-tal costs and utility costs.

STREAM Print stream data summary.

INTERMEDIATE Print intermediate results. This print option applies only toREGRESSION, OPTIMIZATION and CLEANING CASESTUDYcalculations.

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STANDARD Print standard exchanger data sheets. This produces a TEMA-style data sheet for shell and tube, rodbaffle and double pipe ex-changers. An API-style data sheet is produced for air coolersand finned tube exchangers.

EXTENDED Print extended exchanger data sheets. This produces a datasheet with additional performance and mechanical data not in-cluded on the standard data sheet.

ZONES Print zones analysis for each two phase exchanger.

MONITOR Print design monitor report for each “NEW” exchanger. Prints allintermediate design data.

CAUTION: Use of this option can produce lengthy reports foreach new exchanger.

Example:

The following statement would cause only exchanger data and extended data sheets to beprinted.PRINT STANDARD, EXTENDED

ECONOMICS REGRESSION Data Category of Input

Optional statement. This statement defines economic factors affecting utility cost calculations.

Optional entries:

DAYS=350 The number of days the plant is on stream per year. The defaultis 350.

CURRENCY=USDOLLAR The currency units. This entry is used for printout purposesonly. The default is USDOLLAR.

CAUTION: Do not use the “$” sign in this entry. HEXTRAN willtreat it as a delimiter.

EXCHANGERATE=1.0 The exchange rate expressed as number of currency units perUS dollar. This entry is used for converting any built-in costingdata defaults. The default is 1.0.

UTCOST REGRESSION Data Category of Input

Optional statement. This statement defines the cost of utilities.

Optional entries:

OIL=3.50 The cost of fuel oil in currency units per million energy units.This entry applies only to fired heaters. The default is 3.50USDOLLAR/MM Btu (English), or 9.04 USDOLLAR/MM kcal(metric), or 3.32 USDOLLAR/MM kJ (SI).

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GAS=3.50 The cost of fuel gas in currency units per million energy units.This entry applies only to fired heaters. The default is 3.50USDOLLAR/MM Btu (English), 9.04 USDOLLAR/MM kcal (met-ric), or 3.32 USDOLLAR/MM kJ (SI).

ELECTRICITY=0.10 The cost of electricity in currency units per kilowatt-hour. Thisentry applies only to pumps and compressors. The default is0.10 USDOLLAR/kW-hr (English, metric, and SI).

WATER=0.03 The cost of cooling water in currency units per thousand US gal-lons. This entry applies only to water coolers. The default is 0.03USDOLLAR/M gallon (English, metric, and SI)

CAUTION: The volume unit of US gallons is not redefined forMetric and SI units.

HPSTEAM=4.10 The cost of high pressure steam in currency units per thousandweight units. This entry applies only to pumps and compres-sors. The default is 4.10 USDOLLAR/M lb (English), or 9.04USDOLLAR/M kg (metric and SI).

MPSTEAM=3.90 The cost of medium pressure steam in currency units per thou-sand weight units. This entry applies only to pumps and com-pressors. The default is 3.90 USDOLLAR/M lb (English), or 8.60USDOLLAR/M kg (metric and SI).

LPSTEAM=3.60 The cost of low pressure steam in currency units per thousandweight units. This entry applies only to pumps and compres-sors. The default is 3.60 USDOLLAR/M lb (English), or 7.94USDOLLAR/M kg (metric and SI).

REFRIGERANT=0.00 The cost of refrigerant in currency units per million energy units.This entry applies only to coolers. The default is 0.00USDOLLAR/MM Btu (English), 0.00 USDOLLAR/MM kcal (met-ric), or 0.00 USDOLLAR/MM kJ (SI).

HEATINGMEDIUM=0.0 The cost of heating fluid in currency units per million energyunits. This entry applies only to heaters. The default is 0.00USDOLLAR/MM Btu (English), 0.00 USDOLLAR/MM kcal (met-ric), or 0.00 USDOLLAR/MM kJ (SI).

HXCOST REGRESSION Data Category of Input

Optional statement.This statement sets exchanger costing data on a global basis. Exchangercosts are calculated using the costing equation described later on in this Chapter. All entriescan be overridden for specific exchangers using the COST statement.

Optional entries:

BSIZE=1000.0 The base area used in the costing equation. The default is1000.0 ft2 (English), or 93.0 m2 (metric and SI).

BCOST=0.00 The base cost used in the costing equation. The default is 0.00USDOLLAR/ft 2 (English), or 0.00 USDOLLAR/m2 (metric andSI).

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LINEAR=50.00 The linear cost factor used in the costing equation. The default is50.00 USDOLLAR/ft2 (English), or 538.20 USDOLLAR/m2 (met-ric and SI).

CONSTANT=0.00 The constant cost factor used in the costing equation. This entrycan be used to define fixed costs associated with installation ofan exchanger and is not a function of exchanger size. The de-fault is 0.00 USDOLLAR (English, metric, and SI).

EXPONENT=0.60 The exponential cost factor used in the costing equation. The de-fault is 0.60 (English, metric, and SI).

UNIT orSHELL

Defines the basis for exchanger CONSTANT cost factor. UNIT re-sults in the constant cost factor being applied once to each unitregardless of the number of shells in the unit. SHELL results inthe constant cost factor being applied to each shell in the unit.The default is UNIT.

SPECIFICATION REGRESSION Data Category of Input

Mandatory statement. This statement declares the specifications for the Regression calcula-tions. Up to 15 SPECIFICATION statements may be included. At least one SPECIFICATIONstatement is required. SPECIFICATION is not available for SIMULATION calculations.

Note: In regression calculations, there may be more SPECIFICATION statements than VARI-ABLE statements.

STREAM= Stream identifier. STREAM identifies the feed stream whosetemperature is to be set to a given value. Enter up to 12 alpha-numeric characters. This entry must be unique to all otherstream identifiers given on SPECIFICATION statements for theregression calculations. This entry is optional. There is nodefault.

TEMPERATURE=, 0.1 Stream temperature specification and tolerance. TEMPERATUREdefines the value of the stream temperature specification and theabsolute tolerance on the specification. The default tolerance is0.1 F (English), 0.06 C (metric), or 0.06 K (SI).

PRESSURE=, 0.1 Stream pressure specification and tolerance. PRESSURE definesthe value of the stream pressure specification and the absolutetolerance on the specifications. The default tolerance is 0.1 psi(English), 0.007 kg/cm 2 (Metric), or 0.688 kPa (SI).

UNIT= Unit identifier. UNIT identifies the exchanger identifier, UID,whose duty is specified, or a list of UIDs, separated by commas,of the exchanger units whose duties must add up (sum) to aspecified value. Enter up to 12 alphanumeric characters for eachUID. Multiple entries must be separated by commas. This entryis optional. There is no default.

DUTY=, .005 Duty specification and tolerance. DUTY defines the value of theindividual unit duty specification, or multiple unit duty sumspecification, in millions of energy units per unit time, and therelative tolerance on the specification (expressed as an absolute

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fraction). Enter positive values for both the specification and tol-erance. The default tolerance is .005 (English, metric, and SI).

Note: The duty specification may be used on the following heattransfer units:

STE Shell-and-Tube ExchangersRBE Rod Baffle ExchangersDPE Double Pipe ExchangersMTE Multi-Tube ExchangersFTE Finned Tube ExchangersACE Air-Cooled ExchangersCOOLERHEATERFIRED HEATER

Example:PROP STREAM = C1, RATE(W) = 8000, ...

REGRESSIONVARI STREAM = C1, RATE = 1000, 9000VARI STREAM = C3, FRAC = 0.1, 0.4, UNIT = SPL1SPEC UNIT = E1, DUTY = 10.1, 0.004SPEC UNIT = 32, E3, E4, DUTY = 30, 0.006SPEC STRM = C5, PRESSURE = 100, 0.01SPEC STRM = H2, TEMP = 350

UNIT OPS SPLITTER UID = SPL1STRMS FEED = C2, PROD = C3, C4OPER FRAC = 0.3, 0.7

In the above example, REGRESSION varies the rate of stream C1 and the split fraction of SPL1 tomeet 4 specifications for duty, temperature and pressure. Notice the starting flow rate for C1 is8000, on the first variable Statement, which is between the minimum and maximum flowrate.

Also, the variable split fraction for SPLITTER SPL1, varies the fraction of only one splitterproduct, stream C3. The starting value for stream C3, in the unit operation section, is 0.3,which is between the REGRESSION split fraction range.

The first 3 specifications have a value followed by a tolerance entry. The last specification doesnot have a tolerance, but will use the default value of 0.01° F.

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VARIABLE REGRESSION Data Category of Input

Mandatory statement. This statement declares the variables for the Regression calculations.Up to 15 VARIABLE statements may be included. At least one VARIABLE statement is required.VARIABLE is not available for SIMULATION, CASESTUDY, and AREA PAYOUT calculations.

Note: In regression calculations, there may be fewer VARIABLE statements than SPECIFICATIONStatements. There can not be more VARIABLE Statements than SPECIFICATION Statements.

STRM= Stream identifier. STRM defines the stream whose parameter isto be used as a regression variable. Enter up to 12 alphanumericcharacters. There is no default.

RATE= Minimum and maximum feed stream flow rate. RATE defines theminimum and maximum values for the designated feed streamflow rate in weight units per unit time. Enter positive values forboth the minimum and maximum rates. There are no defaults.

RESTRICTIONS: The RATE entry may only be used for feedstreams. The RATE on the PROCESS STREAM statement mustbe within (but not equal to) the specified minimum and maxi-mum rate.

TEMPERATURE= Minimum and maximum feed stream temperature.TEMPERATURE defines the minimum and maximum tempera-ture values for the designated feed stream. Enter values for boththe minimum and maximum temperatures. There are nodefaults.

UNIT= Unit identifier. UNIT identifies the unit identifier, UID, whose dutyis to be varied. Units whose duty can be varied are the Shell-and-Tube exchanger, Shortcut exchanger, Heaters, Coolers, andFired Heaters. To be used as a variable, the designated UNITmust have its duty specified initially in the input data. There isno default.

FRACTION= Minimum and maximum stream split fraction. FRACTION indi-cates that the split fraction for stream “STREAM” in a twowaysplitter is to be varied. These entries are optional. There are nodefaults.The starting value for the split fraction, in the unit op-eration section, must be within (but not equal to) the minimumand maximum REGRESSION split fraction.

RESTRICTION: Enter values between 0.01 and 0.99 for both theminimum and maximum split fraction.

RESTRICTION: Tthe FRACTION entry may only refer to a streamfrom a twoway splitter.

Note: Variable splitters require specifications for STRM, UNITand FRACTION.

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DUTY= Duty minimum and maximum. DUTY defines the minimum andmaximum duty value for the designated unit. Enter positive val-ues for both the minimum and maximum duties. These entriesare optional. There are no defaults.

Note: HEXTRAN needs a starting value for duty on each unit op-eration varied by REGRESSION. Starting values are entered with:

SPEC DUTY = $Rigorous Exchangersor OPER DUTY = $Short Cut Units

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Cleaning Casestudy Category of InputCleaning CASESTUDY calculations provide the ability to evaluate theimpact of cleaning one, several, or all of the exchangers in a flowsheet.CASESTUDY first prepares a base case and then performs the specifiedcleaning case studies.

Simple case studies, which compare the utility consumption base case toeach case, are made by specifying the clean fouling factor after eachexchanger or group of exchangers is cleaned. Complete cleaning cycleanalyses are made by adding economic costs for utilities, and optionally,costs for labor, materials, and lost throughput. Exponential decayalgorithms model the cumulative effects of fouling versus time. Cleaninginterval optimization is then performed by examining the effect of foulingand cleaning on operating costs.

Fouling trend studies and online fouling factor monitoring can beimplemented by performing CASESTUDY runs on a regular basis. AllCASESTUDY runs produce a daily performance file, CLNDBS*, whichsummarizes each exchanger’s fouling factor, U value and duty. TheCLNDBS file is easily converted to a LOTUS 123* (for PC’s) formatspreadsheet file through the HEX123 program available from SIMSCI.

The methodology for cleaning cycle optimization is best described byFigure 4-2. At the start of the run, heat recovery is at its maximum andutility costs are at a minimum. As time passes, fouling resistance of theexchanger begins to increase and the thermal performance degradesresulting in higher utility costs. At time t1, the exchanger is taken offlineand cleaned while the unit continues to operate. This creates a furtherincrease in utility cost since the duty of the exchanger being cleaned mustbe replaced by the fired heater. When the exchanger is brought back onlineat time t2, utility costs returned to their original value. The shaded area inthe figure represetns the utility costs due to fouling. The other costassociated with cleaning is the cost of lost through put and the actual laborand chemical costs. This is represented by the other shaded box betweentimes t1 and t2.

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Figure 4-2: Cleaning Cycle Optimization

HEXTRAN calculates the optimum cleaning interval by preparing 3simulations for each case. The first simulation models the start of runconditions - clean exchangers. The second simulation models the currentconditions, the cost of cleaning today, and the annualized cost of fouling ifthe exchangers were cleaned at this interval throughout the unit’s runlength. If the current fouling factors are not supplied, HEXTRAN needs tocalculate the fouling factor from exchanger TEMPERATUREspecifications. The temperature specifications will be overridden as theduty load shifts in the network due to cleaning, but each uncleanedexchanger will retain its current fouling factor. The third simulation modelsthe cost of fouling if the exchangers were cleaned only once at the end ofthe unit’s run length (HEXTRAN uses a default unit run length of 1050days unless a different run length is supplied with the BASE keyword onthe ECONOMICS statement).

From the 3 simulations, an annualized fouling cost function versus time isderived. The time with the lowest fouling cost is chosen as the optimumcleaning cycle interval. The annualized fouling costs for the cleaning today,at the optimum interval and at the end of run are summarized at the end ofthe HEXTRAN output. The exchanger data sheets and temperature profilesreflect the base case study. If you desire temperature and performance datafor the other case studies, use the PRINT INTERMEDIATE option.

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Cleaning Cycle Optimization

NetworkHeat

Transfer

OperatingCost

t1

t1

t2

t2

t0

t0

ExchangerFouling

ExchangerOff-Line

UtilityCost

CleaningCost

Off-lineUtilityCost

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By default, HEXTRAN uses a linear fouling decay factor. If possible, usean exponential fouling decay factor derived from plant data. This data maybe entered with the THETA keyword on the SPECIFICATION statement.

Note: Because the cleaning cycle optimization calculations are dependentupon reducing the utility costs, the CASESTUDY input file must include atleast one utility consuming unit operation: HEATER, COOLER, orFIREDHEATER.

Table 4-27: Cleaning Casestudy Category of Input

Statement Keywords See ...

Calculation Type SIMULATION or REGRESSION or OPTIMIZATION or CASESTUDY Page 4-104

{TOLERANCE} {TTRIAL=0.01} Page 4-104

{LIMITS} {AREA=200,6000, SERIES=1,10, PARALLEL=1,10, TDAMP=0.00,PDAMP=0.00, TTRIAL=30}

Page 4-104

{CALCULATION} {MINFT=0.80, NOCHECK, DPSMETHOD=STREAM, INCREMENTAL,TWOPHASE=NEW}

Page 4-106

{HTRI or HTFS} See HEXTRAN HTRI Input Guide, orHEXTRAN HTFS Input Guide

{PRINT} {ALL, UNITS, ECONOMICS, STREAM, STANDARD, EXTENDED,ZONES, MONITOR, INTERMEDIATE}

Page 4-107

{ECONOMICS} {DAYS=350, EXCHANGERATE=1.0, CURRENCY=USDOLLAR,THROUGHPUT=0.0, BASE= 1050}

Page 4-108

{UTCOST} {OIL=3.50, GAS=3.50, ELECTRICITY=0.10, WATER=0.03,HPSTEAM=4.10, MPSTEAM=3.90, LPSTEAM=3.60, REFRIGER-ANT=0.00, HEATINGMEDIUM=0.00}

Page 4-108

{HXCOST} {BSIZE=1000, BCOST=0.00, LINEAR=50.00, EXPONENT=0.60, CON-STANT=0.00, UNIT or SHELL}

Page 4-109

{SPECIFICATION} {UNIT, FOUL, DAYS, DATE, LABOR, OFFLINE, THETA} Page 4-110

{CASE} UNIT Page 4-111

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PROPERTY CLEANING CASESTUDY Data Category of Input

This entry must be specified. Only one entry is allowed. Each calculation type is described indetail in the following sections.

Mandatory entries:

SIMULATION or Rating of all rigorous exchanger models and design of shell andtube exchangers. See Shell-and-Tube Heat Exchangers later onin this chapter.

REGRESSION or Solution of flowsheets with more specifications than variables.Rating of all rigorous exchanger models. Useful for reconcilingplant data.

OPTIMIZATION AREA or Design of new shell and tube exchangers to meet a specifiedpayout period. Networks can consist of both OLD (Rating) andNEW (Design) exchangers.

OPTIMIZATIONSPLITFLOW or

Solution of flowsheets to minimize utility costs by varying split-ter fractions. Rating of all rigorous exchanger models. Use tomaximize performance of existing networks.

CLEANING CASESTUDY Multiple flowsheet solutions for specified exchanger fouling fac-tors. Use to evaluate effect of cleaning exchangers.

TOLERANCE CLEANING CASESTUDY Data Category of Input

Optional statement. This statement modifies the default tolerance values. The default toler-ances are suitable for most calculations.

Optional entries:

TTRIAL=0.01 Temperature tolerance for flowsheet heat balance convergence.Flowsheet solution is reached when all stream temperatureschange by less than this amount from one iteration to the next.The default is 0.01 F (English), or 0.006 C (metric and SI).

LIMITS CLEANING CASESTUDY Data Category of Input

Optional statement. This statement defines two groups of information relating to limits on thedesign of shell and tube exchangers and limits on flowsheet calculations. Exchanger design lim-its for AREA, SERIES, and PARALLEL are applied on a global basis unless redefined individuallyfor specified STE exchangers (see Shell-and-Tube Heat Exchangers later on in this chapter).

Optional entries:

AREA=200, 6000 Area per shell for “design”. Area is total outside surface for bareand finned tubes. Enter both a minimum and maximum limit for

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“designing” new exchangers. Entering only one limit is not al-lowed. The default is 200, 6000 ft2 (English), or 19, 557 m2(metric and SI).

Note: For rating shells with an area greater than 6000 ft 2 , theuser must raise the maximum area on the AREA statement. Thiscan also be done on the rigorous exchanger’s TYPE statementwith AREA =.

SERIES=1,10 Number of shells in series per unit. Enter both a minimum andmaximum limit for “designing” new exchangers. This entry hasno effect on old exchangers. The default is 1,10.

RESTRICTION: The SERIES entry may not be used in conjunc-tion with the PARALLEL entry.

PARALLEL=1,10 Number of shells in parallel per unit. Enter both a minimum andmaximum limit for “designing” new exchangers. This entry hasno effect on old exchangers. The default is 1,10.

RESTRICTION: The PARALLEL entry may not be used in con-junction with the SERIES entry.

TDAMP= Fraction of temperature damping. TDAMPING is useful when aflowsheet has difficulties converging and the sum of squares er-ror seems to oscillate between iterations. By default, HEXTRANuses the stream temperature from the previous iteration as anestimate for the next iteration. TDAMP decreases the incre-mental temperature change between iterations by using aweighted average of the current and previous iterationtemperatures.

For example, if TDAMP=0.4, the temperature estimate becomes:

TEMPest = (TEMPprevious) * 0.4 + (TEMPpresent) * 0.6

There are three TDAMP modes:

1. AUTODAMPING By omitting the TDAMP keyword from theinput file, HEXTRAN will automatically use TDAMPINGwhere necessary. Once autodamping starts, HEXTRANadjusts the TDAMP fraction between 0.0 and 0.5 until theflowsheet converges

2. FIXED DAMPING By specifying a TDAMP fraction, auto-damping is disabled, and the TDAMP fraction is used forevery flowsheet iteration. This is useful when a flowsheetneeds a damping fraction greater than 0.5.

3. NO DAMPING To disable temperature damping, specifyTDAMP=0.0.

PDAMP=0.00 Fraction of pressure damping. Operation and use of PDAMP issimilar to TDAMP (described above), except there is no auto-matic pressure damping mode. The default is 0.00.

TTRIAL=30 Maximum number of flowsheet iterations. The default value (30)is sufficient for most applications. This number may be in-creased to a maximum of 99.

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Application: Increase the maximum number of iterations if themaximum temperature error shows a slow convergence. In-creasing the maximum number of iterations will not help if themaximum temperature error shows oscillatory behavior.

CALCULATION CLEANING CASESTUDY Data Category of Input

Optional statement. This statement sets calculation methods for individual exchanges on aglobal basis. Methods can also be selected globally using the CALCULATION statement in theSIMULATION, CASESTUDIES, OPTIMIZATION AREA, OPTIMIZATION SPLIT, or REGRESSIONsections.

Optional entries:

MINFT The minimum log-mean temperature correction factor, Ft, for de-signing NEW exchangers. If an intermediate exchanger designviolates the minimum Ft, shells are added in series to improvethe Ft.

NOCHECK Suppresses HEXTRAN’s geometry consistency checks and pre-vents HEXTRAN from assigning default values to missing ge-ometry data. The main purpose for NOCHECK is to allow theuser to access HTRI or HTFS defaults.

When using NOCHECK, specify either:

■ All exchanger data with HEXTRAN keywords, or.■ ST5/CST2/RKH2 or TASC3

WARNING: Using NOCHECK with inconsistent or missing ge-ometry data may result in abnormal program termination (divi-sion by zero, overflow, etc.)

DPSMTHOD=keyword The pressure drop method for the shellside calculations. Selecteither STREAM (Will's and Johnston's stream analysis tech-nique) or BELL (Kenneth Bell of Delaware University).

The STREAM method is automatically selected whenTWOPHASE = NEW.

INCREMENTAL Performs incremetnal heat flux calculation. Incremental heat fluxcalculations are preformed by running a series of case studiesafter the initial network is solved. The area is incremented by 5%for each OLD exchanger that does not have a performancespeci-fication (outlet temperature, temperature approach, duty, or out-let liquid quality). The results of each case study are summarizedand reported in tabular form. The default is STREAM.

TWOPHASE=NEW Specifies the methods to be used for thermal and hydraulic cal-culations for all rigorous exchanger. The NEW method utilizesModified Chen vaporization for convective boiling and includespredictions for sub-cooled and film boiling. Condensation meth-ods account for flow regime and gravity versus shear effects.Pressure drops are calculated using a stream analysis based

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method. The NEW method automatically sets DPSMETHOD =STREAM.

The OLD method selects algorithms used in versions 5.0x andearlier. Use this method if you wish to make comparison runswith earlier versions of HEXTRAN. The default is NEW.

PRINT CLEANING CASESTUDY Data Category of Input

Optional statement. This statement sets print options on a global basis. The default is to printall reports except the design MONITOR. Entry of any keyword other than ALL turns off allother reports.

Optional entries:

ALL Print all output reports. No other entries are allowed.

UNITS Print unit operation summaries including both rigorous and short-cut units. Exchanger data sheets are not printed with this option.

ECONOMICS Print economic summary of flowsheet including equipment capi-tal costs and utility costs.

STREAM Print stream data summary.

INTERMEDIATE Print intermediate results. This print option will result in all re-quested reports being printed for the base case and each case-study. If not specified, those reports requested will only beproduced for the base case.Example:

PRINT UNITS, INTERMEDIATE

Prints the unit operations summary for the base case and eachcase study. No other reports will be printed except for the case-study summary.

STANDARD Print standard exchanger data sheets. This produces a TEMA-style data sheet for shell and tube, rodbaffle and double pipe ex-changers. An API-style data sheet is produced for air coolersand finned tube exchangers.

EXTENDED Print extended exchanger data sheets. This produces a datasheet with additional performance and mechanical data not in-cluded on the standard data sheet.

ZONES Print zones analysis for each two-phase exchanger.

MONITOR Print design monitor report for each “NEW” exchanger. Prints allintermediate design data.

CAUTION: Use of this option can produce lengthy reports foreach new exchanger.

Example:

The following statement would cause only exchanger data and extended data sheets to be printed.PRINT STANDARD, EXTENDED

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ECONOMICS CLEANING CASESTUDY Data Category of Input

Optional statement. This statement defines economic factors affecting utility cost calculations.

Optional entries:

DAYS=350 The number of days the plant is on stream per year. The defaultis 350.

CURRENCY=USDOLLAR The currency units. This entry is used for printout purposesonly. The default is USDOLLAR.

CAUTION: Do not use the “$” sign in this entry. HEXTRAN willtreat it as a delimiter.

EXCHANGERATE=1.0 The exchange rate expressed as number of currency units perUS dollar. This entry is used for converting any built-in costingdata defaults. The default is 1.0.

UTCOST CLEANING CASESTUDY Data Category of Input

Optional statement. This statement defines the cost of utilities.

Optional entries:

OIL=3.50 The cost of fuel oil in currency units per million energy units.This entry applies only to fired heaters. The default is 3.50USDOLLAR/MM Btu (English), or 9.04 USDOLLAR/MM kcal(metric), or 3.32 USDOLLAR/MM kJ (SI).

GAS=3.50 The cost of fuel gas in currency units per million energy units.This entry applies only to fired heaters. The default is 3.50USDOLLAR/MM Btu (English), 9.04 USDOLLAR/MM kcal (met-ric), or 3.32 USDOLLAR/MM kJ (SI).

ELECTRICITY=0.10 The cost of electricity in currency units per kilowatt-hour. Thisentry applies only to pumps and compressors. The default is0.10 USDOLLAR/kW-hr (English, metric, and SI).

WATER=0.03 The cost of cooling water in currency units per thousand US gal-lons. This entry applies only to water coolers. The default is 0.03USDOLLAR/M gallon (English, metric, and SI)

CAUTION: The volume unit of US gallons is not redefined forMetric and SI units.

HPSTEAM=4.10 The cost of high pressure steam in currency units per thousandweight units. This entry applies only to pumps and compres-sors. The default is 4.10 USDOLLAR/M lb (English), or 9.04USDOLLAR/M kg (metric and SI).

MPSTEAM=3.90 The cost of medium pressure steam in currency units per thou-sand weight units. This entry applies only to pumps and

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compressors. The default is 3.90 USDOLLAR/M lb (English), or8.60 USDOLLAR/M kg (metric and SI).

LPSTEAM=3.60 The cost of low pressure steam in currency units per thousandweight units. This entry applies only to pumps and compres-sors. The default is 3.60 USDOLLAR/M lb (English), or 7.94USDOLLAR/M kg (metric and SI).

REFRIGERANT=0.00 The cost of refrigerant in currency units per million energy units.This entry applies only to coolers. The default is 0.00USDOLLAR/MM Btu (English), 0.00 USDOLLAR/MM kcal (met-ric), or 0.00 USDOLLAR/MM kJ (SI).

HEATINGMEDIUM=0.0 The cost of heating fluid in currency units per million energyunits. This entry applies only to heaters. The default is 0.00USDOLLAR/MM Btu (English), 0.00 USDOLLAR/MM kcal (met-ric), or 0.00 USDOLLAR/MM kJ (SI).

HXCOST CLEANING CASESTUDY Data Category of Input

Optional statement.This statement sets exchanger costing data on a global basis. Exchangercosts are calculated using the costing equation described later on in this Chapter. All entriescan be overridden for specific exchangers using the COST statement.

Optional entries:

BSIZE=1000.0 The base area used in the costing equation. The default is1000.0 ft2 (English), or 93.0 m2 (metric and SI).

BCOST=0.00 The base cost used in the costing equation. The default is 0.00USDOLLAR/ft 2 (English), or 0.00 USDOLLAR/m2 (metric andSI).

LINEAR=50.00 The linear cost factor used in the costing equation. The default is50.00 USDOLLAR/ft2 (English), or 538.20 USDOLLAR/m2 (met-ric and SI).

CONSTANT=0.00 The constant cost factor used in the costing equation. This entrycan be used to define fixed costs associated with installation ofan exchanger and is not a function of exchanger size. The de-fault is 0.00 USDOLLAR (English, metric, and SI).

EXPONENT=0.60 The exponential cost factor used in the costing equation. The de-fault is 0.60 (English, metric, and SI).

UNIT orSHELL

Defines the basis for exchanger CONSTANT cost factor. UNIT re-sults in the constant cost factor being applied once to each unitregardless of the number of shells in the unit. SHELL results inthe constant cost factor being applied to each shell in the unit.The default is UNIT.

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SPECIFICATION CLEANING CASESTUDY Data Category of Input

Mandatory statement. The SPECIFICATION statement is used to define the exchanger foulingfactors for the case studies.

UNIT= Unit identifier. UNIT identifies the exchanger identifier, UID,whose duty is specified, or a list of UIDs, separated by commas,of the exchanger units whose duties must add up (sum) to aspecified value. Enter up to 12 alphanumeric characters for eachUID. Multiple entries must be separated by commas. This entryis optional. There is no default.

FOUL= Total exchanger fouling factor for shell (duct or air) side of ex-changer. Tubeside fouling factor will be set to zero during cas-estudy calculations.

DATE= Date exchanger was last cleaned. Days online is calculatedbased on today's date and date last cleaned. Todays's date maybe supplied on TITLE statement. If not supplied in TITLE state-ment, date will be determined from computer system. Date entrycannot be used in combinations with DAYS entry. There is nodefault.

DAYS= Days online since exchanger was last cleaned. Cannot be used inconjunction with DATE entry. There is no default.

LABOR= Costs associated with cleaning exchanger including labor andchemicals.

OFFLINE= Offline time required to clean exchanger. During this time the ex-changer's duty must be replaced by the other exchangers in thenetwork and the heating utilities.

THETA= Fouling curve decay factor used in equation to predict fouling asa function of time. If not specified, the default value of 1.0 repre-sents a linear fouling trend.

r r tt

rf

THETA

o=

+1

1

where:rf = fouling resistance at time tro = fouling resistance at time tor1 = fouling resistance at time t1

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CASE CLEANING CASESTUDY Data Category of Input

The CASE statement is used to specify which exchangers are to have fouling factor adjust-ments for each case. A maximum of ten CASE statements are allowed. For sensitivity analysis,it is best to evaluate individual exchangers, i.e. Use one exchanger per CASE statement.

Mandatory entry:

UNIT= Specifies the exchanger UID(s) which are to be modified for thiscase study. Enter up to 10 exchanger UIDs separated bycommas.

Example:CASESTUDYSPEC UNIT=E1, FOUL=0.000SPEC UNIT=E2, FOUL=0.001CASE UNIT=E1CASE UNIT=E2CASE UNIT=E1,E2

This example shows a cleaning casestudy run with three casestudies. The first case results incleaning only exchanger E1, the second case results in cleaning only exchanger E2, the thirdcase evaluates the cleaning of both exchangers E1 and E2.

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Split Flow Optimization Category of InputSplit Flow OPTIMIZATION calculations consist of multipleSIMULATION runs with the objective being to minimize the total utilitycosts for the network, including the costs of pumping, air cooling, furnacefiring, etc. Costs and/or savings may be assigned to selected streamsdepending on whether or not the streams are heated or cooled. Theoptimization variables are manipulated to determine the minimum utilitycosts are the split fractions in specified splitters.

Flowsheets for Split Flow OPTIMIZATION calculations may be composedof OLD exchangers and any other unit operations. NEW exchangers are notallowed. The calculation procedure followed during OPTIMIZATIONcalculations begins with an initial network solution identical to thatproduced in a SIMULATION calculation.

Because certain operating constraints are inherent in varying stream splitfractions, such as the pressure drop across an exchanger or the temperatureto which a stream may be heated or cooled, HEXTRAN allows the user tospecify stream temperature and exchanger pressure drop constraints for usein the optimization calculations. When these constraints are violated duringthe calculations, a penalty is added to the objective function which forcesthe solution away from the infeasible region. A result of this approach isthat the constraints are not always rigorously met, although usually theywill be.

Table 4-28: Split Flow Optimization Category of Input

Statement Keywords See ...

Calculation Type SIMULATION or REGRESSION or OPTIMIZATION or CASESTUDY Page 4-113

{TOLERANCE} {TTRIAL=0.01, STRIAL=0.10} Page 4-113

{LIMITS} {TDAMP=0.00, PDAMP=0.00, TTRIAL=30, STRIAL} Page 4-114

{CALCULATION} {NOCHECK, DPSMETHOD=STREAM, INCREMENTAL,TWOPHASE=NEW}

Page 4-115

{PRINT} {ALL, UNITS, ECONOMICS, STREAM, STANDARD, EXTENDED,ZONES, INTERMEDIATE}

Page 4-116

{ECONOMICS} {DAYS=350, EXCHANGERATE=1.0, CURRENCY=USDOLLAR} Page 4-117

{UTCOST} {OIL=3.50, GAS=3.50, ELECTRICITY=0.10, WATER=0.03,HPSTEAM=4.10, MPSTEAM=3.90, LPSTEAM=3.60,REFRIGERANT=0.00, HEATINGMEDIUM=0.00}

Page 4-117

{HXCOST} {BSIZE=1000, BCOST=0.00, LINEAR=50.00, EXPONENT=0.60,CONSTANT=0.00, UNIT or SHELL}

Page 4-118

{VARIABLE} {STREAM, FRACTION} Page 4-119

{CONSTRAINT} STREAM, TEMPERATURE, UNIT, DPTMAX, DPSMAX} Page 4-119

{PARAMETER} {FRACTION=0.01,0.50} Page 4-120

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PROPERTY SPLIT FLOW OPTIMIZATION Data Category of Input

This entry must be specified. Only one entry is allowed. Each calculation type is described indetail in the following sections.

Mandatory entries:

SIMULATION or Rating of all rigorous exchanger models and design of shell andtube exchangers. See Shell-and-Tube Heat Exchangers later onin this chapter.

REGRESSION or Solution of flowsheets with more specifications than variables.Rating of all rigorous exchanger models. Useful for reconcilingplant data.

OPTIMIZATION AREA or Design of new shell and tube exchangers to meet a specifiedpayout period. Networks can consist of both OLD (Rating) andNEW (Design) exchangers.

OPTIMIZATIONSPLITFLOW or

Solution of flowsheets to minimize utility costs by varying split-ter fractions. Rating of all rigorous exchanger models. Use tomaximize performance of existing networks.

CLEANING CASESTUDY Multiple flowsheet solutions for specified exchanger fouling fac-tors. Use to evaluate effect of cleaning exchangers.

TOLERANCE SPLIT FLOW OPTIMIZATION Data Category of Input

Optional statement. This statement modifies the default tolerance values. The default toler-ances are suitable for most calculations.

Optional entries:

TTRIAL=0.01 Temperature tolerance for flowsheet heat balance convergence.Flowsheet solution is reached when all stream temperatureschange by less than this amount from one iteration to the next.The default is 0.01 F (English), or 0.006 C (metric and SI).

STRIAL=0.10 Search trial tolerance for optimization and regression conver-gence. Final solution of an optimization or regression problem isreached when the error sum is less than STRIAL. The default is0.10.

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LIMITS SPLIT FLOW OPTIMIZATION Data Category of Input

Optional statement. This statement defines two groups of information relating to limits on thedesign of shell and tube exchangers and limits on flowsheet calculations. Exchanger design lim-its for AREA, SERIES, and PARALLEL are applied on a global basis unless redefined individuallyfor specified STE exchangers (see Shell-and-Tube Heat Exchangers later on in this chapter).

Optional entries:

TDAMP= Fraction of temperature damping. TDAMPING is useful when aflowsheet has difficulties converging and the sum of squares er-ror seems to oscillate between iterations. By default, HEXTRANuses the stream temperature from the previous iteration as anestimate for the next iteration. TDAMP decreases the incre-mental temperature change between iterations by using aweighted average of the current and previous iterationtemperatures.

For example, if TDAMP=0.4, the temperature estimate becomes:

TEMPest = (TEMPprevious) * 0.4 + (TEMPpresent) * 0.6

There are three TDAMP modes:

1. AUTODAMPING By omitting the TDAMP keyword from theinput file, HEXTRAN will automatically use TDAMPINGwhere necessary. Once autodamping starts, HEXTRANadjusts the TDAMP fraction between 0.0 and 0.5 until theflowsheet converges

2. FIXED DAMPING By specifying a TDAMP fraction, auto-damping is disabled, and the TDAMP fraction is used forevery flowsheet iteration. This is useful when a flowsheetneeds a damping fraction greater than 0.5.

3. NO DAMPING To disable temperature damping, specifyTDAMP=0.0.

PDAMP=0.00 Fraction of pressure damping. Operation and use of PDAMP issimilar to TDAMP (described above), except there is no auto-matic pressure damping mode. The default is 0.00.

TTRIAL=30 Maximum number of flowsheet iterations. The default value (30)is sufficient for most applications. This number may be in-creased to a maximum of 99.

Application: Increase the maximum number of iterations if themaximum temperature error shows a slow convergence. In-creasing the maximum number of iterations will not help if themaximum temperature error shows oscillatory behavior.

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STRIAL= Maximum number of search trial iterations. This entry applies toarea optimization, split flow optimization and regression calcula-tions only. The default number of iterations is listed for eachavailable calculation type in the formulas below.

= 3 * Number of New Exchangers (AREA OPTIMIZATION)

= 10 * number of variable splitters (SPLITFLOWOPTIMIZATION)

= 5 * number of variables, or 10, whichever is greater(REGRESSION)

UTRIAL=5 Maximum number of U-value loop iterations. This entry appliesto area optimization only. The default is 5.

CALCULATION SPLIT FLOW OPTIMIZATION Data Category of Input

Optional statement. This statement sets calculation methods for individual exchanges on aglobal basis. Methods can also be selected globally using the CALCULATION statement in theSIMULATION, CASESTUDIES, OPTIMIZATION AREA, OPTIMIZATION SPLIT, or REGRESSIONsections.

Optional entries:

NOCHECK Suppresses HEXTRAN’s geometry consistency checks and pre-vents HEXTRAN from assigning default values to missing ge-ometry data. The main purpose for NOCHECK is to allow theuser to access HTRI or HTFS defaults.

When using NOCHECK, specify either:

■ All exchanger data with HEXTRAN keywords, or.■ ST5/CST2/RKH2 or TASC3

WARNING: Using NOCHECK with inconsistent or missing ge-ometry data may result in abnormal program termination (divi-sion by zero, overflow, etc.)

DPSMTHOD=keyword The pressure drop method for the shellside calculations. Selecteither STREAM (Will's and Johnston's stream analysis tech-nique) or BELL (Kenneth Bell of Delaware University).

The STREAM method is automatically selected whenTWOPHASE = NEW.

INCREMENTAL Performs incremetnal heat flux calculation. Incremental heat fluxcalculations are preformed by running a series of case studiesafter the initial network is solved. The area is incremented by 5%for each OLD exchanger that does not have a performancespeci-fication (outlet temperature, temperature approach, duty, or out-let liquid quality). The results of each case study are summarizedand reported in tabular form. The default is STREAM.

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TWOPHASE=NEW Specifies the methods to be used for thermal and hydraulic cal-culations for all rigorous exchanger. The NEW method utilizesModified Chen vaporization for convective boiling and includespredictions for sub-cooled and film boiling. Condensation meth-ods account for flow regime and gravity versus shear effects.Pressure drops are calculated using a stream analysis basedmethod. The NEW method automatically sets DPSMETHOD =STREAM.

The OLD method selects algorithms used in versions 5.0x andearlier. Use this method if you wish to make comparison runswith earlier versions of HEXTRAN. The default is NEW.

PRINT SPLIT FLOW OPTIMIZATION Data Category of Input

Optional statement. This statement sets print options on a global basis. The default is to printall reports except the design MONITOR. Entry of any keyword other than ALL turns off allother reports.

Optional entries:

ALL Print all output reports. No other entries are allowed.

UNITS Print unit operation summaries including both rigorous and short-cut units. Exchanger data sheets are not printed with this option.

ECONOMICS Print economic summary of flowsheet including equipment capi-tal costs and utility costs.

STREAM Print stream data summary.

INTERMEDIATE Print intermediate results. This print option applies only toREGRESSION, OPTIMIZATION and CLEANING CASESTUDYcalculations.

STANDARD Print standard exchanger data sheets. This produces a TEMA-style data sheet for shell and tube, rodbaffle and double pipe ex-changers. An API-style data sheet is produced for air coolersand finned tube exchangers.

EXTENDED Print extended exchanger data sheets. This produces a datasheet with additional performance and mechanical data not in-cluded on the standard data sheet.

ZONES Print zones analysis for each two phase exchanger.

MONITOR Print design monitor report for each “NEW” exchanger. Prints allintermediate design data.

CAUTION: Use of this option can produce lengthy reports foreach new exchanger.

Example:

The following statement would cause only exchanger data and extended data sheets to beprinted.PRINT STANDARD, EXTENDED

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ECONOMICS SPLIT FLOW OPTIMIZATION Data Category of Input

Optional statement. This statement defines economic factors affecting utility cost calculations.

Optional entries:

DAYS=350 The number of days the plant is on stream per year. The defaultis 350.

CURRENCY=USDOLLAR The currency units. This entry is used for printout purposesonly. The default is USDOLLAR.

CAUTION: Do not use the “$” sign in this entry. HEXTRAN willtreat it as a delimiter.

EXCHANGERATE=1.0 The exchange rate expressed as number of currency units perUS dollar. This entry is used for converting any built-in costingdata defaults. The default is 1.0.

UTCOST SPLIT FLOW OPTIMIZATION Data Category of Input

Optional statement. This statement defines the cost of utilities.

Optional entries:

OIL=3.50 The cost of fuel oil in currency units per million energy units.This entry applies only to fired heaters. The default is 3.50USDOLLAR/MM Btu (English), or 9.04 USDOLLAR/MM kcal(metric), or 3.32 USDOLLAR/MM kJ (SI).

GAS=3.50 The cost of fuel gas in currency units per million energy units.This entry applies only to fired heaters. The default is 3.50USDOLLAR/MM Btu (English), 9.04 USDOLLAR/MM kcal (met-ric), or 3.32 USDOLLAR/MM kJ (SI).

ELECTRICITY=0.10 The cost of electricity in currency units per kilowatt-hour. Thisentry applies only to pumps and compressors. The default is0.10 USDOLLAR/kW-hr (English, metric, and SI).

WATER=0.03 The cost of cooling water in currency units per thousand US gal-lons. This entry applies only to water coolers. The default is 0.03USDOLLAR/M gallon (English, metric, and SI)

CAUTION: The volume unit of US gallons is not redefined forMetric and SI units.

HPSTEAM=4.10 The cost of high pressure steam in currency units per thousandweight units. This entry applies only to pumps and compres-sors. The default is 4.10 USDOLLAR/M lb (English), or 9.04USDOLLAR/M kg (metric and SI).

MPSTEAM=3.90 The cost of medium pressure steam in currency units per thou-sand weight units. This entry applies only to pumps and

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compressors. The default is 3.90 USDOLLAR/M lb (English), or8.60 USDOLLAR/M kg (metric and SI).

LPSTEAM=3.60 The cost of low pressure steam in currency units per thousandweight units. This entry applies only to pumps and compres-sors. The default is 3.60 USDOLLAR/M lb (English), or 7.94USDOLLAR/M kg (metric and SI).

REFRIGERANT=0.00 The cost of refrigerant in currency units per million energy units.This entry applies only to coolers. The default is 0.00USDOLLAR/MM Btu (English), 0.00 USDOLLAR/MM kcal (met-ric), or 0.00 USDOLLAR/MM kJ (SI).

HEATINGMEDIUM=0.0 The cost of heating fluid in currency units per million energyunits. This entry applies only to heaters. The default is 0.00USDOLLAR/MM Btu (English), 0.00 USDOLLAR/MM kcal (met-ric), or 0.00 USDOLLAR/MM kJ (SI).

HXCOST SPLIT FLOW OPTIMIZATION Data Category of Input

Optional statement.This statement sets exchanger costing data on a global basis. Exchangercosts are calculated using the costing equation described later on in this Chapter. All entriescan be overridden for specific exchangers using the COST statement.

Optional entries:

BSIZE=1000.0 The base area used in the costing equation. The default is1000.0 ft2 (English), or 93.0 m2 (metric and SI).

BCOST=0.00 The base cost used in the costing equation. The default is 0.00USDOLLAR/ft 2 (English), or 0.00 USDOLLAR/m2 (metric andSI).

LINEAR=50.00 The linear cost factor used in the costing equation. The default is50.00 USDOLLAR/ft2 (English), or 538.20 USDOLLAR/m2 (met-ric and SI).

CONSTANT=0.00 The constant cost factor used in the costing equation. This entrycan be used to define fixed costs associated with installation ofan exchanger and is not a function of exchanger size. The de-fault is 0.00 USDOLLAR (English, metric, and SI).

EXPONENT=0.60 The exponential cost factor used in the costing equation. The de-fault is 0.60 (English, metric, and SI).

UNIT orSHELL

Defines the basis for exchanger CONSTANT cost factor. UNIT re-sults in the constant cost factor being applied once to each unitregardless of the number of shells in the unit. SHELL results inthe constant cost factor being applied to each shell in the unit.The default is UNIT.

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VARIABLE SPLIT FLOW OPTIMIZATION Data Category of Input

Mandatory statement. The VARIABLE statement is used to declare the variable stream splitfractions for the optimization calculations. Multiple VARIABLE statements are allowed, andthey may only refer to product streams from a splitter. At least one VARIABLE statement is re-quired.

Example:VARIABLE STREAM=15, FRACTION=0.25,0.45

STREAM=alphanumberic4

Stream identifier. STREAM defines the stream whose split fraction is to be varied. STREAMmust be a product stream from a splitter. Enter up to 12 alphanumeric characters. This entryis required. There is no default.

STREAM= Stream identifier. STREAM defines the stream whose parameteris to be used as a regression variable. Enter up to 12 alphanu-meric characters. There is no default.

FRACTION= Minimum and maximum stream split fraction. FRACTION indi-cates that the split fraction for stream “STREAM” in a twowaysplitter is to be varied. These entries are optional. There are nodefaults.The starting value for the split fraction, in the unit op-eration section, must be within (but not equal to) the minimumand maximum REGRESSION split fraction.

RESTRICTION: Enter values between 0.01 and 0.99 for both theminimum and maximum split fraction.

RESTRICTION: Tthe FRACTION entry may only refer to a streamfrom a twoway splitter.

Note: Variable splitters require specifications for STREAM, UNITand FRACTION.

CONSTRAINT SPLIT FLOW OPTIMIZATION Data Category of Input

Mandatory statement OPTIMIZATION calculations. This statement places minimum or maxi-mum temperature constraints on exchanger product streams, or maximum (shellside or tube-side) pressure drop constraints on any exchanger in the flowsheet. CONSTRAINT is notavailable for SIMULATION, REGRESSION, and CASESTUDY calculations.

CAUTION: The pressure drop constraints are on a per shell basis.

When temperature constraints are specified, hot streams which are being cooled will not becooled below the specified temperature. Likewise, cold streams which are being heated willnot be heated above the specified temperature.

Optional entries:

STREAM= Stream identifier. STRM defines the stream whose minimum ormaximum temperature is to be limited with a constraint. Enterup to 12 alphanumeric characters. There is no default.

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TEMPERATURE= Stream temperature constraint and tolerance. TEMPERATUREdefines the value of the stream temperature constraint and theabsolute tolerance on the constraint. Enter values for both theconstraint and tolerance. There are no defaults.

UNIT= Unit identifier. UNIT identifies the exchanger identifier, UID,whose shellside or tubeside pressure drop is to be constrained.Enter up to 12 alphanumeric characters. There is no default.

DPTMAX= Tubeside pressure drop constraint and tolerance. DPTMAX de-fines the value of the tubeside pressure drop constraint and theabsolute tolerance on the constraint. Enter values for both theconstraint and tolerance. There are no defaults.

CAUTION: DPTMAX is on a per shell basis.

Note: Both DPTMAX and DPSMAX constraints may be specifiedfor the same UID, if desired.

DPSMAX= Shellside pressure drop constraint and tolerance. DPSMAX de-fines the value of the shellside pressure drop constraint and theabsolute tolerance on the constraint. Enter values for both theconstraint and tolerance. There are no defaults.

CAUTION: DPSMAX is on a per shell basis.

Note: Both DPSMAX and DPTMAX constraints may be specifiedfor the same UID, if desired.

PARAMETER SPLIT FLOW OPTIMIZATION Data Category of Input

Mandatory statement for OPTIMIZATION calculations. This statement estimates of the splitfraction “incremental stepsize” and “range” values for the optimization calculations. PARAME-TER is not available for SIMULATION, REGRESSION, and CASESTUDY calculations.

Optional entries:

FRACTION=0.01,0.50 The incremental stepsize sets the amount by which a streamsplit fraction is varied during the search trials for the optimiza-tion calculations. The range is the estimated change in thestream split fraction from the initial flowsheet estimate to the fi-nal optimized solution. The magnitude of this value controls thesize of the “step” taken by the optimization routines. The defaultvalues (0.01 and 0.50) are sufficient for most applications.

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Area Optimization Category of InputOptimization calculations are basically multiple SIMULATION runs withthe objective being to design all NEW exchangers to meet a specifiedpay-back period. Flowsheets for OPTIMIZATION calculations may becomprised of any combination of shortcut and rigorous unit operations withboth OLD or NEW exchangers (STE and HX). OLD exchangers may ormay not have duty/temperature specifications placed on them. NEWexchangers may be either “fixed” or “free”. Fixed NEW exchangers haveprocess specifications placed on them that determine their size independentof economics and calculated payback. However, the costs of NEW fixedexchangers are included in the calculation of payout periods for freeexchangers. Free NEW exchangers are varied in size by the program untiltheir incremental payouts correspond to the user-supplied value. As freeexchangers vary in size, so the size of fixed NEW exchangers may alsohave to vary in order to maintain their process specifications. This changein size, and hence cost, is charged to the free exchanger that caused it and isincluded in the computation of its payout period. The calculation procedurefollowed during OPTIMIZATION calculations begins with an initialsolution of the network identical to a SIMULATION calculation. Default oruser-supplied estimates for the areas of NEW free exchangers are used tocalculate a heat and material balance around the flowsheet.

The next step is to determine the incremental payout period for eachexchanger in the network that does not have a process specification placedon it. Payouts are calculated by increasing the size of each exchanger inturn and computing the effect on installed capital costs and utility costs. Itcan be seen that for a network of 5 free exchangers it is necessary toperform 6 complete flowsheet solutions in order to determine the initialpayout table.

Following the computation of the initial payout table, the program beginsthe optimization calculation sequence. The first step is to recalculate thepayout periods for the free exchangers only during the initial estimate step.The program then increases the size of each exchanger in turn anddetermines the derivatives of payout as a function of area.

After completion of the derivative steps, the program varies the size of allfree exchangers simultaneously in a number of “search trials”. There are nospecific rules as to how many search trials will be required, but the defaultvalue of 3*Number of free NEW exchangers is a good guide.

The user may adjust the size of the step used by the program at thederivative- taking step by using the PARAMETER statement. Generally, avalue of approximately 20 percent of the smallest exchanger to be variedwill give the best results. The user is also required to supply an estimate ofthe total change in area for all new FREE exchangers as a guide to the

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“range” of the solution path. This estimate does not need to be very preciseas it will be adjusted during calculations. However, a good estimate willreduce solution time. Calculations proceed in the optimization loop untilthe sum-of-the-squares error for the payouts of all free exchangers is lessthan a user-supplied tolerance. Calculations are also terminated if thenumber of search trials reaches a user-defined limit. After leaving theoptimization loop, the program re-designs the NEW exchangers andcompares their new overall heat transfer coefficients with those valuescalculated prior to optimization. If the comparison is within the specifiedU-value tolerance, the desired solution has been reached and the finalresults are printed. If the comparison is outside the tolerance, optimizationcalculations are repeated with the updated U-values. This step is repeateduntil the U-value tolerance is met or the maximum number of trials isreached.

Note: Because the payout calculations are based on savings in utility costs,the flowsheet to be optimized must include at least one of the followingunit operations: HEATER, COOLER, FIREDHEATER, COMPRESSOR orPUMP.

Table 4-29: Area Optimization Category of Input

Statement Keywords See ...

Calculation Type SIMULATION or REGRESSION or OPTIMIZATION or CASESTUDY Page 4-123

{TOLERANCE} {TTRIAL=0.01, STRIAL=0.10 UTRIAL=0.04} Page 4-123

{LIMITS} {AREA=200,6000, SERIES=1,10, PARALLEL=1,10, TDAMP=0.00,PDAMP=0.00, TTRIAL=30, STRIAL, UTRIAL=5}

Page 4-124

{CALCULATION} {MINFT=0.80, NOCHECK, DPSMETHOD=STREAM, INCREMENTAL,TWOPHASE=NEW}

Page 4-125

{PRINT} {ALL, UNITS, ECONOMICS, STREAM, STANDARD, EXTENDED,ZONES, MONITOR, INTERMEDIATE}

Page 4-126

{ECONOMICS} {DAYS=350, EXCHANGERATE=1.0, CURRENCY=USDOLLAR} Page 4-127

{UTCOST} {OIL=3.50, GAS=3.50, ELECTRICITY=0.10, WATER=0.03,HPSTEAM=4.10, MPSTEAM=3.90, LPSTEAM=3.60,REFRIGERANT=0.00, HEATINGMEDIUM=0.00}

Page 4-127

{HXCOST} {BSIZE=1000, BCOST=0.00, LINEAR=50.00, EXPONENT=0.60,CONSTANT=0.00, UNIT or SHELL}

Page 4-128

{SPECIFICATION} {PAYOUT=2.0} Page 4-129

{CONSTRAINT} STREAM, TEMPERATURE Page 4-129

{PARAMETER} {AREA=400,4000} Page 4-130

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PROPERTY AREA OPTIMIZATION Data Category of Input

This entry must be specified. Only one entry is allowed. Each calculation type is described indetail in the following sections.

Mandatory entries:

SIMULATION or Rating of all rigorous exchanger models and design of shell andtube exchangers. See Shell-and-Tube Heat Exchangers later onin this chapter.

REGRESSION or Solution of flowsheets with more specifications than variables.Rating of all rigorous exchanger models. Useful for reconcilingplant data.

OPTIMIZATION AREA or Design of new shell and tube exchangers to meet a specifiedpayout period. Networks can consist of both OLD (Rating) andNEW (Design) exchangers.

OPTIMIZATIONSPLITFLOW or

Solution of flowsheets to minimize utility costs by varying split-ter fractions. Rating of all rigorous exchanger models. Use tomaximize performance of existing networks.

CLEANING CASESTUDY Multiple flowsheet solutions for specified exchanger fouling fac-tors. Use to evaluate effect of cleaning exchangers.

TOLERANCE AREA OPTIMIZATION Data Category of Input

Optional statement. This statement modifies the default tolerance values. The default toler-ances are suitable for most calculations.

Optional entries:

TTRIAL=0.01 Temperature tolerance for flowsheet heat balance convergence.Flowsheet solution is reached when all stream temperatureschange by less than this amount from one iteration to the next.The default is 0.01 F (English), or 0.006 C (metric and SI).

STRIAL=0.10 Search trial tolerance for optimization and regression conver-gence. Final solution of an optimization or regression problem isreached when the error sum is less than STRIAL. The default is0.10.

UTRIAL=0.04 U-value trial tolerance for area optimization convergence. Thisentry applies only to area optimization. The default is 0.04.

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LIMITS AREA OPTIMIZATION Data Category of Input

Optional statement. This statement defines two groups of information relating to limits on thedesign of shell and tube exchangers and limits on flowsheet calculations. Exchanger design lim-its for AREA, SERIES, and PARALLEL are applied on a global basis unless redefined individuallyfor specified STE exchangers (see Shell-and-Tube Heat Exchangers later on in this chapter).

Optional entries:

AREA=200, 6000 Area per shell for “design”. Area is total outside surface for bareand finned tubes. Enter both a minimum and maximum limit for“designing” new exchangers. Entering only one limit is not al-lowed. The default is 200, 6000 ft2 (English), or 19, 557 m2(metric and SI).

Note: For rating shells with an area greater than 6000 ft 2 , theuser must raise the maximum area on the AREA statement. Thiscan also be done on the rigorous exchanger’s TYPE statementwith AREA =.

SERIES=1,10 Number of shells in series per unit. Enter both a minimum andmaximum limit for “designing” new exchangers. This entry hasno effect on old exchangers. The default is 1,10.

RESTRICTION: The SERIES entry may not be used in conjunc-tion with the PARALLEL entry.

PARALLEL=1,10 Number of shells in parallel per unit. Enter both a minimum andmaximum limit for “designing” new exchangers. This entry hasno effect on old exchangers. The default is 1,10.

RESTRICTION: The PARALLEL entry may not be used in con-junction with the SERIES entry.

TDAMP= Fraction of temperature damping. TDAMPING is useful when aflowsheet has difficulties converging and the sum of squares er-ror seems to oscillate between iterations. By default, HEXTRANuses the stream temperature from the previous iteration as anestimate for the next iteration. TDAMP decreases the incre-mental temperature change between iterations by using aweighted average of the current and previous iterationtemperatures.

For example, if TDAMP=0.4, the temperature estimate becomes:

TEMPest = (TEMPprevious) * 0.4 + (TEMPpresent) * 0.6

There are three TDAMP modes:

1. AUTODAMPING By omitting the TDAMP keyword from theinput file, HEXTRAN will automatically use TDAMPINGwhere necessary. Once autodamping starts, HEXTRANadjusts the TDAMP fraction between 0.0 and 0.5 until theflowsheet converges

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2. FIXED DAMPING By specifying a TDAMP fraction, auto-damping is disabled, and the TDAMP fraction is used forevery flowsheet iteration. This is useful when a flowsheetneeds a damping fraction greater than 0.5.

3. NO DAMPING To disable temperature damping, specifyTDAMP=0.0.

PDAMP=0.00 Fraction of pressure damping. Operation and use of PDAMP issimilar to TDAMP (described above), except there is no auto-matic pressure damping mode. The default is 0.00.

TTRIAL=30 Maximum number of flowsheet iterations. The default value (30)is sufficient for most applications. This number may be in-creased to a maximum of 99.

Application: Increase the maximum number of iterations if themaximum temperature error shows a slow convergence. In-creasing the maximum number of iterations will not help if themaximum temperature error shows oscillatory behavior.

STRIAL= Maximum number of search trial iterations. This entry applies toarea optimization, split flow optimization and regression calcula-tions only. The default number of iterations is listed for eachavailable calculation type in the formulas below.

= 3 * Number of New Exchangers (AREA OPTIMIZATION)

= 10 * number of variable splitters (SPLITFLOW OPTIMIZATION)

= 5 * number of variables, or 10, whichever is greater(REGRESSION)

UTRIAL=5 Maximum number of U-value loop iterations. This entry appliesto area optimization only. The default is 5.

CALCULATION AREA OPTIMIZATION Data Category of Input

Optional statement. This statement sets calculation methods for individual exchanges on aglobal basis. Methods can also be selected globally using the CALCULATION statement in theSIMULATION, CASESTUDIES, OPTIMIZATION AREA, OPTIMIZATION SPLIT, or REGRESSIONsections.

Optional entries:

NOCHECK Suppresses HEXTRAN’s geometry consistency checks and pre-vents HEXTRAN from assigning default values to missing ge-ometry data. The main purpose for NOCHECK is to allow theuser to access HTRI or HTFS defaults.

When using NOCHECK, specify either:

■ All exchanger data with HEXTRAN keywords, or.■ ST5/CST2/RKH2 or TASC3

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WARNING: Using NOCHECK with inconsistent or missing ge-ometry data may result in abnormal program termination (divi-sion by zero, overflow, etc.)

DPSMTHOD=keyword The pressure drop method for the shellside calculations. Selecteither STREAM (Will's and Johnston's stream analysis tech-nique) or BELL (Kenneth Bell of Delaware University).

The STREAM method is automatically selected whenTWOPHASE = NEW.

INCREMENTAL Performs incremetnal heat flux calculation. Incremental heat fluxcalculations are preformed by running a series of case studiesafter the initial network is solved. The area is incremented by 5%for each OLD exchanger that does not have a performancespeci-fication (outlet temperature, temperature approach, duty, or out-let liquid quality). The results of each case study are summarizedand reported in tabular form. The default is STREAM.

TWOPHASE=NEW Specifies the methods to be used for thermal and hydraulic cal-culations for all rigorous exchanger. The NEW method utilizesModified Chen vaporization for convective boiling and includespredictions for sub-cooled and film boiling. Condensation meth-ods account for flow regime and gravity versus shear effects.Pressure drops are calculated using a stream analysis basedmethod. The NEW method automatically sets DPSMETHOD =STREAM.

The OLD method selects algorithms used in versions 5.0x andearlier. Use this method if you wish to make comparison runswith earlier versions of HEXTRAN. The default is NEW.

PRINT AREA OPTIMIZATION Data Category of Input

Optional statement. This statement sets print options on a global basis. The default is to printall reports except the design MONITOR. Entry of any keyword other than ALL turns off allother reports.

Optional entries:

ALL Print all output reports. No other entries are allowed.

UNITS Print unit operation summaries including both rigorous and short-cut units. Exchanger data sheets are not printed with this option.

ECONOMICS Print economic summary of flowsheet including equipment capi-tal costs and utility costs.

STREAM Print stream data summary.

INTERMEDIATE Print intermediate results. This print option applies only toREGRESSION, OPTIMIZATION and CLEANING CASESTUDYcalculations.

STANDARD Print standard exchanger data sheets. This produces a TEMA-style data sheet for shell and tube, rodbaffle and double pipe

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exchangers. An API-style data sheet is produced for air coolersand finned tube exchangers.

EXTENDED Print extended exchanger data sheets. This produces a datasheet with additional performance and mechanical data not in-cluded on the standard data sheet.

ZONES Print zones analysis for each two phase exchanger.

MONITOR Print design monitor report for each “NEW” exchanger. Prints allintermediate design data.

CAUTION: Use of this option can produce lengthy reports foreach new exchanger.

Example:

The following statement would cause only exchanger data and extended data sheets to be printed.PRINT STANDARD, EXTENDED

ECONOMICS AREA OPTIMIZATION Data Category of Input

Optional statement. This statement defines economic factors affecting utility cost calculations.

Optional entries:

DAYS=350 The number of days the plant is on stream per year. The defaultis 350.

CURRENCY=USDOLLAR The currency units. This entry is used for printout purposesonly. The default is USDOLLAR.

CAUTION: Do not use the “$” sign in this entry. HEXTRAN willtreat it as a delimiter.

EXCHANGERATE=1.0 The exchange rate expressed as number of currency units perUS dollar. This entry is used for converting any built-in costingdata defaults. The default is 1.0.

UTCOST AREA OPTIMIZATION Data Category of Input

Optional statement. This statement defines the cost of utilities.

Optional entries:

OIL=3.50 The cost of fuel oil in currency units per million energy units.This entry applies only to fired heaters. The default is 3.50USDOLLAR/MM Btu (English), or 9.04 USDOLLAR/MM kcal(metric), or 3.32 USDOLLAR/MM kJ (SI).

GAS=3.50 The cost of fuel gas in currency units per million energy units.This entry applies only to fired heaters. The default is 3.50USDOLLAR/MM Btu (English), 9.04 USDOLLAR/MM kcal (met-ric), or 3.32 USDOLLAR/MM kJ (SI).

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ELECTRICITY=0.10 The cost of electricity in currency units per kilowatt-hour. Thisentry applies only to pumps and compressors. The default is0.10 USDOLLAR/kW-hr (English, metric, and SI).

WATER=0.03 The cost of cooling water in currency units per thousand US gal-lons. This entry applies only to water coolers. The default is 0.03USDOLLAR/M gallon (English, metric, and SI)

CAUTION: The volume unit of US gallons is not redefined forMetric and SI units.

HPSTEAM=4.10 The cost of high pressure steam in currency units per thousandweight units. This entry applies only to pumps and compres-sors. The default is 4.10 USDOLLAR/M lb (English), or 9.04USDOLLAR/M kg (metric and SI).

MPSTEAM=3.90 The cost of medium pressure steam in currency units per thou-sand weight units. This entry applies only to pumps and com-pressors. The default is 3.90 USDOLLAR/M lb (English), or 8.60USDOLLAR/M kg (metric and SI).

LPSTEAM=3.60 The cost of low pressure steam in currency units per thousandweight units. This entry applies only to pumps and compres-sors. The default is 3.60 USDOLLAR/M lb (English), or 7.94USDOLLAR/M kg (metric and SI).

REFRIGERANT=0.00 The cost of refrigerant in currency units per million energy units.This entry applies only to coolers. The default is 0.00USDOLLAR/MM Btu (English), 0.00 USDOLLAR/MM kcal (met-ric), or 0.00 USDOLLAR/MM kJ (SI).

HEATINGMEDIUM=0.0 The cost of heating fluid in currency units per million energyunits. This entry applies only to heaters. The default is 0.00USDOLLAR/MM Btu (English), 0.00 USDOLLAR/MM kcal (met-ric), or 0.00 USDOLLAR/MM kJ (SI).

HXCOST AREA OPTIMIZATION Data Category of Input

Optional statement.This statement sets exchanger costing data on a global basis. Exchangercosts are calculated using the costing equation described later on in this Chapter. All entriescan be overridden for specific exchangers using the COST statement.

Optional entries:

BSIZE=1000.0 The base area used in the costing equation. The default is1000.0 ft2 (English), or 93.0 m2 (metric and SI).

BCOST=0.00 The base cost used in the costing equation. The default is 0.00USDOLLAR/ft 2 (English), or 0.00 USDOLLAR/m2 (metric andSI).

LINEAR=50.00 The linear cost factor used in the costing equation. The default is50.00 USDOLLAR/ft2 (English), or 538.20 USDOLLAR/m2 (met-ric and SI).

CONSTANT=0.00 The constant cost factor used in the costing equation. This entrycan be used to define fixed costs associated with installation of

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an exchanger and is not a function of exchanger size. The de-fault is 0.00 USDOLLAR (English, metric, and SI).

EXPONENT=0.60 The exponential cost factor used in the costing equation. The de-fault is 0.60 (English, metric, and SI).

UNIT orSHELL

Defines the basis for exchanger CONSTANT cost factor. UNIT re-sults in the constant cost factor being applied once to each unitregardless of the number of shells in the unit. SHELL results inthe constant cost factor being applied to each shell in the unit.The default is UNIT.

SPECIFICATION AREA OPTIMIZATION Data Category of Input

Mandatory statement for REGRESSION, CASESTUDY, and OPTIMIZATION calculations. Thisstatement declares the specifications for the Regression calculations. Up to 15 SPECIFICA-TION statements may be included. At least one SPECIFICATION statement is required. SPECI-FICATION is not available for SIMULATION calculations.

PAYOUT Incremental payout period in years. Enter a number greater thanzero.

CONSTRAINT AREA OPTIMIZATION Data Category of Input

Mandatory statement. The CONSTRAINT statement is used to place minimum or maximumtemperature constraints on NEW exchangers. Hot streams which are being cooled will not becooled below the specified temperature. Cold streams being heated will not be heated abovethe specified temperature. The exchanger area will be optimized to the specified payout unlessa constraint is met. Exchangers which meet a constraint limit will have a payout less than thespecified payout.

Optional entries:

STREAM= Stream label. Enter the exit stream label (shellside or tubeside)of a new free exchanger.

TEMPERATURE= Stream temperature constraint and tolerance. Both values mustbe entered. There are no defaults.

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PARAMETER AREA OPTIMIZATION Data Category of Input

Mandatory statement for OPTIMIZATION calculations. This statement estimates of the splitfraction “incremental stepsize” and “range” values for the optimization calculations. PARAME-TER is not available for SIMULATION, REGRESSION, and CASESTUDY calculations.

Optional entries:

AREA=400,4000 The incremental area sets the amount by which an exchanger’sarea is varied during the “derivative” trials. The range is the esti-mated change in an exchanger area from initial estimate to finaloptimized solution. The defaults are 400, 4000 ft 2 (English), or37, 372 m 2 (metric and SI).

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Targeting Category of InputTARGETING uses “pinch” technology to provide numerical and graphicalanalyses of the upper and lower bounds for heat recovery problems. Theuser specifies the heat recovery levels, stream definitions and processconstraints. HEXTRAN prepares case studies and plots to help the engineeridentify the optimal heat recovery level (HRAT). The program calculatesheat transfer area, utility requirements, operating costs and plots compositecurves, and user specified process/economic plots.

HEXTRAN uses a composite heat availability method to calculate thefeasible process heat interchange. The user sets up heat recovery level casesby specifying a Heat Recovery Approach Temperature (HRAT) for eachcase.

For each case, HEXTRAN generates a composite curve plot like Figure4-3. The hot composite curve is obtained by summing the duty availablefrom each hot stream over common temperature intervals. The results areaccumulated for each temperature range beginning at the coldesttemperature reached by any of the hot streams. The cold composite curve isprepared similarly.

Individual streams may be allowed to deviate from the network HRAT byuse of the DHRAT keyword on the stream Statement. See the Stream Datacategory of input section, page 4-.

The two curves are moved independently along the X axis until the closestvertical distance between the curves is equal to the specified HRAT. Thissets the amount of recoverable process heat and utility requirements.

HEXTRAN summarizes the cases and plots the user selected economic andprocess parameters. You can specify the plots from any combination ofHEXTRAN’s 20 economic and process plot parameters.

Table 4-30: Targeting Category of Input

Statement Keywords See ...

{SPEC} {HRAT=0.0,THEATING=, TCOOLING=, QPROCESS=, QHEAT-ING=,QCOOLING=, QUTILITIES=, APROCESS=}

Page 4-133

{PARAMETER} {FILM=100 , UVALUE=50, ALPHA=1.0, EXPONENT=1.0, DELTA=0.0MAT=HRAT}

Page 4-134

{PRINT} {ALL, NONE, DUTY, COMPOSITE, GRAND, CASES, SUMMARY} Page 4-137

{PLOT} X=, Y Page 4-13

{HXCOST} {BSIZE=1000, BCOST=0.0, LINEAR=50.0, EXPONENT=0.6, CON-STANT=0.0}

Page 4-138

{ECONOMICS} {DAYS=350, CURRENCY=USDOLLAR, EXCHANGERATE=1.0,RATE=10.0, LIFE=30}

Page 4-139

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TARGETING TARGETING Category of Input

Mandatory statement. This statement specifies that targeting calculations will be performed.Targeting calculations cannot be used in conjunction with SYNTHESIS or any of theFLOWSHEET calculation options.

Optional entries: None

Example:TARGETING

Figure 4-3: Composite Heating/Cooling Curves

A = HRAT (DTMIN)B = QHEATING (Minimum Heating Utility)C = QCOOLING (Minimum Cooling Utility)D = THEATING (Run-up Temperature)E = TCOOLING (Run-down Temperature)F = QPROCESS (Process-process duty)

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Composite Heating/Cooling Curves

100

0 10 20 30 40 50

200

300

400

500

600“A”

“D”

“E”

“C” “F” “B”

Duty—MMBTU/HR

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SPEC TARGETING Category of Input

Optional statement. This statement specifies the heat recovery of the process streams as afunction of various temperatures, duties, and areas.

Optional entries:

HRAT=0.0 Heat Recovery Approach Temperature. Specifies the minimumtemperature difference, or DTmin, between the hot and coldcomposite heat duty curves (Figure 4-3). HRAT sets the corre-sponding heat recovery level of the network. Enter up to 20positive values in any order. Zero corresponds to the maximumtheoretical duty. To determine feasible bounds for HRAT, first runTARGETING with no specification. The default is 0.0 F (English),0.0 C (metric), or 0.0 K (SI).

Example:SPEC HRAT=0.0,10.0,50.0,100.0

THEATING= Maximum runup temperature for cold streams (Figure 4-3).THEATING is the highest temperature to which cold streamsmay be heated before a heating utility is required. SpecifyTHEATING to set the corresponding heat recovery level of thenetwork. Enter up to 20 values in any order. To determine feasi-ble bounds for THEATING, first run TARGETING with no specifi-cations. There is no default.

TCOOLING= Minimum rundown temperature for hot streams (Figure 4-3).TCOOLING is the lowest temperature to which hot streams maybe cooled before a cooling utility is required. Specify TCOOLINGto set the corresponding heat recovery level of the network. En-ter up to 20 values in any order. To determine feasible boundsfor TCOOLING, first run TARGETING with no specifications.There is no default.

QPROCESS= Process-process duty. QPROCESS is the duty exchanged be-tween hot and cold process streams in a network (Figure 4-3).Specify QPROCESS directly as the heat recovery level of the net-work. Enter up to 20 positive values in any order. To determinefeasible bounds for QPROCESS, first run TARGETING with nospecifications.

QHEATING= Heating utility duty. QHEATING is the supplemental duty requiredto heat cold streams (Figure 4-3) above the maximum runuptemperature (Figure 4-3). Specify QHEATING to set the corre-sponding heat recovery level of the network. Enter up to 20positive values in any order. To determine feasible bounds forQHEATING, first run TARGETING with no specifications. There isno default.

QCOOLING= Cooling utility duty. QCOOLING is the supplemental duty re-quired to cool hot streams below the minimum rundown tem-perature (Figure 4-3). Specify QCOOLING to set thecorresponding heat recovery level of the network. Enter up to 20

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positive values in any order. To determine feasible bounds forQCOOLING, first run TARGETING with no specifications. There isno default.

QUTILITIES= Total utilities duty. QUTILITIES is the sum of the heating utilityduty (QHEATING) and the cooling utility duty (QCOOLING).Specify QUTILITIES to set the corresponding heat recovery levelof the network. Enter up to 20 positive values in any order. Todetermine feasible bounds for QUTILITIES, first run TARGETINGwith no specifications. There is no default.

APROCESS= Process-process heat transfer surface area. APROCESS is thearea required to exchange the duty between hot and cold pro-cess streams (Equation 4-26). Specify APROCESS to set thecorresponding heat recovery level of the network. Enter up to 20positive values in any order. To determine feasible bounds forAPROCESS, first run TARGETING with no specifications. Thereis no default.

Note: If the specified area is “actual”, then use an area efficiencyfactor (see PARAMETER statement). Otherwise, APROCESS isassumed to be the “minimum” (target) area of the network.

Note: Solution of AREA specifications is an iterative procedurethat requires significantly more computer time than otherspecifications.

PARAMETER TARGETING Category of Input

Optional statement. This statement defines various heat transfer coefficients and area efficien-cies for targeting calculations.

Optional entries:

FILM=100 Film heat transfer coefficient. FILM is the stream “film and foul-ing” coefficient used to calculate the overall heat transfer coeffi-cient (U-value) for the network. The U-value is used for calculatingduty, area and MTD. Enter an average value to be assigned to allprocess and utility streams. This global value may be overriddenby individual film coefficients on a stream-by-stream basis (seeStream Data section). The default is 100.0 Btu/hr-ft 2 -F (English),488.2 kcal/hr 2 -C (metric), or 567.8 W/m 2 -K (SI).

Note: UVALUE may be used instead of FILM to specify the net-work U-value.

UVALUE=50 Overall heat transfer coefficient. UVALUE is the average (area-weighted) U-value for the network. Enter an average value foruse in calculating duty, area and MTD. This global value may beoverridden by individual film coefficients on a stream-by-streambasis (See Stream Data). The default is 50.0 Btu-hr-ft 2 -F (Eng-lish), 244.1 kcal-hr-m 2 -C (metric), or 283.9 W/m 2 -K (SI).

Note: FILM may be used instead of UVALUE to specify the net-work U-value.

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ALPHA=1.0 Linear area efficiency factor. ALPHA is the ratio of “minimum”(target) network area to the “actual” network area (Equation4-1). Enter a value ( )0 1< ≤α 0 to 1, and use ALPHA to estimateactual network surface area. The default value of 1.0 represents100% efficiency.

Note: EXPONENT may be used in conjunction with ALPHA andDELTA for more accurate estimating.

EXPONENT=1.0 Exponential area efficiency factor. EXPONENT is the value towhich the “minimum” (target) network area is raised to calculatethe “actual” network area (Equation 4-26). Enter a value( exp )1 2< < 1 to 2, and use EXPONENT to estimate the actualnetwork surface area. The default value of 1.0 represents 100%efficiency.

Note: EXPONENT may be used in conjunction with ALPHA andDELTA for more accurate estimating.

DELTA=0.0 Incremental area efficiency factor. DELTA is the value to which the“minimum” (target) network area is added to calculate the “ac-tual” network area (Equation 4-26). Enter a value( )0 1000000< <∆ and use DELTA to estimate the actual networksurface area. The default value 0.0 ft 2 (English) = 0.0 m 2 (met-ric and SI) of zero represents 100% efficiency.

A Aactual minimum=

+1

αδε

where:

Aactual = the actual network area (APROCESS)α = the linear (inverse) area efficiency factor (ALPHA)ε = the exponential area efficiency factor (EXPONENT)δ = the incremental area efficiency factor (DELTA).

UMAT=HRAT Utility Minimum Approach Temperature. The default is HRAT.

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Table 4-31: Allowable Keywords for X and Y

Keyword Definition

HRAT Heat Recovery Approach Temperature

THEATING Minimum runup temperature for hot streams

TCOOLING Maximum runup temperature for cold streams

MTD Network Mean Temperature Difference

QPROCESS Process-process duty

QHEATING Heating utility duty

QCOOLING Cooling utility duty

QUTILITIES Total utilities duty (QH & QC)

APROCESS Process-process heat transfer surface area

AHEATING Heating utility heat transfer surface area

ACOOLING Cooling utility heat transfer surface area

AUTILITIES Total utilities heat transfer surface area

ATOTAL Total network heat transfer surface area

UVALUE Average network U-value

CPROCESS Process-process capital cost

CHEATING Heating utility capital cost

CCOOLING Cooling utility capital cost

CUTILITIES Total utilities capital cost

CTOTAL Total network capital cost

OHEATING Annual heating utility operating cost

OCOOLING Annual cooling utility operating cost

OUTILITIES Annual total utilities operating cost

ANNUAL Annualized network cost

PAYOUT Incremental payout period between cases

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PRINT TARGETING Category of Input

Optional statement. This statement sets print options. Entry of any other keyword turns off allreports except those specified. The default is ALL.

Optional entries:

ALL Prints all results. ALL is the default.

NONE Suppresses printout of all tables, curves and summaries.

Note: Do not use NONE unless the PLOT Statement is used.

DUTY Prints Total Duty, Individual Duty, and Cumulative Duty Tables.

COMPOSITE Prints Composite Duty Table, Composite Duty Curves, and Tem-perature Difference Table.

GRAND Prints Grand Composite Table and Grand Composite Curves.

CASES Prints detailed results for all cases.

SUMMARY Prints summary of results for all cases.

PLOT TARGETING Category of Input

Optional statement. This statement specifies the axis plot variable for keywords. Specify an Xkeyword and a Y keyword for each PLOT statement you enter. You can enter up to 100 sepa-rate PLOT statements.

Mandatory entries:

X= Specifies the X-variable. Select only one keyword (Table 4-31)for each PLOT Statement used. There is no default.

Y= Specifies the Y-variable. Select only one keyword (Table 4-31)for each PLOT Statement used. There is no default.

Examples:PLOT X=HRAT,Y=QPROCESSPLOT X=QPROCESS,Y=APROCESS

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HXCOST TARGETING Category of Input

Optional statement. This statement sets factors used in the cost equation (see eq. (2)) for pro-cess - process exchange area.

Optional entries:

BSIZE=1000 Base exchanger area. BSIZE is used in the general costing equa-tion to estimate the capital cost of network surface area (eq.(2)). Enter a positive value to account for the base cost of sur-face area. Use with BCOST. The default is 1000.0 ft2 (English) or9.29 m 2 (metric and SI).

BCOST=0.0 Base exchanger cost. BCOST is used in the general costingequation to estimate the capital cost of network surface area(eq. (2)). Enter a positive value to account for the base cost ofsurface area. Use with BSIZE. The default is 0.0 USDOLLAR/ft 2

(English) or 0.0 USDOLLAR/m2 (metric and SI). The defaulteliminates the base cost contribution.

LINEAR=50 Linear cost factor. LINEAR is used in the general costing equa-tion to estimate the capital cost of network surface area (eq.(2)). Enter a positive value to account for the linear cost of sur-face area. The default is 50.00 USDOLLAR/ft 2 (English) or538.00 USDOLLAR/m 2 (metric and SI).

EXPONENT=0.6 Exponential cost factor. EXPONENT is used in the general cost-ing equation to estimate the capital cost of network surface area(eq. (2)). Enter a positive or negative value to account for the ex-ponential cost of surface area. The default is 0.6.

CONSTANT=0.0 Constant cost factor. CONSTANT is used in the general costingequation to estimate the capital cost of network surface area(eq. (2)). Enter a positive value to account for the constant costof surface area. The default value (0.0) eliminates the constantcost contribution.

General Costing Equation to Estimate Capital Cost of Network Surface Area: (2)

C A C A A Atotal total base base total base= + +λ ε γ( ) ( ( ) ( ))

where:

Ctotal = the total process-process capital cost (PROCESS)Cbase = the base process-process capital cost (BCOST)Atotal = the total process-process heat transfer surface area (APROCESS)Abase = the base process-process heat transfer surface area (BSIZE)� = the linear cost factor (LINEAR)ε = the exponential cost factor (EXPONENT)γ = the constant cost factor (CONSTANT)

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ECONOMICS TARGETING Category of Input

Optional statement. This statement specifies economic parameters used in the COSTcalculations.

Optional entries:

DAYS=350 On-stream factor. DAYS is the number of days the plant is onstream per year. Used for calculating annual utility consumptionand operating costs. Enter a positive integer less than 366 daysper year. The default is 350 days/year.

CURRENCY=USDOLLAR Currency units. CURRENCY is the currency units for costingdata and the currency label for printout. The default isUSDOLLAR.

EXCHANGERATE=1.0 Exchange rate. EXCHANGERATE is the exchange rate expressedas the number of currency units per US Dollar. Enter a positivevalue for converting any built-in costing data defaults. The de-fault is 1.0 currency/USDOLLAR.

RATE=10.0 Discount or interest rate of return. RATE is the interest rate usedto determine the capital recovery factor and the annualized net-work cost (eq. (3)). Enter as a percent or decimal fraction.Thedefault is 10.0 percent.

LIFE=30 Project life. LIFE is the estimated economic life of the projectused to determine the capital recovery factor and the annualizednetwork cost (eq. (3)). Enter a positive integer in years. The de-fault is 30 years.

Annualized Network Costing Equation: (3)

Ca = Co + Cc (crf))where: R

Ca = the annualized network cost (ANNUAL)Co = the annual total operating cost (OUTILITIES)Cc = the total network capital cost (CTOTAL)crf = the capital recovery factor defined by:

cfri i

i= +

+ −( )

( )1

1 1

η

η

where:

i = the discount or interest rate of return (RATE)η = the project life (LIFE)

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HRAT ModificationIn TARGETING runs, it is possible to modify an individual stream’s HRAT with a DHRAT speci-fication on the PROCESS Statement in the STREAM data section, page 4-. This is useful formodelling streams which exchange heat through a heating medium or third party stream.DHRAT takes into consideration the extra temperature differences which must be maintainedbetween the three streams.

A negative DHRAT value is also acceptable. Reducing the minimum approach temperature withDHRAT selectively upgrades the value of the heat in the system.

Restriction: HRAT and DHRAT must be greater than zero.

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Synthesis Category of InputSYNTHESIS generates optimal networks which contain the minimumnumber of exchangers for a specified heat recovery level. The program isdriven to the minimum equipment requirements, by user specifications fornetwork heat recovery approach temperature (HRAT) and exchangerminimum approach temperature (EMAT). From a single input file,HEXTRAN will perform up to 20 case studies to evaluate the bestcombinations of EMAT and HRAT.

Although SYNTHESIS’ objective is to minimize the required heatexchanger equipment, it also produces networks in the optimum costregion. Process heat exchangers are costed on the basis of their area with ageneralized costing equation. Utility exchangers are costed on the basis oftheir area or duty. Utility costs are accounted for on the UTILITY STRMstatement (see the Stream Data section).

SYNTHESIS uses a modified Temperature Interval method. Hot and coldstreams are ranked by order of decreasing heat capacity flow rates.Temperature boundaries are determined from the user specified inlet andoutlet stream temperatures. Within each pair of boundaries, hot and coldstreams are matched to form a subnetwork. Where possible, adjacentsubnetworks are integrated. HEXTRAN performs additional fine tuninguntil it gets as close as possible to the minimum number of exchangers (No.of Hot Streams + No. of Cold Streams+ No. of Utilities - 1).

The network is further reduced through loop breaking and stream splitting.Split flow networks are produced only if they reduce the number ofrequired exchangers.

Once the network is designed, SYNTHESIS sizes the exchangers with theuser supplied or default film coefficients. Shells are added in series tocomply with the minimum LMTD correction factor, FT. If a maximumshell area is specified, shells are added in parallel and series as needed.

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Table 4-32: Synthesis Category of Input

Statement Keywords See ...

SYNTHESIS Page 4-142

{SPEC} HRAT=,EMAT Page 4-142

{PARAMETER} {FILM=100, UVALUE=50} Page 4-143

{PRINT} {SPLIT=SHORT, UNSPLIT=LAST} Page 4-144

{PLOT} {ALL, HOT, COLD, WIDE, C1, C2, C3, C4, C5, C6, C7, C8, C9,C10

Page 4-144

{HXCOST} {BSIZE=1000, BCOST=0.0, LINEAR=50.0, EXPONENT=0.6,CONSTANT=0.0, UNIT, SHELL}

Page 4-142

{ECONOMICS} {DAYS=350, CURRENCY=USDOLLAR, EXCHANGERATE=1.0} Page 4-146

{LIMITS} {MAXP=10, MAXS=10, MAXAREA=6000, MINFT=0.8, FT1} Page 4-147

SYNTHESIS SYNTHESIS Category of Input

Mandatory statement. This statement specifies that Synthesis calculations will be performed.SYNTHESIS calculations cannot be used in conjunction with TARGETING or any of the flow-sheet calculation options.

SPEC SYNTHESIS Category of Input

Mandatory statement. This statement specifies the heat recovery of the process streams(HRAT) and the exchanger minimum approach temperature (EMAT).

Mandatory entries:

HRAT= Heat Recovery Approach Temperature. HRAT is the minimumtemperature difference, or DTmin between the hot and coldcomposite heat duty curves (Figure 4-3, page 4-132). SpecifyHRAT to set the corresponding heat recovery level of the net-work. To determine feasible bounds for HRAT, first runTARGETING with no specification. Enter up to 20 positive valuesin any order. Valid units are F (English), C (metric), or K (SI).There is no default.

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EMAT= The Exchanger Minimum Approach Temperature. This entry setsthe minimum approach temperature used for any exchanger inthe network. When the final network is calculated, one ex-changer will have its approach temperature equal to EMAT, whileall other exchangers will have approach temperatures greaterthan EMAT. EMAT usually occurs in an exchanger near the net-work’s pinch point. One EMAT value must be specified for eachHRAT value. EMAT must be less than or equal to the HRAT value.However, it is generally not advised to make it equal to HRAT.There is no default.

Examples:SPEC HRAT= 10.0, 50.0, 100.0,*

EMAT= 5.0, 25.0, 50.0

PARAMETER SYNTHESIS Category of Input

Optional statement. This statement defines the film coefficient for each stream.

Optional entries:

FILM=100 Film heat transfer coefficient. FILM is the stream ‘‘film and foul-ing’’ coefficient used to calculate the overall heat transfer coeffi-cient (U-value) for each exchanger. Enter an average value to beassigned to all process and utility streams. The global value maybe overridden by individual stream film coefficients (see StreamData section). The default is 100.0 Btu/hr-ft 2 - o F (English), or488.2 kcal/hr-m 2 -C (metric), or 567.8 Watts/m 2 -K (SI).

Note: UVALUE may be used instead of FILM.

UVALUE=50 Overall heat transfer coefficient. UVALUE is the average (area-weighted) U-value for the network. Enter an average value foruse in calculating duty, area and MTD. The global value may beoverridden by individual stream film coefficients (see the StreamData category of input, page 4-38). The default is 50.0 Btu/hr-ft2 - o F (English), or 244.1 kcal/hr-m 2 -C (metric), or 283.9Watts/m 2 -K (SI).

Note: FILM may be used instead of UVALUE.

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PRINT SYNTHESIS Category of Input

Optional statement. This statement controls the reports for split and unsplit networks.

Optional statements:

SPLIT=SHORT Split network print options. Enter an acceptable keyword fromTable 4-33.

UNSPLIT=LAST Unsplit network print options. Enter an acceptable keyword fromTable 4-33.

Table 4-33: Print Option Keywords

SHORT Short intermediate printout of each network followed by a full output ofthe network containing the mimimum number of services. The short in-termediate printout provides a list including the number of shells, thenumber of splits, total area, total duty, total exchanger cost, and the utilityconsumption cost.

ALL Allows every network generated to be printed in full. This option will pro-duce a lot of output and increase the computation time.

NONE Suppresses all output. Do not use for both the unsplit and split entries.

LAST Allows only the network with the minimum number of services to beprinted.

PLOT SYNTHESIS Category of Input

Optional statement. This statement specifies network plots that diagram the connectivity of the syn-thesized networks. A plot is produced for each network that is specified on the PRINT statement.

Optional entries:

ALL Plot networks for all hot streams and all cold streams.

HOT Plot networks for all hot streams and connected cold streams.

COLD Plot networks for all cold streams and connected hot streams.

WIDE Plot networks using full 132 character width. Default plots use72 character width.

WARNING: Wide plots cannot be properly viewed on a standard80 character display terminal.

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C1, C2, C3, C4,C5, C6, C7, C8,C9, C10=

Character entry. In producing printer plots, some special charac-ters are used to depict the streams and their directions of flow.Different computers and printers may not have the same charac-ters available. Various plot characters can be selected throughinput on the PLOT statement.

C1 = - Horizontal stream connectorC2 = | Vertical stream connectorC3 = | Vertical at right upper cornerC4 = < Horizontal after right upper cornerC5 = V Vertical at right lower corner. Also,

vertical at splitter cornerC6 = - Horizontal after right lower cornerC7 = - Horizontal after splitter cornerC8 = > End of left horizontal streamC9 = < End of right horizontal streamC10 = [ Line crossing

Note: The CHARACTER instruction cannot be continued onto asecond line. The delimiters ‘‘= ’’*", and ‘‘,’’ cannot be used asplot symbols. The other delimiters ‘‘/’’, ‘‘(’’, ‘‘)’’, and ‘‘$’’ can beused.

HXCOST SYNTHESIS Category of Input

Optional statement. This statement sets factors used in the cost equation (see Figure 4-27) forprocess - process exchange area.

Optional entries:

BSIZE=1000 Base exchanger area. BSIZE is used in the general costing equa-tion to estimate the capital cost of network surface area (eq.(4)). Enter a positive value to account for the base cost of sur-face area. Use with BCOST. The default is 1000.0 ft 2 (English) or9.29 m 2 (metric and SI).

BCOST=0.0 Base exchanger cost. BCOST is used in the general costingequation to estimate the capital cost of network surface area(eq. (4)). Enter a positive value to account for the base cost ofsurface area. Use with BSIZE. The default is 0.0 USDOLLAR/ft 2

(English) or 0.0 USDOLLAR/m 2 (metric and SI). The defaulteliminates the base cost contribution.

LINEAR=50 Linear cost factor. LINEAR is used in the general costing equa-tion to estimate the capital cost of network surface area (eq.(4)). Enter a positive value to account for the linear cost of sur-face area. The default is 50.00 USDOLLAR/ft 2 (English) or538.00 USDOLLAR/m 2 (metric and SI).

EXPONENT=0.6 Exponential cost factor. EXPONENT is used in the general cost-ing equation to estimate the capital cost of network surface area(eq. (4)). Enter a positive or negative value to account for the ex-ponential cost of surface area. The default is 0.6.

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CONSTANT=0.0 Constant cost factor. CONSTANT is used in the general costingequation to estimate the capital cost of network surface area(eq. (4)). Enter a positive value to account for the constant costof surface area. The default value (0.0) eliminates the constantcost contribution.

(4)

C A C A A A Ctotal total base base total base= + +λ ε γ (( ) ( ( ) ( )) SCALER )

where:

Ctotal = the total process-process capital cost (PROCESS)Cbase = the base process-process capital cost (BCOST)Atotal = the total process-process heat transfer surface area (APROCESS)Abase = the base process-process heat transfer surface area (BSIZE)λ = the linear cost factor (LINEAR)ε = the exponential cost factor (EXPONENT)γ = the constant cost factor (CONSTANT)

CSCALER = the stream cost function (see the Stream Data category of input, page 4-38

ECONOMICS SYNTHESIS Category of Input

Optional statement. This statement specifies economic parameters used in the COSTcalculations.

Optional entries:

DAYS=350 On-stream factor. DAYS is the number of days the plant is onstream per year. Used for calculating annual utility consumptionand operating costs. Enter a positive integer less than 366 daysper year. The default is 350 days/year.

CURRENCY=USDOLLAR Currency units. CURRENCY is the currency units for costingdata and the currency label for printout. The default isUSDOLLAR.

EXCHANGERATE=1.0 Exchange rate. EXCHANGERATE is the exchange rate expressedas the number of currency units per US Dollar. Enter a positivevalue for converting any built-in costing data defaults. The de-fault is 1.0 currency/USDOLLAR.

RATE=10.0 Discount or interest rate of return. RATE is the interest rate usedto determine the capital recovery factor and the annualized net-work cost (eq. (4)). Enter as a percent or decimal fraction.Thedefault is 10.0 percent.

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LIMITS SYNTHESIS Category of Input

Optional statement. This statement imposes limits on the exchanger design.

Optional entries:

MAXP=10 The maximum allowable number of exchanger shells in parallelin any one service. Any value entered greater than 10 is set to10.

MAXS=10 The maximum allowable number of exchanger shells in series inany one service. Any value entered greater than 10 is set to 10.

MAXAREA=6000 The maximum area of one exchanger shell. The maximum areais never violated unless both the limitations on maximum shellin series and maximum shells in parallel are reached. The defaultis 6000 ft 2 (English), or 55.7 m 2 (metric and SI).

MINFT=0.8 The minimum log-mean temperature correction factor. The mini-mum FT factor supplied is never violated unless the limitationimposed on the maximum number of shells in series has beenmet. In this case, the FT factor is set to the minimum FT factorgiven and a warning message is printed. The default is 0.8.

FT1 This option suppresses FT factor calculations and uses a globalFT factor of 1.0 for all exchangers in the flowsheet.

Additional Features

SYNTHESIS models several stream selective process and economic constraints:

CSCALER Multiplier for HXCOST, eq. (4).

NOSPLIT Prevents SYNTHESIS from splitting the stream.

NOUTILITY SYNTHESIS tries not to match the stream with any utilities.

SINGLE Matches a stream with only one other stream.

TADDITIONAL Provides additional temperature points for streams with phasechange. TSPLIT The minimum temperature for a split hot or coldstream.

For a more detailed discussion of these constraints, please see the Stream Data category of in-put page 4-38.

Film coefficients may be entered as a global value, or on a stream by stream basis. The streamfilm is entered as an average value on the PROPERTY statement in the STREAM DATA cate-gory of input,, or as film versus temperature points in the EXTERNAL DATA category of input,page 4-67. Use of temperature sensitive film data produces more accurate exchanger sizingfor condensing and vaporizing streams.

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Unit Operations Category of InputThe Unit Operations Category of input allows unit operations to beincluded in a simulation. The general format for input is:

unitKeyword NAME=statementName keywords...

statementName keywords...

Table 4-34: Unit Operations Category of Input

Statement Keywords See ...

)

STE UID=, {NAME=, Rating only: REFUNIT= } Page 4-16

TYPE Rating only: OLD,Design only: NEW,TEMA=AES, {HOTSIDE=SHELL, ORIENTATION=HORIZONTAL,FLOW=COUNTERCURRENT,Rating only: AREA=1000.0,Design only: AREA=200.0, 6000.0,UESTIMATE=50.0, UVALUE=, USCALER=1.0}

Page 4-165

TUBESIDE FEED=, PRODUCT=,Rating only: {LENGTH=20.0Design only: {LENGTH=8.0,20.0,4.0,OD=0.75, ID= 0.584 or BWG=14 or THICKNESS=0.083, NUMBER=257,

Rating only: PASS=2,Design only: PASS=2, 16, 2,PATTERN=90, PITCH=1.0, MATERIAL=01, DENSITY=490.8,CONDUCTIVITY=30.0, FOUL=0.002, LAYER=0.0, HI= orHSCALER=1.0,Design only: VELOCITY=0,1000,Rating only: DPSHELL= or DPUNIT=,Design only: DPSHELL=5.0, 15.0 or DPUNIT=, DPSCALER=1.0,PDESIGN=, TDESIGN=}

Page 4-170

{FINS} NUMBER=19.0, {ROOT=0.625, THICKNESS=0.026, HEIGHT=0.0625,AREA=0.508, EFFICIENCY=}

Page 4-174

SHELLSIDE FEED=, PRODUCT=,Rating only: {ID=23.0, SERIES=1, PARALLEL=1,Design only: {ID=8.0, 60.0, SERIES=1, 10, PARALLEL=1, 10,SEALS=, MATERIAL=01, DENSITY=490.8, FOUL=0.002, LAYER=0.0,HO= or HSCALER=1.0,Design only: VELOCITY=0,1000,Rating only: DPSHELL= or DPUNIT=,Design only: DPSHELL=5.0, 15.0 or DPUNIT=,DPSCALER=1.0, PDESIGN=, TDESIGN=}

Page 4-177

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Table 4-34: Unit Operations Category of Input

Statement Keywords See ...

{BAFFLE} NONE or SEGMENTAL=SINGLE,Rating only: {CUT=0.20, NFAR=0.14, SPACING=4.6, INSPACING=,OUTSPACING=,Design only: {CUT=0.2, 0.2, NFAR=0.14,0.14, SPACING=,THICKNESS=0.1875, SHEETS=}

Page 4-181

{TNOZZLE} {ID=, NUMBER=1, 1, NONE, TYPE=CONVENTIONAL} Page 4-188

{SNOZZLE} {ID=, NUMBER=1, 1, NONE, TYPE=CONVENTIONAL, AREA=,LENGTH=, CLEARANCE=}

Page 4-188

{INOZZLE} {ID=, NUMBER=0} Page 4-189

{LNOZZLE} {ID=, NUMBER=0} Page 4-190

{ST5 and/orCST3 and/orRKH3} or

HTRI only Page 4-190

{TASC3} HTFS only Page 4-190

{CALCULATION} {NOCHECK, MINFT=0.8, DPSMETHOD=STREAM, TWOPHASE=NEW} Page 4-191

SPECIFICATION(Optional for Rating)

TEMPERATURE=, and HOT or COLD or SHELL or TUBEor LFRAC=, and HOT or COLD or SHELL or TUBE orDUTY= or HOCI= or COCI= or HIHO=, or HICO=

Page 4-191

{PRINT} {STANDARD, EXTENDED, ZONES, MONITOR} Page 4-193

{COST} {BSIZE=1000.0, BCOST=0.0, LINEAR=50.0, EXPONENT=0.6,CONSTANT=0.0, UNIT or SHELL}

Page 4-193

)

RBERating only

UID=, {NAME=, REFUNIT=} Page 4-195

TYPE OLD, {TEMA=AES, HOTSIDE=SHELL, ORIENTATION=HORIZONTAL,FLOW=COUNTERCURRENT, AREA=1000, UESTIMATE=50, US-CALER=1.0}

Page 4-196

TUBESIDE FEED=, PRODUCT=, {LENGTH=20, OD=0.75, ID=0.584 or BWG=14or THICKNESS=0.083, NUMBER=254, PASS=2, PATTERN=90,PITCH=1.00, MATERIAL=01, DENSITY=490.8, CONDUCTIVITY=30.0,FOUL=0.002, LAYER=0.0, HI=, or HSCALER=1.0, DPSHELL=,DPUNIT=, DPSCALER=1.0, PDESIGN=}

Page 4-197

SHELLSIDE FEED=, PRODUCT=, {ID=23.0, SERIES=1, PARALLEL=1, MATE-RIAL=01, DENSITY=490.8, FOUL=0.002, LAYER=0.0, HO orHSCALER=1.0, DPSHELL= or DPUNIT=, DPSCALER=1.0, PDESIGN=}

Page 4-199

BAFFLE {SPACING=4.6, THICKNESS=1.00, SHEETS=4.0, CLEARANCE=0.125,TYPE=RING}

Page 4-201

{TNOZZLE} {ID=, NONE} Page 4-201

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Table 4-34: Unit Operations Category of Input

Statement Keywords See ...

{SNOZZLE} {TYPE=CONVENTIONAL, ID=, LENGTH=, AREA=, CLEARANCE, NONE} Page 4-202

{ST5 and/orCST3 and/orRKH3} or

HTRI onlySee the HEXTRANHTRI and HTRSInput Guides

{TASC3} HTFS only

{CALCULATION} {NOCHECK, TWOPHASE=NEW} Page 4-202

{SPECIFICATION} TEMPERATURE=, and HOT or COLD or SHELL or TUBE or LFRAC=,and HOT or COLD or DUTY= or HOCI= or COCI= or HIHO=, or HICO=

Page 4-203

{PRINT} {STANDARD, EXTENDED, ZONES} Page 4-204

{COST} {BSIZE=1000, BCOST=0.0, LINEAR=50, EXPONENT=0.6,CONSTANT=0.0, UNIT, SHELL}

Page 4-204

)

DPERating only

UID=, {NAME=} Page 4-206

TYPE OLD, {HOTSIDE=SHELL, ORIENTATION=HORIZONTAL,FLOW=COUNTERCURRENT, AREA=23.6, UESTIMATE=50,USCALER=1.0}

Page 4-207

TUBESIDE FEED=, PRODUCT=, {LENGTH=20, OD=4.50, ID=4.026,THICKNESS=0.237, NPS=, SCHEDULE=, BWG=, MATERIAL=01,DENSITY=490.8, CONDUCTIVITY=30.0, FOUL=0.002, LAYER=0.0, HI=,or HSCALER=1.0, DPSHELL=, DPUNIT=, DPSCALER=1.0, PDESIGN=}

Page 4-208

{FINS} NUMBER=24, {HEIGHT=0.7815, MATERIAL=01, CONDUCTIVITY=30.0,THICKNESS=0.050, AREA=, EFFICIENCY=}

Page 4-210

SHELLSIDE FEED=, PRODUCT=, {ID=6.065, NPS=, SCHEDULE=, SERIES=1,PARALLEL=1, MATERIAL=01, DENSITY=490.8, FOUL=0.002,LAYER=0.0, HO or HSCALER=1.0, DPSHELL= or DPUNIT=,DPSCALER=1.0, PDESIGN=}

Page 4-211

{TNOZZLE} {ID=, NONE} Page 4-212

{SNOZZLE} {ID=, NONE} Page 4-213

{CALCULATION} {NOCHECK, TWOPHASE=NEW} Page 4-213

{SPECIFICATION} TEMPERATURE=, and HOT or COLD or SHELL or TUBE or LFRAC=,and HOT or COLD or DUTY= or HOCI= or COCI= or HIHO=, or HICO=

Page 4-214

{PRINT} {STANDARD, EXTENDED, ZONES} Page 4-215

{COST} {BSIZE=1000, BCOST=0.0, LINEAR=50, EXPONENT=0.6,CONSTANT=0.0, UNIT, SHELL}

Page 4-215

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Table 4-34: Unit Operations Category of Input

Statement Keywords See ...

)

MTERating only

UID=, {NAME=, REFUNIT=} Page 4-217

TYPE OLD, {HOTSIDE=SHELL, ORIENTATION=HORIZONTAL,FLOW=COUNTERCURRENT, AREA=27.0, UESTIMATE=50,USCALER=1.0}

Page 4-218

TUBESIDE FEED=, PRODUCT=, {LENGTH=20, OD=4.50, ID=4.026 orTHICKNESS=0.237 or BWG= or (NPS= and SCHEDULE=), PITCH=1.00,PATTERN=90, NUMBER=7, MATERIAL=01, DENSITY=490.8,CONDUCTIVITY=30.0, FOUL=0.002, LAYER=0.0, HI=, orHSCALER=1.0, DPSHELL= or DPUNIT=, DPSCALER=1.0, PDESIGN=}

Page 4-219

{FINS} NUMBER=24, {HEIGHT=0.12, MATERIAL=01, CONDUCTIVITY=30.0,THICKNESS=0.050, AREA=, EFFICIENCY=}

Page 4-221

SHELLSIDE FEED=, PRODUCT=, {ID=6.065 or (NPS= and SCHEDULE=), SERIES=1,PARALLEL=1, MATERIAL=01, DENSITY=490.8, FOUL=0.002,LAYER=0.0, HO or HSCALER=1.0, DPSHELL= or DPUNIT=,DPSCALER=1.0, PDESIGN=}

Page 4-222

{TNOZZLE} {ID=, NONE} Page 4-223

{SNOZZLE} {ID=, NONE} Page 4-224

{CALCULATION} {NOCHECK, MINFT=0.8, TWOPHASE=NEW} Page 4-224

{PRINT} {STANDARD, EXTENDED, ZONES} Page 4-226

{SPECIFICATION} TEMPERATURE=, and SHELL or TUBE or HOT or COLDor LFRAC=, andHOT or COLD or SHELL or TUBE or DUTY= or HOCI= or COCI= orHIHO=, or HICO=

Page 4-225

{COST} {BSIZE=1000, BCOST=0.0, LINEAR=50, EXPONENT=0.6,CONSTANT=0.0, UNIT or SHELL}

Page 4-227

)

FTE UID=, {NAME=,Rating only: REFUNIT= }

Page 4-228

TYPE Rating only: OLD,Design only: NEW,{HOTSIDE=SHELL, ORIENTATION=HORIZONTAL,FLOW=COUNTERCURRENT,Rating only: AREA=1000.0,Design only: AREA=200.0, 6000.0,UESTIMATE=50.0, UVALUE=, USCALER=1.0}

Page 4-231

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Table 4-34: Unit Operations Category of Input

Statement Keywords See ...

TUBESIDE FEED=, PRODUCT=,Rating only: {LENGTH=20.0Design only: {LENGTH=24,40,2, OD=0.75, ID= 0.584 or BWG=14 orTHICKNESS=0.083 or (NPS= and SCHEDULE=), NUMBER=257,Rating only: PASS=2,Design only: PASS=1,12, PATTERN=INLINE, TPITCH=, LPITCH=,Rating only: ROWS=1, MATERIAL=01, CONDUCTIVITY=30.0Design only: ROWS=2,12, MATERIAL=01, CONDUCTIVITY=30.0,FOUL=0.002, LAYER=0.0, HI= or HSCALER=1.0,Rating only: DPSHELL= or DPUNIT=, SERIES=1, PARALLEL=1Design only: DPSHELL=5.0, 15.0 or DPUNIT=, DPSCALER=1.0}

Page 4-232

{FINS} NUMBER=5, {THICKNESS=0.017, HEIGHT=0.625, AREA=, EFFI-CIENCY=, MATERIAL=20, CONDUCTIVITY=128.3, BOND=0.0}

Page 4-235

DUCTSIDE FEED=, PRODUCT=,Rating only: {WIDTH=, LENGTH=20, FOUL= 0.002, LAYER= 0.0, HO=value, or HSCALER= 1.0,Design only: {WIDTH=5.0,12.0 FOUL= 0.002, LAYER= 0.0, HO= value,or HSCALER= 1.0,Rating only: DPUNIT=Design only: DPUNIT=0.3,0.7 or VELOCITY=, DPSCALER= 1.0,Rating only: PARALLEL=1}Design only: PARALLEL=1,10}

Page 4-236

{TNOZZLE} {ID=, NUMBER=1,1, NONE} Page 4-238

SPECIFICATIONOptional for Rating;Mandatory for Design

TEMPERATURE= and TUBE or DUCT or LFRAC= and TUBE or COLD orDUTY= or HOCI= or COCI= or HIHO=, or HICO=

Page 4-238

{CALCULATION} {NOCHECK, TWOPHASE=NEW} Page 4-239

{PRINT} {STANDARD, EXTENDED, ZONES, MONITOR} Page 4-240

{COST} {BSIZE=1000.0, BCOST=0.0, LINEAR=50.0, EXPONENT=0.6,CONSTANT=0.0, UNIT or SHELL}

Page 4-240

{ACE2} HTRI only Page 4-241

)

ACE UID=, {NAME=, Rating only: REFUNIT= } Page 4-242

TYPE Rating only: OLD,Design only: NEW, {HOTSIDE=TUBE, FLOW=COUNTERCURRENT,Rating only: AREA=79.0,Design only: AREA= UESTIMATE=5.0, USCALER=1.0}

Page 4-244

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Table 4-34: Unit Operations Category of Input

Statement Keywords See ...

TUBESIDE FEED=, PRODUCT=,Rating only: {LENGTH=20.0Design only: {LENGTH=24,40,2, OD=0.75, ID= 0.584 or BWG=14 orTHICKNESS=0.083 or (NPS= and SCHEDULE=), NUMBER=20,Rating only: PASS=2, PATTERN=INLINE, TPITCH=, LPITCH=Design only: PASS=2,12, PATTERN=INLINE, TPITCH=, LPITCH=,Rating only: ROWS=1Design only: ROWS=2,12MATERIAL=01, CONDUCTIVITY=30.0, FOUL=0.002, LAYER=0.0,HI= or HSCALER=1.0,Rating only: DPSHELL= or DPUNIT=, SERIES=1, PARALLEL=1Design only: DPSHELL= or DPUNIT=5.0, 15.0 or VELOCITY=DPSCALER=1.0}

Page 4- 245

{FINS} NUMBER=5, {THICKNESS=0.017, HEIGHT=0.625, AREA=,EFFICIENCY=, MATERIAL=20, CONDUCTIVITY=128.3, BOND=0.0}

Page 4-248

AIRSIDE FEED=, PRODUCT=,Rating only: {WIDTH=, LENGTH=20Design only: {WIDTH=5.0,12.0 FOUL= 0.002, LAYER= 0.0, HO= value,or HSCALER= 1.0,Rating only: DPUNIT=Design only: DPUNIT=0.3,0.7, VELOCITY= DPSCALER= 1.0,Rating only: PARALLEL=1}Design only: PARALLEL=1,10}

Page 4-249

{FAN} Rating only: DRAFT=FORCED,{DIAMETER=,Rating only: NUMBER=1,EFFICIENCY=100.0,Rating only: POWER=,Design only: OPTIMIZATION=}

Page 4-251

{TNOZZLE} {ID=, NUMBER=1,1, NONE} Page 4-252

SPECIFICATIONOptional for Rating;Mandatory for Design

TEMPERATURE=, and TUBE or AIR or LFRAC=, and TUBE or HOT orDUTY= or HOCI= or COCI= or HIHO=, or HICO=}

Page 4-252

{CALCULATION} {NOCHECK, TWOPHASE=NEW} Page 4-253

{COST} {BSIZE=1000.0, BCOST=0.0, LINEAR=50.0, EXPONENT=0.6,CONSTANT=0.0, UNIT or SHELL}

Page 4-254

{PRINT} {STANDARD, EXTENDED, ZONES, MONITOR} Page 4-254

{ACE2} HTRI only Page 4-255

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Table 4-34: Unit Operations Category of Input

Statement Keywords See ...

)

PHE UID=, {NAME=} Page 4-256

TYPE Rating only: OLD, FLOW=COUNTERCURRENT,Design only: NEW, {FLOW=COUNTERCURRENT,Rating only: AREA=1000.0,Design only: AREA=, UESTIMATE=100.0, USCALER=1.0}

Page 4-257

HOTSIDE FEED=, PRODUCT=, {FOUL=0.0005, LAYER=0.0, HHOT= orHSCALER=1.0,Rating only: DPFRAME=, DPSCALER=1.0, PDESIGN=, TDESIGN=Design only: DPFRAME=5.0, 15.0, DPSCALER=1.0, PDESIGN=,TDESIGN=}

Page 4-258

COLDSIDE FEED=, PRODUCT=, {FOUL=0.0005, LAYER=0.0, HCOLD= orHSCALER=1.0,Rating only: DPFRAME=, DPSCALER=1.0, PDESIGN=, TDESIGN=Design only: DPFRAME=5.0, 15.0, DPSCALER=1.0, PDESIGN=,TDESIGN=}

Page 4-259

PACK Required for Rating if APC is not specified on the PLATE statement:SPACE=0.1, DPORT=6, LVERTICAL=48, LHORIZONTAL=, {WIDTH=,Rating only: PARALLEL=1, FCDIR=UP, FCFLUID=COLDDesign only: PARALLEL=1,10, MAXPASSES=1, FCDIR=UP,FCFLUID=COLD}

Page 4-260

PLATEMandatory forRating;Optional for Design

APC=, {NAME=, BETA=30.0,60.0,Mandatory for Rating, Optional for Design if no APC is entered:AEFACTOR=1.17, AREA=6.14, THICKNESS=0.6, MATERIAL=09,CONDUCTIVITY=9.4, GASKET=5}

Page 4-261

ARRANGEMENTRating only

PFIRST=, PSECOND=, NCHOT=, NCCOLD=, HPASS=, CPASS= Page 4-264

{FPLATE} CHNUMBER=, REYNOLDS=, FFACTOR=, or CONST=, and EXPON= Page 4-265

{JPLATE} CHNUMBER=, REYNOLDS=, JFACTOR=, or CONST=, and EXPON= Page 4-266

{HNOZZLE} {ID=, NONE} Page 4-267

{CNOZZLE} {ID=, NONE} Page 4-267

{CALCULATION} {NOCHECK} Page 4-267

SPECIFICATIONOptional for Rating;Mandatory for Design

TEMPERATURE=, and HOTS or COLD or LFRAC=, and HOTS or COLDor DUTY= or HOCI= or COCI= or HIHO=, or HICO=,

Page 4-268

{PRINT} {STANDARD, EXTENDED, MONITOR} Page 4-269

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Table 4-34: Unit Operations Category of Input

Statement Keywords See ...

{COST} {BSIZE=1000.0, BCOST=0.0, LINEAR=50.0, EXPONENT=0.6,CONSTANT=0.0, UNIT or FRAME}

Page 4-270

)

MIXER UID=, {NAME=} Page 4-271

STRMS (orSTREAMS)

FEED=, PRODUCT= Page 4-271

)

SPLITTER UID=, {NAME=} Page 4-273

STRMS (orSTREAMS)

FEED=, PRODUCT= Page 4-273

OPERATION FRACTION= or RATE= Page 4-274

PIPE UID=, {NAME=} Page 4-276

STRMS (orSTREAMS)

FEED=, PRODUCT= Page 4-277

{LINE}and/or

ID=6.065 or NPS= and SCHEDULE=, {LENGTH=0.0, EQLENGTH=0.0,ELEVATION=0.0, ROUGHNESS=0.0018, FRICTION=,NOACCELERATION}

Page 4-277

{FITTINGS}or

ID=6.065, {EQLENGTH=0.0, KFACTOR=0.0, ROUGHNESS=0.0018,FRICTION=, NOACCELERATION }

Page 4-280

{OPERATION} POUT= or DP=0.0 Page 4-281

VALVE UID=, {NAME=} Page 4-283

STRMS (orSTREAMS)

FEED=, PRODUCT= Page 4-283

{OPERATION} POUT= or DP=0.0 Page 4-284

DESALTER UID=, {NAME=} Page 4-285

STRMS (orSTREAMS)

FEED=, PRODUCT=, BRINE= Page 4-285

{OPERATION} TOUT= or DT=0.0, POUT= or DP=0.0, REJECTION=100 Page 4-286

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Table 4-34: Unit Operations Category of Input

Statement Keywords See ...

DECANTER UID=, {NAME=} Page 4-288

STRMS (orSTREAMS)

FEED=, PRODUCT=, WATER= Page 4-288

{OPERATION} TOUT= or DT=0.0, POUT= or DP=0.0, REJECTION=100 Page 4-289

FLASH UID=, {NAME=} Page 4-291

STRMS (orSTREAMS)

FEED=, VAPOR=, LIQUID= Page 4-291

{OPERATION} POUT= or DP=0.0 Page 4-292

)

HX UID=, {NAME=} Page 4-294

TYPE Rating only: OLD,Design only: NEW,TEMA=AES, {HOTSIDE=SHELL, FLOW=COUNTERCURRENT,Rating only: AREA=1000.0,Design only: AREA=200.0, 6000.0,} UVALUE=

Page 4-295

TUBESIDE FEED=, PRODUCT=,Rating only: PASS=2Design only: PASS=2, 16, 2, {DPSHELL=5.0, or DPUNIT=5.0}

Page 4-296

SHELLSIDE FEED=, PRODUCT=,Rating only: SERIES=1, PARALLEL=1,Design only: SERIES=1, 10, PARALLEL=1, 10,{DPSHELL=5.0, or DPUNIT=5.0}

Page 4-297

{CALCULATION} MINFT=0.8 Page 4-298

{SPECIFICATION} DUTY= or TEMPERATURE=, and SHELL or TUBE Page 4-298

{PRINT} STANDARD, {ZONES,} Page 4-299

{COST} {BSIZE=1000.0, BCOST=0.0, LINEAR=50.0, EXPONENT=0.6, CON-STANT=0.0, UNIT or SHELL}

Page 4-299

HEATER UID=, {NAME=} Page 4-301

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Table 4-34: Unit Operations Category of Input

Statement Keywords See ...

STRMS (orSTREAMS)

FEED=, PRODUCT=, Page 4-301

{OPERATION} DUTY= or TOUT= or DT=0.0, TUTILITY=85.0, POUT= or DP=0.0,{UTILITY=HEATINGMEDIUM}

Page 4-302

{COST} {BSIZE=1000.0, BCOST=0.0, LINEAR=50.0, EXPONENT=0.6,CONSTANT=0.0, UNIT or SHELL}

Page 4-303

COOLER UID=, {NAME=} Page 4-305

STRMS (orSTREAMS)

FEED=, PRODUCT=, Page 4-305

{OPERATION} DUTY= or TOUT= or DT=0.0, TUTILITY=85.0, POUT= or DP=0.0,{UTILITY=WATER}

Page 4-307

{COST} {BSIZE=1000.0, BCOST=0.0, LINEAR=50.0, EXPONENT=0.6,CONSTANT=0.0, UNIT or SHELL}

Page 4-307

FIREDHEATER UID=, {NAME=} Page 4-309

STRMS (orSTREAMS)

FEED=, PRODUCT=, Page 4-309

{OPERATION} DUTY= or TOUT= or DT=0.0, TUTILITY=85.0, POUT= or DP=0.0,{UTILITY=OIL, EFFICIENCY=100}

Page 4-310

{COST} {BSIZE=1000.0, BCOST=0.0, LINEAR=50.0, EXPONENT=0.6,CONSTANT=0.0, UNIT or SHELL}

Page 4-311

COMPRESSOR UID=, {NAME=} Page 4-313

STRMS (orSTREAMS)

FEED=, PRODUCT=, Page 4-313

{OPERATION} POUT= or DP=0.0, {REFSTREAM=, EFFICIENCY=100, TSR=35.0,K=1.395, STAGES=1, UTILITY=ELECTRIC}

Page 4-314

{COST} {BSIZE=1000.0, BCOST=0.0, LINEAR=50.0, EXPONENT=0.6,CONSTANT=0.0, UNIT or SHELL}

Page 4-316

PUMP UID=, {NAME=} Page 4-318

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Table 4-34: Unit Operations Category of Input

Statement Keywords See ...

STRMS (orSTREAMS)

FEED=, PRODUCT=, Page 4-318

{OPERATION} POUT= or DP=0.0, {REFSTREAM=, EFFICIENCY=100, TSR=35.0,UTILITY=ELECTRIC}

Page 4-319

{COST} {BSIZE=1000.0, BCOST=0.0, LINEAR=50.0, EXPONENT=0.6,CONSTANT=0.0, UNIT or SHELL}

Page 4-320

MVC UID=, {NAME=} Page 4-322

SPECIFICATION STRM=, TEMPERATURE=, UNIT=, DUTY= Page 4-322

VARIABLE STRM=, FRACTION=, RATE=, TEMPERATURE=, UNIT=, DUTY= Page 4-323

PARAMETER ITER=, SUMSQ=, NOPRINT Page 4-325

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STE, DPE, MTE, ACE, FTE, RBE, PHEUnit Operations Data Category of Input

This mandatory statement introduces the heat exchanger unit and must bethe first line for each heat exchanger unit. The table below provides thekeyword to be used for each type of heat exchanger model:

Keyword entry Description

STE Shell-and-tube heat exchangers of all types, including Kettle reboilers andcondensers.

DPE Double-pipe heat exchangers. Longitudinal fins are allowed.

MTE Multi-tube heat exchangers. Longitudinal fins are allowed.

ACE Air coolers. Fan calculations are included.

FTE Finned-tube exchangers. Any bank of tubes in a rectangular duct with a gasflowing over the tubes.

RBE Heat exchangers with Rod Baffle design.

PHE Plate-and-frame heat exchangers.

The keyword descriptions below apply to all heat exchanger models, unless indicated otherwise.

Mandatory entry:

UID= Identifies the unit operation for reference and printout purposes.Enter up to 12 alphanumeric characters. This entry must beunique to all other unit operations. There is no default.

Optional entries:

NAME= Identifies the unit operation for printout purposes only. Enter upto 12 alphanumeric characters. NAME supplements the UID en-try. There is no default.

REFUNIT= Rating only. Does not apply to PHE or DPE exchangers. Refers toanother heat exchanger defined in the flowsheet that shares com-mon data. This entry is useful where large quantities of data arecommon to several exchangers. Enter up to twelve alphanumericcharacters. The referenced exchanger must be OLD, and musthave all physical and mechanical data supplied. Table 4-35 liststhe data defined as identical to the referenced exchanger unlessredefined.

Examples:STE UID=EX1, NAME=STEXC1...PHE UID=EX2

The keyword descriptions for other statements are given below for specific heat exchangermodels.

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General InformationFluid Property RequirementsAll rigorous heat exchanger models require the following basic data for allstreams:

Number Property Notes

1. Enthalpy Used to compute heat transfer2. Heat capacity Needed for Prandtl number for film coefficients.3. Density Used in Reynolds number determination and velocity

calculations.4. Thermal Used in Prandtl number.conductivity5. Viscosity Used in Reynolds and Prandtl numbers.6. Latent heat Only required for Kettle reboiler calculations.7. Surface Only required for Kettle reboiler tension calculations.

When a stream exists in both liquid and vapor states, both liquid and vaporvalues must be entered for properties 2-5 and the enthalpy values shouldcorrespond to the total enthalpy for the liquid/vapor mixture.In addition, formixed-phase streams, data for the liquid condensate fraction (CFRAC)must be supplied for HEXTRAN to use in determining the liquid/vaporsplit and mixture properties. Similarly, for streams in which water mayexist in either vapor or liquid state, a water liquid fraction table (WFRAC)must be supplied. (Note that this latter requirement is not necessary forstreams defined as WATER or STEAM only, in which case the vapor/liquidfraction is determined from the steam tables.)

Numerous provisions exist in HEXTRAN for generating the requiredproperty data. These have been previously discussed and are as follows:

a) Automatic property generation based on the stream data.b) Internal property data sets for streams with defined compositions or

assay data.c) External property data entered in tabular form or retrieved from stored

files.

Exchanger Costing EquationA general costing equation is used to cost all exchangers. The data entriesare the same for all rigorous models with the exception that costing for aircooled exchangers (ACE) and finned-tube exchangers (FTE) may bequalified on a "per bay" or "per duct" basis and plate-and-frame exchangers(PHE) may be qualified on a "frame" basis versus the terminology "pershell" which is used for the other rigorous models. Heat exchanger costdata may be supplied for individual modules with the HXCOST statementor will default to the global cost data which are supplied or defaulted in theSimulation/Optimization category of input.

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BSIZE=1000.00 Defines the base area used in the costing equation. The defaultis 1000.0 ft 2 (English), or 93.0 m2 (metric and SI).

BCOST=0.00 Defines the base cost used in the costing equation. The defaultis 0.00 USDOLLAR/ft 2 (English), or 0.00 USDOLLAR/m2 (met-ric and SI).

LINEAR=50.00 Defines the linear cost factor used in the costing equation. Thedefault is 50.00 USDOLLAR/ft 2 (English), or 538.20 USDOL-LAR/m 2 (metric and SI).

EXPONENT=0.60 Defines the exponential cost factor used in the costing equation.The default is 0.60 (English, metric and SI).

CONSTANT=0.00 Defines the constant cost factor used in the costing equation.This entry can be used to define fixed costs associated with in-stallation of an exchanger and is not a function of exchangersize. The default is 0.00.

UNIT orSHELL

Defines the basis for the exchanger CONSTANT cost factor. UNITresults in the constant cost factor being applied once to eachunit regardless of the number of shells or frames in the unit.SHELL or FRAME results in the constant cost factor being ap-plied to each shell or each frame in the unit. The default is UNIT.

The cost data defined with the above entries are used in thegeneral equation below:

Heat Exchanger Cost =CONSTANT + LINEAR * AREA + ETERM

where:

ETERM = BCOST * BSIZE * (AREA/BSIZE) ** EXPONENT

and

AREA = area for a single exchanger shell (duct or bay or frame).

For exchangers costed on a per shell base, for example, theabove cost is multiplied by the number of exchangers involvedin the service.

Exchanger Construction MaterialBasic data for the thermal conductivities and densities of many of thecommon metals and alloys are provided by HEXTRAN for use with thevarious rigorous models. These data are requested by entry of theappropriate numeric code for the "MATERIAL" entry on the TUBESIDE orSHELLSIDE (PLATE for PHEs) statements. Table 4-35 below lists theavailable material codes in HEXTRAN.

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The default material code in HEXTRAN is 01 or carbon steel. Materials notavailable in HEXTRAN may be represented by entering a label with up to 8characters for the MATERIAL entry (for printout purposes only) and enteringthe appropriate values with the "DENSITY" and "CONDUCTIVITY" entries.

Table 4-35: Available Material Codes

Material Density Conduc-tivityCode Description Label lb/ft3 kg/m3 Btu/ kcal/

hr.ft.F hr.m.C W/m.K01 Carbon Steel CARB STL 490.8 7862 30.0 44.6 51.902 Carbon - moly steel 0.1C, 0.5 MO CARB MLY 493.2 7900 29.0 43.2 50.203 Chrome - moly steel 1.0 CR,0.5 MO CHRM MLY 490.1 7851 27.0 40.2 46.704 Low chrome steel - 2.25 CR, 1.0 MO LOW CHRM 487.0 7801 25.0 37.2 43.305 Med. chrome steel - 5.0 CR, 0.5 MO MED CHRM 480.7 7700 21.0 31.3 36.306 Straight chrome steel - 12 CR STR CHRM 487.0 7801 14.0 20.8 24.207 304 Stainless steel - 18 Cr,8 Ni 304 S.S. 501.1 8027 9.3 13.8 16.108 310 Stainless steel - 25 Cr, 20 Ni 310 S.S. 501.1 8027 7.8 11.6 13.509 316 Stainless steel - 17 Cr, 12 Ni 316 S.S. 501.1 8027 9.4 14.0 16.310 321 Stainless steel - 18 Cr, 10 Ni 321 S.S. 494.2 7916 9.2 13.7 15.920 Aluminum 1060 - H14 A1060H14 170.0 2723 128.3 190.9 222.121 Aluminum 1100 - annealed A1100 AN 169.3 2712 128.3 190.9 222.122 Aluminum 3003 - H14 annealed A3003H14 171.1 2741 111.0 165.2 192.123 Aluminum 3003 - H25 annealed A3003H25 171.1 2741 111.0 165.2 193.124 Aluminum 6061 - T4 tempered A6061 T4 169.3 2712 95.0 141.4 164.425 Aluminum 6061 - T6 tempered A6061 T6 169.3 2712 95.0 141.4 164.430 Copper COPPER 556.4 8913 225.0 334.8 389.431 Arsenical copper AS COPPR 560.0 8970 187.0 278.3 323.632 Copper Nickel 90/10 CUNI9010 559.0 8954 26.0 38.7 45.033 Copper Nickel 80/20 CUNI8020 558.5 8946 22.0 32.7 38.134 Copper Nickel 70/30 CUNI7030 585.0 9371 17.0 25.3 29.435 Copper Nickel 60/40 CUNI6040 554.7 8885 12.9 19.2 22.340 Red Brass 85 Cu - 15 Zn RED BRAS 546.0 8746 92.0 136.9 159.241 Admiralty 71 Cu - 28 Zn - 1Sn ADMRALTY 531.0 8506 64.0 95.2 110.842 Commercial Brass 55 Cu - 34 Zn COM BRAS 529.0 8474 67.0 99.7 116.043 Muntz Metal 60 Cu - 40 Zn MUNTZ 524.0 8394 71.0 105.7 122.944 Aluminum Bronze 93 Cu - 5 Al AL BRONZ 510.0 8169 48.0 71.4 83.145 Aluminum Brass 78 Cu - 2 Al - 20 Zn AL BRASS 520.0 8330 58.0 86.3 100.450 Nickel annealed NICKEL 556.4 8913 45.2 67.3 78.251 Low Carbon nickel annealed L CRB NI 554.7 8885 35.0 52.1 60.652 Monel Nickel - 70 Ni - 30 Cu MONEL NI 551.2 8829 14.5 21.6 25.153 Inconel 600 76 Ni - 16 Cr - 8 Fe INCNL600 525.3 8414 8.7 12.9 15.160 Titanium - Grade 2 TITANIUM 281.6 4511 9.5 14.1 16.4

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Exchanger Printout OptionsPrintout control is available for individual exchangers via the PRINTstatement. If this statement is not supplied, the printout options default tothe options globally selected (or defaulted) on the Calculation Statement.

STANDARD Print standard TEMA-style data sheet for exchanger. The defaultis that the data sheet will be printed.

EXTENDED Print extended data sheet for exchanger. The default is that thedata sheet will be printed.

ZONES Print zones analysis for exchanger with vaporization/condensa-tion. The default is that the data sheet will be printed.

MONITOR Print design monitor summary for STE, ACE, FTE and PHE thatare designed. The monitor summary will not be printed by de-fault. Note that this entry is not applicable to the other ex-changer models.

Nozzle Pressure DropsThe pressure drops reported on the standard exchanger data sheets includenozzle pressure drops for all rigorous models for both the tube and shellsides, or cold and hot sides for PHEs. Notice that for FTE and ACEshellside is not applicable.

The nozzle inside diameters may be furnished via the TNOZZLE andSNOZZLE statements (CNOZZLE and HNOZZLE for PHEs, respectively)as appropriate where the general format is:TNOZZLE ID=in, out orNONESNOZZLE ID=in, out orNONE

For shell and tube exchangers (STE) and rod baffle exchangers (RBE),additional details may be given for rating calculations involving annularnozzles.

Note that if nozzle data are not supplied by the user, HEXTRAN will sizethe nozzles using standard design rules and then calculate thecorresponding pressure drops. To suppress nozzle sizing and nozzlepressure drop calculations, use the NONE keyword.

Tuning Exchanger ModelsSeveral input parameters are available to tune exchanger models to matchplant data when performing rating calculations for exchangers. Adescription of these entries is given in Table 4-36.

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Table 4-36: Keywords for Tuning ExchangersKeyword InputEntry Statement Description

USCALER TYPE Scaler for computed overall U value. Default is 1.0.HSCALER TUBE Scaler for tubeside film coefficient. Default is 1.0.HSCALER SHELL, DUCT, or AIRSIDE Scaler for shell (duct, air)side coefficient. Default is 1.0.HSCALER HOTSIDE, COLDSIDE Scaler for hotside and coldside film coefficient is plate-and-

frame exchangers. Default is 1.0.HI TUBE Supplied tubeside film coefficient in appropriate units.HO SHELL,DUCT, or AIRSIDE Supplied shell (duct, air) side coefficient in appropriate units.HHOT HOTSIDE Supplied hotside film coefficient in appropriate units.HCOLD COLDSIDE Supplied coldside film coefficient in appropriate units.DPUNIT TUBE or SHELL or DUCT or Supplied constant pressure drop for the service which may

AIRSIDE or HOTSIDE or encompass multiple shells (ducts or bays).COLDSIDE

DPSCALER TUBE or SHELL Scaler for computed pressure drop. Default is 1.0.or DUCT or AIRSIDE orHOTSIDE or COLDSIDE

DPSHELL, TUBE or SHELL Supplied pressure drop for a single shell, bay or duct.DPDUCT, or AIRSIDEDPBAY

DPFRAME HOTSIDE, COLDSIDE Suppliedpressure drop for a single frame

FOUL TUBE or SHELL or Fouling factor. A default value of 0.002 (0.0005 for PHE)AIRSIDE or DUCT or HOTSIDE is used for all rigorous models.or COLDSIDE

LAYER TUBE or SHELL or Fouling layer thickness in appropriate units. Default is 0.AIRSIDE or DUCT or HOTSIDE Note that this entry affects the computed velocities andor COLDSIDE associated properties.

RESTRICTIONS: 1) DPUNIT is mutually exclusive with DPSHELL, DPDUCT, DPBAY, and DPFRAME.2) USCALER and HSCALER should not both be used for a given exchanger.3) Scaling Factors (USCALER, HSCALER, and DPSCALER) should not be used in conjunction with

corresponding supplied constant values (HI, HO, HHOT, HCOLD, DPSHELL, DPUNIT,DPFRAME).

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STE HEAT EXCHANGERS

Table 4-37: Allowable Referenced Data

Statement Allowed Entry

TYPE TEMA, ORIENTATION, FLOW, AREA

TUBESIDE LENGTH, OD, ID, BWG, THICKNESS, NUMBER, PASS, PATTERN, PITCH,MATERIAL, DENSITY, CONDUCTIVITY, FOUL, LAYER

FINS NUMBER, AREA, HEIGHT, ROOT, THICKNESS, EFFICIENCY

TNOZZLE ID, NUMBER, TYPE

SHELLSIDE ID, SERIES, PARALLEL, SEALS, MATERIAL, DENSITY, FOUL, LAYER

BAFFLE TYPE, SEGMENTAL, NONE, NTIW, CUT, NFAR, SPACING, INSPACING,OUTSPACING, THICKNESS, SHEETS

SNOZZLE TYPE, ID, LENGTH, AREA, CLEARANCE, NUMBER

INOZZLE ID, NUMBER

LNOZZLE ID, NUMBER

TYPE UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement defines the basic characteristics of the exchanger.

Mandatory entries:

OLD or Rating only. Identifies the exchanger as an existing exchangerthat is to be rated.

NEW Design only. Identifies the exchanger as a new exchanger that isto be designed.

Examples:STE UID=STE2

TYPE OLDDPE UID=EX23

TYPE NEWTEMA=AES

Specifies the TEMA designation for STE and RBE exchangers only. Enter a three- or four-character designation as described in Figure 4-4. Acceptable TEMA designations are given in Ta-ble 4-36. For J-type (divided flow) shells, enter J1 (or J) for shells with one inlet and two outletnozzles. For J-type shells with two inlet and one outlet nozzles, enter J2. The default is AES.

Note: Design cases with ‘‘P’’, ‘‘S’’, ‘‘T’’, or ‘‘W’’ rear head types require sealing strips (SEALS)to be specified on the SHELL statement.

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Figure 4-4: TEMA Designations

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Acceptable TEMA Designations

Front end head types: A, B, C, N, D

Shell types: E, F, G, H, J (or J1, J2), K, X

Rear end head types: L, M, N, P, S, T, U, W

Acceptable TEMA Designations

Front end head types: A, B, C, N, D

Shell types: E, F, G, H, J, (or J1, J2), , X

Read end head types L, M, N, P, S, T, U, W

UVALUE= Specifies the U-value for the exchanger calculations. Standarddimensional units are Btu/hr-ft2-F (English), kcal/hr-m 2 -C(metric), or W/m 2 -K (SI).

Example:STE UID=HX2B

TYPE OLD, TEMA=NKT, UVALUE=50

Optional entries:

HOTSIDE=SHELL Specifies the side of the exchanger receiving the hotside fluid.Enter SHELL or TUBE. This entry is required for the HTRI option.SHELL is the default.

ORIENTATION=HORIZONTAL Specifies the bundle orientation, which affects both the film co-efficient for condensers and the static head for vertical single-pass tubes and/or shells. Enter HORIZONTAL or VERTICAL. Invertical exchangers, the condensing, or hot fluid, is assumed toflow down and the cold, or boiling fluid, is assumed to flow up.The default is HORIZONTAL.

FLOW=COUNTERCURRENT Specifies the relative flow direction between the shellside fluidand the tubeside fluid. Enter COUNTERCURRENT or COCUR-RENT. This entry affects the calculation of the LMTD correctionfactor (FT). This entry has no effect if the number of shellsidepasses and the number of tubeside passes are not the same.The default is COUNTERCURRENT.

Note: COCURRENT flow does not allow the two outlet tempera-tures to ‘‘cross,’’ which makes it useful for temperature-controlapplications (see Figure 4-5).

AREA=1000 or Rating only. Specifies the shellside effective or “installed” area perunit for OLD exchanger calculations. The area covered by thetubesheets and baffles is subtracted from the outside area of thetubes. For finned tubes, fin area must also be included. If AREA isnot entered, this value will be calculated from the input tube infor-mation. AREA is checked for consistency with tube information.The default is 1000 ft 2 (English), or 92.9 m 2 (metric and SI).

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AREA=200,6000 Design only. Limits the area per shell (see Figure 4-6). Enterminimum and maximum values. Values specified on the LIMITSstatement in the CALCULATION section override the defaults forthis keyword. Default values are 200 and 6000 ft2 (English), or18.58 m2 and 557.43 m2 (metric and SI).

The area for heat transfer is computed using the following for-mula, and is cross-checked against the AREA entry supplied onthe TYPE statement:

AREA= π* OD * (LENGTH - SHEETS) * NUMBER

where:

OD, LENGTH, and NUMBER are defined on TUBE statement

Note that the tube outside diameter in the above calculations canbe determined from the inside diameter and the BirminghamWire Gauge (BWG) or THICKNESS entries on the TUBE state-ment. Conversely, the tube inside diameter can be determinedfrom the outside diameter and either the BWG or THICKNESSentries on the TUBE statement.

UESTIMATE=50 Specifies the initial U-value for the flowsheet energy balance.The default is 50 Btu/hr-ft 2 -F (English), 244.1 kcal/hr-m2-C(metric), or 283.9 W/m 2 -K (SI).

USCALER=1.0 Specifies a multiplier used to adjust the rigorously computedU-value. The default is 1.0.

Example:TYPE OLD, HOTSIDE=TUBE, TEMA=AJ2S, AREA=5000,*

UESTIMATE=60, USCALER=0.9

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Figure 4-5: Fluid Temperature Distribution

Figure 4-6: Dual Design Limits: AREA and ID

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Cooling

Countercurrent Flow

Heating

T1in

T 2out T 1

out

T2in

Cooling

Cocurrent Flow

Heating

T1in

T 2out

T 1out

T2in

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TUBESIDE UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement defines all necessary details for the tubeside of the ex-changer. Tubes may be plain or finned, and several options for defining baffle details areavailable.

Mandatory entries:

FEED= Identifies the feed, or inlet stream and its associated properties.Enter up to twelve alphanumeric characters. The FEED entry willbe printed as a label in the output. There is no default.

PRODUCT= Identifies the product, or outlet stream and its associated prop-erties. Enter up to twelve alphanumeric characters. The PROD-UCT entry will be printed as a label in the output. There is nodefault.

Example:TUBE FEED=CRD1, PRODUCT=CRD2

Optional entries:

LENGTH=20 or Rating only. Specifies the exchanger tube length. For straighttubes, tube length is measured as the distance from the outerface of both tubesheets. For U-bends, tube length is measuredas the distance from the outer face of the tubesheet to the cen-terline of the U-bend radius (see Figure 4-7.) The default value is20 ft (English), or 6.1 m (metric and SI).

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Figure 4-7: Effective Length of a U-tube Bundle

LENGTH=8,20,4 Design only. Specifies minimum, maximum, and incrementallengths. HEXTRAN uses the maximum length to initiate the de-sign and reduces the length by specified increments if the tube-side pressure drop and velocity specifications cannot be met atthe minimum number of passes allowed for the design. The de-fault values are: 8, 20, 4 ft (English), or 2.4, 6.1, 1.2 m (metricand SI).

ID=0.584 and/or Specifies the inside diameter of the tube. This value will be auto-matically computed from the OD and THICKNESS or BWG en-tries for bare tubes. For finned tubes, it is computed from the finROOT diameter and THICKNESS or BWG. The default values are0.584 in. (bare tubes), 0.495 in. (finned tubes) (English), or14.834 mm (bare tubes) and 12.573 mm (finned tubes) (metricand SI).

OD=0.75 Specifies the outside diameter of the tube. The default is 0.75 in.(English), or 19.05 mm (metric and SI).

THICKNESS=0.083 or Specifies the thickness of the tube wall. The default is 0.083 in.(bare tubes), 0.065 in. (finned tubes) (English), or 2.108 mm(bare tubes), 1.651 mm (finned tubes) (metric and SI).

BWG=14 Specifies a value from the Birmingham Wire Gauge, an alternateway todefine tube thickness. The default is 14.

Note: Either BWG or THICKNESS may be given if OD is entered,but not both. If both ID and OD are given, neither BWG norTHICKNESS is allowed.

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L

Bend Radius

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NUMBER=257 This represents the tube count per bundle on a ‘‘per shell’’ basis.For U tubes, NUMBER corresponds to the number of holes inthe tubesheet (twice the number of complete U-tubes). If notspecified, this value will be derived based on the AREA suppliedon the TYPE statement and the SHELL ID, using the tube countmethod described in The Heat Exchanger Design Handbook, sec-tion 4.2.5 (E), Hemisphere Publishing Corporation, New York,1983. The default is 257 (for bare tubes), and 96 (for finnedtubes).

PASS=2 or Rating only. Specifies the number of tube passes per shell. Validentries are integers from 1 to 16, excluding odd numbersgreater than 3. One pass corresponds to true counterflow. Thedefault is 2.

PASS=2,16,2 Design only. Specifies the number of tube passes per shell. En-ter values for minimum, maximum, and incremental (integersfrom 1 to16, separated by commas). HEXTRAN maximizes thenumber of passes up to the pressure drop limit for the shell orservice. If the pressure drop limit is exceeded for the minimumPASS entry, the LENGTH will be reduced.

PATTERN=90 Specifies a tube pattern code. Valid patterns are shown in Figure4-10. Enter 30, 45, 60, or 90. The default is 90.

Figure 4-8: Tube Patterns

PITCH=1.0 Specifies the tube pitch, which is defined as the center-to-centerdistance between adjacent tubes. Tube pitch is typically 1.25times tube outside diameter (OD). You must also account for finHEIGHT when supplying PITCH for finned tubes. The default is1.0 in. (English) or 25.4 mm (metric and SI).

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MATERIAL=01 Specifies the tube material, either by code or by an alphanu-meric name. When an appropriate code number is entered, thethermal conductivity and density are selected from the materialcode table given in Table 4-35, Allowable Material Codes. Alpha-numeric entries are treated as names for printout purposes only.The default is 01 (CARBON STEEL).

DENSITY=490.8 Specifies tube material density. This entry is used to computethe total weight of the exchanger when MATERIAL is specifiedby alphanumeric name. When a valid MATERIAL code is entered,the density value is selected automatically from Table 4-35. Thedefault is 490.8 lb/ft3 (English), or 7862 kg/m3 (metric and SI).

CONDUCTIVITY=30 Specifies tube metal thermal conductivity. This entry is used todetermine the resistance to heat transfer through the tube wall.When a valid MATERIAL code is entered, this value is selectedfrom Table 4-35. The default is 30 Btu/hr-ft-F (English), 44.6kcal/hr-m-C (metric), or 51.9 W/m-K (SI).

FOUL=0.002 Specifies the tubeside fouling resistance based on tubeside area.To simulate a ‘‘clean’’ exchanger, enter a value of zero on bothTUBE and SHELL statements. The default is 0.002 hr-ft 2 -F/Btu(English), 0.00041 hr-m 2 -C/kcal (metric), or 0.00035 m 2 -K/W(SI).

LAYER=0.0 Specifies the tubeside fouling layer thickness. This entry repre-sents the effect of fouling on the tubeside pressure drop. The ef-fect of fouling on heat transfer is represented bythe FOUL entry.The default is 0.0 in. (English), or 0.0 mm (metric and SI).

HI= or Specifies a user-supplied inside film coefficient. This entry over-rides the computed value for both rating and design cases.

HSCALER=1.0 Specifies a multiplier for the computed film coefficient. You can-not use HSCALER if USCALER is specified on the TYPE state-ment. The default is 1.0.

VELOCITY=0,1000 Design only. Specifies the upper and lower limits for tubesidevelocity. Enter lower and upper limits, separated by a comma.The default is 0,1000 ft/sec (English), or 0,305 m/s (metric andSI).

DPSHELL= or Rating only. Specifies the value for pressure drop per bundle.This entry overrides the computed value. You cannot enterDPSHELL and DPUNIT together.

DPSHELL= 5,15 or Design only. Specifies the value for pressure drop per bundle.Enter lower and upper limits to accommodate the specified passarrangement. The defaults are 5, 15 psi (English), 0.35, 1.05kg/cm 2 (metric), or 34.5, 103.4 kPa (SI). You cannot enterDPSHELL and DPUNIT together.

DPUNIT= Rating only. Specifies the value for pressure drop per service.This entry overrides the computed value. There are no defaults.You cannot enter DPSHELL and DPUNIT together.

DPUNIT= Design only. Specifies the value for pressure drop per service.Enter lower and upper limits. There are no defaults. You cannotenter DPSHELL and DPUNIT together.

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DPSCALER=1.0 Specifies an optional multiplier to adjust the computed tubesidepressure drop to more closely approximate actual plant per-formance. The default is 1.0.

PDESIGN= Specifies a user-supplied tubeside design pressure. This entryoverrides the computed value. There is no default.

TDESIGN= Specifies a user-supplied tubeside design temperature. This en-try overrides the computed value. There is no default.

Examples:

(Rating example)TUBE FEED=CRD1, PROD=CRD2, LENGTH=20, OD=0.75,*

BWG=16, NUMBER=400, PASS=4, PATTERN=30,*FOUL=0.005, DPSCALER=1.1, HSCALER=0.9

(Design example)TUBE FEED=CRD1, PROD=CRD2, LENGTH=16,40,4, OD=1.0,*

BWG=14, PASS=2,16,2, PATTERN=60, FOUL=0.004,*DPSHELL=8,12

FINS UNIT OPERATIONS Data Category of Input

Optional statement. This statement specifies details for finned tubes. Acceptable finned tubedimensions are illustrated in Figure 4-9. Table 4-38 lists dimensions of some commonly usedradial low-fin tubes.

Mandatory entries:

NUMBER =19 Specifies the fin density. The default is 19 fins/in. (English), or748 fins/m (metric and SI).

Optional entries:

ROOT= 0.625 Specifies the fin root diameter. The default is 0.625 in (English),or 15.9 mm (metric and SI).

THICKNESS=0.026 Specifies the fin thickness. The default is 0.026 in. (English), or0.668 (metric and SI).

HEIGHT=0.0625 Specifies the fin height. If HEIGHT is not specified, this value willbe calculated from OD and ROOT. If OD and ROOT are not speci-fied, the default value will be used. The default is 0.0625 in.(English), or 1.59 mm (metric and SI).

AREA= Specifies the fin area per unit length of one tube. This entry isused to compute the shellside area in place of the fin geometrysupplied. No consistency check is made between this entry andthe area value determined from NUMBER, HEIGHT, THICKNESSand ROOT. There is no default.

EFFICIENCY= Specifies the fin efficiency. If not specified, HEXTRAN will calcu-late the value.

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Figure 4-9: Tube Dimensions

Examples:FINS NUMBER=26, ROOT=0.75, HEIGHT=0.0625, EFFICIENCY=0.90FINS HEIGHT=0.0625, AREA=0.52

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Table 4-38: Dimensions For Some Commonly Used Radial Low-fin Tubes*

NUMBER = 19 fins/in, HEIGHT = 0.0625 in (1.588 mm)TUBE OD WALL THICKNESS ROOT DIAMETER TUBE ID OUTSIDE AREA

——————- ——————————— ———————- ——————— ———————in mm BWG in mm in mm in mm ft2/ft m2/m

—————-——-—- ——— —— —— ——- ——— ——- ——— —— ———-0.625 15.875 22 0.028 0.711 0.500 12.700 0.444 11.278 0.405 0.1230.625 15.875 20 0.035 0.889 0.500 12.700 0.430 10.922 0.405 0.1230.625 15.875 19 0.042 1.067 0.500 12.700 0.416 10.566 0.405 0.1230.625 15.875 18 0.049 1.245 0.500 12.700 0.402 10.211 0.405 0.1230.625 15.875 16 0.065 1.651 0.500 12.700 0.370 9.398 0.405 0.123

0.750 19.050 22 0.028 0.711 0.625 15.875 0.569 14.453 0.496 0.1510.750 19.050 20 0.035 0.889 0.625 15.875 0.555 14.097 0.496 0.1510.750 19.050 19 0.042 1.067 0.625 15.875 0.541 13.741 0.496 0.1510.750 19.050 18 0.049 1.245 0.625 15.875 0.527 13.386 0.496 0.1510.750 19.050 16 0.065 1.651 0.625 15.875 0.495 12.573 0.496 0.1510.750 19.050 14 0.083 2.108 0.625 15.875 0.459 11.659 0.496 0.1510.750 19.050 13 0.095 2.413 0.625 15.875 0.435 11.049 0.496 0.151

0.875 22.225 20 0.035 0.889 0.750 19.050 0.680 17.272 0.588 0.1790.875 22.225 19 0.042 1.067 0.750 19.050 0.666 16.916 0.588 0.1790.875 22.225 18 0.049 1.245 0.750 19.050 0.652 16.561 0.588 0.1790.875 22.225 16 0.065 1.651 0.750 19.050 0.620 15.748 0.588 0.1790.875 22.225 14 0.083 2.108 0.750 19.050 0.584 14.834 0.588 0.179

1.000 25.400 19 0.042 1.067 0.875 22.225 0.791 20.091 0.678 0.2071.000 25.400 18 0.049 1.245 0.875 22.225 0.777 19.736 0.678 0.2071.000 25.400 16 0.065 1.651 0.875 22.225 0.745 18.923 0.678 0.2071.000 25.400 14 0.083 2.108 0.875 22.225 0.709 18.009 0.678 0.2071.000 25.400 13 0.095 2.413 0.875 22.225 0.685 17.399 0.678 0.2071.000 25.400 12 0.109 2.769 0.875 22.225 0.657 16.688 0.678 0.207

NUMBER = 19 fins/in, HEIGHT = 0.0625 in (1.588 mm)TUBE OD WALL THICKNESS ROOT DIAMETER TUBE ID OUTSIDE AREA

--------------------- ----------------------------------- ------------------------- --------- --------- ------ -------in mm BWG in mm in mm in mm ft2/ft m2/m

------------------- ------- --------- -------- -------- ------- --------- -------- --------- -------- ----------0.625 15.875 16 0.065 1.651 0.500 12.700 0.370 9.398 0.368 0.112

0.750 19.050 16 0.065 1.651 0.625 15.875 0.495 12.573 0.438 0.1340.750 19.050 14 0.083 2.108 0.625 15.875 0.459 11.659 0.438 0.134

0.875 22.225 16 0.065 1.651 0.750 19.050 0.620 15.748 0.520 0.1580.875 22.225 14 0.083 2.108 0.750 19.050 0.584 14.834 0.520 0.158

1.000 25.400 16 0.065 1.651 0.875 22.225 0.745 18.923 0.598 0.1821.000 25.400 14 0.083 2.108 0.875 22.225 0.709 18.009 0.598 0.182

* Kern, Donald Q. and Allan D. Kraus, Extended Surface Heat Transfer, pp. 502-3, McGraw-Hill, New York (1972).

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SHELLSIDE UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement defines all details for the shellside of the exchanger.

Mandatory entries:

FEED= Identifies the feed, or inlet stream and its associated properties.Enter up to twelve alphanumeric characters. The FEED entry willbe printed as a label in the output. There is no default.

PRODUCT= Identifies the product, or outlet stream and its associated prop-erties. Enter up to twelve alphanumeric characters. The PROD-UCT entry will be printed as a label in the output. There is nodefault.

Optional entries:

ID=23 or Rating only. Specifies the shell inside diameter. This entry ischecked for consistency with the supplied values for AREA andtube details. If AREA or tube details are not supplied, the defaultis used. The default for bare tubes is 23 in. (English), or 550mm (metric and SI). The default for finned tubes is 15 in. (Eng-lish), or 400 mm (metric and SI).

ID=8.0,60.0 Design only. Specifies minimum and maximum values for theshell inside diameter. Enter both minimum and maximum allow-able values. The actual shell size is determined by the area re-quired per shell and the tube details. Based on these data andthe TEMA type, HEXTRAN selects a standard shell size from Ta-ble 4-39. Defaults are: 8.0, 60.0 in. (English), or 203.2, 1524.0mm (metric and SI).

Table 4-39: Standard Shell Inside Diametersin (English units)

6.00 8.00 10.00 12.00

13.00 13.25 15.00 15.25

17.00 17.25 19.00 19.25

21.00 21.25 23.00 23.25

24.00 - 60.00 (1.0-in increments)60.00 - 80.00 (2.0-in increments)80.00 - 122.0 (3.0-in increments)

mm (metric and SI)

150.0 - 600.0 (50-mm increments)600.0 - 3100 (100-mm increments)

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SERIES=1 Rating only. Specifies the number of identical shells in series.Enter an integer from 1 to 10. The default is 1. Figure 4-10shows combinations of shells in series and parallel.

Figure 5-10: Shells in Series and Parellel

SERIES=1,10 Design only. Limits the number of exchanger shells in series.Enter minimum and maximum values, separated by a comma.Valid range is 1 to 10. SHELLS in series are incremented from 1to meet the minimum LMTD correction factor, MINFT, which issupplied on the CALCULATION statement or defaulted globally inthe CALCULATION Data Section. In design mode, you cannot en-ter SERIES and PARALLEL keywords together.

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PARALLEL=1 Rating only. Specifies the number of identical shells in parallel.Enter an integer from 1 to 10. The default is 1. Figure 4-10shows combinations of shells in series and parallel.

PARALLEL=1,10 Design only. Limits the number of exchanger shells in parallel.Enter minimum and maximum values, separated by a comma.Valid range is 1 to 10. Shells in parallel are added as required tokeep within the specified limit of area per shell supplied on theTYPE statement. In design mode, you cannot enter SERIES andPARALLEL keywords together. Figure 4-10 shows combinationsof shells in series and parallel.

SEALS= Specifies the number of pairs of sealing strips. Sealing strips areillustrated in Figure 4-11. If not entered, HEXTRAN will use 1pair for each 5 tube rows in the bundle.

Figure 4-11: Sealing Strip Description

MATERIAL=01 Specifies the tube material, either by code or by an alphanu-meric name. When an appropriate code number is entered, thethermal conductivity and density are selected from AllowableMaterial Codes (Table 4-36). Alphanumeric entries are treated asnames for printout purposes only. The default is 01 (CARBONSTEEL).

DENSITY=490.8 Specifies tube material density. This entry is used to computethe total weight of the exchanger when MATERIAL is specifiedby alphanumeric name. When a valid MATERIAL code is entered,the density value is selected automatically from Table 4-36. Thedefault is 490.8 lb/ft3 (English), or 7862 kg/m3 (metric and SI).

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FOUL=0.002 Specifies the shellside fouling resistance based on shellsidearea. To simulate a ‘‘clean’’ exchanger, enter a value of zero forFOUL on both TUBE and SHELL statements. The default is 0.002hr-ft 2 -F/Btu (English), 0.00041 hr-m 2 -C/kcal (metric), or0.00035 m 2 -K/W (SI).

LAYER=0.0 Specifies the shellside fouling layer thickness. This entry repre-sents the effect of fouling on the shellside pressure drop. The ef-fect of fouling on heat transfer is represented by the FOUL entry.The default is 0.0 in. (English), or 0.0 mm (metric and SI).

HO= or Specifies a user-supplied shellside film coefficient. This entryoverrides the computed value for both rating and design cases.

HSCALER=1.0 Specifies a multiplier for the computed film coefficient. Do notuse HSCALER if USCALER is specified on the TYPE statement.The default is 1.0.

VELOCITY=0,1000 Design only. Specifies the upper and lower limits for the shell-side velocity. Enter lower and upper limits, separated by com-mas. The default is 0, 1000 ft/sec (English), or 0, 305 m/s(metric and SI).

DPSHELL= or Rating only. Specifies the value for pressure drop per bundle.This entry overrides the computed value. You cannot enterDPSHELL and DPUNIT together.

DPSHELL=5,15 or Design only. Specifies the value for pressure drop per bundle.Enter lower and upper limits to accommodate the specified shelldesign. The defaults are 5, 15 psi (English), 0.35, 1.05 kg/cm 2

(metric), or 34.5, 103.4 kPa (SI). You cannot enter DPSHELLand DPUNIT together.

DPUNIT= Rating only. Specifies the value for pressure drop per service.This entry overrides the computed value. There are no defaults.You cannot enter DPUNIT and DPSHELL together.

DPUNIT= Design only. Specifies the value for pressure drop per service.Enter lower and upper limits to accommodate the specified shelldesign. There are no defaults. You cannot enter DPSHELL andDPUNIT together.

DPSCALER=1.0 Specifies an optional multiplier to adjust the computed shellsidepressure drop to more closely approximate actual plant per-formance. The default is 1.0.

PDESIGN= Specifies a user-supplied shellside design pressure. This entryoverrides the computed value. There is no default.

TDESIGN= Specifies a user-supplied shellside design temperature. This en-try overrides the computed value. There is no default.

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Examples:

(Rating example)SHELL FEED=AG01, PROD=AG02, ID=28, SERIES=4,*

SEALS=4, FOUL=0.001, PDESIGN=500,*TDESIGN=1000

(Design example)SHELL FEED=AG01, PROD=AG02, ID=20,36,*

SERIES=1,10, FOUL=0.003, DPSHELL=8,16

BAFFLE UNIT OPERATIONS Data Category of Input

Optional statement. This statement specifies details for the baffles and tube sheet.

Optional entries:

SEGMENTAL=SINGLE Specifies the number of segments (or cuts) for each baffle. En-ter SINGLE, DOUBLE, or TRIPLE. (TRIPLE is available for HTRImodels only - see the HEXTRAN HTRI Input Guide). Availablebaffle types are illustrated in Figure 4-12. HEXTRAN does notvary the value of this keyword in design mode. The default isSINGLE.

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Figure 4-12: Segmental Baffle Types

NTIW Specifies that there are no tubes in the baffle windows (see Fig-ure 4-13). You can only use this keyword with SINGLE segmen-tal baffles. HEXTRAN does not vary the value of this keyword indesign mode.

NONE Specifies that the exchanger has no baffles. You can use thiskeyword to design exchangers without baffles, for example, ket-tle reboilers. No other entries are required on the BAFFLE state-ment when NONE is specified.

CUT=0.20 or Rating only. Specifies the baffle ‘‘cut,’’ (ratio of the height of thewindow to the shell inside diameter) as shown in Figure 4-14.Enter the value as a percentage or a fraction. The default is 0.20.

CUT=0.20,0.20 Design only. Enter minimum and maximum values. When bafflecut is allowed to vary during design, HEXTRAN varies both thebaffle cut and the baffle spacing to meet the performance speci-fication for the shell. The linear relationship used to select the

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appropriate combination of cut and spacing is shown in Figure4-16. The default is 0.20, 0.20.

Note: HEXTRAN issues a warning for baffle cuts outside the fol-lowing ranges: 0.10 - 0.49 (SINGLE) and 0.10 - 0.34 (DOUBLE).

NFAR=0.14 or Rating only. Specifies the baffle net free area ratio. This is an al-ternate method for defining the baffle cut (see Figure 4-15).Some common baffle cuts and their equivalent NFAR values arelisted in Table 4-40. You cannot use NFAR with NTIW or CUT.The default is 0.14, corresponding to CUT=0.20.

Figure 4-13: No Tubes in Window (NTIW)

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Figure 4-14: Baffle Cut Definition

Figure 4-15: Net Free Area Ratio Definition

NFAR=0.14,0.14 Design only. Specifies the minimum and maximum baffle netfree area ratio. This is an alternate method for defining the bafflecut (see Figure 4-15). Enter minimum and maximum values.Some common baffle cuts and their equivalent NFAR values arelisted in Table 4-40. You cannot use NFAR with NTIW. The de-fault is 0.14,0.14.

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Baffle Cut Definition

H

D

Baffle Cut =H—D

Net Free Area Ratio Definition

Net Free Ratio =A—

A+B

Net Area“ A“

Net Area“ B“

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Figure 4-16: Dual Design Limits for Cut and Spacing

Table 4-40: Baffle Cut and NFAR Equivalents

CUT NFAR

SINGLE-SEGMENT DOUBLE SEGMENT

0.10 0.05 0.10

0.20 0.14 0.28

0.25 0.20 0.40

0.34 0.30 0.60

0.50 0.50 n/a

SPACING=4.6 Rating only. Specifies the central baffle spacing for exchangers.HEXTRAN assumes that all central baffles are evenly spaced.The defaults are 4.6 in. (bare tubes), 3.00 in. (finned tubes)(English); or 110 mm (bare tubes), 80 mm (finned tubes) (met-ric and SI).

SPACING= Design only. Specifies minimum and maximum central bafflespacings for exchangers. Enter minimum and maximum values.The minimum and maximum values are calculated as 0.2 and1.0 times the shell ID, respectively. HEXTRAN assumes that allcentral baffles are evenly spaced. If the baffle cut varies, SPAC-ING will vary in conjunction with it. The spacing and cut relation-ship is shown in Figure 4-16.

INSPACING= Rating only. Specifies the spacing between the tubesheet andthe inlet baffle (see Figure 4-17). If not specified, this value iscomputed from the SPACING entry.

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Figure 5-17: Baffle Spacing for Exchangers

OUTSPACING= Rating only. Specifies the spacing between the tubesheet andthe outlet baffle (see Figure 4-17). If not specified, this value iscomputed from the SPACING entry.

THICKNESS=0.1875 Specifies the single baffle thickness. Standard baffle thicknessesare listed in Table 4-41. The default is 0.1875 in. (English) or4.763 mm (metric and SI).

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Table 4-41: Standard Baffle Thickness Values*in (English)

BAFFLE SPACING (in)

SHELL ID (in) >24 >36 >48 >60

≤24 ≤36 ≤48 ≤60

8 - 14 0.125 0.1875 0.250 0.375 0.375

15 - 28 0.1875 0.250 0.375 0.375 0.500

29 - 38 0.250 0.3125 0.375 0.500 0.625

39 - 60 0.250 0.375 0.500 0.625 0.625

61 - 100 0.375 0.500 0.625 0.750 0.750

mm (metric and SI)

BAFFLE SPACING (mm)

SHELL ID (mm) >610 >914 >1219 >1524

≤610 ≤914 ≤1219 ≤1524

203 - 356 3.18 4.76 6.35 9.53 9.53

381 - 711 4.76 6.35 9.53 9.53 12.70

737 - 965 6.35 7.94 9.53 12.70 15.88

991 - 1524 6.35 9.53 12.70 15.88 15.88

1549 - 2540 9.53 12.70 15.88 19.05 19.05

* Standards of Tubular Manufacturers Association (TEMA), 6th Edition, 1978.

SHEETS= Specifies the total thickness of both tubesheets. If not specified,TEMA standards will be used. Units are in (English) and mm(metric and SI).

Examples:

(Rating example)BAFFLE SEGMENTAL=SINGLE, CUT=0.15, SPACING=12,*

THICKNESS=0.5

(Design example)BAFFLE SEGMENTAL=DOUBLE, CUT=0.10,0.20,*

SPACING=8,20

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TNOZZLE UNIT OPERATIONS Data Category of Input

Optional Statement. This statement defines the tubeside nozzle characteristics. Nozzles areautomatically included in pressure drop calculations unless NONE is specified on the TNOZZLEstatement. Nozzles are automatically sized when data are not provided.

Optional entries:

ID= Specifies the inside diameters of the inlet and outlet tubesidenozzles. If not entered, HEXTRAN uses a conventional nozzlesize.

NUMBER=1,1 Specifies the number of tubeside nozzles at the inlet and outlet.Enter a value for the number of inlet nozzles, and outlet nozzles,separated by a comma. The default is 1,1.

NONE Suppresses nozzle pressure drop calculations.

TYPE= CONVENTIONAL Specifies the type of tubeside nozzles. Enter CONVENTIONAL,AXIAL, or DISTRIBUTOR. The default is CONVENTIONAL.

Examples:TNOZZLE ID=6,6, NUMBER=1,1,*

SNOZZLE UNIT OPERATIONS Data Category of Input

Optional Statement. This statement defines the shellside nozzle characteristics. Nozzles areautomatically included in pressure drop calculations unless NONE is specified on the SNOZ-ZLE statement. Nozzles are automatically sized when data area not provided.

Optional entries:

ID= Specifies the inside diameters of the inlet and outlet shellsidenozzles. If not entered, HEXTRAN uses a conventional nozzlesize.

NUMBER=1,1 Specifies the number of shellside nozzles at the inlet and outlet.Enter a value for the number of inlet nozzles, and outlet nozzles,separated by a comma. The default is 1,1.

NONE Suppresses nozzle pressure drop calculations.

TYPE= CONVENTIONAL Specifies the type of shellside nozzles. Enter CONVENTIONAL orANNULAR. See Figure 4-18 for the illustration of an annular noz-zle design. The default is CONVENTIONAL.

AREA= Specifies the total groove area for an annular nozzle. Units arein2 (English) and mm2 (metric and SI). There is no default.

LENGTH= Specifies the length of the annular distributor. See Figure 4-18,dimension (note). Units are in. (English) and mm (metric andSI). There is no default.

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CLEARANCE= Specifies the distance between the annular wall and the ex-changer wall for an annular exchanger. See Figure 4-18, dimen-sion (note). Units are in. (English) and mm (metric and SI).There is no default.

Figure 4-18: Annular Nozzle Design

Examples:SNOZZLE ID=8,4, NUMBER=2,1

INOZZLE UNIT OPERATIONS Data Category of Input

Optional Statement. This statement defines the shellside intermediate nozzle characteristics.Nozzles are automatically sized when data are not provided.

Optional entries:

ID= Specifies the inside diameters of the intermediate shellside noz-zles. There is no default.

NUMBER=0 Specifies the number of shellside intermediate nozzles. The de-fault is 0.

Examples:INOZZLE ID=8, NUMBER=1

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LNOZZLE UNIT OPERATIONS Data Category of Input

Optional Statement. This statement defines the shellside liquid nozzle characteristics. Nozzlesare automatically sized when data are not provided.

Optional entries:

ID= Specifies the inside diameters of the shellside liquid nozzles.There is no default.

NUMBER=0 Specifies the number of shellside liquid nozzles. If a value is en-tered here, then the shellside outlet nozzle information on theSNOZZLE statement will be used for vapor outlet nozzle(s). Thedefault is 0.

Examples:LNOZZLE ID=4, NUMBER=1

HTRI UNIT OPERATIONS Data Category of Input

Optional statements. These statements specify HTRI modules will be used for rating or design.See the HEXTRAN HTRI Input Guide for details.

Mandatory entries:

ST5 and/orCST3 and/orRKH3

HTFS UNIT OPERATIONS Data Category of Input

Optional statements. These statements specify the HTFS module will be used for rating or de-sign. See the HEXTRAN HTRI Input Guide for details.

Mandatory entry:

TASC3

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CALCULATION UNIT OPERATIONS Data Category of Input

Optional statement. This statement sets calculation methods for individual exchangers on aglobal basis. Methods can be selected globally using the CALCULATION statement in theSIMULATION, CASESTUDIES, OPTIMIZATION AREA, OPTIMIZATION SPLIT, or REGRESSIONcategories of input.

Optional entries:

NOCHECK Suppresses HEXTRAN geometry consistency checks and pre-vents HEXTRAN from assigning default values to missing ge-ometry data. NOCHECK is designed to allow you to access HTRIor HTFS defaults in place of HEXTRAN defaults. When using NO-CHECK, ensure that all exchanger data are explicitly specified, orthat one of the HTRI (ST5, CST3, RKH3) or HTFS (TASC3) mod-ules is referenced, (see the HTRI and HTFS documentation).

WARNING: Using NOCHECK with inconsistent or missing ge-ometry data may result in abnormal program termination (divi-sion by zero, overflow, etc.).

MINFT=0.8 Specifies the minimum allowable LMTD correction factor (FT).The default is 0.8.

DPSMETHOD=STREAM Specifies the pressure drop calculation method used for shell-side calculations. Enter BELL (Kenneth Bell of Delaware Univer-sity method) or STREAM (stream analysis method). STREAM isthe default.

Reference: ‘‘A New and Accurate Hand Calculation Method forShellside Pressure Drop and Flow Distribution,’’ Wills, M. J. N.,and D. Johnston, Presented at the 22nd Heat Transfer Confer-ence and Exhibition, Niagara Falls, N.Y., 1984.

TWOPHASE=NEW Specifies the methods for thermal and hydraulic calculations forall rigorous exchangers. Enter NEW or OLD. NEW uses theModified Chen vaporization method for convective boiling, andincludes predictions for sub-cooled and film boiling. Condensa-tion methods account for flow regimes and gravity versus sheareffects. Pressure drops are calculated using a stream analysis-based method. NEW automatically sets DPSMETHOD=STREAM.OLD selects algorithms used in versions 5.0x and earlier. Usethis option to make comparison runs with earlier versions ofHEXTRAN. The default is NEW.

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SPECIFICATION UNIT OPERATIONS Data Category of Input

Optional for rating, mandatory for design (unless the exchanger is a part of an exchanger net-work and the heat duty is indirectly specified). This statement specifies exchanger perform-ance criteria. When the exchanger is being rated, HEXTRAN reports the required shellsidefouling factor to match the specified area. For exchangers being designed, this statement de-termines the area required for the desired heat transfer.

TEMPERATURE= and Specifies the outlet temperature of the stream. This keywordmust be used in conjunction with the SHELL, TUBE, HOT, orCOLD keyword to apply the TEMPERATURE to the correctstream. The units are F (English), C (metric), or K (SI). You can-not enter TEMPERATURE with any other specification keywords.There is no default.

SHELL orTUBE orHOT orCOLD or

Specifies the side of the exchanger being used by the TEMPERA-TURE specification. These keywords can also be used withLFRACTION. There is no default.

LFRAC= and Specifies the liquid weight fraction of the stream. Enter a valuefrom 0.0 (all vapor) to 1.0 (all liquid). This keyword must be usedin conjunction with the SHELL, TUBE, HOT, or COLD keyword toapply the LFRACTION to the correct stream. You cannot enterLFRAC with any other specification keywords. There is no default.

SHELL orTUBE orHOT orCOLD or

Specifies the side of the exchanger being used by the TEMPERA-TURE specification. These keywords can also be used withLFRACTION. There is no default.

DUTY= or Specifies the total heat transferred in the exchanger. You cannotuse DUTY with any other specification keywords. Units are:MMBtu/hr (English), MMkcal/hr (metric), and MMkJ/hr (SI).There is no default.

HOCI= orCOCI= orHIHO= orHICO=

Specifies the exchanger approach temperature. Use only one ofthese four and enter a numerical value. Each keyword specifies asubtraction operation where the first set of two characters de-fines a value, and the second set of two characters defines avalue that is subtracted from it. In the operation, H refers to HOTside, C refers to COLD side, I refers to inlet, and O refers to out-let. Therefore, HOCI specifies hot outlet temperature minus coldinlet temperature. You cannot use these keywords with any otherspecification keywords. Valid units are F (English), C (metric andSI). There is no default.

Examples:SPEC TEMP=100, HOTSPEC TEMP=200, SHELLSPEC DUTY=8.5SPEC LFRAC=0.8, HOTSPEC LFRAC=0.9, SHELLSPEC HOCI=40

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PRINT UNIT OPERATIONS Data Category of Input

Optional statement. This statement specifies report print options for the exchanger statement.The default printout options are the global values specified in the CALCULATION section.STANDARD and EXTENDED are defaults. STANDARD will be printed in addition to any speci-fied keywords. EXTENDED will be overwritten by any specified keywords.

Optional entries:

STANDARD Prints the standard TEMA Data Sheet. This is the default.

EXTENDED Prints the Extended Data Sheet. This is the default.

ZONES Prints the zones analysis for two-phase exchangers.

MONITOR Prints the design logic monitor for NEW exchangers.

Examples:PRINT EXTENDED, ZONES

This example prints standard, extended, and zones analysis reports.PRINT MONITOR

This example prints standard and design logic monitor reports.PRINT STANDARD

This example prints only the standard report.PRINT ZONES, MONITOR

This example prints standard, zones analysis, and design logic monitor reports.

COST UNIT OPERATIONS Data Category of Input

Optional statement. This statement provides special costing data for an exchanger. The de-faults are the global values given in the CALCULATION category of input.

Optional Entries:

BSIZE=1000.00 Defines the base area used in the costing equation. The defaultis 1000.0 ft 2 (English), or 93.0 m2 (metric and SI).

BCOST=0.00 Defines the base cost used in the costing equation. The defaultis 0.00 USDOLLAR/ft 2 (English), or 0.00 USDOLLAR/m2 (metricand SI).

LINEAR=50.00 Defines the linear cost factor used in the costing equation. Thedefault is 50.00 USDOLLAR/ft 2 (English), or 538.20 USDOL-LAR/m 2 (metric and SI).

EXPONENT=0.60 Defines the exponential cost factor used in the costing equation.The default is 0.60 (English, metric and SI).

CONSTANT=0.00 Defines the constant cost factor used in the costing equation.This entry can be used to define fixed costs associated with

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installation of an exchanger and is not a function of exchangersize. The default is 0.00.

UNIT orSHELL

Defines the basis for the exchanger CONSTANT cost factor. UNITresults in the constant cost factor being applied once to eachunit regardless of the number of shells or frames in the unit.SHELL results in the constant cost factor being applied to eachshell or each frame in the unit. The default is UNIT.

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RBE HEAT EXCHANGERS

The Rod Baffle Exchanger (RBE) is an adaptation of the shell and tubeexchanger (STE) that uses the rod baffle design developed by PhillipsPetroleum. The model may be used in rating mode only and shellside flowmust be single phase. Tubeside flow may be single or two phase.

Rod baffles are useful for reduction of vibration failure, lowering the shell-side pressure drop, reducing shellside fouling and simplifying exchangercleaning. They are widely used in gas to gas applications. The internal detailsfor rod baffles are illustrated in Figures 4-19 and 4-20 below.

Figure 4-19: Rod Baffle Cage Assembly

Figure 4-20: Rod Baffle Tube Support Rod Layout

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Baffle A

Baffle B

Baffle Ring

Baffle C

Baffle D

Skid Bar

Rods

Rod Baffle Cage Assembly

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Pressure drops across the nozzles are included in the calculations by default,and nozzles are automatically sized when nozzle data are not provided.

For HTRI members, the ST5 and CST3 programs are available as a specialrating option. See the HEXTRAN HTRI Input Guide for further details.

TYPE RBE UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement defines the basic characteristics of the rodbaffleexchanger.

Mandatory entry:

OLD Identifies the exchanger as an existing exchanger that is to berated. There is no default.

Examples:RBE UID=STE2

TYPE OLD

Optional entries:

TEMA=AES Specifies the TEMA designation. Enter a three- or four-characterdesignation as described in Figure 4-19. Acceptable TEMA des-ignations are given in Table 4-38. For J-type (divided flow)shells, enter J1 (or J) for shells with one inlet and two outletnozzles. For J-type shells with two inlet and one outlet nozzles,enter J2. The default is AES.

HOTSIDE=SHELL Specifies the side of the exchanger receiving the hotside fluid.Enter SHELL or TUBE. If not specified, this value is determinedfrom the stream inlet temperatures. SHELL is the default.

ORIENTATION=HORIZONTAL Specifies the exchanger orientation, which affects both the filmcoefficient for condensers and the static head for verticalsingle-pass tubes and/or shells. Enter HORIZONTAL or VERTI-CAL. The default is HORIZONTAL.

FLOW=COUNTERCURRENT Specifies the relative flow direction between the shellside fluidand the tubeside fluid. Enter COUNTERCURRENT or COCUR-RENT. This entry affects the calculation of the LMTD correctionfactor (FT). The default is COUNTERCURRENT.

AREA=1000 or Specifies the shellside effective or “installed” area per unit. Thearea covered by the tubesheets and baffles is subtracted fromthe outside area of the tubes. If AREA is not entered, this valuewill be calculated from the tube information. AREA is checkedfor consistency with tube information. The default is 1000 ft 2

(English) or 92.9 m 2 (metric and SI).

UESTIMATE=50 Specifies the initial U-value for the flowsheet energy balance.The default is 50 Btu/hr-ft 2 -F (English), 244.1 kcal/hr-m2-C(metric), or 283.9 W/m 2 -K (SI).

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USCALER=1.0 Specifies a multiplier used to adjust the rigorously computed U-value to approximate actual plant data. The default is 1.0.

Example:TYPE OLD, HOTSIDE=TUBE, TEMA=AJ2S, AREA=5000,*

UESTIMATE=60, USCALER=0.9

TUBESIDE RBE UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement defines details for the tubeside of the exchanger. Thearea for heat transfer is computed using the following formula, and is cross-checked againstthe AREA entry supplied on the TYPE statement:

AREA= π* OD * (LENGTH - SHEETS) * NUMBER

where:

OD, LENGTH, and NUMBER are defined on TUBE statement

Note that the tube outside diameter in the above calculations can be determined from the in-side diameter and the Birmingham Wire Gauge (BWG) or THICKNESS entries on the TUBEstatement. Conversely, the tube inside diameter can be determined from the outside diameterand either the BWG or THICKNESS entries on the TUBE statement.

Mandatory entries:

FEED= Identifies the feed, or inlet stream, and its associated properties.Enter up to twelve alphanumeric characters. The FEED entry willbe printed as a label in the output. There is no default.

PRODUCT= Identifies the product, or outlet stream, and its associated prop-erties. Enter up to twelve alphanumeric characters. The PROD-UCT entry will be printed as a label in the output. There is nodefault.

Example:TUBE FED=CRD1, PRODUCT=CRD2

Optional entries:

LENGTH=20 or Specifies the exchanger tube length. The default value is 20 ft(English) or 6.1 m (metric and SI).

ID=0.584 and/or Specifies the inside diameter of the tube. This value will be auto-matically computed from the OD and THICKNESS or BWG en-tries. The default values are 0.584 in. (English) or 14.834 mm(metric and SI).

OD=0.75 and/or Specifies the outside diameter of the tube. The default is 0.75 in.(English) or 19.05 mm (metric and SI).

THICKNESS=0.083 or Specifies the thickness of the tube wall. The default is 0.083 in.(English) or 2.108 mm (metric and SI).

BWG=14 Specifies a value from the Birmingham Wire Gauge, an alternateway to define tube thickness. The default is 14.

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Note: Either BWG or THICKNESS may be given if OD is entered,but not both. If both ID and OD are given, neither BWG norTHICKNESS is allowed.

NUMBER= This represents the tube count per bundle on a ‘‘per shell’’ basis.For U-tubes, NUMBER corresponds to the number of holes inthe tubesheet (twice the number of complete U tubes). If notspecified, this value will be derived based on the AREA suppliedon the TYPE statement and the SHELL ID, using the tube countmethod described in The Heat Exchanger Design Handbook,page 3.5-11, Hemisphere Publishing Corporation, New York,1983. There is no default.

PASS=2 or Specifies the number of tube passes per shell. Enter an integerfrom 1 to 16. One pass corresponds to true counterflow. The de-fault is 2.

PATTERN= Specifies a tube pattern code. 90 (square) is the only valid entry.There is no default.

PITCH= Specifies the tube pitch, which is defined as the center-to-centerdistance between adjacent tubes. Tube pitch is typically 1.25times tube outside diameter (OD). There is no default.

MATERIAL=01 Specifies the tube material, either by code or by an alphanu-meric name. When an appropriate code number is entered, thethermal conductivity and density are selected from Table 4-36,Allowable Material Codes. Alphanumeric entries are treated asnames for printout purposes only. The default is 01 (CARBONSTEEL).

DENSITY=490.8 Specifies tube material density. This entry is used to computethe total weight of the exchanger when MATERIAL is specifiedby alphanumeric name. When a valid MATERIAL code is entered,the density value is selected automatically from Table 4-36; how-ever, this entry will override the selected value. The default is490.8 lb/ft3 (English) or 7862 kg/m3 (metric and SI).

CONDUCTIVITY=30 Specifies tube metal thermal conductivity. This entry is used todetermine the resistance to heat transfer through the tube wall.When a valid MATERIAL code is entered, this value is selectedfrom Table 4-36. The default is 30 Btu/hr-ft-F (English), 44.6kcal/hr-m-C (metric), or 51.9 W/m-K (SI).

FOUL=0.002 Specifies the tubeside fouling resistance based on tubeside area.To simulate a ‘‘clean’’ exchanger, enter a value of zero on bothTUBE and SHELL statements. The default is 0.002 hr-ft 2 -F/Btu(English), 0.00041 hr-m 2 -C/kcal (metric), or 0.00035 m 2 -K/W(SI).

LAYER=0.0 Specifies the tubeside fouling layer thickness. This entry repre-sents the effect of fouling on the tubeside pressure drop. (Theeffect of fouling on heat transfer is represented by the FOUL en-try). The default is 0.0 in. (English) or 0.0 mm (metric and SI).

HI= or Specifies an inside film coefficient. This entry overrides thecomputed value.

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HSCALER=1.0 Specifies a multiplier for the computed film coefficient. You can-not use HSCALER if USCALER is specified on the TYPE state-ment. The default is 1.0.

DPSHELL= or Specifies the value for pressure drop per bundle. This entryoverrides the computed value.

DPUNIT= Specifies the value for pressure drop per service. This entryoverrides the computed value. There are no defaults.

DPSCALER=1.0 Specifies an optional multiplier to adjust the computed tubesidepressure drop to more closely approximate actual plant per-formance. The default is 1.0.

PDESIGN= Specifies a tubeside design pressure. This entry overrides thecomputed value. There is no default.

Example:TUBE FEED=CRD1, PROD=CRD2, LENGTH=20, OD=0.75,*

BWG=16, NUMBER=400, PASS=4, PATTERN=30,*FOUL=0.005, DPSCALER=1.1, HSCALER=0.9

SHELLSIDE RBE UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement defines all details for the shellside of the exchanger.

Mandatory entries:

FEED= Identifies the feed, or inlet stream and its associated properties.Enter up to twelve alphanumeric characters. The FEED entry willbe printed as a label in the output. There is no default.

PRODUCT= Identifies the product, or outlet stream and its associated prop-erties. Enter up to twelve alphanumeric characters. The PROD-UCT entry will be printed as a label in the output. There is nodefault.

Optional entries:

ID=23 or Specifies the shell inside diameter. This entry is checked forconsistency with the supplied values for AREA and tube details.If AREA or tube details are not supplied, the default is used. Thedefault is 23 in. (English) or 550 mm (metric and SI).

SERIES=1 Specifies the number of identical shells in series. Enter an inte-ger from 1 to 10. The default is 1.

PARALLEL=1 Specifies the number of identical shells in parallel. Enter an inte-ger from 1 to 10. The default is 1.

MATERIAL=01 Specifies the tube material, either by code or by an alphanu-meric name. When an appropriate code number is entered, thethermal conductivity and density are selected from Table 4-36,Allowable Material Codes. Alphanumeric entries are treated asnames for printout purposes only. The default is 01 (CARBONSTEEL).

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DENSITY=490.8 Specifies tube material density. This entry is used to computethe total weight of the exchanger when MATERIAL is specifiedby alphanumeric name. When a valid MATERIAL code is entered,the density value is selected automatically from Table 4-36; how-ever, this entry overrides the selected value. The default is 490.8lb/ft3 (English) or 7862 kg/m3 (metric and SI).

FOUL=0.002 Specifies the shellside fouling resistance based on shellsidearea. To simulate a ‘‘clean’’ exchanger, enter a value of zero forFOUL on both TUBE and SHELL statements. The default is 0.002hr-ft 2 -F/Btu (English), 0.00041 hr-m 2 -C/kcal (metric), or0.00035 m 2 -K/W (SI).

LAYER=0.0 Specifies the shellside fouling layer thickness. This entry repre-sents the effect of fouling on the shellside pressure drop. (Theeffect of fouling on heat transfer is represented by the FOUL en-try). The default is 0.0 in. (English) or 0.0 mm (metric and SI).

HO= or Specifies a shellside film coefficient. This entry overrides thecomputed value.

HSCALER=1.0 Specifies a multiplier for the computed film coefficient. Do notuse HSCALER if USCALER is specified on the TYPE statement.The default is 1.0.

DPSHELL= or Specifies the value for pressure drop per shell. This entry over-rides the computed value.

DPUNIT= Specifies the value for pressure drop per service. This entryoverrides the computed value. There are no defaults.

DPSCALER=1.0 Specifies an optional multiplier to adjust the computed shellsidepressure drop to approximate actual plant performance. The de-fault is 1.0.

PDESIGN= Specifies a shellside design pressure. This entry overrides thecomputed value. There is no default.

Examples:SHELL FEED=AG01, PROD=AG02, ID=28, SERIES=4,*

SEALS=4, FOUL=0.001, PDESIGN=500,*TDESIGN=1000

SHELL FEED=AG01, PROD=AG02, ID=20,36,*SERIES=1,10, FOUL=0.003, DPSHELL=8,16

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BAFFLE RBE UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement specifies details for baffles and tube sheet.

Mandatory entries:

TYPE=RING Specifies the rod baffle type. Enter RING, CONTOUR orCHORDAL. The default is RING.

SPACING=4.60 Specifies the rod baffle spacing for exchangers. The default is4.60 in. (English) or 110 mm (metric and SI).

THICKNESS=1.00 Specifies the baffle ring thickness. The default is 1.00 in. (Eng-lish) or 25.4 mm (metric and SI).

Optional entries:

SHEETS= Specifies the total thickness of both tubesheets. This entry de-faults to TEMA standards. Units are in. (English) and mm (met-ric and SI).

CLEARANCE=0.125 Specifies baffle ring-to-shell clearance. The default is 0.125 in.(English) or 3.18 mm (metric and SI).

TNOZZLE RBE UNIT OPERATIONS Data Category of Input

Optional Statement. This statement defines the tubeside nozzle characteristics. Nozzles areautomatically included in pressure drop calculations unless NONE is specified on the TNOZZLEstatement. Nozzles are automatically sized when data area not provided.

Optional entries:

ID= Specifies the inside diameters of the inlet and outlet tubesidenozzles. If not entered, HEXTRAN uses a conventional nozzlesize.

NONE Suppresses nozzle pressure drop calculations.

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SNOZZLE RBE UNIT OPERATIONS Data Category of Input

Optional Statement. This statement defines the shellside nozzle characteristics. Nozzles areautomatically included in pressure drop calculations unless NONE is specified on the SNOZ-ZLE statement. Nozzles are automatically sized when data area not provided.

Optional entries:

TYPE= CONVENTIONAL Specifies the type of shellside nozzles. Enter CONVENTIONAL orANNULAR. See Figure 4-18 for the illustration of an annular noz-zle design. The default is CONVENTIONAL.

ID= Specifies the inside diameters of the inlet and outlet shellsidenozzles. If not entered, HEXTRAN uses a conventional nozzlesize.

LENGTH= Specifies the length of the annular distributor. Units are in. (Eng-lish) and mm (metric and SI). There is no default.

CLEARANCE= Specifies the distance between the annular wall and the ex-changer shell wall. Units are in. (English) and mm (metric andSI). There is no default.

AREA= Specifies the total groove area for an annular nozzle. Units arein2 (English) and mm2 (metric and SI). There is no default.

NONE Suppresses nozzle pressure drop calculations.

CALCULATION RBE UNIT OPERATIONS Data Category of Input

Optional statement. This statement sets calculation methods for individual exchangers on aglobal basis. Methods can be selected globally using the CALCULATION statement in theSIMULATION, CASESTUDIES, OPTIMIZATION AREA, OPTIMIZATION SPLIT, or REGRESSIONcategories of input.

Optional entries:

NOCHECK Suppresses HEXTRAN geometry consistency checks and pre-vents HEXTRAN from assigning default values to missing ge-ometry data. NOCHECK is designed to allow you to access HTRIor HTFS defaults in place of HEXTRAN defaults. When usingNOCHECK, ensure that all exchanger data is explicitly specified,or that one of the HTRI (ST5, CST3, RKH3) or HTFS (TASC3)modules is referenced (See the HEXTRAN HTRI and HTFS InputGuides).

WARNING: Using NOCHECK with inconsistent or missing ge-ometry data may result in abnormal program termination (divi-sion by zero, overflow, etc.).

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TWOPHASE= Specifies the methods for thermal and hydraulic calculations forall rigorous exchangers. Enter NEW or OLD. NEW uses theModified Chen vaporization method for convective boiling, andincludes predictions for sub-cooled and film boiling. Condensa-tion methods account for flow regimes and gravity versus sheareffects. Pressure drops are calculated using a stream analysis-based method. NEW automatically sets DPSMETHOD=STREAM.OLD selects algorithms used in versions 5.0x and earlier. Usethis option to make comparison runs with earlier versions ofHEXTRAN. There is no default.

SPECIFICATION RBE UNIT OPERATIONS Data Category of Input

Optional statement. This statement specifies exchanger performance criteria. HEXTRAN calcu-lates the required fouling factor to match the specified area.

LFRAC= and Specifies the liquid weight fraction of the stream. The streammust be specified by the SHELL, TUBE, HOT, or COLD keywordin order to correctly apply the LFRACTION. Enter a value from0.0 (all vapor) to 1.0 (all liquid). There are no defaults.

SHELL orTUBE orHOT orCOLD or

Specifies the side of the exchanger being used by the LFRAC-TION keyword. SHELL and TUBE are also used with the TEM-PERATURE keyword. There are no defaults.

TEMPERATURE= and Specifies the outlet temperature of the stream specified by theSHELL or TUBE keyword. The units are F (English), C (metric),or K (SI). There are no defaults.

SHELL orTUBE or

Specifies the side of the exchanger being used by theTEMPERATURE keyword. SHELL and TUBE are also used withthe LFRACTION keyword. There are no defaults.

DUTY= or Specifies the total heat transferred in the exchanger. You cannotuse DUTY with any other specification keywords. Units are:MMBtu/hr (English), MMkcal/hr (metric), and MMkJ/hr (SI).There are no defaults.

HOCI= orCOCI= orHIHO= orHICO=

Specifies the exchanger approach temperature. Use only one ofthese four and enter a numerical value. Each keyword specifies asubtraction operation where the first set of two characters de-fines a value, and the second set of two characters defines avalue that is subtracted from it. In the operation, H refers to HOTside, C refers to COLD side, I refers to inlet, and O refers to out-let. Therefore, HOCI specifies hot outlet temperature minus coldinlet temperature. You cannot use DUTY with any other specifi-cation keywords. Valid units are F (English), C, (metric and SI).

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PRINT RBE UNIT OPERATIONS Data Category of Input

Optional statement. This statement specifies report print options for the exchanger statement.The default printout options are the global values specified in the CALCULATION section.STANDARD and EXTENDED are defaults. STANDARD will be printed in addition to any speci-fied keywords. EXTENDED will be overwritten by any specified keywords.

Optional entries:

STANDARD Prints the standard TEMA Data Sheet. This is the default.

EXTENDED Prints the Extended Data Sheet. This is the default.

ZONES Prints the zones analysis for two-phase exchangers.

Examples:PRINT EXTENDED, ZONES

This example prints standard, extended, and zones analysis reports.PRINT STANDARD

This example prints only the standard report.PRINT ZONES

This example prints standard and zones analysis reports.

COST RBE UNIT OPERATIONS Data Category of Input

Optional statement. This statement provides special costing data for an exchanger. The de-faults are the global values given in the CALCULATION category of input.

Optional Entries:

BSIZE=1000.00 Defines the base area used in the costing equation. The defaultis 1000.00 ft 2 (English) or 93.0 m2 (metric and SI).

BCOST=0.00 Defines the base cost used in the costing equation. The defaultis 0.00 USDOLLAR/ft 2 (English) or 0.00 USDOLLAR/m2 (metricand SI).

LINEAR=50.00 Defines the linear cost factor used in the costing equation. Thedefault is 50.00 USDOLLAR/FT 2 (English) or 538.20 USDOL-LAR/m2 (metric and SI).

EXPONENT=0.60 Defines the exponential cost factor used in the costing equation.The default is 0.60 (English, metric and SI).

CONSTANT=0.00 Defines the constant cost factor used in the costing equation.This entry can be used to define fixed costs associated with in-stallation of an exchanger and is not a function of exchangersize. The default is 0.00 USDOLLAR.

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UNIT orSHELL

Defines the basis for the exchanger CONSTANT cost factor. UNITresults in the constant cost factor being applied once to eachunit regardless of the number of shells or frames in the unit.SHELL results in the constant cost factor being applied to eachshell or each frame in the unit. The default is UNIT.

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DPE HEAT EXCHANGERS

A double pipe exchanger (DPE) consists of two concentric pipes connectedby end closures. The tubeside flow is through the inner pipe, and theshellside flow is through the annulus formed by the inner and outer pipes.The outer pipe is designated as the shell. Figure 4-21 illustrates a doublepipe exchanger consisting of two shells in series. Note that theseexchangers can have either true countercurrent or cocurrent flow.

The double pipe exchanger available only in rating mode. It providesrigorous thermal and hydraulic performance rating for countercurrent orcocurrent flow. All fluid types are supported on either side of theexchanger, and vaporization and/or condensation are automatically treatedby zone analysis.

Double pipe exchangers are typically constructed from seamless steel piperanging in size from 2-6 inches Nominal Pipe Size (NPS). Tubes rangefrom 0.75 inches to 4 inch NPS and may be bare or have longitudinal fins.Computed pressure drops include the pressure drops across the nozzles bydefault, and nozzles are automatically sized when nozzle data are notprovided.

Figure 4-21: Double Pipe Exchanger

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Two shells in Series

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TYPE DPE UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement defines the basic characteristics of the double pipeexchanger.

The area for heat transfer is computed using the following formula, and is cross-checkedagainst the AREA entry supplied on the TYPE statement:

AREA OD LENGTH= π* *

where:

OD and LENGTH are defined on TUBE statement

Mandatory entries:

OLD Identifies an existing exchanger to be rated. There is no default.

Example:DPE UID=DPE2

TYPE OLD

Optional entries:

HOTSIDE=SHELL Specifies the side of the exchanger receiving the hotside fluid.Enter SHELL or TUBE. If not specified, the hotside stream is de-termined from the stream inlet temperatures. SHELL is thedefault.

ORIENTATION=HORIZONTAL Specifies the exchanger orientation, which affects both the filmcoefficient for condensers. Enter HORIZONTAL or VERTICAL.The default is HORIZONTAL.

FLOW=COUNTERCURRENT Specifies the relative flow direction between the shellside fluidand the tubeside fluid. Enter COUNTERCURRENT or COCUR-RENT. This entry affects the calculation of the LMTD, and theLMTD correction factor (FT). The default is COUNTERCURRENT.

AREA=23.6 Specifies the shellside effective or “installed” area per shell. Thearea covered by the tubesheets and baffles is subtracted fromthe outside area of the tubes. For finned tubes, fin area mustalso be included. If AREA is not entered, this value will be calcu-lated from the input tube information. AREA is checked for con-sistency with tube information. The default for bare tubes is 23.6ft 2 (English), or 2.19 m 2 (metric and SI). The default for finnedtubes is 86.0 ft 2 (English), or 7.99 m 2 (metric and SI).

UESTIMATE=50 Specifies the initial U-value for the flowsheet energy balance.The default is 50 Btu/hr-ft 2 -F (English), 244.1 kcal/hr-m2-C(metric), or 283.9 W/m 2 -K (SI).

USCALER=1.0 Specifies a multiplier used to adjust the rigorously computedU-value. The default is 1.0.

Example:TYPE OLD, HOTSIDE=TUBE, AREA=5000,*

UESTIMATE=60, USCALER=0.9

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TUBESIDE DPE UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement defines all necessary details for the tubeside of the ex-changer.

Mandatory entries:

FEED= Identifies the feed, or inlet stream, and its associated properties.Enter up to twelve alphanumeric characters. The FEED entry willbe printed as a label in the output. There is no default.

PRODUCT= Identifies the product, or outlet stream, and its associatedproperties. Enter up to twelve alphanumeric characters. ThePRODUCT entry will be printed as a label in the output. There isno default.

Example:TUBE FEED=CRD1, PRODUCT=CRD2

Optional entries:

LENGTH=20 or Specifies the exchanger tube length. The default is 20 ft (Eng-lish), or 6.1 m (metric and SI).

ID=4.026 and/or Specifies the inside diameter of the tube. This value will be auto-matically computed from the OD and THICKNESS or BWG en-tries for bare tubes. or if NPS and SCHEDULE are specified. Thedefault is 4.026 in. (English), or 102.26 mm (metric and SI).

OD=4.50 Specifies the outside diameter of the tube. The default is 4.50 in.(English), or 114.3 mm (metric and SI).

THICKNESS=0.237 or Specifies the thickness of the tube wall. The default is 0.237 in.(English), or 6.02 mm (metric and SI).

BWG= or Specifies a value from the Birmingham Wire Gauge, an alternateway to define tube thickness. There is no default.

Note: Either BWG or THICKNESS may be given if OD is entered,but not both. If both ID and OD are given, neither BWG norTHICKNESS is allowed.

NPS= Specifies the nominal pipe size in inches. If supplied, SCHEDULEmust also be supplied. Valid NPS entries are shown in Table4-42.

SCHEDULE= and Specifies the steel pipe schedule. If supplied, NPS must also besuplied. Valid SCHEDULE entries are shown in Table 4-43.

Note: You cannot enter OD, ID, BWG or THICKNESS with NPSand SCHEDULE.

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Table 4-42: Allowable Pipe Nps Values In Inches

0.125 2.0 8.0 24.0

0.25 2.5 10.0 26.0

0.375 3.0 12.0 28.0

0.5 3.5 14.0 30.0

1.0 4.0 16.0 32.0

1.25 5.0 20.0 34.0

1.5 6.0 22.0 36.0

Allowable Pipe Schedule

10, 20, 30, 40, 60, 80, 100, 120, 140, 160

MATERIAL=01 Specifies the tube material, either by code or by an alphanu-meric name. When an appropriate code number is entered, thethermal conductivity and density are selected from the materialcode table given in Table 4-36, Allowable Material Codes. Alpha-numeric entries are treated as names for printout purposes only.The default is 01 (CARBON STEEL).

DENSITY=490.8 Specifies tube material density. This entry is used to computethe total weight of the exchanger when MATERIAL is specifiedby alphanumeric name. When a valid MATERIAL code is entered,the density value is selected automatically from Table 4-36. Thedefault is 490.8 lb/ft3 (English), or 7862 kg/m3 (metric and SI).

CONDUCTIVITY=30 Specifies tube metal thermal conductivity. This entry is used todetermine the resistance to heat transfer through the tube wall.When a valid MATERIAL code is entered, this value is selectedfrom Table 4-36. The default is 30 Btu/hr-ft-F (English), 44.6kcal/hr-m-C (metric), or 51.9 W/m-K (SI).

FOUL=0.002 Specifies the tubeside fouling resistance based on tubeside area.To simulate a ‘‘clean’’ exchanger, enter a value of zero on bothTUBE and SHELL statements. The default is 0.002 hr-ft 2 -F/Btu(English), 0.00041 hr-m 2 -C/kcal (metric), or 0.00035 m 2 -K/W(SI).

LAYER=0.0 Specifies the tubeside fouling layer thickness. This entry repre-sents the effect of fouling on the tubeside pressure drop. The ef-fect of fouling on heat transfer is represented by the FOUL entry.The default is 0.0 in. (English), or 0.0 mm (metric and SI).

HI= or Specifies a user-supplied inside film coefficient. This entry over-rides the computed value for both rating and design cases.

HSCALER=1.0 Specifies a multiplier for the computed film coefficient. You can-not use HSCALER if USCALER is specified on the TYPE state-ment. The default is 1.0.

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DPSHELL= Specifies the value for pressure drop per unit. This entry over-rides the computed value. There are no defaults. You cannot en-ter DPSHELL and DPUNIT together.

DPUNIT= Specifies the value for pressure drop per service. This entryoverrides the computed value. There are no defaults. You cannotenter DPSHELL and DPUNIT together.

DPSCALER=1.0 Specifies an optional multiplier to adjust the computed tubesidepressure drop to more closely approximate actual plant per-formance. The default is 1.0.

PDESIGN= Specifies a tubeside design pressure. This entry overrides thecomputed value. There is no default.

FINS DPE UNIT OPERATIONS Data Category of Input

Optional statement. This statement specifies details for finned tubes. Figure 4-22 illustratesthe longitudinal fin construction for double pipe exchangers. The fins are manufactured asU-channels and welded onto the inner pipe. They are installed in multiples of 4 and can bemade of a different material than the pipe.

Mandatory entries:

None.

Optional entries:

NUMBER =24 Specifies the number of fins per pipe. The default is 24.

HEIGHT=0.7815 Specifies the fin height. If HEIGHT is not specified, this value willbe calculated from inside and outside pipe diameters as: HEIGHT= (SHELL ID - TUBE OD) / 2. The default is 0.7815 in. (English),or 19.85 mm (metric and SI).

MATERIAL=01 Specifies the fin material, either by code or by an alphanumericname. When an appropriate code number is entered, the thermalconductivity and density are selected from Table 4-36, AllowableMaterial Codes. Alphanumeric entries are treated as names forprintout purposes only. The default is 01 (CARBON STEEL).

CONDUCTIVITY=30 Specifies fin metal thermal conductivity. This entry is used todetermine the resistance to heat transfer through the tube wall.When a valid MATERIAL code is entered, this value is selectedfrom Table 4-36; however, this entry overrides the selectedvalue. The default is 30 Btu/hr-ft-F (English), 44.6 kcal/hr-m-C(metric), or 51.9 W/m-K (SI).

THICKNESS=0.050 Specifies the fin thickness. The default is 0.050 in. (English), or1.27 mm (metric and SI).

AREA= Specifies the fin area per unit length of one tube. This entry isused to compute the fin area in place of the fin geometry sup-plied. No consistency check is made between this entry and the

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area value determined from NUMBER, HEIGHT, and THICKNESS.There is no default.

EFFICIENCY= Specifies the fin efficiency. If not specified, HEXTRAN will calcu-late the value.

Examples:FINS NUMBER=26, ROOT=0.75, HEIGHT=0.0625, EFFICIENCY=0.90FINS HEIGHT=0.0635, AREA=0.52

SHELLSIDE DPE UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement defines all details for the shellside of the exchanger.

Mandatory entries:

FEED= Identifies the feed, or inlet, stream and its associated properties.Enter up to twelve alphanumeric characters. The FEED entry willbe printed as a label in the output. There is no default.

PRODUCT= Identifies the product, or outlet, stream and its associatedproperties. Enter up to twelve alphanumeric characters. ThePRODUCT entry will be printed as a label in the output. There isno default.

Optional entries:

ID=6.065 or Specifies the inside diameter of the outer pipe (shell). The de-fault is 6.065 in. (English), or 154 mm (metric and SI).

NPS= and Specifies the nominal pipe size in inches. If supplied, SCHEDULEmust also be supplied. Valid NPS entries are shown in Table4-42.

SCHEDULE= Specifies the steel pipe schedule. If supplied, NPS must also besuplied. Valid SCHEDULE entries are shown in Table 4-43.

SERIES=1 Specifies the number of identical shells in series. Enter an inte-ger from 1 to 10. The default is 1.

PARALLEL=1 Specifies the number of identical shells in parallel. Enter an inte-ger from 1 to 10. The default is 1.

MATERIAL=01 Specifies the outer pipe (shell) material, either by code or by analphanumeric name. When an appropriate code number is en-tered, the thermal conductivity and density are selected fromTable 4-36, Allowable Material Codes. Alphanumeric entries aretreated as names for printout purposes only. The default is 01(CARBON STEEL).

DENSITY=490.8 Specifies outer pipe (shell) material density. This entry is usedto compute the total weight of the exchanger when MATERIAL isspecified by alphanumeric name. When a valid MATERIAL codeis entered, the density value is selected automatically from Table4-36; however, this entry overrides the selection. The default is490.8 lb/ft3 (English), or 7862 kg/m3 (metric and SI).

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FOUL=0.002 Specifies the shellside fouling resistance based on shellsidearea. To simulate a ‘‘clean’’ exchanger, enter a value of zero forFOUL on both TUBE and SHELL statements. The default is 0.002hr-ft 2 -F/Btu (English), 0.00041 hr-m 2 -C/kcal (metric), or0.00035 m 2 -K/W (SI).

LAYER=0.0 Specifies the shellside fouling layer thickness. This entry repre-sents the effect of fouling on the shellside pressure drop. (Theeffect of fouling on heat transfer is represented by the FOUL en-try.) The default is 0.0 in. (English), or 0.0 mm (metric and SI).

HO= or Specifies a user-supplied shellside film coefficient. This entryoverrides the computed value for both rating and design cases.

HSCALER=1.0 Specifies a multiplier for the computed film coefficient. Do notuse HSCALER if USCALER is specified on the TYPE statement.The default is 1.0.

DPSHELL= Specifies the value for pressure drop per shell. This entry over-rides the computed value. There is no default. You cannot enterDPSHELL and DPUNIT together.

DPUNIT= Specifies the value for pressure drop per service. This entryoverrides the computed value. There is no default. You cannotenter DPUNIT and DPSHELL together.

DPSCALER=1.0 Specifies an optional multiplier to adjust the computed shellsidepressure drop to approximate actual plant performance. The de-fault is 1.0.

PDESIGN= Specifies a shellside design pressure. This entry overrides thecomputed value. There is no default.

TNOZZLE DPE UNIT OPERATIONS Data Category of Input

Optional Statement. This statement defines the tubeside nozzle characteristics. Nozzles areautomatically included in pressure drop calculations unless NONE is specified on the TNOZZLEstatement. Nozzles are automatically sized when data area not provided.

Optional entries:

ID= Specifies the inside diameters of the inlet and outlet tubesidenozzles. Enter inlet and outlet values, separated by a comma. Ifnot entered, HEXTRAN uses a conventional nozzle size.

NONE Suppresses nozzle sizing and pressure drop calculations.

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SNOZZLE DPE UNIT OPERATIONS Data Category of Input

Optional Statement. This statement defines the shellside nozzle characteristics. Nozzles areautomatically included in pressure drop calculations unless NONE is specified on the SNOZ-ZLE statement. Nozzles are automatically sized when data area not provided.

Optional entries:

ID= Specifies the inside diameters of the inlet and outlet shellsidenozzles. Enter inlet and outlet values, separated by a comma. Ifnot entered, HEXTRAN uses a conventional nozzle size.

NONE Suppresses nozzle pressure drop calculations.

CALCULATION DPE UNIT OPERATIONS Data Category of Input

Optional statement. This statement sets calculation methods for individual exchangers on aglobal basis. Methods can be selected globally using the CALCULATION statement in theSIMULATION, CASESTUDIES, OPTIMIZATION AREA, OPTIMIZATION SPLIT, or REGRESSIONcategories of input.

Optional entries:

NOCHECK Suppresses HEXTRAN geometry consistency checks and pre-vents HEXTRAN from assigning default values to missing ge-ometry data. NOCHECK is designed to allow you to access HTRIor HTFS defaults in place of HEXTRAN defaults. When using NO-CHECK, ensure that all exchanger data are explicitly specified, orthat one of the HTRI (ST5, CST3, RKH3, ACE2) or HTFS (TASC3)modules is referenced (see the HTRI and HTFS documentation).

WARNING: Using NOCHECK with inconsistent or missing ge-ometry data may result in abnormal program termination (divi-sion by zero, overflow, etc.).

TWOPHASE=NEW Specifies the methods for thermal and hydraulic calculations forall rigorous exchangers. Enter NEW or OLD. NEW uses theModified Chen vaporization method for convective boiling, andincludes predictions for sub-cooled and film boiling. Condensa-tion methods account for flow regimes and gravity versus sheareffects. Pressure drops are calculated using a stream analysis-based method. NEW automatically sets DPSMETHOD=STREAM.OLD selects algorithms used in versions 5.0x and earlier. Usethis option to make comparison runs with earlier versions ofHEXTRAN. The default is NEW.

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SPECIFICATION DPE UNIT OPERATIONS Data Category of Input

Optional statement. This statement specifies exchanger performance criteria. HEXTRAN re-ports the required shellside fouling factor to match the specified area.

Optional entries:

TEMPERATURE= and Specifies the outlet temperature of the stream specified by theSHELL or TUBE keyword. The units are F (English), C (metric),or K (SI). You cannot enter TEMPERATURE with any other speci-fication keywords. There is no default.

SHELL orTUBE or

Specifies the side of the exchanger being used by the TEMPERA-TURE keyword. SHELL and TUBE can also be used with theLFRAC keyword. There is no default.

LFRAC= and Specifies the liquid weight fraction of the stream. Enter a valuefrom 0.0 (all vapor) to 1.0 (all liquid). This keyword must beused in conjunction with the SHELL, TUBE, HOT, or COLD key-word to apply the LFRACTION to the correct stream. You cannotenter LFRAC with any other specification keywords. There is nodefault.

SHELL orTUBE orHOT orCOLD or

Specifies the side of the exchanger being used by the LFRAC-TION keyword. You cannot use these keywords with any otherspecification keywords. There is no default.

DUTY= or Specifies the total heat transferred in the exchanger. You cannotuse DUTY with any other specification keywords. Units are:MMBtu/hr (English), MMkcal/hr (metric), and MMkJ/hr (SI).There is no default.

HOCI= orCOCI= orHIHO= orHICO=

Specifies the exchanger approach temperature. Use only one ofthese four and enter a numerical value. Each keyword specifies asubtraction operation where the first set of two characters de-fines a value, and the second set of two characters defines avalue that is subtracted from it. In the operation, H refers to HOTside, C refers to COLD side, I refers to inlet, and O refers to out-let. Therefore, HOCI specifies hot outlet temperature minus coldinlet temperature. You cannot use these keywords with any otherspecification keywords. Valid units are F (English) or C (metricand SI). There is no default.

Examples:SPEC TEMP=100, HOTSPEC TEMP=200, SHELLSPEC DUTY=8.5SPEC LFRAC=0.8, HOTSPEC LFRAC=0.9, SHELLSPEC HOCI=40

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PRINT DPE UNIT OPERATIONS Data Category of Input

Optional statement. This statement specifies report print options for the exchanger statement.The default printout options are the global values specified in the CALCULATION section.STANDARD and EXTENDED are defaults. STANDARD will be printed in addition to any speci-fied keywords. EXTENDED will be overwritten by any specified keywords.

Optional entries:

STANDARD Prints the standard TEMA Data Sheet. This is the default.

EXTENDED Prints the Extended Data Sheet. This is the default.

ZONES Prints the zones analysis for two-phase exchangers.

MONITOR Prints the design logic monitor for NEW exchangers.

Examples:PRINT EXTENDED, ZONES

This example prints standard, extended, and zones analysis reports.PRINT MONITOR

This example prints standard and design logic monitor reports.PRINT STANDARD

This example prints only the standard report.PRINT ZONES MONITOR

This example prints standard, zones analysis, and design logic monitor reports.

COST DPE UNIT OPERATIONS Data Category of Input

Optional statement. This statement provides special costing data for an exchanger. The de-faults are the global values given in the CALCULATION section.

Optional Entries:

BSIZE=1000.00 Defines the base area used in the costing equation. The defaultis 1000.00 ft 2 (English), or 93.0 m2 (metric and SI).

BCOST=0.00 Defines the base cost used in the costing equation. The defaultis 0.00 USDOLLAR/ft 2 (English), or 0.00 USDOLLAR/m2 (metricand SI).

LINEAR=50.00 Defines the linear cost factor used in the costing equation. Thedefault is 50.00 USDOLLAR/ft 2 (English), or 538.20 USDOLLAR/m 2 (metric and SI).

EXPONENT=0.60 Defines the exponential cost factor used in the costing equation.The default is 0.60 (English, metric and SI).

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CONSTANT=0.00 Defines the constant cost factor used in the costing equation.This entry can be used to define fixed costs associated with in-stallation of an exchanger and is not a function of exchangersize. The default is 0.00.

UNIT orSHELL

Defines the basis for the exchanger CONSTANT cost factor. UNITresults in the constant cost factor being applied once to eachunit regardless of the number of shells or frames in the unit.SHELL results in the constant cost factor being applied to eachshell or each frame in the unit. The default is UNIT.

Figure 4-22: Longitudinal Fin Details

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Double Pipe Cross Section

Shell IDTube ODTube ID

Fin Height

Fin Thickness

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MTE HEAT EXCHANGERS

Multi-tube exchangers (MTEs) are similar in construction to double pipeexchangers, except the inner pipe is replaced with a bundle of tubes. Eachleg of the MTE’s U-tube bundle is welded into a separate shell with ahousing for the return bend.

Figure 4-23: Multi-tube Exchanger

Figure 4-23 shows a typical MTE. The HEXTRAN specifications for thisMTE are:

■ 1 Shell

■ 7 Tubes

■ 1 Tube pass

The MTE model is available only in rating mode. It provides rigorousthermal and hydraulic performance for countercurrent and cocurrent flow.All fluid types are supported on either side of the exchanger, andvaporization and condensation are automatically treated by zone analysis.

Multi-tube exchangers are typically constructed from seamless steel piperanging in size from 3-8 inches Nominal Pipe Size (NPS). Tubes rangefrom 0.75 inches to 1 inch NPS and may be bare or have longitudinal fins.Computed pressure drops include the pressure drops across the nozzles bydefault, and nozzles will be automatically sized when data are not provided.Numerous tuning parameters have been provided for matching plant data asdescribed in Table 4-37.

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Effective Tube Length

Front View Side View

Multi-Tube Exchanger

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TYPE MTE UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement defines the basic characteristics of the rodbaffleexchanger.

Mandatory entries:

OLD Identifies the exchanger as an existing exchanger that is to berated. There is no default.

Examples:MTE UID=STE2

TYPE OLD

Optional entries:

HOTSIDE=SHELL Specifies the side of the exchanger receiving the hotside fluid.Enter SHELL or TUBE. If not specified, this value is determinedfrom the stream inlet temperatures. SHELL is the default.

ORIENTATION=HORIZONTAL Specifies the exchanger orientation, which affects both the filmcoefficient for condensers and the static head for verticalsingle-pass tubes and/or shells. Enter HORIZONTAL or VERTI-CAL. The default is HORIZONTAL.

FLOW=COUNTERCURRENT Specifies the relative flow direction between the shellside fluidand the tubeside fluid. Enter COUNTERCURRENT or COCUR-RENT. This entry affects the calculation of the LMTD correctionfactor (FT). The default is COUNTERCURRENT.

AREA=1000 or Specifies the shellside effective or “installed” area per unit. Thearea covered by the tubesheets and baffles is subtracted fromthe outside area of the tubes. If AREA is not entered, this valuewill be calculated from the tube information. AREA is checkedfor consistency with tube information. The default is 1000 ft 2

(English) or 92.9 m 2 (metric and SI).

UESTIMATE=50 Specifies the initial U-value for the flowsheet energy balance.The default is 50 Btu/hr-ft 2 -F (English), 244.1 kcal/hr-m2-C(metric), or 283.9 W/m 2 -K (SI).

USCALER=1.0 Specifies a multiplier used to adjust the rigorously computedU-value to approximate actual plant data. The default is 1.0.

Example:TYPE OLD, HOTSIDE=TUBE, TEMA=AJ2S, AREA=5000,*

UESTIMATE=60, USCALER=0.9

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TUBESIDE MTE UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement defines details for the tubeside of the exchanger. Thearea for heat transfer is computed using the following formula, and is cross-checked againstthe AREA entry supplied on the TYPE statement:

AREA OD LENGTH SHEETS NUMBER= −π* * ( _ *

where:

OD, LENGTH, and NUMBER are defined on TUBE statement

Note that the tube outside diameter in the above calculations can be determined from the in-side diameter and the Birmingham Wire Gauge (BWG) or THICKNESS entries on the TUBEstatement. Conversely, the tube inside diameter can be determined from the outside diameterand either the BWG or THICKNESS entries on the TUBE statement.

Mandatory entries:

FEED= Identifies the feed, or inlet stream, and its associated properties.Enter up to twelve alphanumeric characters. The FEED entry willbe printed as a label in the output. There is no default.

PRODUCT= Identifies the product, or outlet stream, and its associatedproperties. Enter up to twelve alphanumeric characters. ThePRODUCT entry will be printed as a label in the output. There isno default.

Example:TUBE FEED=CRD1, PRODUCT=CRD2

Optional entries:

LENGTH=20 or Specifies the exchanger tube length. The default value is 20 ft(English) or 6.1 m (metric and SI).

ID=0.584 and/or Specifies the inside diameter of the tube. This value will be auto-matically computed from the OD and THICKNESS or BWG en-tries. The default values are 0.584 in. (English) or 14.834 mm(metric and SI).

OD=0.75 and/or Specifies the outside diameter of the tube. The default is 0.75 in.(English) or 19.05 mm (metric and SI).

THICKNESS=0.083 or Specifies the thickness of the tube wall. The default is 0.083 in.(English) or 2.108 mm (metric and SI).

BWG=14 Specifies a value from the Birmingham Wire Gauge, an alternateway to define tube thickness. The default is 14.

Note: Either BWG or THICKNESS may be given if OD is entered,but not both. If both ID and OD are given, neither BWG norTHICKNESS is allowed.

NPS= Specifies the nominal pipe size in inches. If supplied, SCHEDULEmust also be supplied. Valid NPS entries are shown in Table4-42.

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SCHEDULE= and Specifies the steel pipe schedule. If supplied, NPS must also besuplied. Valid SCHEDULE entries are shown in Table 4-43.

Note: You cannot enter OD, ID, BWG or THICKNESS with NPSand SCHEDULE.

NUMBER= This represents the tube count per bundle on a ‘‘per shell’’ basis.For U tubes, NUMBER corresponds to the number of holes inthe tubesheet (twice the number of complete U tubes). If notspecified, this value will be derived based on the AREA suppliedon the TYPE statement and the SHELL ID, using the tube countmethod described in The Heat Exchanger Design Handbook,page 3.5-11, Hemisphere Publishing Corporation, New York,1983. There is no default.

PASS=2 or Specifies the number of tube passes per shell. Enter an integerfrom 1 to 16. One pass corresponds to true counterflow. The de-fault is 2.

PATTERN= Specifies a tube pattern code. 90 (square) is the only valid entry.There is no default.

PITCH= Specifies the tube pitch, which is defined as the center-to-centerdistance between adjacent tubes. Tube pitch is typically 1.25times tube outside diameter (OD). There is no default.

MATERIAL=01 Specifies the tube material, either by code or by an alphanu-meric name. When an appropriate code number is entered, thethermal conductivity and density are selected from Table 4-36,Allowable Material Codes. Alphanumeric entries are treated asnames for printout purposes only. The default is 01 (CARBONSTEEL).

DENSITY=490.8 Specifies tube material density. This entry is used to computethe total weight of the exchanger when MATERIAL is specifiedby alphanumeric name. When a valid MATERIAL code is entered,the density value is selected automatically from Table 4-36; how-ever, this entry will override the selected value. The default is490.8 lb/ft3 (English) or 7862 kg/m3 (metric and SI).

CONDUCTIVITY=30 Specifies tube metal thermal conductivity. This entry is used todetermine the resistance to heat transfer through the tube wall.When a valid MATERIAL code is entered, this value is selectedfrom Table 4-36. The default is 30 Btu/hr-ft-F (English), 44.6kcal/hr-m-C (metric), or 51.9 W/m-K (SI).

FOUL=0.002 Specifies the tubeside fouling resistance based on tubeside area.To simulate a ‘‘clean’’ exchanger, enter a value of zero on bothTUBE and SHELL statements. The default is 0.002 hr-ft 2 -F/Btu(English), 0.00041 hr-m 2 -C/kcal (metric), or 0.00035 m 2 -K/W(SI).

LAYER=0.0 Specifies the tubeside fouling layer thickness. This entry repre-sents the effect of fouling on the tubeside pressure drop. (Theeffect of fouling on heat transfer is represented by the FOUL en-try). The default is 0.0 in. (English) or 0.0 mm (metric and SI).

HI= or Specifies an inside film coefficient. This entry overrides thecomputed value.

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HSCALER=1.0 Specifies a multiplier for the computed film coefficient. You can-not use HSCALER if USCALER is specified on the TYPE state-ment. The default is 1.0.

DPSHELL= or Specifies the value for pressure drop per bundle. This entryoverrides the computed value.

DPUNIT= Specifies the value for pressure drop per service. This entryoverrides the computed value. There are no defaults.

DPSCALER=1.0 Specifies an optional multiplier to adjust the computed tubesidepressure drop to more closely approximate actual plant per-formance. The default is 1.0.

PDESIGN= Specifies a tubeside design pressure. This entry overrides thecomputed value. There is no default.

Example:TUBE FEED=CRD1, PROD=CRD2, LENGTH=20, OD=0.75,*

BWG=16, NUMBER=400, PASS=4, PATTERN=30,*FOUL=0.005, DPSCALER=1.1, HSCALER=0.9

FINS MTE UNIT OPERATIONS Data Category of Input

Optional statement. This statement specifies details for finned tubes. Figure 4-22 illustratesthe longitudinal fin construction for double pipe exchangers. The fins are manufactured as U-channels and welded onto the inner pipe. They are installed in multiples of 4 and can be madeof a different material than the pipe.

Mandatory entries:

None.

Optional entries:

NUMBER =24 Specifies the number of fins per pipe. The default is 24.

HEIGHT=0.7815 Specifies the fin height. If HEIGHT is not specified, this value willbe calculated from inside and outside pipe diameters as: HEIGHT= (SHELL ID - TUBE OD) / 2. The default is 0.7815 in. (English),or 19.85 mm (metric and SI).

MATERIAL=01 Specifies the fin material, either by code or by an alphanumericname. When an appropriate code number is entered, the thermalconductivity and density are selected from Table 4-36, AllowableMaterial Codes. Alphanumeric entries are treated as names forprintout purposes only. The default is 01 (CARBON STEEL).

CONDUCTIVITY=30 Specifies fin metal thermal conductivity. This entry is used todetermine the resistance to heat transfer through the tube wall.When a valid MATERIAL code is entered, this value is selectedfrom Table 4-36; however, this entry overrides the selectedvalue. The default is 30 Btu/hr-ft-F (English), 44.6 kcal/hr-m-C(metric), or 51.9 W/m-K (SI).

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THICKNESS=0.050 Specifies the fin thickness. The default is 0.050 in. (English), or1.27 mm (metric and SI).

AREA= Specifies the fin area per unit length of one tube. This entry isused to compute the fin area in place of the fin geometry sup-plied. No consistency check is made between this entry and thearea value determined from NUMBER, HEIGHT, and THICKNESS.There is no default.

EFFICIENCY= Specifies the fin efficiency. If not specified, HEXTRAN will calcu-late the value.

Examples:FINS NUMBER=26, ROOT=0.75, HEIGHT=0.0625, EFFICIENCY=0.90FINS HEIGHT=0.0635, AREA=0.52

SHELLSIDE MTE UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement defines all details for the shellside of the exchanger.

Mandatory entries:

FEED= Identifies the feed, or inlet, stream and its associated properties.Enter up to twelve alphanumeric characters. The FEED entry willbe printed as a label in the output. There is no default.

PRODUCT= Identifies the product, or outlet, stream and its associatedproperties. Enter up to twelve alphanumeric characters. ThePRODUCT entry will be printed as a label in the output. There isno default.

Optional entries:

ID=6.065 or Specifies the inside diameter of the outer pipe (shell). The de-fault is 6.065 in. (English), or 154 mm (metric and SI).

NPS= and Specifies the nominal pipe size in inches. If supplied, SCHEDULEmust also be supplied. Valid NPS entries are shown in Table4-42.

SCHEDULE= Specifies the steel pipe schedule. If supplied, NPS must also besuplied. Valid SCHEDULE entries are shown in Table 4-43.

SERIES=1 Specifies the number of identical shells in series. Enter an inte-ger from 1 to 10. The default is 1.

PARALLEL=1 Specifies the number of identical shells in parallel. Enter an inte-ger from 1 to 10. The default is 1.

MATERIAL=01 Specifies the outer pipe (shell) material, either by code or by analphanumeric name. When an appropriate code number is en-tered, the thermal conductivity and density are selected from Ta-ble 4-36, Allowable Material Codes. Alphanumeric entries aretreated as names for printout purposes only. The default is 01(CARBON STEEL).

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DENSITY=490.8 Specifies outer pipe (shell) material density. This entry is usedto compute the total weight of the exchanger when MATERIAL isspecified by alphanumeric name. When a valid MATERIAL codeis entered, the density value is selected automatically from Table4-36; however, this entry overrides the selection. The default is490.8 lb/ft3 (English), or 7862 kg/m3 (metric and SI).

FOUL=0.002 Specifies the shellside fouling resistance based on shellsidearea. To simulate a ‘‘clean’’ exchanger, enter a value of zero forFOUL on both TUBE and SHELL statements. The default is 0.002hr-ft 2 -F/Btu (English), 0.00041 hr-m 2 -C/kcal (metric), or0.00035 m 2 -K/W (SI).

LAYER=0.0 Specifies the shellside fouling layer thickness. This entry repre-sents the effect of fouling on the shellside pressure drop. (Theeffect of fouling on heat transfer is represented by the FOUL en-try.) The default is 0.0 in. (English), or 0.0 mm (metric and SI).

HO= or Specifies a user-supplied shellside film coefficient. This entryoverrides the computed value for both rating and design cases.

HSCALER=1.0 Specifies a multiplier for the computed film coefficient. Do notuse HSCALER if USCALER is specified on the TYPE statement.The default is 1.0.

DPSHELL= Specifies the value for pressure drop per shell. This entry over-rides the computed value. There is no default. You cannot enterDPSHELL and DPUNIT together.

DPUNIT= Specifies the value for pressure drop per service. This entryoverrides the computed value. There is no default. You cannotenter DPUNIT and DPSHELL together.

DPSCALER=1.0 Specifies an optional multiplier to adjust the computed shellsidepressure drop to approximate actual plant performance. The de-fault is 1.0.

PDESIGN= Specifies a shellside design pressure. This entry overrides thecomputed value. There is no default.

TNOZZLE MTE UNIT OPERATIONS Data Category of Input

Optional Statement. This statement defines the tubeside nozzle characteristics. Nozzles areautomatically included in pressure drop calculations unless NONE is specified on the TNOZZLEstatement. Nozzles are automatically sized when data area not provided.

Optional entries:

ID= Specifies the inside diameters of the inlet and outlet tubesidenozzles. Enter inlet and outlet values, separated by a comma. Ifnot entered, HEXTRAN uses a conventional nozzle size.

NONE Suppresses nozzle sizing and pressure drop calculations.

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SNOZZLE MTE UNIT OPERATIONS Data Category of Input

Optional Statement. This statement defines the shellside nozzle characteristics. Nozzles areautomatically included in pressure drop calculations unless NONE is specified on the SNOZ-ZLE statement. Nozzles are automatically sized when data area not provided.

Optional entries:

ID= Specifies the inside diameters of the inlet and outlet shellsidenozzles. Enter inlet and outlet values, separated by a comma. Ifnot entered, HEXTRAN uses a conventional nozzle size.

NONE Suppresses nozzle pressure drop calculations.

CALCULATION MTE UNIT OPERATIONS Data Category of Input

Optional statement. This statement sets calculation methods for individual exchangers on aglobal basis. Methods can be selected globally using the CALCULATION statement in theSIMULATION, CASESTUDIES, OPTIMIZATION AREA, OPTIMIZATION SPLIT, or REGRESSIONcategories of input.

Optional entries:

NOCHECK Suppresses HEXTRAN geometry consistency checks and pre-vents HEXTRAN from assigning default values to missing ge-ometry data. NOCHECK is designed to allow you to access HTRIor HTFS defaults in place of HEXTRAN defaults. When using NO-CHECK, ensure that all exchanger data are explicitly specified, orthat one of the HTRI (ST5, CST3, RKH3, ACE2) or HTFS (TASC3)modules is referenced, (see the HEXTRAN HTRI and HTFS InputGuides).

WARNING: Using NOCHECK with inconsistent or missing ge-ometry data may result in abnormal program termination (divi-sion by zero, overflow, etc.).

MINFT=0.8 Specifies the minimum allowable LMTD correction factor (FT).The default is 0.8.

DPSMETHOD=STREAM Specifies the pressure drop calculation method used for shell-side calculations. Enter BELL (Kenneth Bell of Delaware Univer-sity method) or STREAM (stream analysis method). STREAM isthe default.

Reference: ‘‘A New and Accurate Hand Calculation Method forShellside Pressure Drop and Flow Distribution,’’ Wills, M. J. N.,and D. Johnston, Presented at the 22nd Heat Transfer Confer-ence and Exhibition, Niagara Falls, N.Y., 1984.

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TWOPHASE=NEW Specifies the methods for thermal and hydraulic calculations forall rigorous exchangers. Enter NEW or OLD. NEW uses the Modi-fied Chen vaporization method for convective boiling, and in-cludes predictions for sub-cooled and film boiling. Condensationmethods account for flow regimes and gravity versus shear ef-fects. Pressure drops are calculated using a stream analysis-based method. NEW automatically sets DPSMETHOD=STREAM.OLD selects algorithms used in versions 5.0x and earlier. Use thisoption to make comparison runs with earlier versions of HEX-TRAN. The default is NEW.

SPECIFICATION MTE UNIT OPERATIONS Data Category of Input

Optional statement. This statement specifies exchanger performance criteria. HEXTRAN re-ports the required shellside fouling factor to match the specified area.

Optional entries:

TEMPERATURE= and Specifies the outlet temperature of the stream specified by theSHELL or TUBE keyword. The units are F (English), C (metric),or K (SI). You cannot enter TEMPERATURE with any other speci-fication keywords. There is no default.

SHELL or

TUBE or Specifies the side of the exchanger being used by the TEMPERA-TURE keyword. SHELL and TUBE can also be used with theLFRAC keyword. There is no default.

LFRAC= and Specifies the liquid weight fraction of the stream. Enter a valuefrom 0.0 (all vapor) to 1.0 (all liquid). This keyword must beused in conjunction with the SHELL, TUBE, HOT, or COLD key-word to apply the LFRACTION to the correct stream. You cannotenter LFRAC with any other specification keywords. There is nodefault.

SHELL orTUBE orHOT orCOLD or

Specifies the side of the exchanger being used by the LFRAC-TION keyword. You cannot use these keywords with any otherspecification keywords. There is no default.

DUTY= or Specifies the total heat transferred in the exchanger. You cannotuse DUTY with any other specification keywords. Units are:MMBtu/hr (English), MMkcal/hr (metric), and MMkJ/hr (SI).There is no default.

HOCI= orCOCI= orHIHO= orHICO=

Specifies the exchanger approach temperature. Use only one ofthese four and enter a numerical value. Each keyword specifies asubtraction operation where the first set of two characters de-fines a value, and the second set of two characters defines avalue that is subtracted from it. In the operation, H refers to HOTside, C refers to COLD side, I refers to inlet, and O refers to

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outlet. Therefore, HOCI specifies hot outlet temperature minuscold inlet temperature. You cannot use these keywords with anyother specification keywords. Valid units are F (English) or C(metric and SI). There is no default.

Examples:SPEC TEMP=100, HOTSPEC TEMP=200, SHELLSPEC DUTY=8.5SPEC LFRAC=0.8, HOTSPEC LFRAC=0.9, SHELLSPEC HOCI=40

PRINT MTE UNIT OPERATIONS Data Category of Input

Optional statement. This statement specifies report print options for the exchanger statement.The default printout options are the global values specified in the CALCULATION section.STANDARD and EXTENDED are defaults. STANDARD will be printed in addition to any speci-fied keywords. EXTENDED will be overwritten by any specified keywords.

Optional entries:

STANDARD Prints the standard TEMA Data Sheet. This is the default.

EXTENDED Prints the Extended Data Sheet. This is the default.

ZONES Prints the zones analysis for two-phase exchangers.

MONITOR Prints the design logic monitor for NEW exchangers.

Examples:PRINT EXTENDED, ZONES

This example prints standard, extended, and zones analysis reports.PRINT MONITOR

This example prints standard and design logic monitor reports.PRINT STANDARD

This example prints only the standard report.PRINT ZONES, MONITOR

This example prints standard, zones analysis, and design logic monitor reports.

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COST MTE UNIT OPERATIONS Data Category of Input

Optional statement. This statement provides special costing data for an exchanger. The de-faults are the global values given in the CALCULATION section.

Optional Entries:

BSIZE=1000.00 Defines the base area used in the costing equation. The defaultis 1000.00 ft 2 (English), or 93.0 m2 (metric and SI).

BCOST=0.00 Defines the base cost used in the costing equation. The defaultis 0.00 USDOLLAR/ft 2 (English), or 0.00 USDOLLAR/m2 (metricand SI).

LINEAR=50.00 Defines the linear cost factor used in the costing equation. Thedefault is 50.00 USDOLLAR/ft 2 (English), or 538.20 USDOLLAR/m 2 (metric and SI).

EXPONENT=0.60 Defines the exponential cost factor used in the costing equation.The default is 0.60 (English, metric and SI).

CONSTANT=0.00 Defines the constant cost factor used in the costing equation.This entry can be used to define fixed costs associated with in-stallation of an exchanger and is not a function of exchangersize. The default is 0.00.

UNIT orSHELL

Defines the basis for the exchanger CONSTANT cost factor. UNITresults in the constant cost factor being applied once to eachunit regardless of the number of shells or frames in the unit.SHELL results in the constant cost factor being applied to eachshell or each frame in the unit. The default is UNIT.

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FTE HEAT EXCHANGER

FTE FTE UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement identifies the unit as a finned-tube exchanger. It must bethe first input line for any FTE model.

The finned-tube exchanger (FTE) is a general model which can be used to rate or design anypiece of equipment which has a gas flowing through a rectangular duct over a bank of tubes.Only a horizontal tube arrangement is allowed. The tubeside may have a single-phase or two-phase fluid.

The most common application is for waste heat boilers, but air pre-heaters or coolers mayalso be rated or designed. Note that the air-cooled exchanger (ACE) in HEXTRAN is more con-venient for representation of air coolers and also performs calculations for the fans.

Tubes may be plain or finned and the fins may be of a different metal than the tubes. When aperformance specification is provided, the fouling which corresponds to the specified heattransfer is computed. By default, the presure drop across the tubeside nozzles is included inthe calculations.

Design Process

This section describes the general process performed by HEXTRAN for the design option.

First, the rating module is called using some reasonable assumptions for the various perform-ance and geometric parameters. These include:

� An estimated U-value based on the outside area. The user may input a value or theprogram will assign a value of 5 Btu/hr-ft 2 -F in the English system of units.

� The number of tube passes is set equal to the average between the user-specified up-per and lower limits, subject to a minimum value of 1 pass.

� The number of tube rows is set equal to 4.

� The tube length is set equal to the average value between the user-specified upper andlower values.

Next, knowing the heat duty, the required area, A, is estimated using the followingrelationship:

AQ

U LMTD=

( ))

where:

LMTD = log mean temperature difference

This area is then used to estimate the number of tubes in the bundle, as given by:

NA

L APUL=

( )

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where:

APUL = the tube outside area per tube per unit length L = tube length

With the above information calculated, the existing rating module is then called. The perform-ance values generated by this module are used to systematically modify various parametersand achieve the user-specified constraints. For example, the number of tube rows is modifiedusing the fact that the ductside pressure drop is proportional to ROWS 2.8 , for a given sur-face area.

For the design option, the program attempts to arrive at a reasonable aspect ratio (i.e.,LENGTH/ WIDTH ratio). However, if a very tight tolerance has been specified for bundle (i.e.,bay) width, the aspect ratio criteria are ignored by the program. For this situation, the tubelength constraints may also be violated.

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FTE Design Logic

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TYPE FTE UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement defines the basic characteristics of the finned-tubeexchanger.

Mandatory entries:

OLD or Rating only. Identifies an existing exchanger to be rated.

NEW Design only. Identifies a new exchanger to be designed.

Examples:FTE UID=FTE2

TYPE OLDFTE UID=EX23

TYPE NEW

Optional entries:

HOTSIDE=TUBE Specifies the side of the exchanger receiving the hotside fluid.Enter TUBE or DUCT. If not specified, this value is determinedfrom the stream inlet temperature. TUBE is the default.

FLOW=COUNTERCURRENT Specifies the relative flow direction between the tubeside fluidand the ductside fluid. Enter COUNTERCURRENT or COCUR-RENT. This entry affects the calculation of the LMTD correctionfactor (FT), and, thereby, the MTD. The default isCOUNTERCURRENT.

AREA=79.0 or Rating only. Specifies the effective or “installed” area per bundlefor OLD exchanger calculations. For finned tubes, fin area mustalso be included. If AREA is not entered, this value will be calcu-lated from the input tube information. AREA is checked for con-sistency with tube information. The default is 79.0 ft 2 (English),or 7.34 m 2 (metric and SI) for bare tubes, and 990.0 ft 2 (Eng-lish), or 92.0 m 2 (metric and SI) for finned tubes.

AREA= Design only. Specifies upper and lower limits for effective or “in-stalled” area per bundle. Enter minimum and maximum values.

UESTIMATE=5 Specifies the initial U-value for the flowsheet energy balance.The default is 5 Btu/hr-ft 2 -F (English), 24.4 kcal/hr-m2-C (met-ric), or 28.4 W/m 2 -K (SI).

USCALER=1.0 Specifies a multiplier used to adjust the rigorously computedU-value to approximate actual plant data. The default is 1.0.

Example:TYPE OLD, HOTSIDE=TUBE, AREA=5000,*

UESTIMATE=60, USCALER=0.9

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TUBESIDE FTE UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement defines all necessary details for the tubeside of theexchanger.

Mandatory entries:

FEED= Identifies the feed, or inlet stream and its associated properties.Enter up to twelve alphanumeric characters. The FEED entry willbe printed as a label in the output. There is no default.

PRODUCT= Identifies the product, or outlet stream and its associated proper-ties. Enter up to twelve alphanumeric characters. The PRODUCTentry will be printed as a label in the output. There is no default.

Example:TUBE FED=CRD1, PRODUCT=CRD2

Optional entries:

LENGTH=20 or Rating only. Specifies the exchanger tube length. The default is20 ft (English), or 6.1 m (metric and SI).

LENGTH=24,40,2 Design only. Specifies minimum, maximum, and incrementaltube lengths. HEXTRAN uses the maximum length to initiate thedesign and reduces the length by specified increments if thetubeside pressure drop and velocity specifications cannot bemet at the minimum number of passes allowed for the design.The default values are: 8, 20, 4 ft (English), or 2.4, 6.1, 1.2 m(metric and SI).

Note: A design may be obtained for a fixed tube length (e.g.,LENGTH = 24, 24, 0).

ID=0.584 and/or Specifies the inside diameter of the tube. This value will be auto-matically computed from the OD and THICKNESS or BWG en-tries for bare tubes. The default values are 0.584 in. (English), or14.834 mm (metric and SI).

OD=0.75 Specifies the outside diameter of the tube. The default is 0.75 in.(English), or 19.05 mm (metric and SI).

THICKNESS=0.083 or Specifies the thickness of the tube wall. The default is 0.083 in.(English), or 2.108 mm (metric and SI).

BWG=14 Specifies a value from the Birmingham Wire Gauge, an alternateway to define tube thickness. Valid BWG values are listed in Ta-ble 4-39. The default is 14.

Note: Either BWG or THICKNESS may be given if OD is entered,but not both. If both ID and OD are given, neither BWG norTHICKNESS is allowed.

NUMBER=20 Rating only. Specifies the tube count per bundle. You mustspecify this value if AREA is not specified. Values for LENGTH,OD, and AREA override this entry. The default is 20.

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PASS=2 or Rating only. Specifies the number of tube passes per bundle.The default is 2.

PASS=1,12 Design only. Specifies the upper and lower limit for tube passesper bundle. Enter minimum and maximum values. The defaultsare 1,12.

PATTERN=INLINE Specifies a tube pattern code. Enter INLINE or STAGGERED. Thedefault is INLINE.

TPITCH=0.937 Specifies the tube pitch, which is the center-to-center distancebetween tubes in the direction nor-mal to ductside flow. If notentered, the value will be set equal to 1.25 times the tube diame-ter for bare tubes or 1.25 times the fin OD for finned tubes. Ifvalues are not supplied for TPITCH or for the tube or fin OD, thedefault values will be used. The defaults for bare tubes are 0.94in. (English) and 23.9 mm (metric and SI). The defaults forfinned tubes are 2.5 in. (English) and 63.5 mm (metric and SI).

LPITCH=0.937 Specifies the longitudinal tube pitch, which is the center-to-centerdistance between tubes in direction parallel to ductside flow. If notentered, the value will be set equal to 1.25 times the tube diameterfor bare tubes or 1.25 times the fin OD for finned tubes. If valuesare not supplied for TPITCH or for the tube or fin OD, the defaultvalues will be used. The defaults for bare tubes are 0.94 in. (Eng-lish) and 23.9 mm (metric and SI). The defaults for finned tubesare 2.5 in. (English) and 63.5 mm (metric and SI).

ROWS=1 Rating only. Specifies the number of tube rows per bundle. Thedefault is 1.

ROWS=2,12 Specifies the minimum and maximum number of tube rows perbundle. The defaults are 2,12.

MATERIAL=01 Specifies the tube material, either by code or by an alphanu-meric name. When an appropriate code number is entered, thethermal conductivity and density are selected from the materialcode table given in Table 4-36, Allowable Material Codes. Alpha-numeric entries are treated as names for printout purposes only.The default is 01 (CARBON STEEL).

CONDUCTIVITY=30 Specifies tube metal thermal conductivity. This entry is used todetermine the resistance to heat transfer through the tube wall.When a valid MATERIAL code is entered, this value is selectedfrom Table 4-36. The default is 30 Btu/hr-ft-F (English), 44.6kcal/hr-m-C (metric), or 51.9 W/m-K (SI).

FOUL=0.002 Specifies the tubeside fouling resistance. To simulate a ‘‘clean’’exchanger, enter a value of zero on both TUBE and DUCT state-ments. The default is 0.002 hr-ft 2 -F/Btu (English), 0.00041hr-m 2 -C/kcal (metric), or 0.00035 m 2 -K/W (SI).

LAYER=0.0 Specifies the tubeside fouling layer thickness. This entry repre-sents the effect of fouling on the tubeside pressure drop. (Theeffect of fouling on heat transfer is represented by the FOUL en-try.) The default is 0.0 in. (English), or 0.0 mm (metric and SI).

HI= or Specifies a user-supplied inside film coefficient. This entry over-rides the computed value for rating cases.

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HSCALER=1.0 Rating only. Specifies a multiplier for the computed film coeffi-cient. You cannot use HSCALER if USCALER is specified on theTYPE statement. The default is 1.0.

DPSHELL= or Rating only. Specifies the tubeside pressure drop per bundle.This entry overrides the computed value. You cannot enterDPSHELL and DPUNIT together.

DPSHELL= 5,15 or Design only. Specifies the lower and upper limit for pressuredrop per bundle.The average between the minimum and maxi-mum values will be used as the target pressure drop in obtain-ing a suitable tube bundle. The defaults are 5, 15 psi (English),0.35, 1.05 kg/cm 2 (metric), or 34.5, 103.4 kPa (SI). You cannotenter DPSHELL and DPUNIT together.

DPUNIT= Rating only. Specifies the value for pressure drop per service.This entry overrides the computed value. There are no defaults.You cannot enter DPSHELL and DPUNIT together.

DPUNIT= Design only. Specifies the value for pressure drop per service.Enter lower and upper limits. This keyword is identical toDPSHELL, as only one bundle is designed in each unit. There areno defaults. You cannot enter DPSHELL and DPUNIT together.

VELOCITY=0,1000 Design only. Specifies lower and upper limits for tubeside veloc-ity. Enter minimum and maximum values. The default is 0,1000ft/sec (English), or 0,305 m/s (metric and SI).

Note: A design may be carried out to yield a specified tubesidevelocity (average for single phase and at the inlet for condensa-tion cases). The resulting tubeside pressure drop may not be adesirable value, as the program ignores any tubeside pressuredrop constraints that you enter.

DPSCALER=1.0 Specifies an optional multiplier to adjust the computed tubesidepressure drop to more closely approximate actual plant per-formance. The default is 1.0.

SERIES=1 Rating only. Specifies the number of bundles per bay in series.Enter an integer from 1 to 10. The default is 1.

Note: The design option does not support multiple finned-tubeexchangers in series. However, you can specify multiple unitswithin a network.

PARALLEL=1 Rating only. Specifies the number of bundles per bay in parallel.Enter an integer from 1 to 10. The default is 1.

Note: The finned-tube exchanger may have identical multiple bayswhich are arranged in parallel as determined by the program for thedesign option, or as specified by the user for the rating option.

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Examples:

(Rating example)TUBE FEED=CRD1, PROD=CRD2, LENGTH=20, OD=0.75,*

BWG=16, NUMBER=400, PASS=4, PATTERN=30,*FOUL=0.005, DPSCALER=1.1, HSCALER=0.9

(Design example)TUBE FEED=CRD1, PROD=CRD2, LENGTH=16,40,4, OD=1.0,*

BWG=14, PASS=2,16,2, PATTERN=60, FOUL=0.004,*DPSHELL=8,12

FINS FTE UNIT OPERATIONS Data Category of Input

Optional statement. This statement specifies details for finned tubes.

Optional entries:

NUMBER =5 Specifies the number of fins per unit length. The default is 5fins/in. (English), or 197 fins/m (metric and SI).

THICKNESS=0.017 Specifies the fin thickness. The default is 0.017 in. (English), or0.432 (metric and SI).

HEIGHT=0.625 Specifies the fin height. The default is 0.625 in. (English), or15.87 mm (metric and SI).

AREA= Specifies the fin area per unit length of the tube. This entry isused to compute the shellside area in place of the fin geometrysupplied. Units are ft2/ft (English) or mm2/mm (metric and SI).No consistency check is made between this entry and the areavalue determined from NUMBER, HEIGHT, and THICKNESS.There is no default.

EFFICIENCY= Specifies the fin efficiency. If not specified, HEXTRAN will calcu-late the value.

MATERIAL=20 Specifies a material code or an alphanumeric name (up to 8characters). When an appropriate code number is entered, thethermal conductivity and density are selected from Table 4-36,Available Material Codes. Alphanumeric entries are treated asnames for printout purposes. The default is 20 (ALUMINUM).

CONDUCTIVITY=128.3 Specifies thermal conductivity. This entry is used to determinethe resistance to heat transfer through the fin. When a valid MA-TERIAL code is entered, this value is selected from Table 4-36;however, this entry overrides the selected value. The default is128.3 Btu/hr-ft-F in (English), 190.9 kcal/hr-m-C (metric), and222.1 W/m-K (SI).

BOND Specifies the fin bond resistance between the exchanger fins andthe tube OD. The defaults are 0.0 hr-ft 2 -F/Btu (English units),0.0 hr-m 2 -C/kcal (metric), and 0.0 m 2 -K/W (SI).

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Examples:FINS NUMBER=26, ROOT=0.75, HEIGHT=0.0625, EFFICIENCY=0.90FINS HEIGHT=0.0635, AREA=0.52

DUCTSIDE FTE UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement defines all details for the ductside of the exchanger.

Mandatory entries:

FEED= Identifies the feed, or inlet stream and its associated properties.Enter up to twelve alphanumeric characters. The FEED entry willbe printed as a label in the output. There is no default.

PRODUCT= Identifies the product, or outlet stream and its associatedproperties. Enter up to twelve alphanumeric characters. ThePRODUCT entry will be printed as a label in the output. There isno default.

Optional entries:

WIDTH= Rating only. Specifies the width of the bundle. If not specified, itwill be calculated as the number of tubes per row multiplied bythe transverse pitch.

WIDTH=5,20 Design only. Specifies lower and upper limits for the width of thebundle. Enter minimum and maximum values. If not specified, itwill be calculated as the number of tubes per row multiplied bythe transverse pitch. The defaults are: 5, 20 ft in English units;1.525, 6.096 m in metric and SI.

Note: A design may be obtained for a fixed bay width (e.g.,WIDTH = 5, 5). In this case, the actual bay width will be slightlydifferent from the specified value as the program must yield avalid tube length which has incremental values, while satisfyingthe heat transfer requirement.

LENGTH=20 Rating only. Specifies the length of bundle. This value is used tocalculate air flow velocity. If not specified, this value is set to thetube length. If a tube length is not specified either, the followingdefaults will be used: 20.0 ft (English units) 6.1 m (metric andSI).

FOUL=0.002 Specifies the ductside fouling resistance. To simulate a ‘‘clean’’exchanger, enter a value of zero for FOUL on both TUBE andDUCT statements. The default is 0.002 hr-ft 2 -F/Btu (English),0.00041 hr-m 2 -C/kcal (metric), or 0.00035 m 2 -K/W (SI).

LAYER=0.0 Specifies the ductside fouling layer thickness. This entry repre-sents the effect of fouling on the ductside pressure drop. (Theeffect of fouling on heat transfer is represented by the FOUL en-try.) The default is 0.0 in. (English), or 0.0 mm (metric and SI).

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HO= or Specifies a user-supplied shellside film coefficient. This entryoverrides the computed value for both rating and design cases.

HSCALER=1.0 Specifies a multiplier for the computed film coefficient. Do notuse HSCALER if USCALER is specified on the TYPE statement.The default is 1.0.

DPUNIT= Rating only. Specifies the value for pressure drop per bundle.This entry overrides the computed value. There are no defaults.

DPUNIT= Design only. Specifies lower and upper limits for pressure dropper service. Enter minimum and maximum values. HEXTRAN av-erages the minimum and maximum values for the target pres-sure drop in obtaining a suitable tube bundle. The defaults are0.3,0.7 in. H2O (English), or 7.62,17.8 mm H2O (metric and SI).

DPSCALER=1.0 Specifies an optional multiplier to adjust the computed shellsidepressure drop to more closely approximate actual plant per-formance. The default is 1.0.

VELOCITY= Design only. Specifies lower and upper limits for the ductsideforce velocities. Enter minimum and maximum values. There areno defaults.

Note: A design may be carried out to yield a specified ductsideface velocity; however, the ductside pressure drop may not be adesirable value.

PARALLEL= Rating only. Specifies the number of bays in parallel. There is nodefault.

PARALLEL= Design only. Specifies lower and upper limits for number of baysin parallel. Enter minimum and maximum values. There are nodefaults.

Examples:

(Rating example)DUCT FEED=GASI, PROD=GASO, WIDTH=8, FOUL=0.001,*

HSCALER=0.9, PARA=2

(Design example)DUCT FEED=GASI, PROD=GASO, WIDTH=5,10, FOUL=0.002,*

PARA=1,8

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TNOZZLE FTE UNIT OPERATIONS Data Category of Input

Optional Statement. This statement defines the tubeside nozzle characteristics. Nozzles areautomatically included in pressure drop calculations unless NONE is specified on the TNOZZLEstatement. Nozzles are automatically sized when data area not provided.

Optional entries:

ID= Specifies the inside diameters of the inlet and outlet tubesidenozzles. Enter inlet and outlet values, separated by a comma.Valid units are in. and mm. If not specified, HEXTRAN uses aconventional nozzle size.

NUMBER=1,1 Specifies the number of inlet and outlet nozzles per bundle. En-ter a value for the number of inlet nozzles, and outlet nozzles,separated by a comma. You must enter both values when usingthis keyword. The default is 1,1.

NONE Suppresses nozzle pressure drop calculations.

Examples:TNOZZLE ID=6,6, NUMBER=1,1

SPECIFICATION FTE UNIT OPERATIONS Data Category of Input

Optional for rating, mandatory for design. This statement specifies exchanger performancecriteria. When the exchanger is being rated, HEXTRAN reports the required ductside foulingfactor to match the specified area. For exchangers being designed, this statement determinesthe area required for the desired heat transfer.

Mandatory entries:

TEMPERATURE= and Specifies the outlet temperature of the product stream specifiedby the TUBE or DUCT keyword. The units are F (English), or C(metric and SI). You cannot enter TEMPERATURE with any otherspecification keywords. There is no default.

TUBE orDUCT or

Specifies the side of the exchanger being used by the TEMPERA-TURE keyword. You cannot use DUCT with any other specifica-tion keywords. TUBE can also be used with LFRAC.

LFRAC= and Specifies the liquid weight fraction of the stream. Enter a valuefrom 0.0 (all vapor) to 1.0 (all liquid). This keyword must beused in conjunction with the TUBE or COLD keyword to applythe LFRACTION to the correct stream. You cannot enter LFRACwith any other specification keywords. There is no default.

TUBE orCOLD or

Specifies the side of the exchanger being used by the LFRAC-TION keyword. You cannot use COLD with any other specifica-tion keywords. TUBE can also be used with TEMP.

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DUTY= or Specifies the total heat transferred in the exchanger. You cannotuse DUTY with any other specification keywords. Units are:MMBtu/hr (English), MMkcal/hr (metric), and MMkJ/hr (SI).There is no default.

HOCI= orCOCI= orHIHO= orHICO=

Specifies the exchanger approach temperature. Use only one of thesefour and enter a numerical value. Each keyword specifies a subtrac-tion operation where the first set of two characters defines a value,and the second set of two characters defines a value that is sub-tracted from it. In the operation, H refers to HOT side, C refers toCOLD side, I refers to inlet, and O refers to outlet. Therefore, HOCIspecifies hot outlet temperature minus cold inlet temperature. Youcannot use these keywords with any other specification keywords.Valid units are F (English), C, (metric and +SI). There is no default.

Examples:SPEC TEMP=100, HOTSPEC TEMP=200, DUCTSPEC DUTY=8.5SPEC LFRAC=0.8, HOTSPEC LFRAC=0.9, DUCTSPEC HOCI=40

CALCULATION FTE UNIT OPERATIONS Data Category of Input

Optional statement. This statement sets calculation methods for individual exchangers on aglobal basis. Methods can be selected globally using the CALCULATION statement in theSIMULATION, CASESTUDIES, OPTIMIZATION AREA, OPTIMIZATION SPLIT, or REGRESSIONcategories of input.

Optional entries:

NOCHECK Suppresses HEXTRAN geometry consistency checks and pre-vents HEXTRAN from assigning default values to missing ge-ometry data. NOCHECK is designed to allow you to access HTRIor HTFS defaults in place of HEXTRAN defaults. When using NO-CHECK, ensure that all exchanger data are explicitly specified, orthat f the HTRI ACE2 module is referenced (see the HEXTRANHTRI Input Guide).

WARNING: Using NOCHECK with inconsistent or missing ge-ometry data may result in abnormal program termination (divi-sion by zero, overflow, etc.).

TWOPHASE=NEW Specifies the methods for thermal and hydraulic calculations forall rigorous exchangers. Enter NEW or OLD. NEW uses theModified Chen vaporization method for convective boiling, andincludes predictions for sub-cooled and film boiling. Condensa-tion methods account for flow regimes and gravity versus sheareffects. Pressure drops are calculated using a stream analysis-based method. NEW automatically sets DPSMETHOD=STREAM.OLD selects algorithms used in versions 5.0x and earlier. Use

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this option to make comparison runs with earlier versions ofHEXTRAN. The default is NEW.

COST FTE UNIT OPERATIONS Data Category of Input

Optional statement. This statement provides special costing data for an exchanger. The de-faults are the global values given in the CALCULATION category of input.

Optional Entries:

BSIZE=1000.00 Defines the base area used in the costing equation. The defaultis 1000.00 ft 2 (English), or 93.0 m2 (metric and SI).

BCOST=0.00 Defines the base cost used in the costing equation. The defaultis 0.00 USDOLLAR/ft 2 (English), or 0.00 USDOLLAR/m2 (met-ric and SI).

LINEAR=50.00 Defines the linear cost factor used in the costing equation. Thedefault is 50.00 USDOLLAR/ft 2 (English), or 538.20 USDOL-LAR/m 2 (metric and SI).

EXPONENT=0.60 Defines the exponential cost factor used in the costing equation.The default is 0.60 (English, metric and SI).

CONSTANT=0.00 Defines the constant cost factor used in the costing equation.This entry can be used to define fixed costs associated with in-stallation of an exchanger and is not a function of exchangersize. The default is 0.00.

UNIT orSHELL

Defines the basis for the exchanger CONSTANT cost factor. UNITresults in the constant cost factor being applied once to eachunit regardless of the number of shells or frames in the unit.SHELL results in the constant cost factor being applied to eachshell or each frame in the unit. The default is UNIT.

PRINT FTE UNIT OPERATIONS Data Category of Input

Optional statement. This statement specifies report print options for the exchanger statement.The default printout options are the global values specified in the CALCULATION section.STANDARD and EXTENDED are defaults. STANDARD will be printed in addition to any speci-fied keywords. EXTENDED will be overwritten by any specified keywords.

Optional entries:

STANDARD Prints the standard TEMA Data Sheet. This is the default.

EXTENDED Prints the Extended Data Sheet. This is the default.

ZONES Prints the zones analysis for two-phase exchangers.

MONITOR Prints the design logic monitor for NEW exchangers.

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Examples:PRINT EXTENDED, ZONES

This example prints standard, extended, and zones analysis reports.PRINT MONITOR

This example prints standard and design logic monitor reports.PRINT STANDARD

This example prints only the standard report.PRINT ZONES, MONITOR

This example prints standard, zones analysis, and design logic monitor reports.

HTRI FTE UNIT OPERATIONS Data Category of Input

Optional statement. This statement specifies the HTRI module to be used for rating or design.See the HEXTRAN HTRI Input Guide for details.

Mandatory entries:

ACE2

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ACE HEAT EXCHANGER

ACE ACE UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement identifies the unit as an air-cooled exchanger. It must bethe first input line for any ACE model.

Air-cooled heat exchangers (ACE) employ banks of tubes to cool fluids with ambient air. Theyconsist of one or more tube sections served by one or more axial fans, fan drivers, speed re-ducers, and an enclosing and supporting structure. In forced-draft exchangers, the tube sec-tion is located on the discharge side of the fan. In induced-draft exchangers, the tube sectionis on the intake side of the fan. The tubeside may have a single-phase or two-phase fluid. Onlya horizontal tube arrangement is allowed.

Fan sizes can range from 3 to 28 ft in diameter and may be driven by electric motors, steamturbines, or other types of drivers. Bays with two fans each are popular since this provides abackup in the event of failure of a fan or driver. Multiple tube bundles are often used per fanbay in any number of possible arrangements. Typical plan views for air coolers are illustratedin Figure 4-24.

Figure 4-24: Plan Views of Air Coolers

The air-cooled exchanger module supports most types of bay and tube arrangements for therating option. Calculations are also performed for fans. In rating mode, information on the air-side flow is available by supplying fan power data. When fan power is not supplied, HEXTRANcalculates the power corresponding to the flow of the airside fluid. For the design option, fanpower specification is not allowed.

Tubes may be plain or finned and the fins can be of a different metal than the tubes. When aperformance specification is provided, the fouling which corresponds to the specified heattransfer is computed. By default, the pressure drop across the tubeside nozzles is included inthe calculations.

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Design Process

This section describes the general process performed by HEXTRAN for the design option.

First, the rating module is called using some reasonable assumptions for the various perform-ance and geometric parameters. These include:

� An estimated U-value based on the outside area. The user may input a value or theprogram will assign a value of 5 Btu/hr-ft 2 -F in the English system of units.

� The number of tube passes is set equal to the average between the user-specified up-per and lower limits, subject to a minimum value of 1 pass.

� The number of tube rows is set equal to 4.

� The tube length is set equal to the average value between the user-specified upper andlower values.

Next, knowing the heat duty, the required area, A, is estimated using the following relation-ship:

AQ

U LMTD=

( )

where:

LMTD = log mean temperature difference

This area is then used to estimate the number of tubes in the bundle, as given by:

NA

L APUL=

( )

where:

APUL = the tube outside area per tube per unit length L = tube length

With the above information calculated, the existing rating module is then called. The perform-ance values generated by this module are used to systematically modify various parametersand achieve the user-specified constraints. For example, the number of tube rows is modifiedusing the fact that the ductside pressure drop is proportional to ROWS 2.8, for a given surfacearea.

For the design option, the program attempts to arrive at a reasonable aspect ratio (i.e.,LENGTH/ WIDTH ratio). However, if a very tight tolerance has been specified for bundle (i.e.,bay) width, the aspect ratio criteria are ignored by the program. For this situation, the tubelength constraints may also be violated.

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TYPE ACE UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement defines the basic characteristics of the air-cooled exchanger.

Mandatory entries:

OLD or Rating only. Identifies an existing exchanger to be rated. There isno default.

NEW Design only. Identifies a new exchanger to be designed. There isno default.

Examples:ACE UID=ACE4

TYPE OLDACE UID=EX56

TYPE NEW

Optional entries:

HOTSIDE=TUBE Specifies the side of the exchanger receiving the hotside fluid. En-ter TUBE or AIR. If this keyword is not supplied, the hotside fluidis determined from stream inlet temperatures. This keyword ismandatory for the HTRI ACE2 option. TUBE is the default.

FLOW=COUNTERCURRENT Specifies the flow direction. This entry affects the calculation ofthe LMTD correction factor (FT) and, thereby, the MTD. EnterCOUNTERCURRENT to specify that the tubeside and airside flu-ids flow in opposing directions, or COCURRENT to specify flowin the same direction. The default is COUNTERCURRENT.

AREA=79 or Rating only. Specifies the effective or “installed” area per bun-dle. The area covered by the tubesheets and baffles is subtractedfrom the outside area of the tubes. For finned tubes, fin areamust also be included in the total bundle area. This value ischecked for consistency with the tube information. The default is79 ft 2 (English), or 7.34 m 2 (metric and SI) for bare tubes, and990 ft 2 (English), or 92.0 m 2 (metric and SI) for finned tubes.

AREA= Design only. Limits the area per shell. Enter minimum and maxi-mum values. There are no defaults.

UESTIMATE=5 Specifies the initial U-value for the flowsheet energy balance.The default is 5 Btu/hr-ft 2 -F (English), 24.4 kcal/hr-m2-C (met-ric), or 28.4 W/m 2 -K (SI).

USCALER=1.0 Specifies a scale factor to adjust the rigorously computed U-value. The default is 1.0.

Examples:

(Rating example)TYPE OLD, FLOW=COCUR, AREA=500, UESTIMATE=6,*

USCALER=0.9

(Design example)TYPE NEW, AREA=400,5000, UESTIMATE=5.5

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TUBESIDE ACE UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement defines all necessary details for the tubeside of theexchanger. Tubes may be plain or finned, and several options for defining baffle details are avail-able.

Mandatory entries:

FEED= Identifies the feed, or inlet stream and its associated properties.Enter up to twelve alphanumeric characters. The FEED entry willbe printed as a label in the output. There is no default.

PRODUCT= Identifies the product, or outlet stream and its associated proper-ties. Enter up to twelve alphanumeric characters. The PRODUCTentry will be printed as a label in the output. There is no default.

Optional entries:

LENGTH=20 or Rating only. Specifies the exchanger tube length. The defaultvalue is 20 ft (English), or 6.1 m (metric and SI).

LENGTH=24,40,2 Design only. Specifies minimum, maximum, and incrementaltube lengths. HEXTRAN uses the maximum length to initiate thedesign and reduces the length by the increment specified if thetubeside pressure drop and velocity specifications cannot bemet at the minimum number of passes allowed for the design.The default values are: 8, 20, 4 ft (English), or 2.4, 6.1, 1.2 m(metric and SI).

Note: A design may be obtained for a fixed tube length (e.g.,LENGTH = 24, 24, 0).

ID=0.584 and/or Specifies the inside diameter of the tube. If not specified, thisvalue will be automatically computed from the OD and THICK-NESS or BWG entries. The default values are 0.584 in. (English),or 14.834 mm (metric and SI).

OD=0.75 and/or Specifies the outside diameter of the tube. The default is 0.75 in.(English), or 19.05 mm (metric and SI).

BWG=14 or Specifies an integer value from the Birmingham Wire Gauge, analternate way to define tube thickness. Acceptable values areshown in Table 4-39. The default is 14.

THICKNESS=0.083 Specifies the thickness of the tube wall. The default is 0.083 in.(English), or 2.108 mm (metric and SI).

Note: Either BWG or THICKNESS may be given if OD is entered,but not both. If both ID and OD are given, neither BWG norTHICKNESS is allowed.

NPS= and Specifies the “nominal” pipe size. Enter a value from Table 4-43.You cannot enter both NPS and ID on the same statement. Youmust enter values for NPS and SCHEDULE together. There is nodefault. If neither ID nor an NPS and SCHEDULE combination areentered, the default ID will be used for the pipe inside diameter.

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SCHEDULE= Defines the schedule number for steel pipe. Enter a value fromTable 4-36. You cannot enter both SCHEDULE and ID on thesame statement. An entry for SCHEDULE is required only if NPSis entered. You must enter SCHEDULE and NPS together. Thereis no default. If neither ID nor an NPS and SCHEDULE combina-tion are entered on the LINE statement, the default ID will beused for the pipe inside diameter.

NUMBER= Rating only. Specifies the number of tubes per tube bundle. Thiskeyword is required if AREA is not specified. Values specified forLENGTH or OD keywords on the TYPE statement override thisentry.

PASS=2 or Rating only. Specifies the number of tube passes per bundle. En-ter an integer. The default is 2.

PASS=1,12 Design only. Specifies the upper and lower limit for number oftube passes per bundle. Enter minimum and maximum values.The default is 1,12.

PATTERN=INLINE Specifies a tube pattern code. Enter INLINE or STAGGERED. Thedefault is INLINE.

TPITCH= Specifies the value of the tube pitch, i.e., the center-to-centerdistance between tubes in the direction normal to air flow. If notentered, this value will be set equal to 1.25 times the tube di-ameter for bare tubes, or 1.25 times the fin OD for finned tubes.If values for the tube or fin OD are not specified, the default val-ues will be used.

LPITCH= Specifies the longitudinal tube pitch, which is the center-to-center distance between tubes in direction parallel to air flow. Ifnot entered, the value will be set equal to 1.25 times the tube di-ameter for bare tubes, or equal to 1.25 times the fin OD forfinned tubes. If values for the tube or fin OD are not specified,the default values will be used.

ROWS=1 Rating only. Specifies the number of tube rows per bundle. Enteran integer. The default is 1.

ROWS=2,12 Design only. Specifies the minimum and maximum number oftube rows per bundle. Enter minimum and maximum values. Thedefaults are 2 and 12.

MATERIAL=01 Specifies the tube material, either by code or by an alphanu-meric name. When an appropriate code number is entered, thethermal conductivity and density are selected from Table 4-36,Allowable Material Codes. Alphanumeric entries are treated asnames for printout purposes only. The default is 01 (CARBONSTEEL).

CONDUCTIVITY=30 Specifies tube metal thermal conductivity. This entry is used todetermine the resistance to heat transfer through the tube wall.When a valid MATERIAL code is entered, this value is selectedfrom Table 4-36, however, this entry overrides the selectedvalue. The default is 30 Btu/hr-ft-F (English), 44.6 kcal/hr-m-C(metric), or 51.9 W/m-K (SI).

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FOUL=0.002 Specifies the tubeside fouling resistance based on tubeside area.To simulate a ‘‘clean’’ exchanger, enter a value of zero on bothTUBE and AIRSIDE statements. The default is 0.002 hr-ft 2-F/Btu (English), 0.00041 hr-m 2 -C/kcal (metric), or 0.00035 m2 -K/W (SI).

LAYER=0.0 Specifies the tubeside fouling layer thickness. This entry repre-sents the effect of fouling on the tubeside pressure drop. The ef-fect of fouling on heat transfer is represented by the FOUL entry.The default is 0.0 in. (English), or 0.0 mm (metric and SI).

HI= or Specifies a user-supplied inside film coefficient. This entry over-rides the computed value for rating cases.

HSCALER=1.0 Design only. Specifies a multiplier for the computed film coeffi-cient. You cannot use HSCALER if USCALER is specified on theTYPE statement. The default is 1.0.

DPSHELL= or Rating only. Specifies the tubeside pressure drop per bundle.This entry overrides the computed value. You cannot enterDPSHELL and DPUNIT together.

DPSHELL= 5,15 or Design only. Specifies the minimum and maximum values forpressure drop per bundle. HEXTRAN averages the lower and up-per limits to determine the target pressure drop for the specifiedbundle arrangement. The defaults are 5, 15 psi (English), 0.352,1.055 kg/cm 2 (metric), or 34.47, 103.42 kPa (SI). You cannotenter DPSHELL and DPUNIT together.

DPUNIT= or Rating only. Specifies the minimum and maximum value forpressure drop per service. This entry overrides the computedvalue. There are no defaults. You cannot enter DPSHELL andDPUNIT together.

DPUNIT= Design only. Specifies the value for pressure drop per service.Enter lower and upper limits. This keyword is identical toDPSHELL, as only one bundle is designed in each unit. There areno defaults. You cannot enter DPSHELL and DPUNIT together.

VELOCITY=0,1000 Design only. Specifies lower and upper limits for tubeside veloc-ity. Enter minimum and maximum values. The default is 0,1000ft/sec (English), or 0,305 m/s (metric and SI).

Note: A design may be carried out to yield a specified tubesidevelocity (average for single phase and at the inlet for condensa-tion cases). The resulting tubeside pressure drop may not be adesirable value, as the program ignores any tubeside pressuredrop constraints that you enter.

DPSCALER=1.0 Specifies an optional multiplier for the computed tubeside pres-sure drop. The default is 1.0.

SERIES=1 Rating only. Specifies the number of bundles per bay in series.The default is 1.

PARALLEL=1 Rating only. Specifies the number of bundles per bay in parallel.The default is 1.

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Examples:

(Rating example)TUBE FEED=STM1, PROD=STM2, LENGTH=24, OD=0.75,*

BWG=12, PASS=4, ROWS=6, TPITCH=2,*LPITCH=2, FOUL=0.001, PARALLEL=2

(Design example)TUBE FEED=STM1, PROD=STM2, LENGTH=16,20,2,*

OD=0.75, BWG=12, PASS=2,10,*ROWS=1,12, FOUL=0.002, PARALLEL=1,10

FINS ACE UNIT OPERATIONS Data Category of Input

Optional statement. This statement specifies details for finned tubes.

Mandatory entries:

None.

Optional entries:

NUMBER =5 Specifies the number of fins per unit length. The default is 5fins/in. (English), or 197 fins/m (metric and SI).

THICKNESS=0.017 Specifies the fin thickness. The default is 0.017 in. (English), or0.432 (metric and SI).

HEIGHT=0.625 Specifies the fin height. The default is 0.625 in. (English), or15.9 mm (metric and SI).

AREA= Specifies the fin area per unit length of the tube. This entry isused to compute the fin area in place of the fin geometry sup-plied. Standard dimensional units are: ft 2 /ft for English unitsand m 2 /m for metric and SI. No consistency check is made be-tween this entry and the area value determined from NUMBER,HEIGHT, and THICKNESS. There is no default.

EFFICIENCY= Specifies the fin efficiency. If not specified, HEXTRAN will calcu-late the value.

MATERIAL=20 Specifies the tube material, either by code or by an alphanumericname. When an appropriate code number is entered, the thermalconductivity and density are selected from Table 4-36, AllowableMaterial Codes. Alphanumeric entries are treated as names forprintout purposes only. The default is 20 (ALUMINUM).

CONDUCTIVITY=128.3 Specifies tube metal thermal conductivity. This entry is used todetermine the resistance to heat transfer through the fin. When avalid MATERIAL code is entered, this value is selected from Ta-ble 4-36; however, this entry overrides the selected value. Thedefault is 128.3 Btu/hr-ft-F (English), 190.9 kcal/hr-m-C (met-ric), or 222.1 W/m-K (SI).

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BOND=0.0 Specifies the fin bond resistance between the exchanger fins andthe tube OD. The default is 0.0 hr-ft 2 -F/Btu (English); 0.0 hr-m2 -C/kcal (metric) 0.0 m 2 -K/W (SI). The default is 0.0.

Examples:FINS NUMBER=6, THICKNESS=0.015, HEIGHT=0.6,*

CONDUCTIVITY=140FINS HEIGHT=0.6, AREA=20

AIRSIDE ACE UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement defines all necessary details for the airside of the ex-changer. Fan details are specified on the FAN statement

Mandatory entries:

FEED= Identifies the feed, or inlet stream and its associated properties.Enter up to twelve alphanumeric characters. The FEED entry willbe printed as a label in the output. There is no default.

PRODUCT= Identifies the product, or outlet stream and its associatedproperties. Enter up to twelve alphanumeric characters. ThePRODUCT entry will be printed as a label in the output. There isno default.

Optional entries:

WIDTH= or Rating only. Specifies the width of the bundle. If not specified,this value will be set equal to the number of tubes per row multi-plied by the transverse pitch.

WIDTH=5,20 Design only. Specifies the minimum and maximum width of thebundle. Enter lower and upper limits values in ft (English) or m(metric and SI). The defaults are 5, 20 ft (English) and 1.525,6.096 m (metric and SI).

Note: A design may be obtained for a fixed bay width (e.g.,WIDTH = 5, 5). In this case, the actual bay width will be slightlydifferent from the specified value as the program must yield avalid tube length which has incremental values, while satisfyingthe heat transfer requirement.

LENGTH= Rating only. Specifies bundle length. This value is used to calcu-late the air flow velocity. If not specified, this value is set equalto the tube length. If tube length is not specified, the defaults are20.0 ft (English) and 6.1 m (metric and SI).

FOUL=0.002 Specifies the airside fouling resistance. To simulate a ‘‘clean’’ ex-changer, enter a value of zero on both TUBE and AIRSIDE state-ments. The default is 0.002 hr-ft 2 -F/Btu (English), 0.00041hr-m 2 -C/kcal (metric), or 0.00035 m 2 -K/W (SI).

LAYER=0.0 Specifies the airside fouling layer thickness. This entry repre-sents the effect of fouling on the airside pressure drop. The

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effect of fouling on heat transfer is represented by the FOUL en-try. The default is 0.0 in. (English), or 0.0 mm (metric and SI).

HO= or Specifies a user-supplied outside film coefficient. This entryoverrides the computed value for rating cases.

HSCALER=1.0 Specifies a multiplier for the computed film coefficient. You can-not use HSCALER if USCALER is specified on the TYPE state-ment. The default is 1.0.

DPUNIT= or Rating only. Specifies the airside pressure drop per bundle. Thisentry overrides the computed value. There are no defaults. Youcannot enter DPSHELL and DPUNIT together.

DPUNIT=0.3,0.7 Design only. Specifies the minimum and maximum airside pres-sure drop per bundle. Enter lower and upper limits. HEXTRANcalculates the average between the minimum and maximum val-ues to use as the target pressure drop in obtaining a suitabletube bundle. The defaults are 0.3, 0.7 in. H2O (English) and7.62, 17.8 mm H2O (metric and SI). You cannot enter DPSHELLand DPUNIT together.

DPSCALER=1.0 Specifies an optional multiplier for the computed airside pres-sure drop. The default is 1.0.

VELOCITY= Design only. Specifies the minimum and maximum airside forcevelocities. Enter lower and upper limits in ft/hr (English) or m/s(metric and SI). There are no defaults.

Note: A design may be carried out to yield a specified airsideface velocity; however, the airside pressure drop may not be adesirable value.

PARALLEL= or Rating only. Specifies the number of bundles per bay in parallel.There are no defaults.

PARALLEL= Design only. Specifies the minimum and maximum number ofbundles per bay in parallel. There are no defaults.

Examples:

(Rating example)AIRSIDE FEED=AIR1, PROD=AIR2, WIDTH=8,*

LENGTH=24, FOUL=0.001, PARALLEL=2

(Design example)AIRSIDE FEED=AIR1, PROD=AIR2, WIDTH=5,16,*

DPUNIT=0.4,0.9, PARALLEL=1,6

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FAN ACE UNIT OPERATIONS Data Category of Input

Optional statement. This statement specifies the type of fan installation required.

Mandatory entries:

NONE.

Optional entries:

DRAFT=FORCED Rating only. Specifies the type of fan installation. Enter FORCEDto specify forced-draft fans, which are located on the undersideof the tube bundles, or INDUCED to specify induced-draft fans,which are located above the tube bundle. The default is FORCED.

DIAMETER= Rating only. Specifies the fan diameter. Enter a value in ft (Eng-lish) or m (metric and SI). If this value is not specified, the fandiameter will be calculated as 90 percent of the bay width.

NUMBER=1 Rating only. Specifies the number of fans per bay. Enter an inte-ger value. The default is 1.

EFFICIENCY=100 Specifies combined fan and drive efficiency. Enter a value ex-pressed as a percentage. This entry is used to calculate the fanpower requirement. The default is 100.

POWER= Rating only. Specifies the fan power. Enter a value in hp (Eng-lish) or kW (metric and SI). If a value for this keyword is sup-plied, the fan power will be held constant during calculationsand air flowrate will be calculated. If a value is not supplied, theair flowrate will be held constant at the input value and the re-quired power will be calculated.

OPTIMIZATION=2 Design only. Specifies the value of the ratio of the change incapital costs to the change in annual operating costs. Enter avalue for the payout period (in years) for an incremental changein capital cost resulting from a change in air flowrate. The de-fault is 2.

For example, OPTIM=2 specifies the following sequence: theprogram will first arrive at a design using the user-specified airflowrate. Next, the air flowrate is changed to yield the followingresult: the absolute value of the ratio of change in capital cost tothe change in annual operating cost would be approximatelyequal to 2.

Examples:

(Rating example)FAN DRAFT=INDUCED, DIAM=5, NUMBER=2

(Design example)FAN DRAFT=FORCED, OPTIM=3

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TNOZZLE ACE UNIT OPERATIONS Data Category of Input

Optional statement. This statement specifies the tubeside nozzle data. Unless the NONE optionis used, HEXTRAN includes the nozzle pressure drops in the calculations whether nozzle dataare supplied or not. When data are not supplied, HEXTRAN computes the appropriate sizes.

Optional entries:

ID= This optional keyword is used to supply the inside diameters forinlet and outlet nozzles. Enter an inlet value and an outlet value,separated by a comma. Valid units of measure are inches (Eng-lish) and mm (metric and SI). If not specified, HEXTRAN will usea conventional nozzle size.

NUMBER=1,1 Specifies the number of inlet and outlet nozzles per bundle. Ifone value is supplied, the other must be supplied as well. Thedefaults are 1,1.

NONE Suppresses nozzle sizing and pressure drop calculations. Thiskeyword has no entries.

Examples:TNOZZLE ID=8,2, NUMBER=1,1

SPECIFICATION ACE UNIT OPERATIONS Data Category of Input

Optional for rating, mandatory for design. This statement specifies exchanger performancecriteria. For exchangers being designed, this statement determines the area required for thedesired heat transfer.

Optional entries:

TEMPERATURE= and Rating only. Specifies the outlet temperature of the streamspecified by the TUBE or AIR keyword. You cannot use TEM-PERATURE with any other specification keywords. The units areF (English), C (metric), or K (SI). There is no default.

TUBE orAIR or

Specifies the side of the exchanger being used by the TEMPERA-TURE specification. TUBE can also be used with the LFRAC key-word. There is no default.

LFRACTION= and Specifies the liquid weight fraction of the stream. Enter a valuefrom 0.0 (all vapor) to 1.0 (all liquid). This keyword must beused in conjunction with the TUBE or HOT keyword to apply theLFRACTION to the correct stream. You cannot enter LFRAC withany other specification keywords. There is no default.

TUBE orHOT or

Specifies the side of the exchanger being used by the LFRAC-TION specification. TUBE can also be used with the TEMPERA-TURE keyword. There is no default.

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DUTY= or Specifies the total heat transferred in the exchanger. You cannotuse DUTY with any other specification keywords. Units are:MMBtu/hr (English), MMkcal/hr (metric), and MMkJ/hr (SI).There is no default.

HOCI= orCOCI= orHIHO= orHICO=

Specifies the exchanger approach temperature. Use only one ofthese four and enter a numerical value. Each keyword specifies asubtraction operation where the first set of two characters de-fines a value, and the second set of two characters defines avalue that is subtracted from it. In the operation, H refers toHOT side, C refers to COLD side, I refers to inlet, and O refers tooutlet. Therefore, HOCI specifies hot outlet temperature minuscold inlet temperature. You cannot use DUTY with any otherspecification keywords. Valid units are F (English), C, (metricand SI). There are no defaults.

Examples:SPEC TEMP=100, TUBESPEC LFRAC=0.8, TUBESPEC HOCI=40

CALCULATION ACE UNIT OPERATIONS Data Category of Input

Optional statement. This statement sets calculation methods for individual exchangers on aglobal basis. Methods can be selected globally using the CALCULATION statement in theSIMULATION, CASESTUDIES, OPTIMIZATION AREA, OPTIMIZATION SPLIT, or REGRESSIONcategories of input.

Optional entries:

NOCHECK Suppresses HEXTRAN geometry consistency checks and pre-vents HEXTRAN from assigning default values to missing ge-ometry data. NOCHECK is designed to allow you to access HTRIdefaults in place of HEXTRAN defaults. When using NOCHECK,ensure that all exchanger data are explicitly specified, or that theHTRI ACE2 module is referenced (See the HTRI documentation).

WARNING: Using NOCHECK with inconsistent or missing ge-ometry data may result in abnormal program termination (divi-sion by zero, overflow, etc.).

TWOPHASE= Specifies the methods for thermal and hydraulic calculations forall rigorous exchangers. Enter NEW or OLD. NEW uses theModified Chen vaporization method for convective boiling, andincludes predictions for sub-cooled and film boiling. Condensa-tion methods account for flow regimes and gravity versus sheareffects. Pressure drops are calculated using a stream analysis-based method. NEW automatically sets DPSMETHOD=STREAM.OLD selects algorithms used in versions 5.0x and earlier. Usethis option to make comparison runs with earlier versions ofHEXTRAN. There is no default.

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Examples:CALC TWOPHASE=NEW

COST ACE UNIT OPERATIONS Data Category of Input

Optional statement. This statement provides special costing data for an exchanger. The de-faults are the global values given in the CALCULATION category of input.

Optional Entries:

BSIZE=1000.00 Defines the base area used in the costing equation. The defaultis 1000.00 ft 2 (English), or 93.0 m2 (metric and SI).

BCOST=0.00 Defines the base cost used in the costing equation. The defaultis 0.00 USDOLLAR/ft 2 (English), or 0.00 USDOLLAR/m2 (met-ric and SI).

LINEAR=50.00 Defines the linear cost factor used in the costing equation. Thedefault is 50.00 USDOLLAR/FT 2 (English), or 538.20 USDOL-LAR/m 2 (metric and SI).

EXPONENT=0.60 Defines the exponential cost factor used in the costing equation.The default is 0.60 (English, metric and SI).

CONSTANT=0.00 Defines the constant cost factor used in the costing equation.This entry can be used to define fixed costs associated with in-stallation of an exchanger and is not a function of exchangersize. The default is 0.00 USDOLLAR.

PRINT ACE UNIT OPERATIONS Data Category of Input

Optional statement. This statement specifies report print options for the exchanger statement.The default printout options are the global values specified in the CALCULATION section.STANDARD and EXTENDED are defaults. STANDARD will be printed in addition to any speci-fied keywords. EXTENDED will be overwritten by any specified keywords.

Optional entries:

STANDARD Prints the standard TEMA Data Sheet. This is the default.

EXTENDED Prints the Extended Data Sheet. This is the default.

ZONES Prints the zones analysis for two-phase exchangers.

MONITOR Prints the design logic monitor for NEW exchangers.

Examples:PRINT EXTENDED, ZONES

This example prints standard, extended, and zones analysis reports.PRINT MONITOR

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This example prints standard and design logic monitor reports.PRINT STANDARD

This example prints only the standard report.PRINT ZONES, MONITOR

This example prints standard, zones analysis, and design logic monitor reports.

HTRI ACE UNIT OPERATIONS Data Category of Input

Optional entry:

ACE2 This allows the user to rate or design air coolers using HTRIACE2 module. See the HEXTRAN HTRI Input Guide for details.

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PHE HEAT EXCHANGERS

PHE PHE UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement identifies the unit as a plate-and-frame exchanger. Itmust be the first input line for any PHE model.

Plate-and-frame heat exchangers (PHEs) represent compact devices used for efficient heattransfer. These exchangers are most suited for liquid-liquid applications; however, they are in-creasingly used in condensation and boiling applications as well. Owing to the existence oftrue countercurrent flow within PHEs, they are most competitive when the fluids have verysmall approach temperatures.

The plate-and-frame heat exchanger module in HEXTRAN is flexible and can handle almost anytype of a PHE in the rating option. For example, the hot and cold sides are allowed to have anunequal number of passes. Furthermore, this option allows the user to specify repeated adja-cent channels to occupy just one fluid before the other fluid occupies the next channel(s). Thisis achieved by entering unequal numbers for the NCHOT and NCCOLD keywords on theARRANGEMENT statement.

Both single-phase and two-phase fluids are allowed. However, the two-phase methods involveapproximate correlations based on a homogeneous model. Extreme care must therefore beused when using results for two-phase applications. Although HEXTRAN will accept caseswith a multi-pass on the two-phase side, this is not recommended. In other words, upflowcondensation and downflow boiling should be avoided.

Design Process

This section describes the general process performed by HEXTRAN for the design option. Thedesign option allows you to arrive at a reasonable design by entering a very small amount ofinput information. Even though this option has been thoroughly tested and demonstrated toyield reasonable results, it is recommended that this information not be used to prepare actualproduct specification. Rather, this design option is best used in comparing different types ofheat exchangers that are being considered for a given application.

First, a preliminary design is obtained based on an analytical model. This model uses averageproperties for the two fluids and involves overall calculations with no account made for un-even flow distribution, for example. This gives the total heat transfer area (i.e., the number ofplates), the plate size (if the user did not select a specific plate size), the number of passes(recall that the design option yields the same number of passes for the two fluid sides), andthe effective chevron angle.

This design is next rated using a fully incremental model which uses 20 increments along thelength of the plates and up to 200 increments along the pack length. This model computes theactual flowrate in each channel. Parameters of the pack is gradually fine-tuned, based on ana-lytically guided techniques, until the design criteria are reasonably satisfied.

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TYPE PHE UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement defines the basic characteristics of the plate-and-frameexchanger.

Mandatory entries:

OLD or Rating only. Identifies an existing exchanger to be rated. There isno default.

NEW Design only. Identifies a new exchanger to be designed. There isno default.

Examples:PHE UID=ACE4

TYPE OLDPHE UID=EX56

TYPE NEW

Optional entries:

FLOW=COUNTERCURRENT Specifies the flow direction of the first hot and cold channelswithin the plate pack. Enter COUNTERCURRENT to specify thatthe hotside and coldside fluids flow in opposing directions, orCOCURRENT to specify flow in the same direction. The default isCOUNTERCURRENT.

AREA=1000 or Rating only. Specifies the effective or “installed” area per frame.The default is 1000 ft 2 (English), or 92.9 m 2 (metric and SI).

AREA= Design only. Specifies minimum and maximum area for frame.There are no defaults.

UESTIMATE=100 Specifies the initial U-value for the flowsheet energy balance.The default is 100 Btu/hr-ft 2 -F (English), 488 kcal/hr-m2-C(metric), or 568 W/m 2 -K (SI).

USCALER=1.0 Specifies a scale factor to adjust the rigorously computed U-value. The default is 1.0.

Examples:

(Rating example)TYPE OLD, FLOW=COCUR, AREA=500,*

USCALER=0.9

(Design example)TYPE NEW, FLOW=COUNTER, AREA=200,1000,*

USCALER=0.9

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HOTSIDE PHE UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement specifies details for the hotside of the exchanger.

Mandatory entries:

FEED= Identifies the feed, or inlet stream and its associated properties.Enter up to twelve alphanumeric characters. The FEED entry willbe printed as a label in the output. There is no default.

PRODUCT= Identifies the product, or outlet stream and its associated prop-erties. Enter up to twelve alphanumeric characters. The PROD-UCT entry will be printed as a label in the output. There is nodefault.

Optional entries:

FOUL=0.0005 Specifies the hotside fouling resistance. To simulate a ‘‘clean’’exchanger, enter a value of zero on both HOTSIDE and COLD-SIDE statements. The default is 0.0005 hr-ft 2 -F/Btu (English),0.0001 hr-m 2 -C/kcal (metric), or 0.000088 m 2 -K/W (SI).

LAYER=0.0 Specifies the hotside fouling layer thickness. This entry repre-sents the effect of fouling on the hotside pressure drop. The ef-fect of fouling on heat transfer is represented by the FOUL entry.The default is 0.0 in. (English), or 0.0 mm (metric and SI).

HHOT= or Specifies the hotside film coefficient. This entry overrides thecomputed value for rating cases. HHOT is not recommended fordesign calculations. There is no default.

HSCALER=1.0 Specifies a multiplier for the computed hotside film coefficient.You cannot use HSCALER with HHOT, or if USCALER is specifiedon the TYPE statement. The default is 1.0.

DPFRAME= or Rating only. Specifies the airside pressure drop per frame. Thisentry overrides the computed value. There are no defaults. Youcannot enter DPSHELL and DPUNIT together.

DPFRAME=5,15 Design only. Specifies the minimum and maximum airside pres-sure drop per bundle. Enter lower and upper limits. HEXTRANcalculates the average between the minimum and maximum val-ues to use as the target pressure drop in obtaining a suitableplate and pack arrangement. The defaults are 5,15 psi (English)and 0.352,1.055 kg/cm2 (metric), and 34.47,103.42 kPa (SI).

Note: HEXTRAN’s primary objective is to satisfy heat transferrequirements. Therefore, pressure drop constraints entered forthe design option are treated as ‘‘soft’’ constraints, and may beviolated in order to satisfy the heat transfer requirements.

DPSCALER=1.0 Specifies an optional multiplier for the computed pressure drop.The default is 1.0.

PDESIGN= Design only. Specifies the design pressure. Enter a value in psi(English), kg/cm2 (metric), or kPa (SI) units. There is no default.

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TDESIGN= Design only. Specifies the design temperature. Enter a value in F(English), or C (metric and SI) units. There is no default.

Examples:

(Rating example)HOTS FEED=HOT1, PROD=HOT2, FOUL=0.0008,*

LAYER=0.005, DPSCALER=1.1

(Design example)HOTS FEED=HOT1, PROD=HOT2, FOUL=0.0006,*

DPFRAME=6,12, LAYER=0.008

COLDSIDE PHE UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement specifies details for the coldside of the exchanger.

Mandatory entries:

FEED= Identifies the feed, or inlet stream and its associated properties.Enter up to twelve alphanumeric characters. The FEED entry willbe printed as a label in the output. There is no default.

PRODUCT= Identifies the product, or outlet stream and its associated prop-erties. Enter up to twelve alphanumeric characters. The PROD-UCT entry will be printed as a label in the output. There is nodefault.

Optional entries:

FOUL=0.0005 Specifies the coldside fouling resistance. To simulate a ‘‘clean’’exchanger, enter a value of zero on both HOTSIDE and COLD-SIDE statements. The default is 0.0005 hr-ft 2 -F/Btu (English),0.0001 hr-m 2 -C/kcal (metric), or 0.000088 m 2 -K/W (SI).

LAYER=0.0 Specifies the coldside fouling layer thickness. This entry repre-sents the effect of fouling on the coldside pressure drop. The ef-fect of fouling on heat transfer is represented by the FOUL entry.The default is 0.0 in. (English), or 0.0 mm (metric and SI).

HCOLD= or Specifies the coldside film coefficient. This entry overrides thecomputed value for rating cases. HCOLD is not recommendedfor design calculations. There is no default.

HSCALER=1.0 Specifies a multiplier for the computed coldside film coefficient.You cannot use HSCALER with HCOLD, or if USCALER is speci-fied on the TYPE statement. The default is 1.0.

DPFRAME= or Rating only. Specifies the airside pressure drop per frame. Thisentry overrides the computed value. There is no default.

DPFRAME=5,15 Design only. Specifies the minimum and maximum airside pres-sure drop per bundle. Enter lower and upper limits. HEXTRANcalculates the average between the minimum and maximum val-ues to use as the target pressure drop in obtaining a suitable

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plate and pack arrangement. The defaults are 5,15 psi (English)and 0.352,1.055 kg/cm2 (metric), and 34.47,103.42 kPa (SI).

Note: HEXTRAN’s primary objective is to satisfy heat transferrequirements. Therefore, pressure drop constraints entered forthe design option are treated as ‘‘soft’’ constraints, and may beviolated in order to satisfy the heat transfer requirements.

DPSCALER=1.0 Specifies an optional multiplier for the computed pressure drop.The default is 1.0.

PDESIGN= Design only. Specifies the design pressure. Enter a value in psi(English), kg/cm2 (metric), or kPa (SI) units. There is no default.

TDESIGN= Design only. Specifies the design temperature. Enter a value in F(English), or C (metric and SI) units. There is no default.

Examples:

(Rating example)COLD FEED=CLD1, PROD=CLD2, FOUL=0.001,*

LAYER=0.006, HSCALER=0.9

(Design example)COLD FEED=CLD1, PROD=CLD2, FOUL=0.001,*

DPFRAME=6,10, HSCALER=0.9

PACK PHE UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement specifies details for the plate pack.

Mandatory entries:

SPACE=0.1 Specifies the average channel spacing. This keyword is requiredfor rating, unless APC is supplied on the PLATE statement. Thedefault is 0.1 in. (English) or 2.54 mm (metric and SI).

DPORT=6 Specifies the port diameter in the plate. This keyword is requiredfor rating, unless APC is supplied on the PLATE statement. Thedefault is 6 in. (English) or 152.4 mm (metric and SI).

LVERTICAL=48 Specifies the vertical distance between port centers. This key-word is required for rating, unless APC is supplied on the PLATEstatement. The default is 48 in. (English) or 1219.2 mm (metricand SI).

LHORIZONTAL= Specifies the horizontal distance between port centers. This key-word is required for rating, unless APC is supplied on the PLATEstatement. There is no default.

WIDTH= Specifies the actual flow width within a channel. If a value is notsupplied, it is computed as the sum of LHORI and DPORT. Thereis no default.

PARALLEL= Rating only. Specifies the number of identical frames in parallel.Enter one value. The default is 1.

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PARALLEL=1,10 Design only. Specifies lower and upper limits for identicalframes in parallel. Enter minimum and maximum values. The de-fault is 1,10.

MAXPASSES=1 Design only. Specifies the maximum number of passes allowedon both sides of the exchanger. PHEs must have an equalnumber of passes for the two fluid sides. The maximum value is6. The default is 1.

Note: Designs can be obtained with a maximum of only sixpasses. However, in the rating option, up to 12 passes are al-lowed as long as the total number of plate groups does not ex-ceed 12.

FCDIR=UP Specifies the fluid flow direction in the channel nearest to thestationary end plate. Enter UP or DOWN. The default is UP.

FCFLUID=COLD Specifies the fluid type in the channel nearest to the stationaryend plate. Enter HOT or COLD. The default is COLD.

Examples:

(Rating example)PACK SPACE=0.12,DPORT=8, LVERT=42, LHORI=22,*

PARA=2, FCDIR=DOWN, FCFLUID=HOT

(Design example)PACK SPACE=0.12,DPORT=8, LVERT=44, LHORI=24,*

PARA=1,5, MAXPASS=2

PLATE PHE UNIT OPERATIONS Data Category of Input

Mandatory for rating, optional for design. This statement specifies details for the exchangerplate.

Optional entries:

BETA=30,60 Specifies the minimum and maximum values for the chevron an-gle. This is the corrugation angle, which is measured from anormal to the main flow direction (see Figure 4-26). If only oneplate is used for rating, enter the single BETA value twice (e.g.,BETA=42, 42). This keyword is required for rating cases if APCis not entered on the PLATE statement. It is optional for designcases. The defaults are 30,60.

AEFACTOR=1.17 Specifies the surface area enhancement factor. This representsthe ratio of the actual heat transfer area to the projected area.This keyword is required for rating cases, but is optional for de-sign cases if no APC is entered. The default is 1.17.

AREA=6.14 Specifies the heat transfer area of one side of one plate. Thiskeyword is required for rating cases, but is optional for designcases if no APC is entered. The default is 6.14 ft 2 (English) or0.570 m 2 (metric and SI).

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APC= Specifies the Automatic Plate Code. You must enter a value withthis keyword. See Table 4-44 for valid codes. There is no default.

NAME= Specifies the plate classification. Enter up to 8 alphanumericcharacters. There is no default.

Note: The BETA value supplied can only be overridden if the APCkeyword is also used. If no APC key word is used and not allplate information is entered, then HEXTRAN will scan the entiredata bank for design cases and the user-supplied BETA value willbe overridden.

THICKNESS=0.6 Specifies the plate thickness (in mm) for all three unit types. Thedefault is 0.6 mm.

MATERIAL=09 Defines the plate material specification. Enter a material code(an integer), or an alphanumeric name (up to 8 characters). SeeTable 4-36 for valid entries. The default code is 09, and the de-fault name is 316S.S.

CONDUCTIVITY=9.4 Specifies the thermal conductivity of the plate material. The de-faults are 9.4 Btu/hr-ft-F (English), 14.0 kcal/hr-m-C (metric), or16.3 W/m-K (SI).

GASKET=5 Specifies the gasket material code for printing purposes only.Table 4-45 lists the gasket materials presently available. The de-fault is 5 (Nitrile).

Examples:PLATE BETA=25,50, AEFACTOR=1.2, AREA=8.5PLATE BEAT=25,55,APC=100, NAME=TEST,*

THICKNESS=0.65, CONDUCTIVITY=12

Table 4-44 shows the “PLATES” file contained in HEXTRAN. This file contains all the necessaryplate information for the 16 plate types presently in the HEXTRAN databank. The data in thefile are stored in 11 columns which are described in Table 4-45. You can modify or extend(i.e., add new plates) the data in the file, provided that you enter all data in English units andthat you follow the format for each entry exactly. Use caution when adding new entries, as the‘‘PLATES’’ file is read in by HEXTRAN using a formatted Fortran READ statement.

Table 4-44: Plate Databank (as stored in the ASCII file “PLATES”)Col 1 Col 2 Col 3 Col 4 Col 5 Col 6 Col 7 Col 8 Col 9 Col 10 Col 11

100 SIM01A 30.0 60.0 -1.0 0.100 1.170 2.000 1.690 6.000 24.000

110 SIM02A 30.0 60.0 -1.0 0.100 1.170 2.500 2.240 5.500 32.000

120 SIM03A 30.0 60.0 -1.0 0.100 1.170 3.000 3.660 8.000 38.000

130 SIM04A 30.0 60.0 -1.0 0.100 1.170 4.000 3.640 12.000 32.000

132 SIM04B 30.0 60.0 -1.0 0.100 1.170 4.000 4.420 12.000 38.000

140 SIM05A 30.0 60.0 -1.0 0.100 1.170 6.000 3.800 12.000 32.000

142 SIM05B 30.0 60.0 -1.0 0.100 1.170 6.000 6.140 12.000 48.000

150 SIM06A 30.0 60.0 -1.0 0.100 1.170 8.000 5.460 16.000 36.000

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Figur4-26: Definition of Chevron Angle (b)

Column 1 The Automatic Plate Code (APC) 100 through 174. These codesrepresent 16 arbitrary plate types which may not be availablefrom any manufacturer. New entries may have any three-digit in-teger as long as they are different from the existing ones.

Column 2 The plate identification (up to 8 alphanumeric characters).

Column 3 The low value of the chevron angle (BETA). The chevron angle isstrictly defined here as the angle of corrugation measured froma normal to the main flow direction. See Figure 4-26.

Column 4 The high value of the chevron angle.

Column 5 This is a third chevron angle for future use. Any arbitrary valuemay be entered. This value will be ignored by the program.

Column 6 The average channel spacing (in.).

Column 7 The surface area enhancement factor.

Column 8 The port diameter in plates (in.).

Column 9 The effective heat transfer area of one side of a plate (ft 2 ).

Column 10 The horizontal distance between port centers (in.).

Column 11 The vertical distance between port centers (in.).

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Table 4-45: Gasket Material Codes AvailableCode Material

1 Chlorosulphonated Polythene

2 EPDM

3 Fluoroelastomer Grade B

4 Fluoroelastomer Grade GF

5 Nitrile

6 Polychloroprene

7 Resin Cured Butyl

8 Silicone

9 Viton

ARRANGE-MENTS

PHE UNIT OPERATIONS Data Category of Input

This statement is valid for rating cases only. You can enter up to 12 separate ARRANGEMENTstatements, in correct sequence, for any one problem. The default PHE has an area of 1000 ft2 and a plate code (APC) of 142.

Mandatory entries:

PFIRST= Specifies the plate type of the first plate within the plate group.Enter 1 or 2 to specify the first or second BETA value entered onthe PLATE statement. There is no default.

PSECOND= Specifies the plate type of the first plate within the plate group.Enter 1 or 2 to specify the first or second BETA value entered onthe PLATE statement. There is no default.

Note: If the PHE has only one plate type, you must enter 1 forboth PFIRST and PSECOND.

NCHOT= Specifies the number of hot channels within the plate group. En-ter an integer. There is no default.

NCCOLD= Specifies the number of cold channels within the plate group.Enter an integer. There is no default.

HPASS= Specifies the hot pass number within the plate group. Enter aninteger. There is no default.

CPASS= Specifies the cold pass number within the plate group. Enter aninteger. There is no default.

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ARRANGE ExamplesARRA PFIR=1, PSEC=1, NCHOT=60, NCCO=60, HPASS=1, CPASS=1ARRA PFIR=1, PSEC=2, NCHO=100, NCCO=100, HPASS=1, CPASS=1

This example shows a diagram of a one-pass PHE with two plate groups, and the ARRANGE-MENT statements required to specify it. Each stream shown within a plate group representsmultiple substreams within that plate group. We will assume that the first plate group contains60 channels each (for hot and cold sides) and the channels are made of plates having a chev-ron angle of 30°. We will also assume that the second plate group has 100 channels each, andthat the channels are made of plates having chevron angles of 30° and 60°. This means thatthe channels are 1/1 and 1/2 for the plate groups one and two, respectively.ARRA PFIR=1, PSEC=1, NCHOT=60, NCCO=60, HPASS=1, CPASS=2ARRA PFIR=1, PSEC=2, NCHO=100, NCCO=100, HPASS=1, CPASS=1

This example shows a diagram of a PHE having one pass for the hot side and two passes forthe cold side, and using the parameters introduced in the previous example, the ARRANGE-MENT statements required to specify it.

FPLATE PHE UNIT OPERATIONS Data Category of Input

Optional statement. This statement specifies channel f- values for the exchanger.

Optional entries:

CHNUMBER= Specifies the channel number (the first plate type + second platetype - 1). Enter 1, 2 or 3. There is no default.

REYNOLDS= Specifies Reynolds numbers for f- or jN -factors. You must entera total of four values. If only two valid Reynolds numbers areavailable, for example, enter a zero for the other two values.There are no defaults.

FFACTOR= Specifies f factors corresponding to the Reynolds numbers en-tered above. You must enter a total of four values. If fewer thanfour valid numbers are available, enter a zero for each of themissing values. There are no defaults.

JFACTOR= Specifies the jN -factors corresponding to the Reynolds numbersentered above. You must enter a total of four values. If fewerthan four valid numbers are available, enter a zero for each ofthe missing values. There are no defaults.

CONST= Specifies coefficient values for the f- or jN -factor correlation.Enter three values using the following relationship:

f=CONST /Re EXPON (a)

j N=CONST x Re EXPON (b)

Note: The jN factor relates to the well-known Colburn j-factor asfollows:

jN=j x Re.

EXPON= Specifies exponent values for the f- or jN -factor correlation. En-ter three values using the relationship given above for CONST.

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JPLATE PHE UNIT OPERATIONS Data Category of Input

Optional statement. This statement specifies jN -factor values for the exchanger.

Optional entries:

CHNUMBER= Specifies the channel number (the first plate type + second platetype - 1). Enter 1, 2 or 3. There is no default.

REYNOLDS= Specifies Reynolds numbers for f- or jN -factors. You must entera total of four values. If only two valid Reynolds numbers areavailable, for example, enter a zero for the other two values.There are no defaults.

FFACTOR= Specifies f factors corresponding to the Reynolds numbers en-tered above. You must enter a total of four values. If fewer thanfour valid numbers are available, enter a zero for each of themissing values. There are no defaults.

JFACTOR= Specifies the jN -factors corresponding to the Reynolds numbersentered above. You must enter a total of four values. If fewerthan four valid numbers are available, enter a zero for each ofthe missing values. There are no defaults.

CONST= Specifies coefficient values for the f- or jN -factor correlation.Enter three values using the following relationship:

f=CONST /Re EXPON (a)

jN=CONST x Re EXPON (b)

Note: The jN factor relates to the well-known Colburn j-factor asfollows:

jN=j x Re.

EXPON= Specifies exponent values for the f- or jN -factor correlation. En-ter three values using the relationship given above for CONST.There is no default.

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HNOZZLE PHE UNIT OPERATIONS Data Category of Input

Optional statement. This statement specifies nozzle data for the hotside. Unless the NONE op-tion is used, HEXTRAN includes the nozzle pressure drops in the calculations whether nozzledata are supplied or not.

Mandatory entries:

ID= Specifies the inside diameters for the inlet and outlet nozzles.Valid units are in. (English) and mm (metric and SI). If valuesare not supplied, HEXTRAN uses the port diameter in the plates.There are no defaults.

NONE Suppresses nozzle pressure drop calculations. There is no default.

CNOZZLE PHE UNIT OPERATIONS Data Category of Input

Optional statement. This statement specifies nozzle data for the coldside. Unless the NONE op-tion is used, HEXTRAN includes the nozzle pressure drops in the calculations whether nozzledata are supplied or not.

Mandatory entries:

ID= Specifies the inside diameters for the inlet and outlet nozzles.Valid units are in. (English) and mm (metric and SI). If valuesare not supplied, HEXTRAN uses the port diameter in the plates.There are no defaults.

NONE Suppresses nozzle pressure drop calculations. There is no default.

CALCULATION PHE UNIT OPERATIONS Data Category of Input

Optional statement. This statement sets calculation methods for individual exchangers on aglobal basis. Methods can be selected globally using the CALCULATION statement in theSIMULATION, CASESTUDIES, OPTIMIZATION AREA, OPTIMIZATION SPLIT, or REGRESSIONcategories of input.

Optional entries:

NOCHECK Suppresses HEXTRAN geometry consistency checks and pre-vents HEXTRAN from assigning default values to missing ge-ometry data. When using NOCHECK, ensure that all exchangerdata is explicitly specified.

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WARNING: Using NOCHECK with inconsistent or missing ge-ometry data may result in abnormal program termination (divi-sion by zero, overflow, etc.).

SPECIFICATION PHE UNIT OPERATIONS Data Category of Input

Optional for rating, mandatory for design. This statement specifies exchanger performancecriteria. For exchangers being designed, this statement determines the area required for thedesired heat transfer.

Mandatory entry:

TEMPERATURE= or Design only. Specifies the outlet temperature of the streamspecified by the HOTS or COLD keyword. Valid units are F (Eng-lish), C (metric), or K (SI). This keyword must be used in con-junction with the HOTS or COLD keyword. You cannot use thiskeyword with any other specification keywords. There is nodefault.

Optional entries:

TEMPERATURE= and Rating only. Specifies the outlet temperature of the streamspecified by the HOTS or COLD keyword. The units are F (Eng-lish), C (metric), or K (SI). This keyword must be used in con-junction with the HOTS or COLD keyword. You cannot use thiskeyword with any other specification keywords. There is nodefault.

HOTS orCOLD or

Specifies the side of the exchanger being used by the TEMPERA-TURE specification. You can also use HOTS and COLD with theLFRAC keyword. There is no default.

LFRACTION= and Specifies the liquid weight fraction of the tubeside productstream. It enables HEXTRAN to apply the LFRACTION to the cor-rect stream. Enter a value from 0.0 (all vapor) to 1.0 (all liquid).This keyword must be used in conjunction with the HOTS orCOLD keyword. You cannot use this keyword with any otherspecification keywords. There is no default.

HOTS orCOLD or

Specifies the side of the exchanger being used by the TEMPERA-TURE specification. You can also use HOTS and COLD with theLFRAC keyword. There is no default.

DUTY= or Specifies the total heat transferred in the exchanger. You cannotuse DUTY with any other specification keywords. Units are:MMBtu/hr (English), MMkcal/hr (metric), and MMkJ/hr (SI). Youcannot use this keyword with any other specification keywords.There is no default.

HOCI= orCOCI= orHIHO= orHICO=

Specifies the exchanger approach temperature. Use only one ofthese four and enter a numerical value. Each keyword specifies asubtraction operation where the first set of two characters de-fines a value, and the second set of two characters defines avalue that is subtracted from it. In the operation, H refers to HOT

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side, C refers to COLD side, I refers to inlet, and O refers to out-let. Therefore, HOCI specifies hot outlet temperature minus coldinlet temperature. You cannot use this keyword with any otherspecification keywords. Valid units are F (English), C, (metricand SI). There are no defaults.

Examples:SPEC TEMP=100, HOTSIDESPEC HOCI=40

PRINT PHE UNIT OPERATIONS Data Category of Input

Optional statement. This statement specifies report print options for the exchanger statement.The default printout options are the global values specified in the CALCULATION section.STANDARD and EXTENDED are defaults. STANDARD will be printed in addition to any speci-fied keywords. EXTENDED will be overwritten by any specified keywords.

Optional entries:

STANDARD Prints the standard TEMA Data Sheet. This is the default.

EXTENDED Prints the Extended Data Sheet.

ZONES Prints the zones analysis for two-phase exchangers.

MONITOR Prints the design logic monitor for NEW exchangers.

Examples:PRINT EXTENDED, ZONES

This example prints standard, extended, and zones analysis reports.PRINT MONITOR

This example prints standard and design logic monitor reports.PRINT STANDARD

This example prints only the standard report.PRINT ZONES, MONITOR

This example prints standard, zones analysis, and design logic monitor reports.

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COST PHE UNIT OPERATIONS Data Category of Input

Optional statement. This statement provides special costing data for a plate-and-frame ex-changer. The defaults are the global values given in the SIMULATION category of input.

Optional Entries:

BSIZE=1000.00 Defines the base area used in the costing equation. The defaultis 1000.00 ft 2 (English), or 93.0 m2 (metric and SI).

BCOST=0.00 Defines the base cost used in the costing equation. The defaultis 0.00 USDOLLAR/ft 2 (English), or 0.00 USDOLLAR/m2 (metricand SI).

LINEAR=50.00 Defines the linear cost factor used in the costing equation. Thedefault is 50.00 USDOLLAR/FT 2 (English), or 538.20 USDOL-LAR/m 2 (metric and SI).

EXPONENT=0.60 Defines the exponential cost factor used in the costing equation.The default is 0.60 (English, metric and SI).

CONSTANT=0.00 Defines the constant cost factor used in the costing equation.This entry can be used to define fixed costs associated with in-stallation of an exchanger and is not a function of exchangersize. The default is 0.00 USDOLLAR.

UNIT or FRAME Defines the basis for the exchanger CONSTANT cost factor. UNITresults in the constant cost factor being applied once to eachunit regardless of the number of shells or frames in the unit.FRAME results in the constant cost factor being applied to eachframe in the unit. The default is UNIT.

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MIXER UNIT

MIXER MIXER UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement identifies the unit operation as a mixer. This statementmust be the first statement for each mixer defined in the flowsheet.

This section describes the input data required for mixers. These unit operations are used tocombine feed streams.

A mixer can have from two to six feed streams, and one product stream. HEXTRAN sets theoutlet pressure from the mixer equal to the lowest of the feed stream pressures.

Mandatory entry:

UID= Identifies the unit operation for reference and printout purposes.Enter up to twelve alphanumeric characters. This entry must beunique to all other unit operations. There is no default.

Example:MIXER UID=MIX1

Optional entry:

NAME= Identifies the unit operation for printout purposes only. Enter upto twelve alphanumeric characters. NAME supplements the UIDentry.

Example:MIXER UID=MIX5,NAME=MIXER-05

STREAMS MIXER UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement identifies the feed or product streams in the mixer. Thisstatement and all entries on the statement are required.

Mandatory entries:

FEED= Identifies the feed, or inlet, stream(s) and its associated fluidproperties. Enter up to twelve alphanumeric characters for eachof two to six feed streams, separated by commas. You must en-ter at least two feed streams for a mixer. This entry must beunique to all other feed streams of other units in the flowsheet.However, this entry may be the same as a product stream identi-fier from another unit. The entries for FEED and PRODUCT maynot be the same for a given mixer unit. There is no default. TheFEED entry will be printed out as a label in the output.

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PRODUCT= Identifies the product, or outlet, stream and its associated fluidproperties. Enter up to twelve alphanumeric characters. This en-try must be unique to all other product streams of other units inthe flowsheet. However, it can be the same as a feed streamidentifier to another unit. The entries for PRODUCT and FEEDmay not be the same for a given mixer unit. There is no default.The PRODUCT entry will be printed out as a label in the output.

Examples:MIXER UID=MIXM

STRMS FEED=S1,S2,PRODUCT=STOTMIXER UID=MIX3

STRMS FEED=1,2,3,4,5,6,PRODUCT=7

Optional entries:

None

MIXER Examples:MIXER UID=MIX1,NAME=FEEDBLND

STRMS FEED=1,1A,1B,2,2A,PRODUCT=TOTF

This example shows the individual feed streams 1, 1A, 1B, 2 and 2A combined into a singleproduct stream, TOTF. By default, the pressure of stream TOTF is equal to the lowest of the in-dividual feed stream pressures. Also by default, the physical property data for product streamTOTF is identical to the first feed stream, stream 1. This example would not produce adequateresults for most cases. See the following example for information on defining new physicalproperty data for product streams that result from mixing two or more feed streams.STREAM DATA

PROP STREAM=1,SETNO=1,...PROP STREAM=2,SETNO=2,...PROP STREAM=3,SETNO=3,...PROP STREAM=4,REFSTRM=1,2,3,SETNO=4

TEMP=100,TOUT=200,PRES=60...UNIT OPERATION DATA

MIXER UID=MX1STREAMS FEED=1,2,3,PRODUCT=4

This example shows a mixer (MX1) rigorously mixing the compositions and/or assays of thefeed streams (streams 1,2,3). The resulting product stream (stream 4) has new physical prop-erty data defined by the shaded PROP STREAM statement in the STREAM DATA section.

If all the feed streams to the mixer were defined as point access streams, there is no need toreference the product stream to all its feed streams. In the above example, you would not needto define feed stream 4 if streams 1, 2, and 3 did not have a SETNO entry.

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SPLITTER UNIT

SPLITTER SPLITTER UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement identifies the unit operation as a splitter. This statementmust be the first statement for each splitter defined in the flowsheet.

This section describes the input data required for splitters. These unit operations are used tosplit feed streams.

A splitter can have only one feed stream, and from two to six product streams. HEXTRAN setsthe outlet stream pressure(s) equal to the feed stream pressure. Splitters are allowed one vari-able flowrate product stream.

Mandatory entries:

UID= Identifies the unit operation for reference and printout purposes.Enter up to twelve alphanumeric characters. This entry must beunique to all other unit operations. There is no default.

Example:SPLITTER UID = SPL1

Optional entries:

NAME= Identifies the unit operation for printout purposes only. Enter upto twelve alphanumeric characters. NAME supplements the UIDentry.

Example:SPLITTER UID = SP01,NAME = FEEDSPLT

STREAMS SPLITTER UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement identifies the feed or product streams in the splitter. Thisstatement and all entries on the statement are required.

Mandatory entries:

FEED= Identifies the feed, or inlet, stream and its associated fluid proper-ties. Enter up to twelve alphanumeric characters. This entry mustbe unique to all other feed streams of other units in the flowsheet.However, this entry may be the same as a product stream identi-fier from another unit. The entries for FEED and PRODUCT maynot be the same for a given splitter unit. There is no default. TheFEED entry will be printed out as a label in the output.

PRODUCT= Identifies the product, or outlet, stream(s) and the associatedfluid properties. Enter up to four alphanumeric characters foreach of two to six entries. You must enter at least two product

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streams for a splitter. This entry must be unique to all otherproduct streams of other units in the flowsheet. However, it canbe the same as a feed stream identifier to another unit. The en-tries for PRODUCT and FEED may not be the same for a givensplitter unit. There is no default. The PRODUCT entry will beprinted out as a label in the output.

Examples:SPLITTER UID=SP1

STRMS FEED=CRUD,PRODUCT=CUT1,CUT2,*CUT3,CUT4

SPLITTER UID=SPL7,NAME=BYPASSSTRMS FEED=AG01,PRODUCT=AG02,AG03

Optional entries:

None

OPERATION SPLITTER UNIT OPERATION Data Category of Input

Mandatory statement. This statement is used to define the split ratios for the product streamsfrom the splitter. Use with either the FRACTION or the RATE keyword.

Mandatory Entries:

FRACTION= or Defines the product stream flow fraction on a weight basis. En-ter from two to six entries, separated by commas. You mustsupply a corresponding entry for each product stream in order.

Values for the entries must add up to 1.0. Enter a constant valuegreater than zero, but less than one. There is no default.

RATE= Defines the product stream flowrates on a weight basis. Enterfrom two to six entries, separated by commas. You must supplya corresponding entry for each product stream in order.

HEXTRAN has two product split calculation options:

1. RELATIVE product flowrates. Enter non-zero flowrates foreach product stream; for example:

OPERATION RATE=1000000, 1000000, 2000000

HEXTRAN sums and normalizes the product rates into flowratefractions. As the feed rate changes, each product stream rate isproportionately adjusted.

2. VARIABLE and FIXED product flowrates. One of the productstreams can have a variable flowrate while the flowrates ofthe other product streams are fixed. Enter a zero flowrate forthe variable rate product stream, and non-zero flowrates forthe fixed rate product streams, for example:

OPER RATE=30, 40, 0.0

As the feed rate changes, only the variable product stream ratechanges.

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RESTRICTION: You can specify only one variable flowrate ineach splitter.

Examples:OPERATION FRACTION=0.25,0.75OPERATION RATE=1000000, 3000000

Both of these OPERATION statements produce identical results. The normalized stream flowfractions for the second OPERATION statement are computed as follows:

first stream flow fraction =first stream flow rate

sumof stream flow rates

=1000000

1000000 3000000+

= 1000000/4000000

= 0.25

The second stream flow fraction is calculated in an identical manner.SPLITTER UID=SPL2

STRMS FEED=GAS0,PRODUCT=LIGH,MED,HVYOPERATION FRACTION=0.20,0.30,0.50

SPLITTER UID=SPO5STRMS FEED=MUK,PRODUCT=PURG,RECYOPERATION RATE=200,250000

Optional Entries:

None.

SPLITTER Examples:SPLITTER UID=SPL2,NAME=BYPASS

STRMS FEED=100,*PRODUCT=101,102

OPERATION FRACTION=0.95,0.05

This example shows a splitter (SPL2) splitting a feed stream into two product streams, 101and 102. 95 percent of the feed stream is split into stream 101, and the remaining 5 percent issplit into stream 102.STREAM DATA

PROP STREAM=WATR, WATER(W)=100, TEMP=80...UNIT OPERATION DATASPLITTER UID=VSPL, NAME=VARYSPL

STRMS FEED=WATR, PROD=W1,W2,W3OPER RATE=30, 40, 0.0

This example shows a feed stream split by rate (lbs/hr - English units). This results in 30lbs/hr of the feed split to stream W1, 40 lbs/hr split to stream W2, and the remainder, 30lbs/hr, split to stream W3. If the feed stream (WATR) rate changes, streams W1 and W2 re-main at constant flowrate, and stream W3’s flowrate is varied.

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PIPE UNIT

PIPE PIPE UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement identifies the unit operation as a pipe. This must be thefirst statement for each pipe defined in the flowsheet. This section describes the input data re-quired for pipe lines and fittings. These unit operations simulate pressure drops in piping andfittings, between heat exchangers and other pieces of equipment. The PIPE unit operation op-erates adiabatically and allows only one feed and one product stream.

The PIPE unit operation offers two calculation methods:

� A rigorous pressure drop calculation, in which you specify the characteristics and di-mensions of the pipe and fittings.

� A shortcut pressure drop method, in which you specify either the unit outlet pressure,or pressure drop.

The rigorous calculations for pipe lines and fittings utilize the well-known Beggs-Brill-Moodypressure drop method, developed to handle all ranges of multiphase flow for any pipe angle.This method is the default in SIMSCI’s Simulation Program, PIPEPHASETM .

The PIPE unit operation provides the following features:

� Calculates rigorous adiabatic pressure drop

� Handles both single and two-phase fluids

� Includes LINES and FITTINGS

� Accounts for pressure drop due to:Friction lossesElevation changesAcceleration changes

� Accepts entries for length or equivalent length

� Accepts entries for pipe roughness and Moody Friction Factor

Mandatory entry:

UID= Identifies the unit operation for reference and printout purposes.Enter up to twelve alphanumeric characters. This entry must beunique to all other unit operations. There is no default.

Example:PIPE UID=PIP1

Optional entry:

NAME= Identifies the unit operation for printout purposes only. Enter upto twelve alphanumeric characters. NAME supplements the UIDentry. There is no default.

Example:PIPE UID=PIP2,NAME=TRANSFER

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STREAMS PIPE UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement identifies feed and product streams in the pipe.

Mandatory entries:

FEED= Identifies the feed, or inlet, stream and its associated fluidproperties. Enter up to twelve alphanumeric characters. TheFEED entry will be printed out as a label in the output. There isno default.

PRODUCT= Identifies the product, or outlet, stream and its associated fluidproperties. Enter up to twelve alphanumeric characters. ThePRODUCT entry will be printed out as a label in the output.There is no default.

Example:STRMS FEED=OIL1,PRODUCT=OIL2

Optional entries:

None.

LINE PIPE UNIT OPERATIONS Data Category of Input

Optional statement. This statement defines the various dimensions and characteristics for thepipe. This statement is recommended when using the rigorous calculation method (for exam-ple, when simulating two-phase fluid transfer lines, or thermosiphon reboiler piping).

For each PIPE statement, you must use one LINE and/or one FITTINGS statement, or oneOPERATION statement. You cannot use the LINE statement and the OPERATION statement onthe same PIPE unit statement.

Mandatory entries:

None.

Optional entries:

ID=6.065 or Defines the “actual” pipe inside diameter. ID is used to computethe line pressure drop and velocity. Use ID when the exact insidepipe diameter is known (e.g., fouled lines) or when the diametercannot be described using Nominal Pipe Size (NPS) and PipeSchedule (e.g., non-standard or metric line sizes). Enter a valuein the range 0.25 - 144.0 in. (English), or 6.35 - 3657.6 mm(metric and SI). An entry for ID excludes any other method fordefining pipe diameter (for example, you cannot use the DIMEN-SION statement to redefine standard dimensional units). Youcannot enter both ID and an NPS and SCHEDULE combinationon the same LINE statement.

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The default is 6.065 in. (English), or 154.051 mm (metric andSI). If neither ID nor an NPS and SCHEDULE combination areentered on the LINE statement, the default ID will be used for thepipe inside diameter.

NPS= and Nominal Pipe Size. NPS defines the “nominal” pipe size ininches. NPS is used with SCHEDULE to compute the line pres-sure drop and velocity. Enter a value for the nominal pipe sizefrom Table 4-16. An entry for NPS is required only if SCHEDULEis entered on the same LINE statement. You must enter valuesfor both NPS and SCHEDULE. You cannot enter both NPS and IDon the same LINE statement.

There is no default. If neither ID nor an NPS and SCHEDULEcombination are entered on the LINE statement, the default IDwill be used for the pipe inside diameter.

SCHEDULE= Defines the schedule number for steel pipe. SCHEDULE is usedwith NPS to compute the line pressure drop and velocity. Enter avalue for pipe schedule from Table 4-17. An entry for SCHEDULEis required only if NPS is entered on the same LINE statement.You must enter values for both SCHEDULE and NPS. You cannotenter both SCHEDULE and ID on the same LINE statement.

There is no default. If neither ID nor an NPS and SCHEDULEcombination are entered on the LINE statement, the default IDwill be used for the pipe inside diameter.

LENGTH=0.0 or Defines the total “actual” length of a pipe. LENGTH is used tocalculate the pressure drop in a straight piece of pipe with nobends or fittings. Enter a value in the range 0.0 to 10,000 ft(English), or 0 to 3048 m (metric and SI). You cannot enter bothLENGTH and EQLENGTH on the same LINE statement. The de-fault is 0.0 ft (English), or 0.0 m (metric and SI).

EQLENGTH=0.0 Defines the total “equivalent” length of a pipe, including bendsand fittings, expressed in length units. Use EQLENGTH to calcu-late the pressure drop for a length of pipe with several 90 degreebends and valves. Enter a value in the range 0 to 10,000 ft (Eng-lish), or 3 to 3048 m (metric and SI). The value of EQLENGTHentered includes the straight pipe length, and the “equivalent”length of the bends and valves in length units. The default is 0.0ft (English), or 0.0 m (metric and SI).

Note: To specify multiple sections of piping with varying diame-ters and lengths, you can use a single PIPE statement with theEQLENGTH keyword, or multiple PIPE statements with theLENGTH keyword.

Recommendation: If the available data is in L/D units (numberof equivalent pipe diameters), multiply the value by the equiva-lent diameter to obtain length units.

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ELEVATION=0.0 Defines the net change in elevation for a line. Use ELEVATION inconjunction with LENGTH to describe an inclined section of pipe(Figure 4-25). Enter a positive value for net “upward” flow or anegative number for net “downward” flow. The valid range is +/-500 ft (English), or +/- 152.40 m (metric and SI). The absolutevalue entered for ELEVATION cannot exceed the value enteredfor LENGTH or EQLENGTH. The default is 0.0 ft (English), or 0.0m (metric and SI).

ROUGHNESS=0.0018 or Defines the “absolute” pipe roughness. Enter a value in the range0.0 to 0.5 in. (English), or 0.0 - 12.7 mm (metric and SI). The de-faults are 0.0018 in. (English), or 0.04572 mm (metric and SI).

FRICTION= Defines the dimensionless Moody Friction Factor used in thepressure drop calculations. The friction factor is calculated usingthe iterative Colebrook-White equation. Enter a value in therange 0.0 to 0.10. The default value is calculated on the basis ofthe values specified for the pipe.

NOACCELERATION Sets the acceleration pressure gradient to zero. Under certainhigh velocity or high pressure drop conditions, the Beggs andBrill acceleration term may become unrealistically large, andmay dominate the equation. When this is the case, using theNOACCELERATION keyword to set the term to zero will producemore accurate results. Note that the Beggs and Brill equationwas not developed for the critical flow region.

Figure 4-25: Inclined Pipe Section

Examples:LINE NPS=6,SCHEDULE=40,LENGTH=20.0, ELEVATION=10.0LINE NPS=6, SCHEDULE=40, LENGTH=40, FRICTION=0.005LINE ID=8.0, LENGTH=90.0, ROUGHNESS=0.0018LINE ID=4, LENGTH=30, NOACCELERATION

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NetElevation(+75 ft)

Length = 200 ft

Inclined Pipe Section

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FITTINGS PIPE UNIT OPERATIONS Data Category of Input

Optional statement. This statement defines various dimensions and characteristics of thefittings.

Use the FITTINGS statement when data for the “total resistance coefficient” (KFACTOR) isavailable. The FITTINGS statement may also be used with an EQLENGTH entry.

For each PIPE statement, you must use one LINE and/or one FITTINGS statement, or one OP-ERATION statement. You cannot use the FITTINGS statement and the OPERATION statementon the same PIPE statement.

Mandatory entries:

None.

Optional entries:

ID=6.065 Defines the “equivalent” actual pipe inside diameter to be usedfor the fitting calculations. Enter a value in the range 0.24 -144.0 in. (English), or 6.35 - 3657.6 mm (metric and SI). Thedefault is 6.065 in. (English), or 154.051 mm (metric and SI).

EQLENGTH=0.0 or Defines the total “equivalent” length of the fittings (bends,valves, etc.) expressed in length units. Use EQLENGTH to calcu-late the pressure drop for a length of pipe with several 90 degreebends and valves. Typically, lengths of straight pipe are charac-terized using LINE statements, while valves and fittings are char-acterized with the FITTINGS statement.

Note: You can perform the same calculation using the KFACTORkeyword (pg. ref).

Enter a value in the range 0 - 10,000 ft (English), or 0 - 3048 m(metric and SI) to specify the straight pipe length and the “equiva-lent” length of the bends and valves in length units. You cannotuse EQLENGTH and KFACTOR on the same FITTINGS statement.The default is 0.0 ft (English), or 0.0 m (metric and SI).

Note: To specify multiple sections of piping with varying diame-ters and lengths, you can use a single PIPE statement with theEQLENGTH keyword, or multiple PIPE statements with theEQLENGTH or KFACTOR keywords.

Recommendation: If the available input data is in L/D units(number of equivalent pipe diameters), multiply the value by theequivalent diameter to obtain length units.

ROUGHNESS=0.0078 or Defines the absolute pipe roughness for the fittings. Enter avalue in the range 0.0 - 0.5 in. (English), or 0.0 12.7 mm (metricand SI). You cannot enter ROUGHNESS and KFACTOR on thesame FITTINGS statement. The default is 0.0018 in. (English), or0.04572 mm (metric and SI).

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FRICTION= or Defines the dimensionless Moody Friction Factor used in thepressure drop calculations. The friction factor is calculated usingthe iterative Colebrook-White equation. Enter a value in therange 0.0 - 0.10. You cannot enter FRICTION and KFACTOR onthe same FITTINGS statement. The default value is calculated byHEXTRAN using an iterative technique.

KFACTOR=0.0 Defines the total resistance coefficient for multiple bends, fit-tings, valves, and exit losses. Use KFACTOR to specify a “totalresistance coefficient” (KFACTOR) for the pressure drop calcula-tions when describing a multi-sectional line with various typesof fittings. Consult a suitable reference source (e.g., Flow of Flu-ids Through Valves, Fittings, and Pipe, Technical Paper 410Crane Co., 1980) to determine the total resistance coefficient.

Note: You can perform the same calculation using theEQLENGTH keyword.

Enter a value in the range 0.0 - 100.0. You cannot enter KFAC-TOR and EQLENGTH, ROUGHNESS, or FRICTION on the sameFITTINGS statement. The default is 0.0.

Examples:FITTINGS ID=6.0,KFACTOR=2.5FITTINGS ID=8.0,EQLENGTH=175.0, ROUGHNESS=0.009FITTINGS ID=8.0,ROUGHNESS=0.002, EQLENGTH=100.0

OPERATION PIPE UNIT OPERATIONS Data Category of Input

Optional statement. This statement specifies either the outlet pressure or pressure drop for ashortcut pipe unit.

For each PIPE statement, you must use one OPERATION statement, or one LINE and/or oneFITTINGS statement. You cannot use the OPERATION statement and the LINE and FITTINGSstatements on the same PIPE statement.

Mandatory entries:

None.

Optional entries:

POUT = value or Defines the outlet pressure for a shortcut pipe unit. This key-word enables HEXTRAN to calculate the pressure drop. You can-not enter DP and POUT on the same OPERATION statement. Thestandard dimensional units are psi (English), kg/cm 2 (metric),or kPa (SI). The default is equal to the unit inlet pressure.

DP=0.0 Defines the pressure drop for a shortcut pipe unit. Enter a posi-tive value to indicate a pressure decrease in the unit, or a nega-tive value to indicate a pressure increase in the unit. The defaultis 0.0 psi (English), 0.0 kg/cm 2 (metric), or 0.0 kPa (SI).

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Examples:OPERATION POUT=100.0OPERATION DP=2.5

PIPE Examples:PIPE UID=PIP1,NAME=EXAMPLE1

STRMS FEED=FLO1,PRODUCT=FLO2LINE NPS=6,SCHEDULE=40, LENGTH=225.0,ELEVATION=10.0,*

ROUGHNESS=0.0011FITTING ID=6.065,EQLENGTH=190.0

This example calculates the pressure drop for 225 feet of 6 inch nominal, schedule 40 pipewith a total elevation change of 10 feet. The pipe absolute roughness is 0.0011 inches, and theinternal Moody friction factor calculations are to be used. It also calculates the pressure lossesin a 6.065 inch diameter fitting with an equivalent pipe length of 190 feet.PIPE UID=PIP2,NAME=EXAMPLE2

STRMS FEED=FLOX,PRODUCT=FLOYLINE LENGTH=45.0,ELEVATION=45.0

This example calculates the pressure drop for a 45 foot downward vertical line. All other val-ues are set to the program defaults, including the pipe diameter, which defaults to 6.065inches.PIPE UID=PIP7

STRMS FEED=AG01,PRODUCT=AG02OPERATION POUT=150

.

.

.FLASH UID=FLS3

STRMS FEED=AG02,LIQUID=LIQA, VAPOR=VAPA...

This example illustrates the use of the OPERATION statement to set the pressure of a productstream (AG02) to a desired value (150) before feeding it to a flash drum (FLS3). (Any unit op-eration could be specified).

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VALVE UNIT

VALVE VALVE UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement identifies the unit operation as a valve. This statementmust be the first statement for each valve defined in the flowsheet.

This section describes the input data required for valves. This unit operation simulates pres-sure drops in valves between heat exchangers and other pieces of equipment. The VALVE unitoperation operates adiabatically and allows only one feed and one product stream.

The VALVE unit operation offers the shortcut pressure drop method only.

Mandatory entry:

UID= Identifies the unit operation for reference and printout purposes.Enter up to twelve alphanumeric characters. This entry must beunique to all other unit operations. There is no default.

Example:VALVE UID=VAL1

Optional entry:

NAME= Identifies the unit operation for printout purposes only. Enter upto twelve alphanumeric characters. NAME supplements the UIDentry. There is no default.

Example:VALVE UID=VA-1,NAME=LETDOWN

STREAMS VALVE UNIT OPERATIONS Data Category of Input

Optional statement. This statement identifies feed or product streams in the valve.

Mandatory entries:

FEED= Identifies the feed, or inlet, stream and its associated fluidproperties. Enter up to twelve alphanumeric characters. TheFEED entry will be printed out as a label in the output. There isno default.

PRODUCT= Identifies the product, or outlet, stream and its associated fluidproperties. The PRODUCT entry will be printed out as a label inthe output. There is no default.

Example:STREAMS FEED=A121,PRODUCT=A122

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OPERATION VALVE UNIT OPERATIONS Data Category of Input

Optional statement. This statement specifies either the outlet pressure or pressure drop for ashortcut valve unit.

Mandatory entries:

None.

Optional entries:

POUT= or Defines the outlet pressure for a shortcut valve unit. This key-word enables HEXTRAN to calculate the pressure drop. You can-not enter DP and POUT on the same OPERATION statement. Thedefault is psi (English), kg/cm 2 (metric), or kPa (SI). The defaultvalue is equal to the unit inlet pressure.

DP=0.0 Defines the pressure drop for a shortcut valve unit. Enter a posi-tive value to indicate a pressure decrease in the unit; or a nega-tive value to indicate a pressure increase in the unit. The defaultis 0.0 psi (English), 0.0 kg/cm 2 (metric), or 0.0 kPa (SI).

Example:OPERATION POUT=150.0OPERATION DP=10.0

VALVE Example:VALVE UID=VAL1,NAME=CNT-VLVE

STREAMS FEED=HIPR,PRODUCT=LOPROPERATION DP=75.0

This example shows a control valve (VAL1) reducing the pressure of stream HIPR by 75.0pressure units, resulting in product stream LOPR.

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DESALTER UNIT

DESALTER DESALTER UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement identifies the unit operation as a desalter. This statementmust be the first statement for each desalter defined in the flowsheet. Desalters simulate theremoval of brine from a process stream. DESALTER and DECANTER are essentially the sameunit operation differentiated by the keywords BRINE and WATER respectively.

Desalters have one feed, one hydrocarbon product, and brine as a second product stream. Nohydrocarbons are removed from the brine stream.

Mandatory entry:

UID= Identifies the unit operation for reference and printout purposes.Enter up to twelve alphanumeric characters. This entry must beunique to all other unit operations. There is no default.

Example:DESALTER UID=DES1

Optional entry:

NAME= Identifies the unit operation for printout purposes only. Enter upto twelve alphanumeric characters. NAME supplements the UIDentry. There is no default.

Example:DESALTER UID=DSLT,NAME=DESALT50

STREAMS DESALTER UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement identifies the feed, product, and brine product streamsin the desalter.

Mandatory entries:

FEED= Identifies the feed, or inlet, stream and its associated fluid proper-ties. Enter up to twelve alphanumeric characters. This entry mustbe unique to all other feed streams of other units in the flowsheet.However, this entry can be the same as a product stream identifierfrom another unit. Entries for FEED, PRODUCT, and BRINE cannotbe the same for a given desalter. There is no default. The FEED en-try will be printed out as a label in the output.

PRODUCT= Identifies the product, or outlet, stream and its associated fluidproperties. Enter up to twelve alphanumeric characters. This en-try must be unique to all other product streams of other units inthe flowsheet. However, this entry can be the same as a feed

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stream identifier to another unit. Entries for FEED, PRODUCT,and BRINE cannot be the same for a given desalter. There is nodefault. The PRODUCT entry will be printed out as a label in theoutput.

BRINE= Identifies the brine product stream and its associated fluid proper-ties. Enter up to twelve alphanumeric characters. This entry mustbe unique to all other product streams of other units in the flow-sheet. However, this entry can be the same as a feed stream iden-tifier to another unit. Entries for FEED, PRODUCT, and BRINEcannot be the same for a given desalter. There is no default. TheBRINE entry will be printed out as a label in the output.

Example:STRMS FEED=CRUD,PRODUCT=CRU1,BRINE=WATR

Optional entries:

None.

OPERATION DESALTER UNIT OPERATIONS Data Category of Input

Optional statement. This statement defines the various temperatures, pressures, and parame-ters for the desalter.

Mandatory entries:

None.

Optional entries:

TOUT= or Defines the outlet temperature for a desalter. TOUT enables HEX-TRAN to calculate the temperature drop. You cannot enter TOUTand DT on the same OPERATION statement. The standard di-mensional units are: F (English), C (metric), and K (SI). The de-fault is equal to the unit inlet temperature.

DT=0.0 Defines the temperature drop for a desalter. Enter a positivevalue to indicate a temperature decrease in the unit; or a nega-tive value to indicate a temperature increase. You cannot enterTOUT and DT on the same OPERATION statement. The default is0.0 F (English), 0.0 C (metric), or 0.0 K (SI).

POUT= or Defines the outlet pressure for a desalter. POUT enables HEX-TRAN to calculate the pressure drop. You cannot enter POUTand DP on the same OPERATION statement. The standard di-mensional units are: psi (English), kg/cm 2 (metric), and kPa(SI). The default value is equal to the unit inlet pressure.

DP=0.0 Defines the pressure drop for a desalter. Enter a positive value toindicate a pressure decrease in the unit, or a negative value toindicate a pressure increase. You cannot enter POUT and DP onthe same OPERATION statement. The default is 0.0 psi (Eng-lish), 0.0 kg/cm 2 (metric), or 0.0 kPa (SI).

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Examples:OPERATION DT=5.0,DP=15.0,REJECTION=0.99OPERATION TOUT=135,DP=74,REJECTION=80.0

REJECTION=100 Defines the percentage or fraction of all the water present in thefeed that is rejected from the unit. Enter a value greater thanzero. Entries less than or equal to 1.0 are taken as a fraction. En-tries greater than 1.0 are taken as a percentage. The default is100.

Example:REJECTION=0.95REJECTION=95

Both examples specify 95% of the water in the FEED stream being removed in the BRINEstream.

DESALTER Example:DESALTER UID=DES1,NAME=DESALT=1

STRMS FEED=CRUD,*PRODUCT=CRU2,*

BRINE=WAT1OPERATION DP=10.0,DT=15.0,*

REJECTION=98.0

This example shows a crude oil stream (CRUD) flowing through a desalter unit to remove cor-rosive salts. Plant data shows that the pressure drop for the unit is 10.0, and that the outletstream is 15 degrees cooler than the inlet. In addition, 98 percent of the feed water is removedin the brine stream.

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DECANTER UNIT

DECANTER DECANTER UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement identifies the unit operation as a decanter. This state-ment must be the first statement for each decanter defined in the flowsheet. DECANTERSsimulate the removal of water from a process stream. DESALTER and DECANTER are essen-tially the same unit operation differentiated by the keywords BRINE and WATER, respectively.

Decanters have one feed, one hydrocarbon product, and water as a second product stream.No hydrocarbons are removed from the water streams.

Mandatory entry:

UID= Identifies the unit operation for reference and printout purposes.Enter up to twelve alphanumeric characters. This entry must beunique to all other unit operations. There is no default.

Example:DECANTER UID=DEC3

Optional entry:

NAME= Identifies the unit operation for printout purposes only. Enter upto twelve alphanumeric characters. NAME supplements the UIDentry. There is no default.

Example:DECANTER UID=DSLT, NAME=DECANT-3

STREAMS DECANTER UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement identifies the feed, product, and water product streamsin the decanter.

Mandatory entries:

FEED= Identifies the feed, or inlet, stream and its associated fluid prop-erties. Enter up to twelve alphanumeric characters. This entrymust be unique to all other feed streams of other units in theflowsheet. However, this entry can be the same as a productstream identifier from another unit. Entries for FEED, PRODUCT,and BRINE cannot be the same for a given decanter. There is nodefault. The FEED entry will be printed out as a label in theoutput.

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PRODUCT= Identifies the product, or outlet, stream and its associated fluidproperties. Enter up to twelve alphanumeric characters. This en-try must be unique to all other product streams of other units inthe flowsheet. However, this entry can be the same as a feed streamidentifier to another unit. Entries for FEED, PRODUCT, and BRINEcannot be the same for a given decanter. There is no default. ThePRODUCT entry will be printed out as a label in the output.

WATER= Identifies the water product stream and its associated fluid prop-erties. Enter up to twelve alphanumeric characters. This entrymust be unique to all other water streams of other units in theflowsheet. However, this entry can be the same as a feed streamidentifier to another unit. Entries for FEED, PRODUCT, and BRINEcannot be the same for a given decanter. There is no default. TheWATER entry will be printed out as a label in the output.

Example:STRMS FEED=HCGO,PRODUCT=HGO1, WATER=WAT3

Optional entries:

None.

OPERATION DECANTER UNIT OPERATIONS Data Category of Input

Optional statement. This statement defines the various temperatures, pressures, and parame-ters for the decanter.

Mandatory entries:

None.

Optional entries:

TOUT= or Defines the outlet temperature for a decanter. TOUT enablesHEXTRAN to calculate the temperature drop. You cannot enterTOUT and DT on the same OPERATION statement. The standarddimensional units are: F (English), C (metric), and K (SI). Thedefault is equal to the unit inlet temperature.

DT=0.0 Defines the temperature drop for a decanter. Enter a positivevalue to indicate a temperature decrease in the unit; or a nega-tive value to indicate a temperature increase. You cannot enterTOUT and DT on the same OPERATION statement. The default is0.0 F (English), 0.0 C (metric), or 0.0 K (SI).

POUT= Defines the outlet pressure for a decanter. POUT enables HEX-TRAN to calculate the pressure drop. You cannot enter POUTand DP on the same OPERATION statement. The standard di-mensional units are: psi (English), kg/cm 2 (metric), and kPa(SI). The default value is the same as the unit inlet pressure.

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DP=0.0 Defines the pressure drop for a desalter. Enter a positive value toindicate a pressure decrease in the unit, or a negative value toindicate a pressure increase. You cannot enter POUT and DP onthe same OPERATION statement. The default is 0.0 psi (Eng-lish), 0.0 kg/cm 2 (metric), or 0.0 kPa (SI).

Examples:OPERATION DT=10.0,DP=15.0,REJECTION=0.99OPERATION TOUT=200,DP=20.0,REJECTION=70.0OPERATION TOUT=175

REJECTION=100 Defines the percentage or fraction of all the water present in thefeed that is rejected from the unit. Enter a value greater thanzero. Entries less than or equal to 1.0 are taken as a fraction. En-tries greater than 1.0 are taken as a percentage. The default is100.

Examples:REJECTION=0.80REJECTION=80

Both examples specify 80% of the water in the FEED stream being removed in the WATERstream.

DECANTER Example:DECANTER UID=DEC1,NAME=COLD-SEP

STRMS FEED=WET1,*PRODUCT=DRY1,WATER=WATR

OPERATION DP=0.0,TOUT=100.0,*REJECTION=99.5

This example shows a mixture of water and light oil entering a decanter to separate the oil andwater phases. A heating element maintains the decanter temperature at 100 degrees. Thepressure drop in the unit is negligible (DP=0.0) and all but 0.5 percent of the water is removedfrom the oil.

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FLASH DRUM UNIT

FLASH FLASH DRUM UNIT OPERATIONS Data Category of Input

This statement identifies the unit operation as a flash drum. This must be the first statementfor each flash drum defined in the flowsheet.

This unit operation is used to separate the liquid and vapor components of a stream at a speci-fied product pressure.

A flash drum has one feed stream and two product streams. The liquid and vapor rates fromthe flash drum are computed from condensate weight fraction and enthalpy data at the speci-fied product pressure. The FLASH DRUM operates adiabatically.

To use the FLASH statement, you must supply ENTHALPY and CFRAC data for the feed streamto the unit. If water or steam is present in the feed, WFRAC data is also required.

Mandatory entry:

UID= Identifies the unit operation for reference and printout purposes.Enter up to twelve alphanumeric characters. This entry must beunique to all other unit operations. There is no default.

Example:FLASH UID=FLS1

Optional entry:

NAME= Identifies the unit operation for printout purposed only. Enter upto twelve alphanumeric characters. NAME supplements the UIDentry. There is no default.

Example:FLASH UID=FLS3,NAME=PREFLASH

STREAMS FLASH DRUM UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement identifies feed, and vapor and liquid product streams inthe flash drum.

Mandatory entries:

FEED= Identifies the feed, or inlet, stream and its associated fluid prop-erties. Enter up to twelve alphanumeric characters. This entrymust be unique to all other feed streams of other units in theflowsheet. However, this entry may be the same as a productstream identifier from another unit. The entries for FEED, VA-POR, and LIQUID cannot be the same for a give flash drum unit.There is no default. The FEED entry will be printed out as a labelin the output.

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VAPOR= Identifies the vapor stream and its associated fluid properties.Enter up to twelve alphanumeric characters. This entry must beunique to all other vapor streams of other units in the flowsheet.However, this entry may be the same as a feed stream identifierto another unit. The entries for FEED, VAPOR, and LIQUID can-not be the same for a given flash drum unit. There is no default.The VAPOR entry will be printed out as a label in the output.

LIQUID= Identifies the liquid stream and its associated fluid properties.Enter up to twelve alphanumeric characters. This entry must beunique to all other liquid streams of other units in the flowsheet.However, this entry can be the same as a feed stream identifierto another unit. The entries for FEED, VAPOR, and LIQUID can-not be the same for a given flash drum unit. There is no default.The LIQUID entry will be printed out as a label in the output.

Example:STRMS FEED=MIX1,VAPOR=VAP1,LIQUID=LIQ1

Optional entries:

None.

OPERATION FLASH DRUM UNIT OPERATIONS Data Category of Input

Optional statement. This statement specifies either the outlet pressure or pressure drop for aflash drum.

Mandatory entries:

POUT=orDP=0.0

POUT defines the outlet pressure for a flash drum. This keywordenables HEXTRAN to calculate the pressure drop. Standard di-mensional units are: psi (English), kg/cm 2 (metric), and kPa(SI). The default values are equal to the unit inlet pressure. Youcannot enter POUT and DP on the same OPERATION statement.

DP defines the pressure drop for a flash drum. Enter a positivevalue to indicate a pressure decrease in the unit, or a negativevalue to indicate a pressure increase in the unit. The defaultvalue is 0.0 psi (English), or 0.0 kg/cm 2 (metric), or 0.0 kPa(SI).

Examples:OPERATION DP=10.0OPERATION POUT=130.5

Optional entries:

None.

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FLASH ExamplesSTREAM DATA

PROP STREAM=1,SETNO=1,...PROP STREAM=2,SETNO=2,PRES= 60,TOUT = 60,*

REFPHASE=V,REFSTREAM=1,PHASE=VPROP STREAM=3,SETNO=3,PRES = 60,TOUT = 60,*

REFPHASE=L,REFSTREAM=1,PHASE=L..UNIT OPS

FLASH UID=F2STREAMS FEED=1,LIQUID=2,VAPOR=3

In the above example, a stream (1) is flashed adiabatically to separate the liquid and vaporphases. The resulting liquid (2) and vapor (3) product streams have new physical propertydata sets, which are defined by the REFSTRM statements in the STREAM DATA section.Without the REFSTRM statements, the product streams would retain the properties of the feedstream by default.STREAM DATA

PROP STREAM=1, RATE=1000, COMP=1, 50/2,25/3,25,*TEMP=100, PRES=35

.

.

.UNIT OPERATIONS

FLASH UID=F2STREAMS FEED=1, LIQUID=2, VAPOR=3

In the above example, the flash product streams do not need to be defined, because the feedstream uses point access (no SETNO entry is given). Therefore, HEXTRAN will rigorously cal-culate the properties for streams 2 and 3.

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SHORTCUT HEAT EXCHANGER UNIT

HX HX UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement identifies the unit as a shortcut exchanger. This state-ment must be the first input line for any HX model.

The shortcut exchanger (HX) in HEXTRAN is designed for problems that do not require rigor-ous heat transfer coefficients and pressure drop calculations. The shortcut exchanger sup-ports all TEMA type exchangers as defined in the Standards of the Tubular ExchangerManufacturers Association, Sixth Edition, 1978. All fluid types are supported on either side ofthe exchanger, and vaporization and/or condensation are automatically treated by zone analy-sis. Section 40.1 defines the fluid property requirements for the calculations.

The HX statement can be used in either rating (OLD) or design (NEW) mode. The performancerating for OLD exchangers is calculated based on the supplied area and U-value. For NEW ex-changers, the required area and number of exchanger shells is calculated based on the tem-perature or duty specification and the supplied U-value.

Performance specifications are optional for OLD exchanger calculations. When a specificationis provided, the required effective heat transfer area is calculated to match the specified heattransfer and supplied U-value. NEW shortcut exchangers require specifications for SIMULA-TION and REGRESSION calculations. Specifications for OPTIMIZATION AREA calculations areoptional for NEW exchangers.

You can specify which printed reports, calculation options, and exchanger costing details youwant using the PRINT, CALCULATION, and COST statements. Defaults for these statements areset by the global values in the Calculation Data Section.

Rigorous Shell and Tube exchangers (STE) can be converted to shortcut exchangers (HX) bysubstituting “HX” for “STE” and adding the UVALUE entry to the TYPE statement. You mustalso remove the UESTIMATE keyword from any converted statement.

Mandatory entries:

UID= Identifies the unit operation for reference and printout purposes.Enter up to twelve alphanumeric characters. This entry must beunique to all other unit operations. There is no default.

Optional entries:

NAME= Identifies the unit operation for printout purposes only. Enter upto twelve alphanumeric characters. NAME supplements the UIDentry.

Example:HX UID=HX1,NAME=EXCH-1

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TYPE HX UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement defines the basic characteristics of the shortcut exchanger.

Mandatory entries:

OLD or Rating only. OLD specifies that performance is calculated basedon the supplied area and U-value.

NEW Design only. NEW specifies that the required area and number ofexchanger shells will be calculated based on the temperature orduty specification and the supplied U-value.

Examples:HX UID=HX2

TYPE OLDHX UID=EX23

TYPE NEW

TEMA=AES Specifies the TEMA designation. Enter a three- or four-characterdesignation as described in Figure 4-1. Acceptable TEMA desig-nations are given in Table 4-11. The default is AES.

For J-type (divided flow) shells, enter J1 (or J) for shells withone inlet and two outlet nozzles. For J-type shells with two inletand one outlet nozzles, enter J2.

UVALUE= Specifies the U-Value for the shortcut exchanger calculations.Standard dimensional units are Btu/hr-ft2-F (English), kcal/hr-m2 -C (metric), or W/m 2 -K (SI).

Example:HX UID=HX2B

TYPE OLD,TEMA=NKT,UVALUE=50

Optional entries:

HOTSIDE=SHELL Specifies the side of the exchanger receiving the hotside fluid.Enter SHELL or TUBE. SHELL is the default.

FLOW=COUNTERCURRENT Specifies the flow direction. Enter COUNTERCURRENT or CO-CURRENT. This entry affects the calculation of the LMTD andLMTD correction factor (FT). The default is COUNTERCURRENT.

AREA=1000 or Rating only. Specifies the effective or “installed” area per unit forOLD exchanger calculations. The default is 1000 ft 2 (English),or 92.9 m 2 (metric and SI).

AREA=200,6000 Design only. Specifies the area value per SHELL (not per UNIT asfor OLD exchangers). Enter minimum and maximum values forarea. Values specified on the LIMITS statement in the CALCULA-TION section override the defaults for this keyword. Default valuesare 200 and 6000 ft2 (English), or 18.6 m2 and 557 m2 (metric andSI).

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Example:HX UID=HX2B

TYPE OLD,TEMA=NKT,UVALUE=50,*HOTS=SHELL,FLOW=COUNTERCURRENT,*AREA=500

TUBESIDE HX UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement defines all necessary details for the tubeside of theexchanger.

Mandatory entries:

FEED= Identifies the feed, or inlet stream and its associated properties.Enter up to twelve alphanumeric characters. The FEED entry willbe printed as a label in the output. There is no default.

PRODUCT= Identifies the product, or outlet stream and its associatedproperties. Enter up to twelve alphanumeric characters. ThePRODUCT entry will be printed as a label in the output. There isno default.

Example:HX UID=HX2B

TUBE FEED=FID1,PROD=PID2

Optional entries:

PASS=2 or Rating only. Specifies the number of tube passes per shell. Enteran integer from 1 to 16. One pass corresponds to true counter-flow. The default is 2.

PASS=2,16,2 Design only. Specifies the number of tube passes per shell. En-ter values for minimum, maximum, and incremental (integersfrom 1 to16, separated by commas). The shortcut exchangerdoes not vary the number of tube passes during design. Thevalue is held constant at the specified minimum value. However,the maximum and incremental entries are required.

DPSHELL=5.0 or Specifies the value for pressure drop per bundle. The default is5.0 psi (English), or 0.35 kg/cm2 (metric), or 34.5 kPa (SI).

DPUNIT=5.0 Specifies the value for pressure drop per service. The default is5.0 psi (English), or 0.35 kg/cm2 (metric), or 34.5 kPa (SI).

Example:HX UID=HX2B

TYPE NEWTUBE FEED=FID1,PROD=PID2,PASS=2,8,2,*

PSHELL=4.5

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SHELLSIDE HX UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement defines the necessary details for the shellside of theshortcut exchanger.

Mandatory entries:

FEED= Identifies the feed, or inlet stream and its associated properties.Enter up to twelve alphanumeric characters. The FEED entry willbe printed as a label in the output. There is no default.

PRODUCT= Identifies the product, or outlet stream and its associated prop-erties. Enter up to twelve alphanumeric characters. The PROD-UCT entry will be printed as a label in the output. There is nodefault.

Example:HX UID=HX2B

SHELL FEED=FID2,PROD=PID4

Optional entries:

SERIES=1 Rating only. Specifies the number of shells in series. Enter an in-teger from 1 to 10. The default is 1.

SERIES=1,10 Design only. Limits the number of exchanger shells in series.Enter minimum and maximum values, separated by a comma.Valid range is 1 to 10. SHELLS in series are incremented from 1to meet the minimum LMTD correction factor, MINFT, which issupplied on the CALCULATION statement or defaulted globally inthe CALCULATION Data Section.

PARALLEL=1 Rating only. Specifies the number of shells in parallel. Enter aninteger from 1 to 10. The default is 1.

PARALLEL=1,10 Design only. Limits the number of exchanger shells in parallel.Enter minimum and maximum values, separated by a comma.Valid range is 1 to 10. Shells in parallel are added as required tokeep within the specified limit of area per shell supplied on theTYPE statement.

DPSHELL=5.0 Specifies the pressure drop per shell. The default is 5.0 psi(English), or 0.35 kg/cm 2 (metric), or 34.5 kPa (SI).

DPUNIT=5.0 Specifies the pressure drop per service. The default is 5.0 psi(English), or 0.35 kg/cm 2 (metric), or 34.5 kPa (SI).

Example:HX UID=XRTR

TYPE OLDTUBE FEED=FID5,PROD=PID7,SERIES=2,*

DPSHELL=5.5

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CALCULATION HX UNIT OPERATIONS Data Category of Input

Optional statement. This statement defaults to the global value specified on the CALCULATIONstatement in the Calculation Data section.

Mandatory entries:

MINFT=0.8 Specifies the minimum allowable LMTD correction factor. Entera value between 0.5 and 1. Values smaller than 0.5 are accept-able, but not practical. Additional shells are added in series asneeded to keep the “FT” factor above this threshold. The defaultis 0.8.

Example:HX UID=HXRT,*

MINFT=0.5

SPECIFICA-TION

HX UNIT OPERATIONS Data Category of Input

Optional for Rating; mandatory for Design. This statement specifies performance criteria forOLD or NEW shortcut exchangers. This statement determines the area necessary for thespecified heat transfer for NEW exchangers.

Mandatory entries:

DUTY= or Specifies the total heat transferred in the exchanger. You cannotuse DUTY and TEMP on the same entry. Standard dimensionalunits are MMBtu/hr (English), MMkcal/hr (metric), and MMkJ/hr(SI).

TEMPERATURE= and Specifies the outlet temperature of the exchanger. Use in con-junction with either the SHELL or TUBE entry. You cannot useTEMP and DUTY on the same entry. Standard dimensional unitsare F (English), C (metric), and K (SI).

SHELLSIDE orTUBESIDE

Specifies which outlet the temperature specification applies to.You cannot use SHELL or TUBE with the DUTY keyword.

SPECIFICATION Examples:SPEC DUTY=10.8

This example specifies the DUTY for an exchanger as 10.8 million energy units per time unit.SPEC TEMP=127,SHELL

This example specifies a shell outlet temperature of 127 degrees. Note that it is always mostaccurate to place outlet temperature specifications on the stream with the smallest flow rate.

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PRINT HX UNIT OPERATIONS Data Category of Input

Optional statement. This statement specifies printout options. If the PRINT statement is omit-ted, the printout options default to the global values specified on the CALCULATION statementin the Calculation Data section. See Section ... for a discussion of the global print options forexchangers.

Optional entries:

STANDARD Prints a standard TEMA data sheet.

ZONES Prints a zones analysis for a two-phase exchanger.

COST HX UNIT OPERATIONS Data Category of Input

Optional statement. This statement provides special costing data for an exchanger. If the COSTstatement is omitted, the cost defaults to the global values specified in the Calculation Section.

The data defined by the COST statement are used in the general equation below:

Heat Exchanger Cost = CONSTANT + LINEAR * AREA + ETERM

where:

ETERM = BCOST * BSIZE * (AREA/BSIZE) ** EXPONENT

and

AREA = area for a single exchanger shell (duct or bay or frame).

For exchangers costed on a per shell base, for example, the above cost is multiplied by thenumber of exchangers involved in the service.

Mandatory entries:

BSIZE=1000.00 Defines the base area used in the costing equation. The defaultis 1000.00 ft 2 (English), or 93.0 m2 (metric and SI).

BCOST=0.00 Defines the base cost used in the costing equation. The defaultis 0.00 USDOLLAR/ft 2 (English) = 0.00 USDOLLAR/m2 (metricand SI).

LINEAR=50.00 Defines the linear cost factor used in the costing equation. Thedefault is 50.00 USDOLLAR/FT 2 (English) = 538.20 USDOL-LAR/m 2 (metric and SI).

EXPONENT=0.60 Defines the exponential cost factor used in the costing equation.The default is 0.60 (English, metric and SI).

CONSTANT=0.00 Defines the constant cost factor used in the costing equation.This entry can be used to define fixed costs associated with in-stallation of an exchanger and is not a function of exchangersize. The default is 0.00 USDOLLAR (English, metric & SI).

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UNIT orSHELL

Defines the basis for the exchanger CONSTANT cost factor. UNITresults in the constant cost factor being applied once to eachunit regardless of the number of shells or frames in the unit.SHELL results in the constant cost factor being applied to eachshell or each frame in the unit. The default is UNIT.

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SHORTCUT HEATER UNIT

HEATER HEATER UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement identifies the unit operation as a heater. This statementmust be the first statement for each heater defined in the flowsheet. This unit operation simu-lates heat gains or any type of heater which may use a heating medium.

HEATERS have one feed and one product stream. In addition, capital costs for each unit opera-tion may be calculated if desired. Operating costs are calculated if the required entries aregiven with the UTCOST statement (SIMULATION category of input, page 4-9.

Capital costs for the HEATERs are computed with a generalized costing equation if a COSTstatement is given for each unit.

Note: There is no default utility costs for the UTILITY=HEATINGMEDIUM entry. Operatingcosts for a HEATER using this utilitywill only be calculated if the required entry is given withthe UTCOST statement.

Mandatory entry:

UID= Identifies the unit operation for reference and printout purposes.Enter up to twelve alphanumeric characters. This entry is re-quired and must be unique to all other unit operations. There isno default.

Optional entry:

NAME= Identifies the unit operation for printout purposes only. Enter upto twelve alphanumeric characters. NAME supplements the UIDentry. There is no default.

Examples:HEATER UID=HTR4HEATER UID=HTR1,NAME=HOT-OIL

STREAMS HEATER UNIT OPERATIONS Data Category of Input

The STRMS statement is used to identify feed or product streams in the heater. This statementand all entries on the statement are required.

FEED= Identifies the feed, or inlet, stream and its associated fluid prop-erties. Enter up to twelve alphanumeric characters. This entrymust be unique to all other feed streams in the flowsheet. How-ever, this entry can be the same as a product stream identifierfrom another unit. FEED and PRODUCT cannot be the same agiven HEATER unit. The FEED entry will be printed out as a labelin the output. There is no default.

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PRODUCT= Identifies the product, or outlet, stream and its associated fluidproperties. Enter up to twelve alphanumeric characters. This en-try must be unique to all other product streams in the flowsheet.However, this entry can be the same as a feed stream identifierto another unit. FEED and PRODUCT cannot be the same a givenHEATER unit. The PRODUCT entry will be printed out as a labelin the output. There is no default.

Example:STRMS FEED=CLD1,PRODUCT=HOT1

OPERATION HEATER UNIT OPERATIONS Data Category of Input

The OPERATION statement is used to define the various temperatures, pressures, and parame-ters for the HEATER. This statement and all entries on the statement are optional.

Optional entries:

DUTY= Specifies the heater duty in millions of energy units per hour.Enter a value greater than or equal to zero. You cannot enterDUTY and TOUT or DT on the same OPERATION statement.There is no default.

TOUT= Specifies the outlet stream temperature. This entry enables HEX-TRAN to calculate the temperature rise. The default value is thesame as the unit inlet temperature. Standard dimensional unitsare: F (English), C (metric) and K (SI). You cannot enter TOUTand DUTY or DT on the same OPERATION statement. There isno default.

DT=0.0 Specifies the temperature rise. You cannot enter DT and DUTYor TOUT on the same OPERATION statement The default is 0.0F (English), 0.0 C (metric), or 0.0 K (SI).

TUTILITY=85 Specifies the utility stream supply temperature. This entry isused to calculate the operating costs for the HEATER, and onlyapplies if UTILITY=AIR is entered on the OPERATION statement.The defaults are 85.0 F (English), 29.4 C (metric), or 302.6 K(SI).

POUT= Specifies the outlet stream pressure. This entry enables HEX-TRAN to calculate the pressure drop. The standard dimensionalunits are: psi (English), kg/cm 2 (metric), and kPa (SI). You can-not enter POUT and DP on the same OPERATION statement. Thedefault is the value of the unit inlet pressure.

DP=0.0 Specifies the pressure drop. You cannot enter DP and POUT onthe same OPERATION statement.The defaults are 0.0 psi (Eng-lish), 0.0 kg/cm 2 (metric), and 0.0 kPa (SI).

UTILITY=HEATINGMEDIUM Specifies the UTILITY stream type. Enter AIR or HEATINGME-DIUM. This entry is used to determine the operating costs forthe heater based on the UTCOST statement (SIMULATION

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category of input). If you specify UTILITY=HEATINGMEDIUM,you must include an entry for HEATINGMEDIUM on the UTCOSTstatement in order to calculate operating costs for the HEATER.The default is HEATINGMEDIUM.

Examples:OPERATION DUTY=2.75,DP=5.0,*

UTILITY=HEATINGMEDIUMOPERATION TOUT=300,POUT=100,*

DTUTILITY=100OPERATION DT=70,DP=3.5,TUTILITY=275,*

TUTILITY=30,*UTILITY=HEATINGMEDIUM

COST HEATER UNIT OPERATIONS Data Category of Input

Optional statement. This statement defines the basis and cost factor data used in the general-ized costing equation to calculate the HEATER capital costs. If the COST statement is not used,then capital costs will not be calculated. There is no default utility cost for the UTILITY= HEAT-INGMEDIUM entry. Operating costs will only be calculated if the required entries are specifiedon the UTCOST statement (see the SIMULATION category of input).

Note: The form of the generalized costing equation may be altered by entering a value of zerofor one or more of the terms. You cannot, however, enter a value of zero for the base size.

The generalized costing equation is:

EQUIPMENT COST = (CONSTANT + (LINEAR*TOTALSIZE) + ETERM) * CSTF

where:

CONSTANT =constant cost factor.

LINEAR=linear cost factor.

TOTALSIZE = total size. The basis chosen will depend on the type of equipment to becosted.

Possible bases are area, heat duty, and power. These apply to exchangers, heaters/cool-ers/fired heaters, or compressors/pumps, respectively.

ETERM =BCOST * BSIZE * NTS * (TOTALSIZE/NTS/BSIZE) ** EXPONENT

BSIZE =base size. The basis chosen will depend on the type of equipment to becosted. Possible bases are area, heat duty, and power.

BCOST = the base cost defined as the cost per unit area, duty, or power.

NTS = total number of exchanger shells. This entry is set to 1.0 when costing equipmentother exchangers.

EXPONENT =exponential factor

CSTF = stream cost factor. This entry applies only to exchanger costing.

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Optional entries:

BSIZE=1.0 Specifies the base duty in millions of energy units used in thegeneralized costing equation. Enter a value greater than zero.The default is 1.0 MMBtu (English), 1.0 MMkcal (metric), or 1.0MMkJ (SI).

BCOST= Specifies the base cost per million energy units for the general-ized costing equation. Units are currency units per million en-ergy units. Enter a value greater than or equal to zero. Thedefault is 0.0 USDOLLAR/MMBtu (English), 0.0 USDOL-LAR/MMkcal (metric), or 0.0 USDOLLAR/MMkJ (SI).

LINEAR= Specifies the linear cost factor in the generalized costing equa-tion. Units are currency units per million energy units. Use thiskeyword when the heater cost is a simple function of the powerrequired. Enter a value greater than or equal to zero. The defaultis 0.0 USDOLLAR/MMBtu (English), 0.0 USDOLLAR/MMkcal(metric), or 0.0 USDOLLAR/MMkJ (SI).

EXPONENT=0.6 Specifies the exponential cost factor in the generalized costingequation. Enter a real value greater than or equal to zero. Thisentry has no effect unless a nonzero entry is also given forBCOST. The default is 0.6 (dimensionless).

CONSTANT=0.0 Specifies the constant cost factor used in the generalized cost-ing equation. You can use this keyword to enter fixed costs as-sociated with the installation of the HEATER (e.g., interconnectpiping and valves). Enter a value greater than or equal to zero.Valid units are currency units. This cost is not a function ofheater duty. The default is 0.0 USDOLLAR.

Examples:COST LINEAR=2.1,CONSTANT=13000COST BCOST=1600,BSIZE=1700,*

CONSTANT=300000,EXPONENT=0.66

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SHORTCUT COOLER UNIT

COOLER COOLER UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement identifies the unit operation as a cooler. This statementmust be the first statement for each cooler defined in the flowsheet. Thisunit operation simu-lates water coolers, air coolers, or heat losses (e.g., losses from long pipe runs, etc.) and anyother type of cooler which may use a refrigerant.

This unit operation has one feed and one product stream. In addition, capital costs for eachunit operation may be calculated if desired. Operating costs are calculated if the required en-tries are given with the UTCOST statement (SIMULATION category of input, page 4-9.

Capital costs for the COOLER are computed with a generalized costing equation if a COSTstatement is given for each unit.

Note: Thereis no default utility costs for the UTILITY=REFRIGERANT entry. Operating costs fora COOLER using these utilities will only be calculated if the required entry is given with theUTCOST statement.

Mandatory entry:

UID= Identifies the unit operation for reference and printout purposes.Enter up to twelve alphanumeric characters. This entry is re-quired and must be unique to all other unit operations. There isno default.

Optional entry:

NAME= Identifies the unit operation for printout purposes only. Enter upto twelve alphanumeric characters. NAME supplements the UIDentry. There is no default.

Examples:COOLER UID=COOLCOOLER UID=CLR1,NAME=RUN-DOWN

STREAMS COOLER UNIT OPERATIONS Data Category of Input

The STRMS statement is used to identify feed or product streams in the cooler. This statementand all entries on the statement are required.

FEED= Identifies the feed, or inlet, stream and its associated fluid prop-erties. Enter up to twelve alphanumeric characters. This entrymust be unique to all other feed streams in the flowsheet. How-ever, this entry can be the same as a product stream identifierfrom another unit. FEED and PRODUCT cannot be the same agiven COOLER. The FEED entry will be printed out as a label inthe output. There is no default.

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PRODUCT= Identifies the product, or outlet, stream and its associated fluidproperties. Enter up to twelve alphanumeric characters. This en-try must be unique to all other product streams in the flowsheet.However, this entry can be the same as a feed stream identifierto another unit. FEED and PRODUCT cannot be the same a givenHEATER unit. The PRODUCT entry will be printed out as a labelin the output. There is no default.

Example:STREAMS FEED=K1,PRODUCT=K2

OPERATION COOLER UNIT OPERATIONS Data Category of Input

The OPERATION statement is used to define the various temperatures, pressures, and parame-ters for the COOLER

Optional entries:

DUTY= Specifies the cooler duty in millions of energy units per hour.Enter a value greater than or equal to zero. You cannot enterDUTY and TOUT or DT on the same OPERATION statement.There is no default.

TOUT= Specifies the outlet stream temperature. This entry enables HEX-TRAN to calculate the temperature drop. The default value is thesame as the unit inlet temperature. Standard dimensional unitsare: F (English), C (metric) and K (SI). You cannot enter TOUTand DUTY or DT on the same OPERATION statement. There isno default.

DT=0.0 Specifies the temperature drop. You cannot enter DT and DUTYor TOUT on the same OPERATION statement The default is 0.0F (English), 0.0 C (metric), or 0.0 K (SI).

TUTILITY=85 Specifies the utility stream supply temperature. This entry isused to calculate the operating costs for the COOLER, and onlyapplies if UTILITY=AIR is entered on the OPERATION statement.The defaults are 85.0 F (English), 29.4 C (metric), or 302.6 K(SI).

DTUTILITY=20.0 Specifies the utility stream temperature drop. This entry is usedto calculate the operating costs for the COOLER, and only ap-plies if the UTILITY=WATER entry is entered on the OPERATIONstatement. The defaults are 20.0 F (English), 11.1 C (metric), or11.1 K (SI).

POUT= Specifies the outlet stream pressure. This entry enables HEX-TRAN to calculate the pressure drop. The standard dimensionalunits are: psi (English), kg/cm 2 (metric), and kPa (SI). You can-not enter POUT and DP on the same OPERATION statement. Thedefault is the value of the unit inlet pressure.

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DP=0.0 Specifies the pressure drop. You cannot enter DP and POUT onthe same OPERATION statement. The defaults are 0.0 psi (Eng-lish), 0.0 kg/cm 2 (metric), and 0.0 kPa (SI).

UTILITY=WATER Specifies the UTILITY stream type. Enter AIR, WATER. orREFRIGERANT. This entry is used to determine the operatingcosts for the heater based on the UTCOST statement. If youspecify UTILITY=REFRIGERANT, you must include an entry forREFRIGERANT on the UTCOST statementin order to calculateoperating costs for the HEATER. The default isHEATINGMEDIUM.

Examples:OPERATION DUTY=3.75,DP=5.0,UTILITY=WATEROPERTION TOUT=10,POUT=105,DTUTILITY=30.0OPERATION DT=60,DP=5.0,TUTILITY=35.0,*

DTUTILITY=30.0,*UTILITY=REFRIGERANT

COST COOLER UNIT OPERATIONS Data Category of Input

Optional statement. This statement defines the basis and cost factor data used in the general-ized costing equation to calculate the COOLER capital costs. If the COST statement is notused, then capital costs will not be calculated. There is no default utility cost for the UTILITY=REFRIGERANT entry. Operating costs will only be calculated if the required entries are speci-fied on the UTCOST statement (SIMULATION category of input, page 4-9.

Note: The form of the generalized costing equation may be altered by entering a value of zerofor one or more of the terms. You cannot, however, enter a value of zero for the base size.

The generalized costing equation is:

EQUIPMENT COST = (CONSTANT + (LINEAR*TOTALSIZE) + ETERM) * CSTF

where:

CONSTANT = constant cost factor.

LINEAR = linear cost factor.

TOTALSIZE = total size. The basis chosen will depend on the type of equipment to be costed.

Possible bases are area, heat duty, and power. These apply to exchangers, heaters/cool-ers/fired heaters, or compressors/pumps, respectively.

ETERM = BCOST * BSIZE * NTS * (TOTALSIZE/NTS/BSIZE) ** EXPONENT

BSIZE = base size. The basis chosen will depend on the type of equipment to be costed.

Possible bases are area, heat duty, and power.

BCOST = the base cost defined as the cost per unit area, duty, or power.

NTS =total number of exchanger shells. This entry is set to 1.0 when costing equipmentother exchangers.

EXPONENT =exponential factor

CSTF =stream cost factor. This entry applies only to exchanger costing.

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Optional entries:

BSIZE=1.0 Specifies the base duty in millions of energy units used in the gener-alized costing equation. Enter a value greater than zero. The default is1.0 MMBtu (English), 1.0 MMkcal (metric), or 1.0 MMkJ (SI).

BCOST= Specifies the base cost per million energy units for the general-ized costing equation. Units are currency units per million en-ergy units. Enter a value greater than or equal to zero. Thedefault is 0.0 USDOLLAR/MMBtu (English), 0.0 USDOL-LAR/MMkcal (metric), or 0.0 USDOLLAR/MMkJ (SI).

LINEAR= Specifies the linear cost factor in the generalized costing equa-tion. Units are currency units per million energy units. Use thiskeyword when the heater cost is a simple function of the powerrequired. Enter a value greater than or equal to zero. The defaultis 0.0 USDOLLAR/MMBtu (English), 0.0 USDOLLAR/MMkcal(metric), or 0.0 USDOLLAR/MMkJ (SI).

EXPONENT=0.6 Specifies the exponential cost factor in the generalized costingequation. Enter a real value greater than or equal to zero. Thisentry has no effect unless a nonzero entry is also given forBCOST. The default is 0.6 (dimensionless).

CONSTANT=0.0 Specifies the constant cost factor used in the generalized cost-ing equation. You can use this keyword to enter fixed costs as-sociated with the installation of the HEATER (e.g., interconnectpiping and valves). Enter a value greater than or equal to zero.Valid units are currency units. This cost is not a function ofheater duty. The default is 0.0 USDOLLAR.

Examples:COST LINEAR=2.1,CONSTANT=13000COST BCOST=1600,BSIZE=1700,*

CONSTANT=300000,EXPONENT=0.66COST BCOST=0.68COST BCOST=0.070,BSIZE=170COOLER UID=CLR1,NAME=GAS-COOL

STRMS FEED=A1,PRODUCT=A2OPERATION UTILITY=WATER,*TUTILITY=85,*DTUTILITY=25.0,DP=5.0,*

TOUT=125 In this example, a medium gasoline stock is to be cooled to 125degrees before being sent to an off-plot storage tank. Coolingwater is available at 85 degrees with a maximum allowable re-turn temperature of 110 degrees. The pressure drop across thecooler is approximately 5 pressure units.

UTCOST HEATINGMEDIUM=3.90...HEATER UID=HTR1, NAME=HOT-OILSTREAMS FEED=101,PRODUCT=101AOPERATION TOUT=290,DP=0.0

In this example, a heating medium circulation loop is used topreheat a reactor feed stream to 290 degrees. The heat ex-changer pressure drop is negligible. Cost for the heating me-dium is 3.90 currency units per million energy units.

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FIRED HEATER UNIT

FIRED-HEATER

FIRED HEATER UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement identifies the unit operation as a firedheater. This state-ment must be the first statement for each firedheater defined in the flowsheet.

FIREDHEATERS are process furnaces, such as those used for in-plant heating medium sys-tems or chemical/petroleum feed pre-heaters. FIREDHEATERS have one feed and one productstream. You can calculate the capital cost of the unit. Operating costs are always calculated.

Mandatory entry:

UID= Identifies the unit operation for reference and printout purposes.Enter up to twelve alphanumeric characters. This entry is requiredand must be unique to all other unit operations. There is no default.

Optional entry:

NAME= Identifies the unit operation for printout purposes only. Enter upto twelve alphanumeric characters. NAME supplements the UIDentry. There is no default.

Examples:FIREDHEATER UID=FRD1FIREDHEATER UID=FIRE,NAME=VACHEATR

STREAMS FIRED HEATER UNIT OPERATIONS Data Category of Input

The STRMS statement is used to identify feed or product streams in the firedheater.

Mandatory entries:

FEED= Identifies the feed, or inlet, stream and its associated fluid prop-erties. Enter up to twelve alphanumeric characters. This entrymust be unique to all other feed streams in the flowsheet. How-ever, this entry can be the same as a product stream identifierfrom another unit. FEED and PRODUCT cannot be the same agiven FIREDHEATER unit. The FEED entry will be printed out as alabel in the output. There is no default.

PRODUCT= Identifies the product, or outlet, stream and its associated fluidproperties. Enter up to twelve alphanumeric characters. This en-try must be unique to all other product streams in the flowsheet.However, this entry can be the same as a feed stream identifierto another unit. FEED and PRODUCT cannot be the same a givenFIREDHEATER unit. The PRODUCT entry will be printed out as alabel in the output. There is no default.

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Example:STRMS FEED=CRU1,PRODUCT=CRU2

OPERATION FIRED HEATER UNIT OPERATIONS Data Category of Input

Optional statement. This statement specifies the various temperatures, pressures, and pa-rameters for the FIREDHEATER.

Optional entries:

DUTY= Specifies the FIREDHEATER duty in millions of energy units perhour. Enter a value greater than or equal to zero. You cannot en-ter DUTY and TOUT or DT on the same OPERATION statement.There is no default.

TOUT= Specifies the outlet stream temperature. This entry enables HEX-TRAN to calculate the temperature rise. The default value is thesame as the unit inlet temperature. Standard dimensional unitsare: F (English), C (metric) and K (SI). You cannot enter TOUTand DUTY or DT on the same OPERATION statement. There isno default.

DT=0.0 Specifies the temperature rise. You cannot enter DT and DUTYor TOUT on the same OPERATION statement The default is 0.0F (English), 0.0 C (metric), or 0.0 K (SI).

POUT= Specifies the outlet stream pressure. This entry enables HEX-TRAN to calculate the pressure drop. The standard dimensionalunits are: psi (English), kg/cm 2 (metric), and kPa (SI). You can-not enter POUT and DP on the same OPERATION statement. Thedefault is the value of the unit inlet pressure.

DP=0.0 Specifies the pressure drop. You cannot enter DP and POUT onthe same OPERATION statement.The defaults are 0.0 psi (Eng-lish), 0.0 kg/cm 2 (metric), and 0.0 kPa (SI).

UTILITY=OIL Specifies the UTILITY stream type. Enter OIL or GAS. This entryis used to determine the operating costs for the FIREDHEATERbased on the UTCOST statement. The default is OIL.

EFFICIENCY=100 Specifies the overall efficiency of the FIREDHEATER expressedas a percentage or fraction. Enter a value greater than zero. En-tries less than or equal to 1.0 are interpreted as fractions. En-tries greater than 1.0 are interpreted as percentages. The defaultis 100 percent.

Examples:OPERATION DUTY=17.75,DP=37.5,*

EFFICIENCY=0.81OPERATION TOUT=690,POUT=16.7,*

UTILITY=OILOPERATION DT=225.0,POUT=450.0

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COST FIRED HEATER UNIT OPERATIONS Data Category of Input

Optional statement. This statement defines the basis and cost factor data used in the general-ized costing equation to calculate the FIREDHEATER capital costs. If the COST statement is notused, then capital costs will not be calculated. There is no default utility cost for the UTILITY=HEATINGMEDIUM entry. Operating costs will only be calculated if the required entries arespecified on the UTCOST statement (SIMULATION category of input, page 4-9.

Note: The form of the generalized costing equation may be altered by entering a value of zerofor one or more of the terms. You cannot, however, enter a value of zero for the base size.

The generalized costing equation is:

EQUIPMENT COST = (CONSTANT + (LINEAR*TOTALSIZE) + ETERM) * CSTF

where:

CONSTANT =constant cost factor.

LINEAR =linear cost factor.

TOTALSIZE =total size. The basis chosen will depend on the type of equipment to be costed.

Possible bases are area, heat duty, and power. These apply to exchangers, heaters/coolers/firedheaters, or compressors/pumps, respectively.

ETERM =BCOST * BSIZE * NTS * (TOTALSIZE/NTS/BSIZE) ** EXPONENT

BSIZE =base size. The basis chosen will depend on the type of equipment to be costed.

Possible bases are area, heat duty, and power.

BCOST =the base cost defined as the cost per unit area, duty, or power.

NTS =total number of exchanger shells. This entry is set to 1.0 when costing equipmentother exchangers.

EXPONENT =exponential factor

CSTF =stream cost factor. This entry applies only to exchanger costing.

Optional entries:

BSIZE=1.0 Specifies the base duty in millions of energy units used in thegeneralized costing equation. Enter a value greater than zero.The default is 1.0 MMBtu (English), 1.0 MMkcal (metric), or 1.0MMkJ (SI).

BCOST= Specifies the base cost per million energy units for the general-ized costing equation. Units are currency units per million en-ergy units. Enter a value greater than or equal to zero. Thedefault is 0.0 USDOLLAR/MMBtu (English), 0.0 USDOL-LAR/MMkcal (metric), or 0.0 USDOLLAR/MMkJ (SI).

LINEAR= Specifies the linear cost factor in the generalized costing equa-tion. Units are currency units per million energy units. Use thiskeyword when the FIREDHEATER cost is a simple function of thepower required. Enter a value greater than or equal to zero. Thedefault is 0.0 USDOLLAR/MMBtu (English), 0.0 USDOL-LAR/MMkcal (metric), or 0.0 USDOLLAR/MMkJ (SI).

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EXPONENT=0.6 Specifies the exponential cost factor in the generalized costingequation. Enter a real value greater than or equal to zero. Thisentry has no effect unless a nonzero entry is also given forBCOST. The default is 0.6 (dimensionless).

CONSTANT=0.0 Specifies the constant cost factor used in the generalized cost-ing equation. You can use this keyword to enter fixed costs as-sociated with the installation of the FIREDHEATER (e.g.,interconnect piping and valves). Enter a value greater than orequal to zero. Valid units are currency units. This cost is not afunction of FIREDHEATER duty. The default is 0.0 USDOLLAR.

Examples:COST LINEAR=2.25, CONSTANT=10000COST BCOST=3500,BSIZE=1100,*

CONSTANT=450000,EXPONENT=0.06

General Examples:

Example 1:DIMENSION ENGLISH..FIREDHEATER UID=FIRE,NAME=CRUDEHTRSTRMS FEED=CRU1,*

PRODUCT=CRU2OPERATION UTILITY=OIL,*

EFFICIENCY=82,TOUT=650,*POUT=450

COST LINEAR=2500,*CONSTANT=16000

In this example, a furnace is used to heat crude oil to 650 degrees F at a pressure of 450 psia.The furnace is oil fired with an overall efficiency of 82 percent. The operating costs are calcu-lated using the default oil cost of 3.50 USDOLLAR/ MMBtu. The furnace capital cost is calcu-lated using a linear cost factor of 5,500 USDOLLAR/MMBtu and a constant cost factor of175,000 USDOLLAR.

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COMPRESSOR UNIT

COMPRESSOR COMPRESSOR UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement identifies the unit operation as a compressor. This state-ment must be the first statement for each compressor defined in the flowsheet.

These unit operation computes the pressure-volume energy required to modify a stream pres-sure for a gas stream.

This unit operation is adiabatic and has only one feed and one product stream. The programcalculates the power required, and using an overall efficiency value, calculates the operatingcost. In addition, capital costs for each unit operation may be calculated if desired. Operatingcosts are always calculated.

The compressor may have multiple stages, if desired. The calculations assume equal work foreach stage, and inter-cooling to the initial inlet temperature between stages.

Mandatory entry:

UID= Identifies the unit operation for reference and printout purposes.Enter up to twelve alphanumeric characters. This entry is re-quired and must be unique to all other unit operations. There isno default.

Optional entry:

NAME= Identifies the unit operation for printout purposes only. Enter upto twelve alphanumeric characters. NAME supplements the UIDentry. There is no default.

Example:COMPRESSOR UID=CMP1COMPRESSOR UID=CMP2,NAME=H2-COMPR

STREAMS COMPRESSOR UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement identifies the feed or product streams in the compressor.

Mandatory entries:

FEED= Identifies the feed, or inlet, stream and its associated fluid prop-erties. Enter up to twelve alphanumeric characters. This entrymust be unique to all other feed streams in the flowsheet. How-ever, this entry can be the same as a product stream identifierfrom another unit. FEED and PRODUCT cannot be the same for agiven compressor unit. The FEED entry will be printed out as alabel in the output. There is no default.

PRODUCT=

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Identifies the product, or outlet, stream and its associated fluidproperties. Enter up to twelve alphanumeric characters. This en-try must be unique to all other product streams in the flowsheet.However, this entry can be the same as a feed stream identifierto another unit. FEED and PRODUCT cannot be the same for agiven compressor unit. The PRODUCT entry will be printed outas a label in the output. There is no default.

Examples:STREAMS FEED=1,PRODUCT=3STREAMS FEED=LOWP,PRODUCT=HIPR

OPERATION COMPRESSOR UNIT OPERATIONS Data Category of Input

Optional statement. This statement defines the various pressures and parameters for thecompressor.

Mandatory entries:

POUT= Specifies the outlet stream pressure. This entry enablesHEXTRAN to calculate the pressure drop. The standard dimen-sional units are: psi (English), kg/cm 2 (metric), and kPa (SI).You cannot enter POUT and DP on the same OPERATION state-ment. The default is the value of the unit inlet pressure.

DP=0.0 Specifies the pressure drop. You cannot enter DP and POUT onthe same OPERATION statement. The default is 0.0 psi (Eng-lish), 0.0 kg/cm 2 (metric), or 0.0 kPa (SI).

REFSTREAM= Specifies the downstream flowsheet stream identifier applicableto the POUT specification. Enter up to twelve alphanumeric char-acters. This entry indirectly specifies the compressor outletpressure. If you specify a DP value, the only valid entry forREFSTREAM is the PRODUCT entry on the STREAMS statement.The default is the same as the product stream identifier given onthe STRMS statement.

Example:DIMENSION ENGLISHUNIT OPERATION..COMPRESSOR UID=CMP1,NAME=BOOSTER

STREAMS FEED=A10,PRODUCT=A11OPERATION POUT=500,*REFSTRM=A14

.

.FLASH UID=FLS1,NAME=DEMISTER

STREAMS FEED=A14,LIQUID=LQ14,*VAPOR=VP14OPERATION DP=0.01

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In this example, the product stream from a compressor goes through three heat exchangersand then enters a flash drum. The compressor inlet pressure is 100 psia and the desired flashdrum inlet pressure is 500 psia.

EFFICIENCY=100 Specifies the overall efficiency for both the compressor anddriver (e.g., steam turbine, electric motor) combined, expressedas a percentage or fraction. Enter a value greater than zero. En-tries less than or equal to 1.0 are interpreted as fractions. En-tries greater than 1.0 are interpreted as percentages. The defaultis 100 percent.

TSR=35.0 Specifies the “Theoretical Steam Rate” for a steam turbine, ifused. Enter a value greater than zero. You cannot use TSR ifUTILITY=ELECTRIC is specified. The default is 35.0 lbm/kwhr(English), or 15.876 kg/kwhr (metric and SI).

K=1.395 Specifies the ratio of specific heat at constant pressure dividedby the specific heat at constant volume for the vapor to be com-pressed (Cp/Cv). Enter a value greater than zero. The default is1.395.

STAGES=1 Specifies the number of stages of compression with inter-cooling of the feed back to the unit inlet temperature for eachstage. Enter a value greater than zero. For example, an entry of 2indicates 2 stages of compression with one inter-cooler. The de-fault is 1.

UTILITY=ELECTRIC Specifies the compressor drive type. Enter ELECTRIC,HPSTEAM, MPSTEAM, or LPSTEAM, corresponding to an elec-tric motor, or high, medium, or low pressure steam (turbinesonly). This entry is used to determine the operating costs for thecompressor based on the UTCOST statement The default isELECTRIC.

Examples:OPERATION POUT=175.0,EFFICIENCY=0.70OPERATION DP=500,STAGES=3,*

EFFICIENCY=90.0OPERATION DP=90.0,UTILITY=HPSTEAM,*TSR=37.5OPERATION POUT=400,EFFICIENCY=0.75,*UTILITY=ELECTRIC,K=1.43OPERATION DP=275,EFFICIENCY=83.0,*STAGES=5,UTILITY=LPSTEAMOPERATION POUT=1700,EFFICIENCY=0.86,*STAGES=9 TSR=17.5,*UTILITY=HPSTEAMOPERATION POUT=975,UTILITY=ELECTRIC,*EFFICIENCY=78.0

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COST COMPRESSOR UNIT OPERATIONS Data Category of Input

Optional statement. This statement defines the basis and cost factor data used in the general-ized costing equation (Equation 66.1) to calculate the COMPRESSOR capital costs. If the COSTstatement is not used, then capital costs will not be calculated. Operating costs are alwayscalculated.

Note: The form of the generalized costing equation may be altered by entering a value of zerofor one or more of the terms. You cannot, however, enter a value of zero for the base size.

The generalized costing equation is:

EQUIPMENT COST = (CONSTANT + (LINEAR*TOTALSIZE) + ETERM) * CSTF

where:

CONSTANT= constant cost factor.

LINEAR= linear cost factor.

TOTALSIZE = total size. The basis chosen will depend on the type of equipment to becosted.

Possible bases are area, heat duty, and power. These apply to exchangers, heaters/cool-ers/compressors, or compressors/pumps, respectively.

ETERM=BCOST * BSIZE * NTS * (TOTALSIZE/NTS/BSIZE) ** EXPONENT

BSIZE =base size. The basis chosen will depend on the type of equipment to be costed.

Possible bases are area, heat duty, and power.

BCOST=the base cost defined as the cost per unit area, duty, or power.

NTS =total number of exchanger shells. This entry is set to 1.0 when costing equipmentother exchangers.

EXPONENT =exponential factor

CSTF =stream cost factor. This entry applies only to exchanger costing.

Optional entries:

BSIZE=1.0 Specifies the base power unit size used in the generalized cost-ing equation. Enter a value greater than zero. The default is 1.0hp (English) or 1.0 kW (metric and SI).

BCOST= Specifies the base cost per power unit for the generalized cost-ing equation. Units are currency per power unit. Enter a valuegreater than or equal to zero. The default is 0.0 USDOLLAR/hp(English), or 0.0 USDOLLAR/kW (metric and SI).

LINEAR= Specifies the linear cost factor in the generalized costing equa-tion. Units are currency per power unit. Use this keyword whenthe compressor cost is a simple function of the power required.Enter a value greater than or equal to zero. The default is 0.0 US-DOLLAR/hp (English), or 0.0 USDOLLAR/kW (metric and SI).

EXPONENT=0.6 Specifies the exponential cost factor in the generalized costingequation. Enter a real value greater than or equal to zero. Thisentry has no effect unless a nonzero entry is also given forBCOST. The default is 0.6 (dimensionless).

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CONSTANT=0.0 Specifies the constant cost factor used in the generalized cost-ing equation. You can use this keyword to enter fixed costs as-sociated with the installation of the compressor (for example,knock out drums, inter-connect piping and valves). Enter a valuegreater than or equal to zero. Valid units are currency units. Thiscost is not a function of compressor duty. The default is 0.0USDOLLAR.

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PUMP UNIT

PUMP PUMP UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement identifies the unit operation as a pump. This statementmust be the first statement for each pump defined in the flowsheet.

These unit operation computes the pressure-volume energy required to modify a stream pres-sure for a liquid stream.

This unit operation is adiabatic and has only one feed and one product stream. The programcalculates the power required, and using an overall efficiency value, calculates the operatingcost. In addition, capital costs for each unit operation may be calculated if desired. Operatingcosts are always calculated.

Mandatory entry:

UID= Identifies the unit operation for reference and printout purposes.Enter up to twelve alphanumeric characters. This entry is re-quired and must be unique to all other unit operations. There isno default.

Optional entry:

NAME= Identifies the unit operation for printout purposes only. Enter upto twelve alphanumeric characters. NAME supplements the UIDentry. There is no default.

Examples:PUMP UID=PMP1PUMP UID=P012,NAME=HOT-CIRC

STREAMS PUMP UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement identifies the feed or product streams in the pump.

Mandatory entries:

FEED= Identifies the feed, or inlet, stream and its associated fluid prop-erties. Enter up to twelve alphanumeric characters. This entrymust be unique to all other feed streams in the flowsheet. How-ever, this entry can be the same as a product stream identifierfrom another unit. FEED and PRODUCT cannot be the same for agiven pump. The FEED entry will be printed out as a label in theoutput. There is no default.

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PRODUCT= Identifies the product, or outlet, stream and its associated fluidproperties. Enter up to twelve alphanumeric characters. This en-try must be unique to all other product streams in the flowsheet.However, this entry can be the same as a feed stream identifierto another unit. FEED and PRODUCT cannot be the same for agiven pump. The PRODUCT entry will be printed out as a label inthe output. There is no default.

Examples:STREAMS FEED=1,PRODUCT=2STREAMS FEED=AG01,PRODUCT=AG02

OPERATION PUMP UNIT OPERATIONS Data Category of Input

Optional statement. This statement defines the various pressures and parameters for thepump.

POUT= Specifies the outlet stream pressure. This entry enables HEX-TRAN to calculate the pressure rise. The standard dimensionalunits are: psi (English), kg/cm 2 (metric), and kPa (SI). You can-not enter POUT and DP on the same OPERATION statement. Thedefault is the value of the unit inlet pressure.

DP=0.0 Specifies the pressure rise. You cannot enter DP and POUT onthe same OPERATION statement. The default is 0.0 psi (Eng-lish), 0.0 kg/cm 2 (metric), or 0.0 kPa (SI).

REFSTREAM= Specifies the downstream flowsheet stream identifier applicableto the POUT specification. Enter up to twelve alphanumeric char-acters. This entry indirectly specifies the pump outlet pressure.If you specify a DP value, the only valid entry for REFSTREAM isthe PRODUCT entry on the STRMS statement. The default is thesame as the product stream identifier given on the STRMSstatement.

Example:DIMENSION ENGLISHUNIT OPERATION..PUMP UID=CMP1,NAME=BOOSTERSTRMS FEED=A10,PRODUCT=A11OPERATION POUT=500,*REFSTRM=A14..FLASH UID=FLS1,NAME=DEMISTER

STRMS FEED=A14,LIQUID=LQ14,*VAPOR=VP14OPERATION DP=0.01

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In this example, the product stream from a pump goes through three heat exchangers andthen enters a flash drum. The compressor inlet pressure is 100 psia and the desired flashdrum inlet pressure is 500 psia.

EFFICIENCY=100 Specifies the overall efficiency for both the pump and driver(e.g., steam turbine, electric motor) combined, expressed as apercentage or fraction. Enter a value greater than zero. Entriesless than or equal to 1.0 are interpreted as fractions. Entriesgreater than 1.0 are interpreted as percentages. The default is100 percent.

TSR=35.0 Specifies the “Theoretical Steam Rate” for a steam turbine, ifused. Enter a value greater than zero. You cannot use TSR ifUTILITY=ELECTRIC is specified. The default is 35.0 lbm/kwhr(English), or 15.876 kg/kwhr (metric and SI).

UTILITY=ELECTRIC Specifies the pump drive type. Enter ELECTRIC, HPSTEAM,MPSTEAM, or LPSTEAM, corresponding to an electric motor, orhigh, medium, or low pressure steam (turbines only). This entryis used to determine the operating costs for the pump based onthe UTCOST statement. The default is ELECTRIC.

COST PUMP UNIT OPERATIONS Data Category of Input

Optional statement. This statement defines the basis and cost factor data used in the general-ized costing equation (Equation 66.1) to calculate the PUMP capital costs. If the COST state-ment is not used, then capital costs will not be calculated. There is no default utility cost forthe UTILITY= HEATINGMEDIUM entry. Operating costs will only be calculated if the requiredentries are specified on the UTCOST statement.

Note: The form of the generalized costing equation may be altered by entering a value of zerofor one or more of the terms. You cannot, however, enter a value of zero for the base size.

The generalized costing equation is:

EQUIPMENT COST = (CONSTANT + (LINEAR*TOTALSIZE) + ETERM) * CSTF

where:

CONSTANT =c onstant cost factor.

LINEAR =l inear cost factor.

TOTALSIZE =t otal size. The basis chosen will depend on the type of equipment to becosted.

Possible bases are area, heat duty, and power. These apply to exchangers, heaters/cool-ers/compressors, or compressors/pumps, respectively.

ETERM=BCOST * BSIZE * NTS * (TOTALSIZE/NTS/BSIZE) ** EXPONENT

BSIZE =base size. The basis chosen will depend on the type of equipment to be costed.

Possible bases are area, heat duty, and power.

BCOST =the base cost defined as the cost per unit area, duty, or power.

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NTS =total number of exchanger shells. This entry is set to 1.0 when costing equipmentother exchangers.

EXPONENT =exponential factor

CSTF = stream cost factor. This entry applies only to exchanger costing.

Optional entries:

BSIZE=1.0 Specifies the base power unit size used in the generalized cost-ing equation. Enter a value greater than zero. The default is 1.0hp (English) or 1.0 kW (metric and SI).

BCOST= Specifies the base cost per power unit for the generalized cost-ing equation. Units are currency per power unit. Enter a valuegreater than or equal to zero. The default is 0.0 USDOLLAR/hp(English), or 0.0 USDOLLAR/kW (metric and SI).

LINEAR= Specifies the linear cost factor in the generalized costing equa-tion. Units are currency per power unit. Use this keyword whenthe pump cost is a simple function of the power required. Entera value greater than or equal to zero. The default is 0.0 USDOL-LAR/hp (English), or 0.0 USDOLLAR/kW (metric and SI).

EXPONENT=0.6 Specifies the exponential cost factor in the generalized costingequation. Enter a real value greater than or equal to zero. Thisentry has no effect unless a nonzero entry is also given forBCOST. The default is 0.6 (dimensionless).

CONSTANT=0.0 Specifies the constant cost factor used in the generalized cost-ing equation. You can use this keyword to enter fixed costs as-sociated with the installation of the compressor (for example,inter-connect piping and valves). Enter a value greater than orequal to zero. Valid units are currency units. This cost is not afunction of compressor duty. The default is 0.0 USDOLLAR.

General Examples:COMPRESSOR UID=CMP1,NAME=HP-100

STRMS FEED=30,PRODUCT=31OPERATION UTILITY=ELECTRIC,*EFFICIENCY=74,POUT=575,*

STAGES=6COST LINEAR=2.6,CONSTANT=19500

This example defines an electrically driven compressor with an overall efficiency of 74 percent.The outlet pressure is 575, and is achieved using six (6) stages of compression. Inter-coolingbetween stages reduces the horsepower required.

Capital costs for the compressor are calculated using a linear cost factor of 2.6 currency unitsper power unit. Fixed costs for the compressor are 19,500 currency units.PUMP UID=PO1,NAME=BOOSTER

STRMS FEED=3,PRODUCT=3AOPERATION UTILITY=LPSTREAM,*

EFFICIENCY=55,TSR=52.0,*POUT=200,REFSTREAM=3D

COST LINEAR=2.5,CONSTANT=15000

This example shows the pressure of fluid stream 3A set to the level required so that the down-stream pressure of stream 3D is 200. The pump is driven with low pressure steam and has anoverall efficiency of 55 percent. The turbine theoretical steam rate is estimated at 55 lbm/kw-hr.

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MULTI-VARIABLE CONTROLLER

MVC MVC UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement identifies the unit operation as a multivariable controller.Only one MVC unit operation is allowed in a single HEXTRAN problem. This statement must bethe first statement for an MVC defined in the flowsheet.

This chapter describes the input data required for the MULTIVARIABLE CONTROLLER (MVC)unit operation. The MVC is an expanded form of the basic feedback controller in which up to15 conditions may be specified by the simultaneous adjustment of up to 15 operating vari-ables. The MVC can be used with SIMULATION or CASESTUDY calculations only.

Specifications may be placed on stream temperatures, or individual exchanger duty, or thesum of several different exchanger duties. Variables are feed stream rates and temperatures,heat exchanger duties, and the split fractions in simple two-way splitters. The number ofspecifications must equal the number of variables.

Mandatory entry:

UID= Identifies the unit operation for reference and printout purposes.Enter up to twelve alphanumeric characters. This entry is re-quired and must be unique to all other unit operations. There isno default.

Optional entry:

NAME= Identifies the unit operation for printout purposes only. Enter upto twelve alphanumeric characters. NAME supplements the UIDentry. There is no default.

Examples:MVC UID=MVC1MVC UID=MVC2,NAME=FEED-SET

SPECIFICA-TION

MVC UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement defines the specifications for the MVC unit operation.You must enter at least one SPECIFICATION statement per MVC. Up to 15 specification state-ments may be included for a single MVC unit. You must enter an equal number of SPECIFICA-TION and VARIABLE statements for the MVC.

Optional entries:

STRM= Identifies the stream whose temperature is to be set to a givenvalue. Enter up to twelve alphanumeric characters. This entrymust be unique to all other stream indentifiers given on SPECI-FICATION statements for the MVC. There is no default.

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TEMPERATURE=.01 Defines the value of the stream temperature specification andthe absolute tolerance on the specification. Enter values for boththe specification and tolerance. The default is 01 F (English),.006 C (metric), or .006 K (SI).

UNIT= Identifies an exchanger or list of exchangers whose DUTY isspecified. Enter a single UID, or a list of UIDs, whose duties addup (sum) to the value specified on the DUTY keyword. Multipleentries must be separated by commas. There is no default.

DUTY=.005 Specifies the duty of the individual UNIT, or the multiple UNITduty sum, and the relative tolerance on the specification. Duty isspecified in millions of energy units per unit time, and toleranceis specified as an absolute fraction. Enter positive values forboth the duty specification and tolerance. The default toleranceis.005 MMBtu/hr (English), .005 MMkcal/hr (metric), or .005MMkJ/hr (SI).

Examples:SPECIFICATION STREAM=10,*

TEMPERATURE=200,0.1SPECIFICATION UNIT=STE2,*

DUTY=10.75,0.005

VARIABLE MVC UNIT OPERATIONS Data Category of Input

Mandatory statement. This statement defines the variables for the MVC unit operation. Youmust enter at least one VARIABLE statement per MVC. Up to 15 VARIABLE statements may beincluded for a single MVC unit. You must enter an equal number of VARIABLE and SPECIFICA-TION statements for the MVC.

Optional entries:

STRM= Identifies the stream whose temperature is to be set to a givenvalue. Enter up to twelve alphanumeric characters. This entrymust be unique to all other stream indentifiers given on SPECI-FICATION statements for the MVC. There is no default.

FRACTION= Indicates that the split fraction for the specified STRM in a two-way splitter is to be varied. Enter positive values for both theminimum and maximum split fraction. You can only use theFRACTION entry for splitters with two product streams. Youmust identify the splitter on the UNIT entry. There are nodefaults.

RATE= Specifies the minimum and maximum values for the designatedfeed stream flow rate in weight units per unit time. Enter positivevalues for both the minimum and maximum rates. You can onlyuse RATE for feed streams. There are no defaults.

TEMPERATURE= Specifies the minimum and maximum temperature values forthe designated feed stream. Enter values for both the minimum

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and maximum temperatures. Units are F (English), C (metric), K(SI). There are no defaults.

UNIT= Identifies a shell-and-tube exchanger, shortcut exchanger,heater, cooler, or fired heaters whose duty is to be varied, or thetwo-way splitter whose stream split fraction is to be varied. En-ter a UID. Only two-way splitters can have their stream splitfractions used as a variable. To be used as a variable, the desig-nated unit must have its duty specified initially in the input data,or be a two-way splitter. There is no default.

DUTY= Specifies the minimum and maximum duty value for the desig-nated unit. Enter positive values for both the minimum andmaximum duties. Units are MMBtu/hr (English), MMkcal/hr(metric), or MMkJ/hr (SI). There are no defaults.

Figure 4-28: MVC Example

Examples:VARIABLE STREAM=3,RATE=10000,40000VARIABLE UNIT=HX01,DUTY=10,20

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MVC Example

NapthaProduct

NapthaPumparound

ATM-BTMS

Crude1

19

20

40

39

2242

21

2

8

3

4

9

7

11 13

36

14

1210

41

5

HE-01

HE-0221 MMBTU/Hr

HE-04HE-05

350 F

HE-06

SP-02SP-01

HE-03 MX-01

MX-02

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PARAMETER MVC UNIT OPERATIONS Data Category of Input

Optional statement. This statement specifies the control options for the MVC unit.

Optional entries:

ITER= Specifies the maximum number of MVC iterations that will be at-tempted in order to solve a problem. The default is the numberof controller variables, multiplied by five, or10, whichever islarger.

SUMSQ= Defines the minimum target sum of squares error for the MVCcalculations. At each iteration, a function is generated which isthe sum of the squares of the differences between the calculatedand specified temperature values, plus the sum of the squares ofthe relative differences in the duty specifications. Each term inthe summation is multiplied by the ratio of the default to thegiven tolerance for that particular specification.

Giving a tolerance on a specification that is lower than the de-fault has the effect of weighting the error on that specificationrelative to those specifications that are using default tolerances.Convergence is achieved when this weighted function value isreduced below the SUMSQ value. If no entry is made, SUMSQdefaults to the sum of the squares of the default tolerances oneach specification.

NOPRINT Suppresses intermediate printout from the controller. The finalsolution will always be printed. The use of this keyword is notrecommended when first attempting a run with the MVC. Theextra information generated during the solution will be useful inthe event that satisfactory convergence is not achieved.

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Chapter 5Technical ReferenceGeneral Information

HEXTRAN contains a number of rigorous heat exchanger models:

■ Shell-and-tube heat exchangers of all types, including Kettle reboilersand condensers.

■ Double-pipe heat exchangers.

■ Multi-tube heat exchangers.

■ Ai-rcoolers.

■ Finned-tube exchangers.

■ Heat exchangers with rod baffle design.

■ Plate-and-frame heat exchangers.

For all heat exchanger models, the following basic design equation holds:

(1)δ δ� �� � �= ∆

where:

q = heat transferred in elemental length of exchanger dz

Uo = overall heat transfer coefficient

T = overall bulk temperature difference between the twostreams

A = element of surface area in exchanger length dz

Once an appropriate mean heat-transfer coefficient, and temperaturedifference is defined, equation (1) may be rewritten for the entire exchangeras follows:

(2)� � � � � ��� � � ��� ��= = −∆

where:

Q = total exchanger heat duty

Uom = overall mean heat-transfer coefficient

Ao = total exchanger area

Tm = mean temperature difference

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Figure 5-1: Countercurrent and Cocurrent Flows

For countercurrent or cocurrent flows as shown in Figure 6-1, theappropriate expression for the mean temperature difference is thelogarithmic mean, i.e.:

For countercurrent flows,

(3)( ) ( )∆� ����

� � � �

� �

� �

��

�� ��� ��� ��

�� ���

���

= =− − −

−−

� � � �

� �

���

��

For cocurrent flows,

(4)( ) ( )∆� ����

� � � �

� �

� �

��

�� �� ��� ���

�� ��

��� �

= =− − −

−−

� � � �

� �

���

��

where:

Tlm = LMTD = logarithmic mean temperature difference

superscript 1 denotes one side of the heat exchanger

superscript 2 denotes the other side of the heat exchanger

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In actual fact, the flows are not generally ideally countercurrent orcocurrent. The flow patterns are usually mixed as a result of flow reversals(e.g., in exchangers with more than one tube or shell pass), bypassedstreams, or streams which are not well mixed. F-factors have been derivedby Bowman et al. to account for these non-ideal flow patterns and are usedto correct equations (3) and (4). For multipass heat exchangers, where theratio of shell passes to tube passes given is not 1:2 (e.g., for a 2 shell- and 6tubepass exchanger), the F-factors actually used are those computed forexchangers with the ratio of one shell to two tubepasses (i.e., for 2 shell-and 4 tubepasses).

PipesHEXTRAN contains calculations for single liquid or gas phase or mixedphase pressure drops in pipes. The PIPE unit operation uses transportproperties such as vapor and/or liquid densities for single-phase flow, andsurface tension for vapor-liquid flow. The transport property data neededfor these calculations are obtained from a number of transport calculationmethods available in HEXTRAN. These include the PURE and PETROmethods for viscosities. Table 5-1 shows the thermodynamic methodswhich may be used to generate viscosity and surface tension data.

Table 5-1: Thermodynamic Generators for Viscosity andSurface Tension

Viscosity Surface Tension

PURE (V & L) PURE

PETRO (V & L) PETRO

TRAPP (V & L)

API (L)

SIMSCI (L)

KVIS (L)

Basic CalculationsAn energy balance taken around a steady-state single-phase fluid flowsystem results in a pressure drop equation of the form:

� � � � � � � �� �� � �� � �� � ��� � �= + +�

(5)

total friction elevation acceleration

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The pressure drop consists of a sum of three terms:

■ the reversible conversion of pressure energy into a change in elevationof the fluid,

■ the reversible conversion of pressure energy into a change in fluidacceleration, and

■ the irreversible conversion of pressure energy into friction loss.

The individual pressure terms are given by:

(6)� � � �� �� � � �� = ρ � �

(7)� � � ��� ��� �� � = ρ φ

(8)� � � � �� �� � � �� =ρ ν

where:

l and g refer to the liquid and gas phases

P = the pressure in the pipe

L = the total length of the pipe

d = the diameter of the pipe

f = friction factor

ρ = fluid density

v = fluid velocity

gc = acceleration due to standard earth gravity

g = acceleration due to gravity

φ = angle of inclination

(dP/dL)t = total pressure gradient

(dP/dL)f = friction pressure gradient

(dP/dL)e = elevation pressure gradient

(dP/dL)acc = acceleration pressure gradient

For two-phase flow, the density, velocity, and friction factor are oftendifferent in each phase. If the gas and liquid phases move at the samevelocity, then the "no slip" condition applies. Generally, however, theno-slip condition will not hold, and the mixture velocity, vm, is computedfrom the sum of the phase superficial velocities:

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(9)� � �� �� �= +

where:

vsl = superficial liquid velocity = volumetric liquid flowrate/cross sectional area of pipe

vgl = superficial gas velocity = volumetric gas flowrate/crosssectional area of pipe

Equations (6), (7), and (8) are therefore rewritten to account for these phaseproperty differences:

(10)� � � �� �� � � �� �� �� �� = ρ � �

(11)� � � ��� �� �� � �� = ρ φ

(12)� � � � � � �� �� � �� �� �� �� ��=ρ

where:

ρtp = fluid density = ρlHL+ρgHg

HL,Hg = liquid and gas holdup terms subsript tp refers to the twophases

Pressure Drop Correlations

Beggs-Brill-Moody (BBM)

For the pressure drop elevation term, the friction factor, f, is computed fromthe relationship:

(13)� � � � �� �� �� � �� �= =

The exponent s is given by:

(14)� � � � �= − + − +� � � � � � ��� �� ���� ���� ���� �� �

(15)� � �� �= − < <��� � � �� ��� �� � ��

(16)� �� �= ��� � �λ �

where:

fn = friction factor obtained from the moody diagram for asmooth pipe

λL = no-slip liquid holdup = vsl/(vsl + vsg)

vsl = superficial liquid velocity

vsg = superficial gas velocity

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The liquid holdup term, HL, is computed using the following correlations:

(17)� � ��

��

�= � � �λ Λ

(18)HL = HL0, when = 0

HL = HL0 , when

( ){ }Ψ = + − −� � �� ���� ���� � �� ���� � � � ��� � � �λ λ φ φ� �

��

��

� � �

where:

NFr = Froude number

NLV = liquid vwlocity number

a, b, c, d, e, f, g = constants

The BBM method calculates the elevation and acceleration pressure dropterms using the relationship given in equations (7) and (8) (or equations(11) amd (12) for two-phase flow).

Rigorous Heat ExchangerHEXTRAN contains a shell-and-tube heat exchanger module which willrigorously rate most standard heat exchangers defined by the TubularExchanger Manufacturers Association (TEMA). Shell-and-tubeside heattransfer coefficients, pressure drops, and fouling factors are calculated. TheTEMA types available in HEXTRAN are given in Figure 5-4.

Heat Transfer Correlations

Shellside

The Bell-Delaware method is used to compute the heat transfer coefficienton the shellside for single-phase conditions. The method accounts for theeffect of leakage streams in the shellside. The shellside heat transfercoefficient is given by:

(19)� � � � � � ����� � � � �=

where:

h = average shellside heat transfer coefficient

hideal = shellside heat transfer coefficient for an ideal tube bank

Jc = correction factor for baffle cut and spacing

Jl = correction factor for baffle-leakage effects

Jb = correction factor for bundle bypass flow effects

Js = correction factor for inlet and outlet baffle spacing

Jr = correction factor for adverse temperature-gradient build-up

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The correction factor, Jc, is a function of the fraction of the total tubes inthe crossflow; Jl is a function of the tube-to-baffle leakage area, and theshell-to-baffle leakage area; Jb is a function of the fraction of crossflowarea available for bypass flow and the Reynolds number; Js is a function ofthe baffle spacing; Jr is a function of the number of baffles. The Bellmethod is used to compute these correction factors.

The heat transfer coefficient for an ideal tube bank, hideal, is obtained fromthe following relationships:

(20)

( )�

� �

� ��� ���

� ��

��� ��

� �

=+ −−

����

� ���� �

� �

� � � �

(21)� � ��� �� ��� ��� �

��= ���� � � �

(22)( )� � ��� ���� �� �� �� ���� � � � � �

�= + +�� � � �

(23)�

� �

�����

�� ����= � �

where:

NReG = Reynolds number as defined by Gnielinski =��

� �� � � �

ε µ

NPr = Prandlt number =�

�µ

W = total mass flow rate in shellside

c = specific heat of fluid

εF = shell void fraction

Ds = shell inside diameter

lb = baffle spacing

µb = fluid viscosity at bulk temperature

NNu = Nusselt number

k = thermal conductivity of shellside fluid

L = effective length of shell

subscripts tur, and lam refer to the turbulent and laminar flowregimes, and bund refers to the tube bundle.

Alternatively, the user may supply the shellside heat transfer coefficient directly.

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Tubeside

For turbulent flow in circular tubes, the tubeside heat transfer coefficient isobtained from the Sieder-Tate equation:

(24)�

��

�� ��� ��

= =

���� � � � �

� ��

��

µµ

where:µw = fluid viscosity at the wall temperature

The above relationship holds for the following flow regimes:

��

���

>< <

>

�����

�� ���

��

where:

NNu = Nusselt number

NRe = Reynolds number =��

�� �µ

NPr = Prandlt number

L = tube length

D = effective tube diameter

W = total mass flow rate in tubeside

At = cross sectional tube area

For laminar flow regimes, NRe < 2000, a different relationship is used forthe heat transfer coefficient, depending on the value of the Graetz number.The Graetz number, NGz, is defined as:

(25)� � �

��� ��=

For NGz < 100, a relationship first developed by Hausen is used:

(26)�

���

��

��

= ++

���

���

� ����� �

� ��

��

µµ

For NGz > 100, the Sieder-Tate relationship is used:

(27)� ��� ��

�=

���

� �

� ��

µµ

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For transition flow regimes where 2000 < NRe < 10000, the tubeside filmcoefficient is obtained by interpolation between those values calculated forthe laminar and turbulent flow regimes:

(28)�

� � ������

���� ��

��=− −

+� � � �

�����

����

where:

htrans = heat transfer film coefficient for the transition regime

hturb = heat transfer film coefficient for the turbulent flow regime

hlam = heat transfer film coefficient for the laminar flow regime

The user may also supply the film coefficients directly.

Pressure Drop Correlations

Shellside

The shellside pressure drop may be determined by one of two methods; theBell-Delaware method, or the stream analysis method (default). TheBell-Delaware method uses the following procedure.

First, the pressure drop for an ideal window section is calculated using thefollowing correlations:

For NRe < 100,

(29)∆

� �

��

� �

=′ −

+

+

��� �

�µρ� � �� � �� � � �� ρ

For NRe > 100,

(30)∆� �

� ���

� �

=+� � ��

� � �

ρ

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The pressure drop for an ideal crossflow section is then calculated:

(31)∆

� � �

���

=

� ��

ρµµ

where:

fk = the friction factor for the ideal tube bank calculated at theshellside Reynolds number

gc = gravitational force conversion factor = 4.18 x 108

lbm-ft/lbf-hr

Nc = number of tubes in one crossflow section

Ncw = number of crossflow rows in each window

Sm = minimum cross sectional area between rows of tubes forflow normal to tube direction

Sw = cross sectional area of flow through window

Do = outside exchanger diameter

Dw = equivalent diameter of a window

p = tube pitch, center-to-center spacing of tubes in tube bundle

ρ = fluid density

The actual shellside pressure drop is obtained by accounting for the effectsof bypasses and leakages, and is given by:

(14)[ ]∆ ∆ ∆ ∆ � � � � � ��

�� � �� � � �� � �� � �

= − + + +

� �� � �

where:

∆Ps = actual shellside pressure drop

Nb = number of segmental baffles

Rb = bundle bypass flow correction factor

Rl = baffle leakage effects correction factor

Rs = correction factor for unequal baffle spacing effects

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The stream analysis method, as presented in 1984 by Willis and Johnson, is aniterative, analytical method. At each iteration the crossflow resistance, Rc, thewindow flow resistance, Rw, the tube to baffle resistance, Rt-b, the shell tobaffle resistance, Rs-b, the leakage resistance, Rl, the flowrate through thewindowed area, Ww, the crossflow pressure drop, ∆Pc, the window pressuredrop, ∆Pw, and the crossflow fraction, Fc are calculated as follows:

(33)� �������� � �� � ��� ������ � = � � � � �ρ

(34)

��

=

��

��� �

� �

� ��

ρ

(35)� ���� �� � �� ����� ����!���� �� � �� ����� ��� �− = − − − −� � ��� � �!��� � �ρ µ

(36)� ���� ����� �� ����� ����!���� ����� �� ������ �− = − − − −� � ����� � �!��� � �ρ µ

(37)( )� ���� � �� � � � �= − −�

(38)��

� �

=

++

� �

(39)∆ � � �= �

(40)∆ � �� � �= �

(41)"

=� � �∆ �

where:Sc = crossflow area

Dc = crossflow equivalent diameter

Iterations are stopped once the value of Fc meets the following criterion:

(42)� ��

� �

" "

"

���� ����

����

<−�

���

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The shellside end space pressure drops at the inlet and outlet of theexchanger, ∆Ps,in, and ∆Ps,out, and the actual shellside pressure drop, ∆Pss,are then calculated using the equations:

(43)∆ � �� �� � �� ��� �= �

(44)� �������� � � � �� �� � � �� � � � � � �= ρ

(45)∆ � �� ��� � ��� ���� �= �

(46)� �������� � � � �� �� � �� � � � � � �=�

ρ

(47)∆∆ ∆ ∆ ∆

��

� �� � � � ���

=+ − + +� �� � � ��

where:

∆Ps,in = mean shellside end space pressure drop at exchanger inlet

∆Ps,out = mean shellside end space pressure drop at exchanger outlet

Rs,in = end space resistance at exchanger inlet

Rs,out = end space resistance at exchanger outlet

= denotes an average

Tubeside

The tubeside pressure drop, ∆Pts, is calculated as the sum of the pressuredrops in the tubes plus the pressure drops in the return bends:

(48)∆"# ��

$ � ��

� �

=�

� � ��� µ

(49)∆�#

$ ��

=�

���� ��

� �� � �

(50)∆ ∆ ∆ �� � �= +

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where:

∆Pt = pressure drop in tubes

∆Pr = pressure drop in return tubes

∆Pts = total pressure drop in the tubeside

µc = fluid viscosity factor

F = friction factor

Gt = mass flux

L = tube length

n = number of tube passes

Di = tube inner diameter

Sp = specific gravity of fluid

The friction factor, F, and viscosity factor, µc are computed using differentcorrelations for each flow regime:

For turbulent flows, NRe > 2800,

(51)µ

µµ

�=

� ���

(52)��� � ��� ���� ��

����� � ���" �= − −

For laminar flows, NRe < 2100,

(53)µ

µµ

�=

� ��

(54)��� � ��� ���� ��

��� � ��� ��" �= − −

For transition flow regimes, 2100 < NRe < 2800, F and µc are obtained byinterpolation between the laminar and turbulent values:

(55)µµ µ

µ

��� ��

��

�=

− −+

� � �� � � �

����

���

(56)"

" " �"��� ��

��=− −

+� � � �

�����

���

Fouling FactorsIn most exchanger applications, the resistance to heat transfer increaseswith use as a result of scaling caused by crystallization or deposition of finematerial. These factors may or may not increase the pressure drop in theexchanger. For both the tubeside and shellside, the user may input separate

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factors to account for thermal and pressure drop resistances due toexchanger fouling.

Thermal fouling resistances cannot be calculated analytically. Tables forthermal heat transfer coefficients (the inverse of thermal resistances) for anumber of common industrial applications may be obtained from standardreferences on heat exchangers such as Perry’s handbook, or the book by Kern.

HEXTRAN also allows the user to account for the effect of fouling onpressure drop by inputting a thickness of fouling layer.

References1. Perry, R. H., and Chilton, C. H., 1984, Chemical Engineers Handbook,

6th Ed.2. Kern, 1950, Process Heat Transfer, McGraw-Hill, N.Y.3. Gnielinski, V., 1979, Int. Chem. Eng., 19(3), 380-400.4. Willis, M. J. N., and Johnston, D., 1984, A New and Accurate Hand

Calculation Method for Shellside Pressure Drop and Flow Distribution,paper presented at the 22nd Heat Transfer Conference, Niagara Falls,N.Y.

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IndexAACE

design process 4-243plan views 4-242specifications 3-18statement 4-159

ACE2ACE 4-255FTE 4-241

Acentric factor 4-26ACOOLING, PLOT keyword 4-136ADD

building an input file 3-25OUTDIMENSION statement 4-17

ADEW 4-70AEFACTOR 4-261AHEATING, PLOT keyword 4-136AIRSIDE statement, ACE 4-249ALL

PLOT statement 4-144PRINT statement 4-17, 4-79, 4-86, 4-94,

4-107, 4-116, 4-126, 4-137ALPHA, PARAMETER statement 4-135ANNUAL, PLOT keyword 4-136Annualized network costing equation 4-139Annular nozzle design 4-189APC, PLATE, PHE 4-262API

petroleum stream 4-56statement, component data 4-26statement, stream data 4-50

APROCESSPLOT keyword 4-136SPEC statement 4-134

Aqueous dewpoint 4-70AREA

ACE 4-244ACE TYPE 4-244DIMENSION statement 4-10DPE 4-207FINS

ACE 4-248DPE 4-210FTE 4-235MTE 4-222STE 4-174

FTE 4-231FTE TYPE 4-231

HX 4-295HX TYPE 4-295LIMITS statement 4-77, 4-84, 4-92,

4-104, 4-124MTE 4-218OUTDIMENSION statement 4-15PARAMETER statement 4-130PHE 4-257PHE TYPE 4-257PLATE, PHE 4-261RBE 4-196SNOZZLE

RBE 4-202STE 4-188

STE 4-167STE TYPE 4-168

ARRANGEMENTS statement, PHE 4-264Assay

curve 3-6data

API gravity 4-26characterization 4-24cutpoints 4-26molecular weight 4-24specific gravity 4-24

stream 4-44Asterisk character 4-5ATOTAL, PLOT keyword 4-136AUTILITIES, PLOT keyword 4-136AVERAGE

API statement 4-50MW statement 4-51SPGR statement 4-50WATSONK statement 4-51

Average property valueassay stream 4-45petroleum stream 4-56pure component stream 4-42supplying 4-63

BBaffle

building an input file 3-28cut

definitions 4-184NFAR equivalents 4-185

segmental types 4-182spacing 4-186statement

RBE 4-201

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STE 4-181thickness values 4-187

BANK, LIBID statement 4-23Base area

See BSIZEBase cost

See BCOSTBCOST

ACE 4-254compressor 4-316cooler 4-308DPE 4-215fired heater 4-311FTE 4-240heater 4-304HX 4-299HXCOST statement

flowsheet calculation 4-81, 4-88, 4-96,4-109, 4-118, 4-128

synthesis calculation 4-145targeting calculation 4-138

MTE 4-227PHE 4-270pump 4-321RBE 4-204STE 4-161, 4-193utility stream 4-60

Beggs-Brill-Moody method 4-276BETA, PLATE, PHE 4-261Binary interaction parameters, user-supplied 4-30BLEND

assay stream 4-44changes to 1-4

BONDACE 4-249FTE 4-235

BRINE, DESALTER STRMS 4-286BSIZE

ACE 4-254compressor 4-316cooler 4-308DPE 4-215fired heater 4-311FTE 4-240heater 4-304HX 4-299HXCOST statement

flowsheet calculation 4-81, 4-88, 4-96,4-109, 4-118, 4-128

synthesis calculation 4-145targeting calculation 4-138

MTE 4-227PHE 4-270

pump 4-321RBE 4-204STE 4-161, 4-193utility stream 4-60

Bubbleexternal property data types 4-70point 4-70

Building an input filecalculation type section 3-27component data section 3-26general data category 3-25internal property data section 3-27stream data section 3-26thermodynamic data section 3-26unit operations data section 3-28

Bundle orientation, STE 4-167BWG

ACE 4-245DPE 4-208FTE 4-232MTE 4-219RBE 4-197STE 4-171

BWRS statement 4-36

CC1-C10, PLOT statement 4-145Calculation

building an input filestatement 3-25type section 3-27

methodsthermodynamic property 4-34transport properties 4-35

optionswater property 4-36water solubility 4-36

statementACE 4-253DPE 4-213flowsheet calculation 4-78, 4-85, 4-93,

4-106, 4-115, 4-125FTE 4-239general data section 4-19HX 4-298MTE 4-224PHE 4-267RBE 4-202STE 4-191

CASE statement, flowsheet calculation 4-82CASES, PRINT statement 4-137Categories of input

component data 4-21external property data 4-67

Index HEXTRAN Input ManualI-2 June 2002

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flowsheet calculation 4-75general data 4-7internal property data 4-64stream data 4-38synthesis 4-141thermodynamic data 4-30unit operations 4-148

CCOOLING, PLOT keyword 4-136CFRACTION, external property data types 4-70Characterization methods 4-25CHARACTERIZE, ASSAY statement 4-24CHEATING, PLOT keyword 4-136Chevron angle, definition 4-263CHNUMBER

FPLATE 4-265JPLATE 4-266

Cleaning casestudycalculation 3-11overview 4-101PROPERTY statement 4-76, 4-91, 4-104,

4-113, 4-123CLEARANCE

BAFFLE, RBE 4-201SNOZZLE

RBE 4-202STE 4-189

CNOZZLE statement, PHE 4-267COCI

ACE 4-253DPE 4-214FTE 4-239MTE 4-225PHE 4-268RBE 4-203STE 4-192

Cocurrent flows 5-2COLD

DPE 4-214FTE 4-238MTE 4-225PHE 4-268PLOT statement 4-144RBE 4-203STE 4-192

COLDSIDE statement, PHE 4-259Comments 4-3Compatibility with prior versions 1-3Component data

building an input file 3-26category of input 4-21

Componentsfixed properties 4-26

library 4-23non-library 4-22petroleum pseudocomponents 4-24solid 4-22synthetic fuel 4-22temperature-dependent properties 4-27

COMPOSITE, PRINT statement 4-137COMPOSITION

LIGHTENDS statement 4-52pure component stream 4-41

CompressorCOST statement 4-316OPERATION statement 4-314specifications 3-21statement 4-313STREAMS statement 4-313

CONDUCTIVITYDIMENSION statement 4-10FINS

ACE 4-248DPE 4-210FTE 4-235MTE 4-221

METHOD statement 4-33OUTDIMENSION statement 4-15PLATE, PHE 4-262statement 4-28TUBESIDE

ACE 4-246DPE 4-209FTE 4-233MTE 4-220RBE 4-198STE 4-173

CONSTFPLATE 4-265JPLATE 4-266

CONSTANTACE 4-254compressor 4-317cooler 4-308DPE 4-216fired heater 4-312FTE 4-240heater 4-304HX 4-299HXCOST statement

flowsheet calculation 4-81, 4-89, 4-97,4-109, 4-118, 4-128

synthesis calculation 4-146targeting calculation 4-138

MTE 4-227PHE 4-270

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pump 4-321RBE 4-204STE 4-161, 4-193utility stream 4-60

CONSTRAINT statement 4-82, 4-119, 4-129Continuing a statement 4-5CONVERSION, ASSAY statement 4-24COOLER statement 4-305Cooling utility duty 4-133CORRELATION 4-28COST statement

ACE 4-254compressor 4-316cooler 4-307DPE 4-215fired heater 4-311FTE 4-240heater 4-303HX 4-299MTE 4-227PHE 4-270pump 4-320RBE 4-204STE 4-193utility stream 4-60

Countercurrent flows 5-2CP statement 4-28CPASS, ARRANGEMENTS, PHE 4-264CPROCESS, PLOT keyword 4-136CRACKING, D86 statement 4-46Critical

compressibility 4-26pressure 4-27temperature 4-27volume 4-27

CSCALERexternal property data types 4-70network synthesis 4-62synthesis calculation 4-147

CST3, STE 4-190CTOTAL, PLOT keyword 4-136CURRENCY, ECONOMICS statement

flowsheet calcuation 4-80, 4-87, 4-95,4-108, 4-117, 4-127

synthesis calculation 4-146targeting calculation 4-139

Curve fitting procedure 4-24Cut

dual design limits 4-185STE BAFFLE 4-182

CUTILITIES, PLOT keyword 4-136CUTPOINTS statement 4-26

DD1160 statement 4-47D2887 statement 4-48D86 statement 4-46DATA

API 4-50D1160 4-48D2887 4-48D86 4-46MW 4-51SPGR 4-50statement

component data section 4-29external property data 4-68

TBP 4-47WATSONK 4-51

Databank order 4-23DATE

building an input file 3-25entry 4-8

DAYS, ECONOMICS statementflowsheet calculation 4-80, 4-87, 4-95,

4-108, 4-117, 4-127synthesis calculation 4-146targeting calculation 4-139

DECANT, WATER statement 4-35Decanter

specifications 3-20statement 4-288

DefaultMETHOD statement 4-33values 4-3

DELTA, PARAMETER statement 4-135DEMAT, network synthesis 4-63Density

DIMENSION statement 4-10liquid 4-22METHOD statement 4-32OUTDIMENSION statement 4-15SHELLSIDE

DPE 4-211MTE 4-223RBE 4-200STE 4-179

standard 4-27statement, component data section 4-28TUBESIDE

DPE 4-209MTE 4-220RBE 4-198STE 4-173

Desalter

Index HEXTRAN Input ManualI-4 June 2002

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specifications 3-20statement 4-285

DESCRIPTION statementbuilding an input file 3-25general data section 4-9

Descriptive text, general data section 4-7DEWP, external property data types 4-70Dewpoint 4-70DHRAT, network synthesis 4-62DIAMETER, ACE FAN 4-251DIMENSION

buildiing an input file 3-25statement 4-9

Dimensional unitsallowable 4-13external property data 4-72standard 4-12

Dimensions, radial low-fin tubes 4-176Dipole moment 4-22Distillation data, stream data section 4-46DP

compressor 4-314cooler 4-307decanter 4-290desalter 4-286fired heater 4-310flash drum 4-292heater 4-302PGEN statement 4-65pipe 4-281pump 4-319valve 4-284

DPEillustration 4-206specifications 3-16statement 4-159

DPFRAMECOLDSIDE 4-259HOTSIDE 4-258

DPORT, PACK, PHE 4-260DPSCALER

AIRSIDE, ACE 4-250COLDSIDE, PHE 4-260DUCTSIDE, FTE 4-237HOTSIDE, PHE 4-258SHELLSIDE

DPE 4-212MTE 4-223RBE 4-200STE 4-180

TUBESIDEACE 4-247DPE 4-210

FTE 4-234MTE 4-221RBE 4-199STE 4-174

DPSHELLSHELLSIDE

DPE 4-212HX 4-297MTE 4-223RBE 4-200STE 4-180

TUBESIDEACE 4-247DPE 4-210FTE 4-234HX 4-296MTE 4-221RBE 4-199STE 4-173

DPSMAX, CONSTRAINT statement 4-120DPSMETHOD

MTE CALCULATION 4-224STE CALCULATION 4-191

DPTMAX, CONSTRAINT statement 4-120DPUNIT

AIRSIDE, ACE 4-250DUCTSIDE, FTE 4-237SHELLSIDE

DPE 4-212HX 4-297MTE 4-223RBE 4-200STE 4-180

TUBESIDEACE 4-247DPE 4-210FTE 4-234HX 4-296MTE 4-221RBE 4-199STE 4-173

DRAFT, FAN, ACE 4-251DT

cooler 4-306decanter 4-289desalter 4-286fired heater 4-310heater 4-302PGEN statement 4-65

DTUTILITY, cooler 4-306Dual design limits 4-169DUCT, FTE SPECIFICATION 4-238DUCTSIDE statement, FTE 4-236

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DUTYACE 4-253cooler 4-306DPE 4-214external property data types 4-70fired heater 4-310flowsheet calculation

specification 4-97variable 4-100

FTE 4-239heater 4-302HX 4-298MTE 4-225MVC

specification 4-323variable 4-324

PHE 4-268PRINT statement 4-137RBE 4-203STE 4-192utility stream 4-61

EECONOMICS

building an input file 3-27PRINT statement 4-79, 4-86, 4-94,

4-107, 4-116, 4-126statement

flowsheet calculation 4-80, 4-87, 4-95,4-108, 4-117, 4-127

synthesis calculation 4-146targeting calculation 4-139

Effective length of a U-tube bundle 4-171EFFICIENCY

compressor 4-315FAN, ACE 4-251FINS

ACE 4-248DPE 4-211FTE 4-235MTE 4-222STE 4-174

fired heater 4-310pump 4-320

ELECTRICITY, UTCOST statement 4-80, 4-88,4-96, 4-108, 4-117, 4-128

ELEVATION, PIPE LINE 4-279EMAT. SPEC statement 4-143End point temperatures 4-25ENERGY

DIMENSION statement 4-10OUTDIMENSION statement 4-15

ENGLISHDIMENSION statement 4-9

OUTDIMENSION statement 4-15ENTHALPY

external property data types 4-70METHOD statement 4-32statement 4-28

EQLENGTHPIPE FITTINGS 4-280PIPE LINE 4-278

Equation of stateBWRS 4-36LKP 4-36Peng-Robinson 4-36Soave-Redlich-Kwong 4-36

Exchanger Minimum Approach TemperatureSee EMAT

EXCHANGERATE, ECONOMICS statementflowsheet calculation 4-80, 4-87, 4-95,

4-108, 4-117, 4-127synthesis calculation 4-146targeting calculation 4-139

EXPFAC 4-29EXPON

FPLATE 4-265JPLATE 4-266

EXPONENTACE 4-254compressor 4-316cooler 4-308DPE 4-215fired heater 4-312FTE 4-240heater 4-304HX 4-299HXCOST statement

flowsheet calculation 4-81, 4-89, 4-97,4-109, 4-118, 4-129

synthesis calculation 4-145targeting calculation 4-138

MTE 4-227PARAMETER statement 4-135PHE 4-270pump 4-321RBE 4-204STE 4-161, 4-193utility stream 4-60

Exponential area efficiency factor 4-135EXTENDED, PRINT

ACE 4-254DPE 4-215FTE 4-240MTE 4-226PHE 4-269RBE 4-204

Index HEXTRAN Input ManualI-6 June 2002

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Page 390: Hextran Keyword v9

statement 4-79, 4-87, 4-95, 4-107, 4-116,4-127STE 4-193

External property dataadditional units 4-73category of input 4-67default dimensions 4-72types 4-70, 4-74

FFAN statement, ACE 4-251FCDIR, PACK, PHE 4-261FCFLUID, PACK, PHE 4-261Feed

AIRSIDE, ACE 4-249COLDSIDE, PHE 4-259COMPRESSOR STRMS 4-313COOLER STRMS 4-305DECANTER STRMS 4-288DESALTER STRMS 4-285DUCTSIDE, FTE 4-236FIREDHEATER STRMS 4-309FLASH STRMS 4-291HEATER STRMS 4-301HOTSIDE, PHE 4-258MIXER STRMS 4-271PIPE STRMS 4-277PUMP STRMS 4-318SHELLSIDE

DPE 4-211HX 4-297MTE 4-222RBE 4-199STE 4-177

SPLITTER STRMS 4-273stream flow rate 4-99TUBESIDE

ACE 4-245DPE 4-208FTE 4-232HX 4-296MTE 4-219RBE 4-197STE 4-170

VALVE STRMS 4-283FFACTOR

FPLATE 4-265JPLATE 4-266

Filecompatibility 1-3input, building 3-22statement, external property data 4-71

FILL, LIBID statement 4-23FILM

coefficient 4-60DIMENSION statement 4-10external property data types 4-70OUTDIMENSION statement 4-15PARAMETER statement 4-134, 4-143utility stream 4-60

FINS statementACE 4-248DPE 4-210FTE 4-235MTE 4-221STE 4-174

Fired heaterspecifications 3-21statement 4-309

FIT, ASSAY statement 4-24FITTINGS statement, PIPE 4-280Flash drum

specifications 3-20statement 4-291

FLOWACE 4-244DPE 4-207FTE 4-231HX 4-295MTE 4-218PHE 4-257RBE 4-196STE 4-167

Flowsheetcalculations, category of input 4-75iterations 4-78, 4-85, 4-93, 4-105,

4-114, 4-125Fluid temperature distribution 4-169FLUSH

assay stream 4-45pure component stream 4-42

FOULAIRSIDE, ACE 4-249COLDSIDE, PHE 4-259DUCTSIDE, FTE 4-236HOTSIDE, PHE 4-258SHELLSIDE

DPE 4-212MTE 4-223RBE 4-200STE 4-180

TUBESIDEACE 4-247DPE 4-209FTE 4-233MTE 4-220RBE 4-198

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STE 4-173FPLATE statement, PHE 4-265FRACTION

LIGHTEND 4-52MVC 4-323PARAMETER 4-120PRINT 4-18SPLITTER 4-274VARIABLE 4-99, 4-119

FRAME, COST, PHE 4-270FRICTION

PIPE FITTINGS 4-281PIPE LINE 4-279

FT1, LIMITS statement 4-147FTE

design process 4-228specifications 3-17statement 4-159

FugacityPHI keyword 4-33vapor 4-31

GGAS, UTCOST statement 4-80, 4-87, 4-96,

4-108, 4-117, 4-127Gasket

material codes 4-264PHE PLATE 4-262

General databuilding an input file 3-25category of input 4-7

GENERAL, PRINT statement 4-17Geometry consistency checks 4-78, 4-85, 4-93,

4-106, 4-115, 4-125Global settings 3-1GPSA, WATER statement 4-35GRAND, PRINT statement 4-137Gravity

ASSAY statement 4-24methods 4-25stream data 4-50

HHCOLD, COLDSIDE, PHE 4-259Heat exchangers 5-6Heat Recovery Approach Temperature

See HRATHEATER statement 4-301Heating utility duty 4-133HEATINGMEDIUM, UTCOST statement 4-81,

4-88, 4-96, 4-109, 4-118, 4-128HEIGHT, FINS

ACE 4-248DPE 4-210

FTE 4-235MTE 4-221STE 4-174

HENRY, METHOD statement 4-33Henry’s Law 4-31HHOT, HOTSIDE, PHE 4-258HI

ACE 4-247DPE 4-209FTE 4-233MTE 4-220RBE 4-198STE 4-173

HICOACE 4-253DPE 4-214FTE 4-239MTE 4-225PHE 4-268RBE 4-203STE 4-192

High pressure steam cost 4-81, 4-88, 4-96,4-108, 4-117, 4-128

HIHOACE 4-253DPE 4-214FTE 4-239MTE 4-225PHE 4-268RBE 4-203STE 4-192

HNOZZLE statement, PHE 4-267HO

AIRSIDE, ACE 4-250DUCTSIDE, FTE 4-237SHELLSIDE

DPE 4-212MTE 4-223RBE 4-200STE 4-180

HOCIACE 4-253DPE 4-214FTE 4-239MTE 4-225PHE 4-268RBE 4-203STE 4-192

HOTACE 4-252DPE 4-214MTE 4-225PLOT statement 4-144

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Page 392: Hextran Keyword v9

RBE 4-203STE 4-192

HOTS, PHE 4-268HOTSIDE

ACE 4-244DPE 4-207FTE 4-231HX 4-295MTE 4-218PHE 4-258RBE 4-196STE 4-167

HPASS, PHE ARRANGEMENTS 4-264HPSTEAM, UTCOST statement 4-81, 4-88, 4-96,

4-108, 4-117, 4-128HRAT

modifying 4-140PLOT keyword 4-136SPEC statement 4-133, 4-142

HSCALERAIRSIDE, ACE 4-250COLDSIDE, PHE 4-259DUCTSIDE, FTE 4-237HOTSIDE, PHE 4-258SHELLSIDE

DPE 4-212MTE 4-223RBE 4-200STE 4-180

TUBESIDEACE 4-247DPE 4-209FTE 4-234MTE 4-221RBE 4-199STE 4-173

HTFS statement, STE 4-190HTRI statement

ACE 4-255FTE 4-241STE 4-190

HX statement 4-294HXCOST

building an input file 3-28statement

flowsheet calculation 4-81, 4-88, 4-96,4-109, 4-118, 4-128

synthesis calculation 4-145targeting calculation 4-138

Hydraulic calculation method 4-79, 4-86, 4-94,4-106, 4-116, 4-126

IID

CNOZZLE, PHE 4-267HNOZZLE, PHE 4-267INOZZLE, STE 4-189LNOZZLE, STE 4-190PIPE

FITTINGS 4-280LINE 4-277

SHELLSIDEDPE 4-211MTE 4-222RBE 4-199STE 4-177

SNOZZLEDPE 4-213MTE 4-224RBE 4-202STE 4-188

TNOZZLEACE 4-252DPE 4-212FTE 4-238MTE 4-223RBE 4-201STE 4-188

TUBESIDEACE 4-245DPE 4-208FTE 4-232MTE 4-219RBE 4-197STE 4-171

INCHECK, CALCULATION statement 4-19Inclined pipe section 4-279Incremental

area efficiency factor 4-135stepsize 4-120

Initial point temperatures 4-25Initial U-value, STE 4-168INOZZLE statement, STE 4-189Input

data checking 4-19file, building 3-22

INSPACING, STE BAFFLE 4-185INTERMEDIATE, PRINT statement 4-79, 4-94,

4-107, 4-116, 4-126Internal property data

building an input file 3-27category of input 4-64

ITER, MVC PARAMETER 4-325Iterations 4-78, 4-85, 4-93, 4-105, 4-114, 4-125

JJFACTOR

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Page 393: Hextran Keyword v9

FPLATE 4-265JPLATE 4-266

KK, compressor 4-315Keenan & Keyes Steam Tables 4-20Keywords

changes to 1-4continuing a statement 4-5conventions 4-6default values 4-3layout 4-5qualifiers 4-3statements 4-2text comments 4-3

KFACTOR, PIPE FITTINGS 4-281K-value

METHOD statement 4-32user-supplied 4-30

LLAPI, external property data types 4-70Latent

external property data types 4-70heat 4-28statement 4-28

LAYERAIRSIDE, ACE 4-249COLDSIDE, PHE 4-259DUCTSIDE, FTE 4-236HOTSIDE, PHE 4-258SHELLSIDE

DPE 4-212MTE 4-223RBE 4-200STE 4-180

TUBESIDEACE 4-247DPE 4-209FTE 4-233MTE 4-220RBE 4-198STE 4-173

LCONDUCTIVITY, external property data types4-70LCP, external property data types 4-70LDENSITY, external property data types 4-70LENGTH

AIRSIDE, ACE 4-249DUCTSIDE, FTE 4-236PIPE LINE 4-278SNOZZLE

RBE 4-202STE 4-188

TUBESIDEACE 4-245DPE 4-208FTE 4-232MTE 4-219RBE 4-197STE, design 4-171STE, rating 4-170

LFRACACE 4-252DPE 4-214FTE 4-238MTE 4-225phase-fixed

assay stream 4-46pure component stream 4-42

PHE 4-268RBE 4-203STE 4-192

LHORIZONTAL, PACK, PHE 4-260LIBID

building an input file 3-26statement 4-23

Library components, defining 3-3LIFE, ECONOMICS statement 4-139LIGHTEND, stream data 4-52Limits

dual design for cut and spacing 4-185statement

building an input file 3-27flowsheet calculation 4-77, 4-84, 4-92,

4-104, 4-114, 4-124synthesis calculation 4-147

LINE statement, PIPE 4-277LINEAR

See Linear cost factorLinear area efficiency factor 4-135Linear cost factor

ACE 4-254compressor 4-316cooler 4-308DPE 4-215fired heater 4-311FTE 4-240heater 4-304HX 4-299HXCOST statement

flowsheet calculation 4-81, 4-88, 4-97,4-109, 4-118, 4-128

synthesis calculation 4-145targeting calculation 4-138

MTE 4-227PHE 4-270

Index HEXTRAN Input ManualI-10 June 2002

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Page 394: Hextran Keyword v9

pump 4-321RBE 4-204STE 4-161, 4-193utility stream 4-60

LiquidAPI gravity 4-70density 4-70FLASH STRMS 4-292fraction

See LFRACheat capacity 4-70molar volume 4-22petroleum stream 4-56specific gravity 4-70surface tension 4-70thermal conductivity 4-70viscosity 4-70Watson characterization factor 4-70

LIQVOLUMEDIMENSION 4-10OUTDIMENSION 4-15

LKP statement 4-36LN 4-29LNOZZLE statement, STE 4-190LOG 4-29Low pressure steam cost 4-81, 4-88, 4-96, 4-109,

4-118, 4-128LPITCH, TUBESIDE

ACE 4-246FTE 4-233

LPSTEAM, UTCOST statement 4-81, 4-88, 4-96,4-109, 4-118, 4-128

LSPGRAVITY, external property data types 4-70LUOPK, external property data types 4-70LVERTICAL, PACK, PHE 4-260LVISCOSITY, external property data types 4-70

MMATCH, LIGHTEND statement 4-52MATERIAL

codes, gasket 4-264FINS

ACE 4-248DPE 4-210FTE 4-235MTE 4-221

PLATE, PHE 4-262SHELLSIDE

DPE 4-211MTE 4-222RBE 4-199STE 4-179

TUBESIDEACE 4-246

DPE 4-209FTE 4-233MTE 4-220RBE 4-198STE 4-173

MAXAREA, LIMITS statement 4-147MAXP, LIMITS statement 4-147MAXPASSES, PACK, PHE 4-261MAXS, LIMITS statement 4-147Medium pressure steam cost 4-81, 4-88, 4-96,

4-108, 4-117, 4-128METHOD

building an input file 3-26statement 4-32

METRICDIMENSION statement 4-10OUTDIMENSION statement 4-15

MINFTHX 4-298LIMITS statement 4-147MTE 4-224STE 4-191

Mixerspecifications 3-19statement 4-271

Modified Chen vaporization 4-79, 4-86, 4-94,4-106, 4-116, 4-126

Molecular weightASSAY statement 4-24component data 4-26methods 4-25

MOLVOL statement 4-22MONITOR

ACE 4-254DPE 4-215FTE 4-240MTE 4-226PHE 4-269PRINT statement 4-79, 4-87, 4-95,

4-107, 4-116, 4-127STE 4-193

MPSTEAM, UTCOST statement 4-81, 4-88,4-96, 4-108, 4-117, 4-128

MTD, PLOT keyword 4-136MTE

illustration 4-217specifications 3-17statement 4-159

Multipleentries 4-3thermodynamic and transport methods 3-8

MVCillustration 4-324

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specifications 3-22statement 4-322

MWASSAY statement 4-24statement

component data 4-26stream data 4-51

NNAME

ACE 4-159assay stream 4-44compressor 4-313cooler 4-305decanter 4-288desalter 4-285DPE 4-159fired heater 4-309flash drum 4-291FTE 4-159heater 4-301HX 4-294mix/flash stream 4-55mixer 4-271MTE 4-159MVC 4-322petroleum stream 4-57PHE

PLATE 4-262statement 4-159

pipe 4-276pump 4-318pure component stream 4-41RBE 4-159splitter 4-273STE 4-159utility stream 4-61valve 4-283water/steam stream 4-58

NBPASSAY statement 4-25component data 4-27

NCCOLD, ARRANGEMENTS, PHE 4-264NCHOT, ARRANGEMENTS, PHE 4-264Net free area ratio

See NFARNetwork mean temperature difference 4-136NEW

ACE 4-244FTE 4-231HX 4-295PHE 4-257STE 4-165

NEWS, PRINT statement 4-18

NFARdefinition 4-184STE BAFFLE

design 4-184rating 4-183

No tubes in window 4-183NOACCELERATION, PIPE LINE 4-279NOBLEND, assay stream 4-45NOCHECK

ACE 4-253CALCULATION statement 4-78, 4-85,

4-93, 4-106, 4-115, 4-125DPE 4-213FTE 4-239MTE 4-224PHE 4-267RBE 4-202STE 4-191

NOMATCH, LIGHTEND statement 4-52NONCONDENSIBLE, petroleum stream 4-56NONE

BAFFLE, STE 4-182CNOZZLE, PHE 4-267HNOZZLE, PHE 4-267PRINT statement

general data 4-17targeting calculation 4-137

SNOZZLEMTE 4-224RBE 4-202SNOZZLE 4-213STE 4-188

TNOZZLEACE 4-252DPE 4-212FTE 4-238MTE 4-223RBE 4-201STE 4-188

Nonlibrarycomponents, defining 3-4

statement 4-22NOPETRO, PGEN statement 4-66NOPRINT, MVC PARAMETER 4-325Normal boiling point

See NBP

NORMALIZELIGHTEND statement 4-53pure component stream 4-41

NOSPLITnetwork synthesis 4-62synthesis calculation 4-147

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NOUTILITYnetwork synthesis 4-62synthesis calculation 4-147

Nozzle, annular design 4-189NPS

allowed valuesDPE 4-209

PIPE LINE 4-278SHELLSIDE

DPE 4-211MTE 4-222

TUBESIDEACE 4-245DPE 4-208MTE 4-219

NTIWillustration 4-183STE BAFFLE 4-182

NUMBERFAN, ACE 4-251FINS

ACE 4-248DPE 4-210FTE 4-235MTE 4-221STE 4-174

INOZZLE, STE 4-189LNOZZLE, STE 4-190SNOZZLE, STE 4-188TNOZZLE

ACE 4-252FTE 4-238STE 4-188

TUBESIDEACE 4-246FTE 4-232MTE 4-220RBE 4-198STE 4-172

OOCOOLING, PLOT keyword 4-136OD, TUBESIDE

ACE 4-245DPE 4-208FTE 4-232MTE 4-219RBE 4-197STE 4-171

OHEATING, PLOT keyword 4-136OIL, UTCOST statement 4-80, 4-87, 4-95,

4-108, 4-117, 4-127OLD

ACE 4-244

DPE 4-207FTE 4-231HX 4-295MTE 4-218PHE 4-257RBE 4-196STE 4-165

On-stream factor 4-139OPERATION statement

compressor 4-314cooler 4-306decanter 4-289desalter 4-286fired heater 4-310flash drum 4-292heater 4-302pipe 4-281pump 4-319splitter 4-274valve 4-284

OPTIMIZATIONAREA

calculations, overview 3-12PROPERTY statement 4-76, 4-91,

4-104, 4-113, 4-123FAN, ACE 4-251SPLITFLOW, PROPERTY statement 4-76,

4-91, 4-104, 4-113, 4-123ORIENTATION

DPE 4-207MTE 4-218RBE 4-196STE 4-167

OUTDIMENSIONbuidling an input file 3-25statement 4-15

OUTILITIES, PLOT keyword 4-136OUTSPACING, STE BAFFLE 4-186Overall heat transfer coefficient

See UVALUEOverriding units of measure 4-10

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PPACK statement, PHE 4-260PARALLEL

AIRSIDE, ACEdesign 4-250rating 4-250

DUCTSIDE, FTEdesign 4-237rating 4-237

LIMITS statement 4-77, 4-84, 4-92,4-105, 4-124

PACK, PHEdesign 4-261rating 4-260

SHELLSIDEDPE 4-211HX 4-297MTE 4-222RBE 4-199STE 4-179

TUBESIDEACE 4-247FTE 4-234

PARAMETER statementflowsheet calculation 4-82, 4-120, 4-130MVC 4-325synthesis calculation 4-143targeting calculation 4-134

PASS, TUBESIDEACE 4-246FTE 4-233HX 4-296MTE 4-220RBE 4-198STE 4-172

PATTERN, TUBESIDEACE 4-246FTE 4-233MTE 4-220RBE 4-198STE 4-172

PAYOUT, PLOT keyword 4-136PBASIS

DIMENSION 4-11OUTDIMENSION 4-16

PC statement 4-27PDAMP, LIMITS statement 4-78, 4-85, 4-93,

4-105, 4-114, 4-125PDESIGN

COLDSIDE, PHE 4-260HOTSIDE, PHE 4-258SHELLSIDE

DPE 4-212

MTE 4-223RBE 4-200STE 4-180

TUBESIDEDPE 4-210MTE 4-221RBE 4-199STE 4-174

PERCENTLIGHTEND statement 4-52PRINT statement 4-18

PetroleumPGEN statement 4-66pseudocomponents, defining 3-5statement 4-24

PFE, specifications 3-18PFIRST, ARRANGEMENTS, PHE 4-264PGEN 4-64

building an input file 3-27CALCULATION statement 4-19internal property data 4-64

PHASEmix/flash stream 4-54phase-fixed assay stream 4-46phase-fixed pure component stream 4-42separation 4-30statement 4-22temperature and pressure-fixed assay stream4-45temperature and pressure-fixed pure componentstream 4-42

PHEdesign process 4-256statement 4-159

PHI, METHOD statement 4-33Pipe

schedule, allowed 4-209specifications 3-19statement 4-276

PITCH, TUBESIDEMTE 4-220RBE 4-198TUBESIDE 4-172

Platedatabank 4-262statement, PHE 4-261

PLOTkeywords 4-136statement

synthesis calculation 4-144targeting calculation 4-137

pname

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(AVG)assay stream 4-45petroleum stream 4-56pure component stream 4-42

(SETNO)assay stream 4-45mix/flash stream 4-55petroleum stream 4-56pure component stream 4-42

statement 4-68Point access 4-41POUT

assay stream 4-45compressor 4-314cooler 4-306decanter 4-289desalter 4-286fired heater 4-310flash drum 4-292heater 4-302mix/flash stream 4-55petroleum stream 4-57pipe 4-281pump 4-319pure component stream 4-42valve 4-284water/steam stream 4-58

POWERDIMENSION statement 4-10FAN, ACE 4-251OUTDIMENSION statement 4-16

PPOINTS, PGEN statement 4-65PR statement 4-36PRES

D1160 statement 4-48D86 statement 4-46mix/flash stream 4-54petroleum stream 4-56phase-fixed assay stream 4-46phase-fixed pure component stream 4-42TBP statement 4-47temperature and pressure-fixed assay stream4-45temperature and pressure-fixed pure componentstream 4-42water/steam stream 4-58

Pressuredamping, fraction 4-78, 4-85, 4-93, 4-105,

4-114, 4-125DATA statement 4-68DIMENSION statement 4-10drop constraint

shellside 4-120

tubeside 4-120internal property data 4-65OUTDIMENSION statement 4-16PGEN statement 4-65SPECIFICATION statement 4-97

PRINTbuilding an input file

calculation type section 3-27general data section 3-25

options keywords, synthesis 4-144statement

ACE 4-254changes to syntax 1-4DPE 4-215flowsheet calculation 4-79, 4-86, 4-94,

4-107, 4-116, 4-126FTE 4-240general data 4-17HX 4-299MTE 4-226PHE 4-269RBE 4-204STE 4-193synthesis calculation 4-144targeting calculation 4-137

Printout options 3-2PROBLEM entry 4-8PROC, changes to 1-4Process-process

duty 4-133heat transfer surface area 4-134

PRODUCTAIRSIDE, ACE 4-249building an input file 3-25COLDSIDE, PHE 4-259DUCTSIDE, FTE 4-236HOTSIDE, PHE 4-258SHELLSIDE

DPE 4-211HX 4-297MTE 4-222RBE 4-199STE 4-177

STRMScompressor 4-314cooler 4-306decanter 4-289desalter 4-285fired heater 4-309heater 4-302mixer 4-272pipe 4-277pump 4-319

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Page 399: Hextran Keyword v9

splitter 4-273valve 4-283

TUBESIDEACE 4-245DPE 4-208FTE 4-232HX 4-296MTE 4-219RBE 4-197STE 4-170

PROJECTbuilding an input file 3-25entry 4-8life 4-139

PROPbuilding an input file 3-26changes to 1-4

Propertiestables of 3-10variable, pure component 4-28

PROPERTYbuilding an input file 3-26generation, internal 4-19keywords 4-59prediction methods 4-23PRINT statement 4-17statement

flowsheet calculation 4-76, 4-83, 4-91,4-104, 4-113, 4-123

mix/flash stream 4-53network synthesis 4-62petroleum stream 4-56stream data 4-44water/steam stream 4-58

values 4-69WATER statement 4-35

PSECOND, ARRANGEMENTS, PHE 4-264Pump

specifications 3-21statement 4-318

Pure component variable properties 4-28PXTRAPOLATE, PGEN statement 4-65

QQCOOLING

PLOT keyword 4-136SPEC statement 4-133

QHEATINGPLOT keyword 4-136SPEC statement 4-133

QPROCESSPLOT keyword 4-136SPEC statement 4-133

Qualifiers, keyword 4-3

QUTILITIESPLOT keyword 4-136SPEC statement 4-134

RRackett parameter 4-22Radius of gyration 4-22RATE

assay stream 4-44ECONOMICS statement

synthesis calculation 4-146targeting calculation 4-139

LIGHTEND statement 4-52MVC VARIABLE 4-323PRINT statement 4-18pure component stream 4-41splitter 4-274VARIABLE statement 4-99

RBEspecifications 3-16statement 4-159

Reference streamSee REFSTREAM

REFPHASE, mix/flash stream 4-55REFRIGERANT, UTCOST statement 4-81, 4-88,

4-96, 4-109, 4-118, 4-128REFSTREAM

compressor 4-314mix/flash stream 4-53pump 4-319

REFUNIT 4-159Regression

calculation 3-11overview 4-90PROPERTY statement 4-76, 4-91, 4-104,

4-113, 4-123REJECTION, DECANTER 4-290REPLACE

building an input file 3-25OUTDIMENSION statement 4-17

REYNOLDSFPLATE 4-265JPLATE 4-266

Rigorous heat exchangers 5-6Bell-Delaware method 5-6, 5-9fouling layer thickness 5-14fouling resistance 5-14shellside heat transfer correlations 5-6shellside pressure drop correlations 5-9Sieder-Tate equation 5-8stream analysis method 5-11TEMA exchanger types 5-6tubeside heat transfer correlations 5-8tubeside pressure drop correlations 5-12

Index HEXTRAN Input ManualI-16 June 2002

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RKH3, STE 4-190Rod baffle

cage assembly 4-195tube support rod layout 4-195

ROOT, FINS, STE 4-174ROUGHNESS

PIPE FITTINGS 4-280PIPE LINE 4-279

ROWS, TUBESIDEACE 4-246FTE 4-233

SSample input file 3-22Schedule

pipeallowed values, DPE 4-209LINE 4-278

SHELLSIDEDPE 4-211MTE 4-222

TUBESIDEACE 4-246DPE 4-208MTE 4-220

Sealing strip descriptions 4-179SEALS, SHELLSIDE, STE 4-179Search trial

iterations 4-78, 4-93, 4-115, 4-125tolerance 4-76, 4-91, 4-113, 4-123

Segmentalbaffle types, illustration 4-182STE BAFFLE 4-181

SERIESLIMITS statement 4-77, 4-84, 4-92,

4-105, 4-124SHELLSIDE

DPE 4-211HX 4-297MTE 4-222RBE 4-199STE 4-178

TUBESIDEACE 4-247FTE 4-234

SETassay stream 4-44changes to 1-4METHOD statement 4-33pure component stream 4-41

SETN, pname statement 4-68SETNO

assay stream 4-44changes to 1-4

mix/flash stream 4-55pure component stream 4-41

SFORMAT, PRINT statement 4-18SHEETS, RBE BAFFLE 4-201SHELL

COSTDPE 4-216FTE 4-240HX 4-300MTE 4-227RBE 4-205STE 4-161, 4-194

HXCOST statement 4-81, 4-89, 4-97, 4-109,4-118, 4-129

inside diameters, standard 4-177SPECIFICATION

DPE 4-214MTE 4-225RBE 4-203STE 4-192

utility stream 4-60Shells

in parallel 4-77, 4-84, 4-92, 4-105, 4-124in series 4-77, 4-84, 4-92, 4-105, 4-124in series and parallel 4-178

SHELLSIDEbuilding an input file 3-28DPE 4-211HX SPECIFICATION 4-298HX statement 4-297MTE 4-222RBE 4-199STE 4-177

Shortcutcooler 3-21heat exchanger 3-20heater 3-21

SI entryDIMENSION statement 4-10OUTDIMENSION statement 4-15

Simulationbuilding an input file 3-27calculation 3-11overview 4-83PROPERTY statement 4-76, 4-83, 4-91,

4-104, 4-113, 4-123SINGLE

network synthesis 4-62synthesis calculation 4-147

SITE entry 4-8Slash character 4-3SNOZZLE statement

DPE 4-213

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MTE 4-224RBE 4-202STE 4-188

Solid-liquid equilibrium 4-31Solubility

parameter 4-22WATER statement 4-35

SOLUPARA statement 4-22SPACE, PACK, PHE 4-260Spacing

dual design limits 4-185RBE BAFFLE 4-201STE BAFFLE 4-185

SPEC statementsynthesis calculation 4-142targeting calculation 4-133

Specificgravity 4-26heat 4-28

SPECIFICATIONACE 4-252building an input file 3-28DPE 4-214flowsheet calculation 4-82, 4-97,

4-110, 4-129FTE 4-238HX 4-298MTE 4-225MVC 4-322PHE 4-268RBE 4-203STE 4-192

SPGRpetroleum stream 4-56statement

component data 4-26stream data 4-50

SplitPRINT statement 4-144stream temperature limitation 4-62

Split flow optimizationcalculations 3-12overview 4-112

Splitterspecifications 3-19statement 4-273

SRK, statement 4-36ST5, STE 4-190STAGES, compressor 4-315Standard

ACE 4-254density 4-27DPE 4-215

FTE 4-240MTE 4-226PHE 4-269PRINT statement 4-79, 4-86, 4-95, 4-107,

4-116, 4-126RBE 4-204STE 4-193

Statements, continuing 4-5STDDENSITY statement 4-27STDVAPOR

DIMENSION statement 4-11OUTDIMENSION statement 4-16

STEbuilding an input file 3-28keywords 4-165specifications 3-15statement 4-159

STEAMpetroleum stream 4-56water/steam stream 4-58

Streamdata

building an input file 3-26category of input 4-38, 4-40entering 3-10

fluid fraction, initial rate 4-41ID

assay stream 4-44length, changes to 1-4mix/flash stream 4-53MW statement 4-52petroleum stream 4-56PGEN statement 4-65pure component stream 4-41SPGR statement 4-50utility stream 4-60water/steam stream 4-58

PRINT statement 4-17split fraction 4-99, 4-119statement

API 4-50changes to 1-4D1160 4-48D2887 4-49D86 4-46LIGHTEND 4-53PRINT 4-79, 4-86, 4-94, 4-107,

4-116, 4-126TBP 4-47WATSONK 4-51

STRIAL

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LIMITS statement 4-78, 4-93, 4-115, 4-125TOLERANCE statement 4-76, 4-91,

4-113, 4-123STRM

changes to 1-4flowsheet calculation

CONSTRAINT statement 4-119, 4-129SPECIFICATION statement 4-97VARIABLE statement 4-99, 4-119

MVCSPECIFICATION statement 4-322VARIABLE statement 4-323

STRMS statementcompressor 4-313cooler 4-305decanter 4-288desalter 4-285fired heater 4-309flash drum 4-291heater 4-301mixer 4-271pipe 4-277pump 4-318splitter 4-273valve 4-283

Structure group 4-22SUMMARY, PRINT statement 4-137SUMSQ, MVC PARAMETER 4-325Surface

DIMENSION statement 4-10external property data types 4-70METHOD statement 4-33OUTDIMENSION statement 4-16tension 4-28

SYNCOMP statement 4-22SYNLIQ statement 4-22Synthesis

calculation 3-14category of input 4-141

SYSTEM, METHOD statement 4-32

TTabular

properties 4-63statement 4-29

TADDITIONALnetwork synthesis 4-62synthesis calculations 4-147

Targetingcalculations, overview 3-13overview 4-131

TASC3, STE 4-190TBP

PRINT statement 4-17

stream data 4-47TBPCUTS, ASSAY statement 4-26TBPEP

ASSAY statement 4-25TBPIP

ASSAY statement 4-25TC statement 4-27TCOOLING

PLOT keyword 4-136SPEC statement 4-133

TDAMP, LIMITS statement 4-77, 4-84, 4-92,4-105, 4-114, 4-124

TDESIGNCOLDSIDE, PHE 4-260HOTSIDE, PHE 4-259SHELLSIDE, STE 4-180TUBESIDE, STE 4-174

TEMAdesignations 4-166HX 4-295RBE 4-196STE 4-165

TEMPD1160 statement 4-48D2887 statement 4-49D86 statement 4-46mix/flash stream 4-54petroleum stream 4-56phase-fixed stream

assay 4-46pure component 4-42

TBP statement 4-47temperature and pressure-fixed stream

assay 4-45pure component 4-42

utility stream 4-60water/steam stream 4-58

TemperatureCONSTRAINT statement 4-120, 4-129damping, fraction 4-77, 4-84, 4-92, 4-105,

4-114, 4-124DIMENSION statement 4-10end point 4-25initial point 4-25OUTDIMENSION statement 4-16PGEN statement 4-65pname statement 4-68rundown for hot streams 4-133runup for cold streams 4-133

SPECIFICATIONACE 4-252

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DPE 4-214FTE 4-238HX 4-298MTE 4-225MVC 4-323PHE 4-268RBE 4-203statement 4-97STE 4-192

tolerance 4-76, 4-84, 4-91, 4-104,4-113, 4-123

VARIABLEMVC 4-323statement 4-99

THEATINGPLOT keyword 4-136SPEC statement 4-133

Thermalconductivity 4-28cracking 4-46properties 4-19

Thermodynamiccapabilities, additional 3-9data

binary interaction data 4-30building an input file 3-26liquid activity methods 4-30

methodBenedict-Webb-Rubin-Starling 4-36defining 3-6Lee-Kessler-Plöcker 4-36multiple 3-8Peng-Robinson 4-36set, assigning 4-41Soave-Redlich-Kwong 4-36statement 4-32

property calculation methods 4-34systems, predefined 4-34

THICKNESSBAFFLE

RBE 4-201STE 4-186

FINSACE 4-248DPE 4-210FTE 4-235MTE 4-222STE 4-174

PLATE, PHE 4-262TUBESIDE

ACE 4-245DPE 4-208FTE 4-232

MTE 4-219RBE 4-197STE 4-171

TIMEDIMENSION statement 4-10OUTDIMENSION statement 4-16

TITLEbuding an input file 3-25statement 4-8

TNOZZLE statementACE 4-252DPE 4-212FTE 4-238MTE 4-223RBE 4-201STE 4-188

TOLERANCEbuilding an input file 3-27statement 4-76, 4-84, 4-91, 4-104,

4-113, 4-123Total utilities duty 4-134TOUT

assay stream 4-45cooler 4-306cooler cost 4-308decanter 4-289desalter 4-286fired heater 4-310heater 4-302mix/flash stream 4-55petroleum stream 4-57pure component stream 4-42utility stream 4-60water/steam stream 4-58

TPITCH, TUBESIDEACE 4-246FTE 4-233

TPOINTS, PGEN statement 4-65Transport

methodmultiple 3-8statement 4-33

propertiescalculation methods 4-35overview 3-8thermodynamic data 4-30

systems, predefined 4-34TSPLIT, network synthesis 4-62TSR

compressor 4-315pump 4-320

TTRIAL

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LIMITS statement 4-78, 4-85, 4-93, 4-105,4-114, 4-125

TOLERANCE statement 4-76, 4-84, 4-91,4-104, 4-113, 4-123

Tubedimensions 4-175patterns 4-172radial low-fin, dimensions 4-176SPECIFICATION

ACE 4-252DPE 4-214FTE 4-238MTE 4-225RBE 4-203STE 4-192

TUBESIDEbuilding an input file 3-28statement

ACE 4-245DPE 4-208FTE 4-232HX 4-296, 4-298MTE 4-219RBE 4-197STE 4-170

TUTILITYcooler 4-306heater 4-302

TWOPHASE CALCULATIONACE 4-253DPE 4-213FTE 4-239MTE 4-225RBE 4-203statement 4-79, 4-86, 4-94, 4-106, 4-116,4-126STE 4-191

TXTRAPOLATE, PGEN statement 4-65TYPE statement

ACE 4-244BAFFLE, RBE 4-201building an input file 3-28DPE 4-207FTE 4-231HX 4-295MTE 4-218PHE 4-257RBE 4-196SNOZZLE

RBE 4-202STE 4-188

STE 4-165TNOZZLE, STE 4-188

UUESTIMATE

ACE 4-244DPE 4-207FTE 4-231MTE 4-218PHE 4-257RBE 4-196STE 4-168

UIDACE 4-159compressor 4-313cooler 4-305decanter 4-288desalter 4-285DPE 4-159fired heater 4-309flash drum 4-291FTE 4-159heater 4-301HX 4-294length, changes to 1-4mixer 4-271MTE 4-159MVC 4-322PHE 4-159pipe 4-276pump 4-318RBE 4-159splitter 4-273STE 4-159valve 4-283

UMAT, PARAMETER statement 4-135UNIFAC method

component data 4-22thermodynamic data 4-31

UNITCASE statement 4-111CONSTRAINT statement 4-120COST

DPE 4-216FTE 4-240HX 4-300MTE 4-227PHE 4-270RBE 4-205STE 4-161, 4-194

HXCOST statement 4-81, 4-89, 4-97,4-109, 4-118, 4-129

PRINT statement 4-18SPECIFICATION

MVC 4-323statement 4-97, 4-110

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utility stream 4-60VARIABLE

MVC 4-324statement 4-99

Unit operationsbuilding an input file 3-28category of input 4-148

Units of measureallowable 4-13compatibility with PRO/II 1-3input, specifying 4-9output dimensions 4-15overriding 4-10overview 3-2standard 4-12

UNITS, PRINT statement 4-79, 4-86, 4-94,4-107, 4-116, 4-126

UNIWAAL method 4-31UNSPLIT, PRINT statement 4-144UOPK, petroleum stream 4-56USCALER

ACE 4-244DPE 4-207FTE 4-231MTE 4-218PHE 4-257RBE 4-197STE 4-168

USERbuilding an input file 3-25statement 4-8

UTCOSTbuilding an input file 3-27statement 4-80, 4-87, 4-95, 4-108,

4-111, 4-117, 4-127Utility

compressor 4-315cooler 4-307fired heater 4-310heater 4-302Minimum Approach Temperature

See UMATpump 4-320statement 4-60

UTRIALLIMITS statement 4-78, 4-115, 4-125TOLERANCE statement 4-76, 4-123

U-tube bundle, effective length 4-171U-value

DIMENSION statement 4-10HX 4-295loop iterations 4-78, 4-115, 4-125OUTDIMENSION statement 4-16

PARAMETER statementsynthesis calculation 4-143targeting calculation 4-134

PLOT keyword 4-136STE 4-167trial tolerance 4-76, 4-123

VVALUE, DATA statement 4-69Valve

specifications 3-19statement 4-283

Van der Waal’s area and volume 4-22VAPI, external property data types 4-70Vapor

API gravity 4-70density 4-70FLASH STRMS 4-292heat capacity 4-70petroleum stream 4-56pressure 4-28specific gravity 4-70thermal conductivity 4-70viscosity 4-70Watson characterization factor 4-70

VAPVOLUMEDIMENSION statement 4-10OUTDIMENSION statement 4-16

VARIABLE statementflowsheet calculations 4-82, 4-99, 4-119MVC 4-323

VC statement 4-27VCONDUCTIVITY, external property data types4-70VCP, external property data types 4-70VDENSITY, external property data types 4-70VELOCITY

AIRSIDE, ACE 4-250DUCTSIDE, FTE 4-237SHELLSIDE, STE 4-180TUBESIDE

ACE 4-247FTE 4-234STE 4-173

VISCOSITYcomponent data 4-28DIMENSION statement 4-11METHOD statement 4-33OUTDIMENSION statement 4-16

VP statement 4-28VSPGRAVITY, external property data types 4-70VUOPK, external property data types 4-70VVISCOSITY, external property data types 4-70

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WWater

CALCULATION statement 4-19DECANTER STRMS 4-289petroleum stream 4-56property calculation options 4-36pure, properties 4-35solubility, calculation options 4-36UTCOST statement 4-80, 4-88, 4-96,

4-108, 4-117, 4-128water/steam stream 4-58

WATER 4-35Watson characterization factor 4-56WATSONK, stream data 4-51Weight fraction 4-70WFRACTION, external property data types 4-70WIDE, PLOT statement 4-144WIDTH

AIRSIDE, ACE 4-249DUCTSIDE, FTE 4-236PACK, PHE 4-260

WTDIMENSION statement 4-11OUTDIMENSION statement 4-16

XX, PLOT statement 4-137XBLEND

assay stream 4-44changes to 1-4

XDENSITYDIMENSION statement 4-11OUTDIMENSION statement 4-16

YY, PLOT statement 4-137

ZZC statement 4-26ZONES, PRINT

ACE 4-254DPE 4-215FTE 4-240HX 4-299MTE 4-226PHE 4-269RBE 4-204statement 4-79, 4-87, 4-95, 4-107,

4-116, 4-127STE 4-193

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Index HEXTRAN Input ManualI-24 June 2002

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