Pipephase UG Libre

PIPEPHASE 9.1

Users Guide

PIPEPHASE 9.1 Users Guide The software described in this guide is furnished under a written agreement and may be used only in accordance with the terms and conditions of the license agreement under which you obtained it.. The technical documentation is being delivered to you AS IS and Invensys Systems, Inc. makes no warranty as to its accuracy or use. Any use of the technical documentation or the information contained therein is at the risk of the user. Documentation may include technical or other inaccuracies or typographical errors. Invensys Systems, Inc. reserves the right to make changes without prior notice.

Copyright Notice 2006 Invensys Systems, Inc. All rights reserved. No part of the material protected by this copyright may be reproduced or utilized in any form or by any means, electronic or mechanical, including photocopying, recording, broadcasting, or by any information storage and retrieval system, without permission in writing from Invensys Systems, Inc.

Trademarks PIPEPHASE, NETOPT, and Invensys SIMSCI-ESSCOR are trade-

marks of Invensys plc, its subsidiaries and affiliates.

TACITE is a trademark of Institut Franais du Petrole (IFP).

OLGAS 1.1, OLGAS TWO-PHASE, and OLGAS THREE-PHASE are

trademarks of SCANDPOWER A/S.

Windows 98, Windows ME, Windows NT, Windows 2000, Win-

dows XP, Windows 2003, and MS-DOS are trademarks of

Microsoft Corporation.

Compaq Visual Fortran is a trademark of Compaq Computer Cor-

poration.

Adobe, Acrobat, Exchange and Reader are trademarks of Adobe

Systems, Inc.

All other products may be trademarks of their respective owners.

U.S. GOVERNMENT RESTRICTED RIGHTS LEGEND

The Software and accompanying written materials are provided with restricted rights. Use, duplication, or disclosure by the Gov-ernment is subject to restrictions as set forth in subparagraph (c) (1) (ii) of the Rights in Technical Data And Computer Software clause at DFARS 252.227-7013 or in subparagraphs (c) (1) and (2) of the Commercial Computer Software-Restricted Rights clause at 48 C.F.R. 52.227-19, as applicable. The Contractor/Manufacturer is: Invensys Systems, Inc. (Invensys SIMSCI-ESS-COR) 26561 Rancho Parkway South, Suite 100, Lake Forest, CA 92630, USA.

Printed in the United States of America, March 2006.

PIPEPHASE 9.1 Users Guide iii

Contents

Introduction

About This Manual . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . v

About PIPEPHASE . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . v

About SIMSCI - ESSCOR. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .vi

Where to find additional help . . . . . . . . . . . . . . . . . . . . . . . . . . . . .vi

Online Documentation . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .vi

Online Help . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .vi

Other Documentation . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . vii

Chapter 1 Getting Started

Starting PIPEPHASE . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .1-1

Exiting PIPEPHASE . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .1-2

Manipulating the PIPEPHASE Window . . . . . . . . . . . . . . . . . . . .1-3

Changing Window Size. . . . . . . . . . . . . . . . . . . . . . . . . . . . . .1-3

Working with On-screen Color Coding Cues . . . . . . . . . . . . . . . .1-3

Using the Menus . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .1-4

Choosing a Menu Item . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .1-5

Using the Toolbar Buttons . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .1-5

Using the File Manipulation Buttons . . . . . . . . . . . . . . . . . . .1-6

Using the Structure and Unit Operation Buttons . . . . . . . . . .1-6

Using the Calculation Option, Optimization, and Property Buttons . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .1-7

Using the Zoom and Redraw Buttons . . . . . . . . . . . . . . . . . . .1-7

Using PIPEPHASE . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .1-8

Defining the Application. . . . . . . . . . . . . . . . . . . . . . . . . . . . .1-8

Global Settings . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .1-11

Defining Fluid Properties . . . . . . . . . . . . . . . . . . . . . . . . . . .1-13

Defining Properties for Compositional Fluids . . . . . . . . . . .1-14

Defining Properties for Non-compositional Fluids. . . . . . . .1-20

Defining Properties for Mixed Compositional/Non-Compositional Fluids . . . . . . . . . . . . . . . . . . . . . . . . . .1-23

Generating and Using Tables of Properties. . . . . . . . . . . . . .1-24

Sources . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .1-24

iv Contents

Structure of Network Systems . . . . . . . . . . . . . . . . . . . . . . . 1-25

PIPEPHASE Flow Devices . . . . . . . . . . . . . . . . . . . . . . . . . 1-28

Pressure Drop Calculations. . . . . . . . . . . . . . . . . . . . . . . . . . 1-30

Equipment Items . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 1-37

Heat Transfer Calculations . . . . . . . . . . . . . . . . . . . . . . . . . . 1-40

Sphering or Pigging . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 1-41

Reservoirs and Inflow Performance Relationships. . . . . . . . 1-41

Production Planning and Time-stepping. . . . . . . . . . . . . . . . 1-42

Subsurface Networks and Multiple Completion Modeling . 1-44

Case Studies . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 1-47

Nodal Analysis . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 1-49

Starting the PIPEPHASE Results Access System (RAS) . . . . . . 1-53

Starting the PIPEPHASE Excel Report. . . . . . . . . . . . . . . . . . . . 1-55

Chapter 2 Tutorial

Introduction . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 2-1

Problem Description . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 2-1

Building the Network . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 2-3

Entering Optimization Data. . . . . . . . . . . . . . . . . . . . . . . . . . . . . 2-20

Specifying Print Options . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 2-28

Running the Simulation . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 2-29

Viewing and Plotting Results . . . . . . . . . . . . . . . . . . . . . . . . . . . 2-30

Using the RAS to Plot Results. . . . . . . . . . . . . . . . . . . . . . . . . . . 2-31

Generate and View Excel Report. . . . . . . . . . . . . . . . . . . . . . . . . 2-33

Including Operating Costs . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 2-34

PIPEPHASE 9.1 Users Guide v

Introduction

About This Manual

The PIPEPHASE Users Guide provides an introduction to

PIPEPHASE. It describes how the interface modules work and

includes a step-by-step tutorial to guide you through a PIPEPHASE

example optimization problem. Also covered in this guide is

PIPEPHASE Keywords. An outline of this guide is provided below.

About PIPEPHASE

PIPEPHASE is a simulation program which predicts steady-state

pressure, temperature, and liquid holdup profiles in wells, flow-

lines, gathering systems, and other linear or network configurations

of pipes, wells, pumps, compressors, separators, and other facilities.

The fluid types that PIPEPHASE can handle include liquid, gas,

steam, and multiphase mixtures of gas and liquid.

Several special capabilities have also been designed into PIPEP-

HASE including well analysis with inflow performance; gas lift

analysis; pipeline sphering; and sensitivity (nodal) analysis. These

additions extend the range of the PIPEPHASE application so that

the full range of pipeline and piping network problems can be

solved.

Chapter 1 Introduction Introduces the manual, the program, and SIMSCI.

Chapter 2 Getting Started Explains how to use PIPEPHASE.

Chapter 3 Tutorial Provides a step-by-step tutorial for the optimiza-tion of an off-line pipeline design.

vi

About SIMSCI - ESSCOR

SimSci-Esscor, a business unit of Invensys Systems, Inc., is a leader

in the development and deployment of industrial process simulation

software and systems for a variety of industries, including oil and

gas production, petroleum refining, petrochemical and chemical

manufacturing, electrical power generation, mining, pulp and paper,

and engineering and construction. Supporting more than 750 client

companies in over 70 countries, SimSci-Esscor solutions enable cli-

ents to minimize capital requirements, optimize facility perfor-

mance, and maximize return on investment.

For more information, visit SimSci - Esscor Web site at http://

www.simsci-esscor.com.

Where to find additional help

Online Documentation

PIPEPHASE online documentation is provided in the form of .PDF

files that are most conveniently viewed using Adobe Acrobat

Reader 5.0 or Acrobat Exchange 5.0. You can install Adobe Acro-

bat Reader 5.0 from the product CD, which requires 5 MB of disk

space beyond that required to for PIPEPHASE. Online manuals are

stored in the Manuals directory and they remain on the CD when you install the program. To access these files, open the PIPEPHASE

ONLINE HELP.HLP file in the Bin directory and click the appropri-

ate link to navigate to the corresponding PDF.

Online Help

PIPEPHASE comes with online Help, a comprehensive online ref-

erence tool that accesses information quickly. In Help, commands,

features, and data fields are explained in easy steps. Answers are

available instantly, online, while you work. You can access the elec-

tronic contents for Help by selecting Help/Contents from the menu

bar. Context-sensitive help is accessed using the F1 key or the

Whats This? button by placing the cursor in the area in question.

PIPEPHASE 9.1 Users Guide vii

Other Documentation

The table below outlines the other existing PIPEPHASE documen-

tation available in a hardcopy form.

Where to Find Additional Help

If you want to... See...

Quickly learn how to simulate a simple flowsheet using PIPEPHASE

This document

Obtain detailed information on the capabilities and use of PIPEPHASE

This document

Learn how to install PIPEPHASE PIPEPHASE Installation Guide

Obtain basic information on PIPEPHASE keywords

PIPEPHASE Keyword Manual

See simulation examples PIPEPHASE Application Briefs

To learn more on Well and Surface Models Well and Surface Examples

Obtain detailed information on using PIPEPHASE w/ NETOPT

NETOPT Users Guide

Obtain detailed information on using PIPEPHASE w/ TACITE

TACITE Users Guide

Obtain basic information on PIPEPHASE calculation methods

Online Help

Obtain detailed information of component and thermodynamic properties

SIMSCI Component and Thermodynamic Data Input Manual

PIPEPHASE 9.1 Users Guide 1-1

Chapter 1Getting Started

Starting PIPEPHASE

If you do not see a PIPEPHASE 9.1 icon in a SIMSCI group

window or in your Program Manager window, see the

troubleshooting section in the PIPEPHASE Installation Guide.

To start PIPEPHASE:

Double-click on the PIPEPHASE 9.1 icon.

The main PIPEPHASE window appears.

Figure 1-1: The PIPEPHASE Main Window

1-2 Getting Started

You can now open a new simulation file (select File/New), open an

existing file (select File/Open), or import a keyword file (select File/

Import Keyword File). The elements of the PIPEPHASE main window

are described in Table 1-1.

To learn how to build a network, enter data, and run and optimize a

simulation, see Chapter 2, Tutorial.

Exiting PIPEPHASE

To exit PIPEPHASE, do one of the following:

Choose Exit on the File menu

Double-click on the Control-menu box in the upper left hand corner of the PIPEPHASE main window .

Table 1-1: PIPEPHASE Main Window Components

Component Description

Control-menu Box Displays a menu with commands for sizing, moving and closing the active window.

Title Bar Identifies the application and the name of the open file; can be used to move the entire window.

Minimize Button Enables you to reduce the application to an icon.

Maximize/Restore Button (Not shown)

Enables you to enlarge a window to full-screen or restore a window to its default size.

Menu Bar Identifies the menus available in PIPEPHASE: File, Edit, View, General, Special Features, and Help.

Toolbar Provides push button access to various File, Edit, View, General, Special Features, and Help menu options.

Main Window Provides the repository for placing sources, sinks, or junction, adding links, and calculator or hydrates units, i.e., for drawing the network diagram.

Horizontal Scroll Bar Provides a sliding scale for moving the flowsheet right or left in the PIPEPHASE main window.

Vertical Scroll Bar Provides a sliding scale for moving the flowsheet up or down in the PIPEPHASE main window.

Status Bar Provides guidance, focus and error messages for the active feature or object.

Border Handles Enables you to quickly change window height, width, or size by grabbing the corresponding border handle and dragging it to a new position.


Manipulating the PIPEPHASE Window

The PIPEPHASE window offers a variety of features that enable

you to customize how PIPEPHASE appears relative to the full

screen and relative to other applications.

Changing Window Size

The Windows interface provides tools for resizing each window.

Some tools automatically change a window to a particular size and

orientation, others enable you to control the magnification.

To display the control-menu box:

Click on the control-menu box in the top left hand corner of the PIPEPHASE main window or use .

Select the Move option from the menu.

Working with On-screen Color Coding Cues

PIPEPHASE provides the standard visual cue (grayed out text and

icons) for unavailable menu items and toolbar buttons. In addition,

on the network, PIPEPHASE uses colored borders liberally to

indicate the current status of the simulation.

Note: PIPEPHASE does not support multiple sessions for two

different files located in the same directory.

Tools Description/Action

Minimize/Maximize Buttons

By clicking on the minimize and maximize buttons, you can automatically adjust the size of a window.

Border Handles You can use the window border to manually change the size of the main window. The border works like a handle that you can grab with the cursor and drag to a new position.

Control Menu You can also use the Control menu to Restore, Move, Size, Minimize, or Maximize a window.

Window Position You can change the position of the main window (or any pop-up window) by clicking on the title bar and dragging the window to a new position.

Control-menu Box You can also use the control-menu box to move a window.

Table 1-2: Flowsheet Color Codes

Color Significance

Red Required data. Actions or data required of the user. On the main PIPEPHASE windows and Link PFD only.

Blue Data you have supplied.

1-4 Getting Started

Using the Menus

The names of the PIPEPHASE main menus appear on the menu bar.

From these menus, you can access most PIPEPHASE operations.

To display a menu:

Click on the menu name or press where n is the underlined letter in the menu name.

For example, to display the File menu, either click on File, or press

.

Burgundy Calculated data.

Gray Data field not available to you.

Table 1-2: Flowsheet Color Codes

Color Significance

Figure 1-2: File Menu Figure 1-3: Edit Menu

Figure 1-4: View Menu Figure 1-5: General Menu


Choosing a Menu Item

To choose a menu item, do one of the following:

Click on the desired item.

Use the arrow keys to highlight the item then press .

Use the accelerator keys.

Using the Toolbar Buttons

Figure 1-8: Toolbar Buttons

The toolbar contains four groups of buttons:

File Manipulation Buttons

Structure and Unit Operation Buttons

Calculation Options, Optimization, and Property Buttons

Zoom and Redraw Buttons

Figure 1-6: Special Features Menu Figure 1-7: Help Menu

Note: Grayed out icons indicate that the functions are

currently in passive mode and will become active when

necessary.

1-6 Getting Started

Using the File Manipulation Buttons

These buttons enable you to open a new or existing simulation,

import a keyword file, save a simulation, run a simulation, or view

or print an output. These buttons duplicate menu options available

on the File menu.

Using the Structure and Unit Operation Buttons

These buttons enable you to add sources, sinks, junction, calculator

units, or hydrate units to the flowsheet.

Button Menu Item Description

New Enables you to create a new simulation.

Open Enables you to open an existing simulation.

Import Keyword File Enables you to import an existing input file.

Save Enables you to save an open simulation.

Run Enables you to run the simulation.

Excel Reports Enables you to create Excel Reports.

Print Enables you to print the output file or the flowsheet.


Enables you to add a source to the flowsheet.

Enables you to add a sink to the flowsheet.

Enables you to add a junction to the flowsheet.

Enables you to add a Manifold unit to the flowsheet.

Enables you to add a calculator unit to the flowsheet.

Enables you to add a hydrate unit to the flowsheet.


Using the Calculation Option, Optimization, and Property Buttons

These buttons enable you to customize your calculation options,

input dimensions, and global defaults, add optimization, and add

component and thermodynamic or PVT data. These buttons

duplicate menu options available on the General menu.

Using the Zoom and Redraw Buttons

These buttons allow you to refresh, zoom in and out, search an

object/Device on the flowsheet.


Input Units of Measurement

Enables you to specify your input units of measurements.

Component Library Enables you to specify your component slate for compositional fluids.

PVT Data Enables you to specify your thermodynamic or PVT data.

Calculation Methods Enables you to enter network calculation methods.

Global Defaults Enables you to enter global defaults.

Optimization Data Enables you to enter network optimization data.


Enables you to zoom in on the flowsheet.

Enables you to zoom out of the flowsheet.

Enables you to zoom in 100%, i.e., display the entire simulation in the main window.

Enables you to refresh the flowsheet.

Enables you to search an object/device in a flowsheet.

1-8 Getting Started

Using PIPEPHASE

Defining the Application

This section contains information about the way PIPEPHASE

works, the data that you need to supply, and the correlations used.

This section is arranged according to what you want to do, the type

of fluid you have, and the type of pipeline network. For each of the

capabilities of PIPEPHASE, this chapter explains which data you

are required to provide and which data you may optionally supply.

Throughout this section, the right hand column (See...) provides the

title of the GUI window where you can input that data, or the

manual where additional information can be found.

The first thing you should do before using PIPEPHASE is to decide

what type of application you have. This depends on:

The properties of the fluid(s) flowing through the piping sys-tem,

The flowrates and conditions at which those fluids enter and leave the piping system,

The structure and elements of the piping system, and

Other special processes you want to simulate, such as Gas Lift Analysis.

Properties of Fluids

There are seven types of fluids modeled in PIPEPHASE:

Compositional

Mixed phases

Liquid

Vapor

Compositional Blackoil

Non-compositional:

Blackoil

Gas Condensate

Gas


Liquid

Steam

The fluid type controls how the program is able to obtain the

physical properties necessary for pressure drop and heat transfer

calculations either from the PIPEPHASE databank, from built-in

empirical correlations, or from user-supplied input. Steam is a

special case of a non-compositional fluid, for which PIPEPHASE

uses the GPSA steam tables.

Compositional fluids are defined as mixtures of chemical

components with a known composition. For compositional fluids,

PIPEPHASE will calculate the phase separation whenever

prevailing process fluid conditions are required. However, you may

instruct PIPEPHASE to assume the fluid is one phase at all times,

thus reducing the time the program takes to solve by continually

bypassing the vapor-liquid equilibrium (flash) calculation.

Non-compositional gases and liquids are single-phase. Blackoil is a

liquid-dominated, two-phase model. Gas Condensate is a gas-

dominated, two-phase model. Steam is a single component, two-

phase model.

Optimization

PIPEPHASE can optimize network problems of virtually any size.

You can minimize or maximize any objective function or even tune

your simulation to match measured data, while satisfying

operational or design constraints. A PIPEPHASE model can be

optimized over time resulting in efficient optimized design,

planning, forecasting, and operation of a field.

Link to Reservoir Simulator Models

PIPEPHASEs Reservoir Interface allows you to link the network

simulator to link to Reservoir Simulation models such as the

Eclipse reservoir simulation model. This integrated solution

provides greater simulation consistency and accuracy, resulting in

savings of millions of dollars over the lifetime of a field in terms of

planning and scheduling.

Flows and Conditions of Fluids

Fluids enter piping systems at sources and leave at sinks. Fluids

with different properties may enter at different sources, but they

must all be of the same type.

1-10 Getting Started

In general, you have to assign flowrates, temperatures and pressures

to sources and/or sinks. For compositional fluids, you also have to

assign compositions to the source fluids. The exceptions are

explained below in What PIPEPHASE Calculates.

Gaslift and Sphering

Two special applications, relevant to oil production and gas

transportation, can be modeled with PIPEPHASE. You can use

PIPEPHASE to investigate the effects of lift gas on well production

and optimize the allocation of limited lift gas for multiple wells.

Sphering or Pigging is used to increase gas flow efficiency in wet

gas and gas dominated multiphase pipelines.

Piping Structure

Before providing input problem data to PIPEPHASE, it is important

that you convert the structure of the piping system into a simpler

schematic representation of the relevant nodes (i.e., sources,

junctions, and sinks) and links. You must label each node and link

both uniquely and logically for future reference.

What PIPEPHASE Calculates

PIPEPHASE solves the equations that define the relationship

between pressure drop and flowrate. PIPEPHASE can also

calculate heat losses and gains.

With a single link, PIPEPHASE will calculate the pressure drop for

a known flowrate. Alternatively, for a given pressure drop,

PIPEPHASE will calculate the flowrate.

With a network configuration, you may supply a combination of

known flowrates and pressures at sources and/or sinks and

PIPEPHASE will calculate the unknowns. The combination of

knowns that you are allowed to supply are explained later on.

Rating, Design, Case Studies, and Nodal Analysis

PIPEPHASE works in both rating and design modes. In rating

mode, you supply data about the pipes, fittings and equipment and

PIPEPHASE calculates the pressure and temperature profiles. In

design mode, PIPEPHASE calculates line sizes. Case Studies can

be performed in either mode. Nodal Analyses can be performed on

single links.


Global Settings

Before you provide PIPEPHASE with information about the fluid

and piping structure of your problem, global parameters may be set

and the problem definition described. Choices can be made on

control of the simulation, define the input units, specify how much

output you want, and set global defaults for use throughout the

simulation.

Units of Measurement

PIPEPHASE allows you to construct a group of units of measure

(or dimensions) which are to be used throughout the entire

simulation input. However, you can locally override individual

units of measure where necessary. The output will always be in the

units supplied on the Input Dimensions window, unless specific

output overrides or supplements are provided on the Output

Dimensions window.

To provide... See...

Descriptive text You can further describe the problem using up to four lines of 60 characters each. This description appears once at the top of each page.

Simulation Description

If you are using the Case Study facility, you may add one line of description for each case study. You will find further details about case studies later in this chapter.


If you are using the Nodal Analysis facility, you may add two lines of description, one for inflow and one for outflow. You will find further details about nodal analysis later in this chapter.


Input data

checking

You may use PIPEPHASE just to check your input syntax and topology and not to perform any calculations.

Run Simulation and View Results

To provide... See...

Input units Global units of measurement are defined at the beginning of the input. PIPEPHASE has four pre-selected sets for user convenience: Petroleum, English, Metric, and SI. You should select the set closest to your requirements. You can then re-define units of measurement either globally at the start of the input or individually when you supply the data. If you do not select a set, PIPEPHASE defaults to the Petroleum set.

Input Dimensions


Printout Options

PIPEPHASE generates a great deal of data during its calculations.

The default printout is normally sufficient for most engineering

applications. You may increase or decrease the amount of output

depending upon your requirements.

Defaults

Many of PIPEPHASEs data items are defaulted. If you do not

explicitly specify an item or a calculation method, the program will

automatically assign a value or method. These values for example

29 BTU/hr-ft-oF for pipe thermal conductivity and the Moody

method for single-phase pressure drop calculations have been

selected to be reasonable for normal engineering purposes, but are

not necessarily the best for your particular application. They are

there for your convenience and are not intended to replace

engineering judgement. You should check that you do not get

invalid results through their use.

To set the... See...

Output units The default units of measurement for output are the same as those defined globally for the input. You may define a separate set of units for the output.

Output Dimensions

Input reprint You will always get a reprint of your input file. PIPEPHASE then reprints its interpretation of the input. You may suppress this interpretation for the output.

Print Options

Iterative results

During solution of a network, PIPEPHASE iterates until it converges to within the set tolerance. You can request a printout that shows intermediate results. This can be useful in helping converge large or sensitive networks.

Print Options

Flash results In a compositional run, PIPEPHASE prints out phase equilibrium details and the properties of the phases at each node. This output can be suppressed.

Print Options

Devices You can request a range of detail for different devices. In addition, special outputs are produced for sphering.

Print Options

Properties output

PIPEPHASE can output all properties used in the detailed calculations.

Print Options

Plotting options

In addition to tabular data, plots of pressure and temperature versus distance may be requested. The Taitel-Dukler flow regime map may also be produced for links operating in two-phase flow. Phase Envelope and Nodal Analysis plots may also be generated.

Print Options

Results Access System (RAS)

Using the PIPEPHASE RAS, you may examine data that have been produced by a run of the program. You may also print or plot the results using EXCEL.

PIPEPHASE RAS Main Window

Optimizer Output

You can set the printout level of optimizer cycle results and control the output of the intermediate results.

Print Options


For convenience, PIPEPHASE allows you to change some defaults

globally at the start of the input.

Defining Fluid Properties

PIPEPHASE requires the properties of the fluid to calculate

pressure drops and heat transfer, and phase ratios. There are two

major classifications of fluid models: compositional and non-

compositional.

A fluid model is compositional when it can be defined in terms of

its individual components either directly or through an assay curve.

PIPEPHASE will then predict the fluids properties by applying the

appropriate mixing rules to the pure component properties. Unless

PIPEPHASE is instructed otherwise, it will perform phase

equilibrium calculations for the fluid and determine the quantity

and properties of the liquid and vapor phases.

A fluid model is non-compositional when it is defined with average

correlated properties.

To define... See...

Flow device parameters

You can specify global values for the pipe, riser, tubing and annulus inside diameter, the surrounding medium, and the parameters associated with pressure drop and heat transfer. You can override these settings for individual pipes.

Global Defaults

Heat Transfer You can define the heat transfer from pipes, risers, tubings, and annuli as an overall coefficient or by defining the parameters - viscosity, conductivity, velocity, etc. - for the surrounding soil, air, or water. You can select a medium and optionally override these settings for individual pipes. You can globally suppress heat transfer calculations and then reinstate them for individual pipes, risers, tubings, and annuli.

Global Defaults

Pressure drop methods

You can globally set the pressure drop method and the Palmer parameters for liquid holdup. You can override the pressure drop method for individual pipes, risers, tubings, and annuli.

Global Defaults

Transitional flow

You can globally set the transitional Reynolds Number between laminar and turbulent flow regimes.

Global Defaults

Limits You can change the maximum and minimum values of temperature and pressure for flash calculations. If the program detects conditions outside these limits, warning messages will be presented in the output.

Global Defaults


Defining Properties for Compositional Fluids

PIPEPHASE requires thermodynamic and transport properties to

calculate phase splits, pressure drops, and heat transfer.

All required properties of compositional fluids are predicted from

the properties of the pure components. These are mixed to get the

properties of the fluid.

There are three methods for defining a component:

Selecting individual components from the PIPEPHASE library,

Defining individual components as petroleum pseudocomponents,

Defining an assay curve and having PIPEPHASE divide it into petroleum cuts.

The compositional fluid can be defined in terms of any combination

of these options. You can have different compositions at each

source.

Water as a Special Component

PIPEPHASE can rigorously predict phase separations involving

more than one liquid phase. However, there is a simplified way of

dealing with water in hydrocarbon systems. Because water is only

sparingly soluble in oil, a hydrocarbon system with a significant

amount of water will often form two liquid phases. PIPEPHASE

will handle calculations involving water in hydrocarbons by one of

three methods:

Rigorous three-phase flash to calculate composition in three phases.

It can calculate the solubility of water in the hydrocarbon phase and put the excess water into a pure aqueous phase. All the

aqueous phase properties will be calculated separately from

those of the hydrocarbon phase.

It can assume that the water is completely soluble.

Library Components

The SIMSCI library contains over 1700 components. A full list is

available in the SIMSCI Component and Thermodynamic Data

Input Manual. For all components, the databank contains data for

all the fixed properties and temperature-dependent properties

necessary to carry out phase equilibrium calculations. For all


common components, the databank also contains a full set of

transport properties necessary to carry out pressure drop and heat

transfer calculations. If you need to supplement the data, or override

the library data with your own, you may do so.

Non-library Components

You may use components not found in the SIMSCI library. You

must input all the necessary data for thermodynamic and transport

properties. If you need help in determining data for such

components, you may use SIMSCIs DATAPREP program.

Petroleum Pseudocomponents

To define hydrocarbon pseudocomponents, you must supply at least

two of the following three parameters:

Molecular weight

Gravity

Normal boiling point

PIPEPHASE will predict the third if you omit it. PIPEPHASE uses

industry-standard characterization methods to predict all fixed and

temperature-dependent property data for each pseudocomponent.

You may select the method most suitable for your own mixture.

To specify... See...

Library components

All fixed property data may be accessed from the SIMSCI databank. All you need to do is supply the name of the component.

Component Data, Library Component Data

You may override the SIMSCI constant properties for any or all of the components.

Component Data, Edit Library Component

You may override the SIMSCI variable (temperature-dependent) properties for any or all of the components.


Non-library components

If you want to use a component that is not in the SIMSCI Bank, you must supply its name and all the required properties.


To supply ... See...

Pseudocomponents

Define petroleum pseudocomponents by supplying at least two of the following: molecular weight, gravity, and normal boiling point.

Component Data, Library Component Data

Property calculation methods

You may select the method PIPEPHASE will use to calculate the properties of your pseudocomponents.

Component Data


Assay Curve

If your fluid is defined by an assay curve (TBP, D86, D2887, or

D1160), PIPEPHASE will divide it into a number of cuts. You can

control the number of cuts and the ranges they cover. Each of the

cuts is then treated as a pseudocomponent, as described previously.

You may also define a lightends analysis to go with the assay curve.

Additional Component Capabilities

All the features of SIMSCIs industry-standard component property

databank and methods have been incorporated into PIPEPHASE.

These are summarized in Table 1-3. For details of these methods

and their applicability, please consult the SIMSCI Component and

Thermodynamic Data Input Manual, in the chapter detailed below.

Fixed Property Data

You can supply your own fixed property data to override the data that PIPEPHASE predicts.

Component Data

Variable Property Data

You can supply your own temperature-dependent property data to override the data that PIPEPHASE predicts.

Component Data


Assay Data You supply an assay curve, and PIPEPHASE will divide it into petroleum cuts. You supply it in the form of D86, D1160, D2887, TBP, or TBP at 10 mm Hg curves.

Component Data

You must also supply gravity as API or specific gravity or UOP K-factor either as a curve against percent vaporized or as an average value.

Component Data

PIPEPHASE will calculate molecular weight data, or you may supply it as an average or a curve against percent vaporized.

Component Data

You may define the number of petroleum fractions to be generated and their temperature ranges.

Component Data, Temperature Cut Points

You may select the method PIPEPHASE will use to calculate the properties of the generated petroleum fractions.

Component Data

Mixed component types

You can mix defined components and pseudocomponents with assay data by defining a lightends composition and rate for each source.

Component Data



Thermodynamic Properties and Phase Separation

PIPEPHASE can use a generalized correlation, an equation of state,

or a liquid activity method to calculate thermodynamic properties at

the flowing conditions and hence predict the split between the

liquid and vapor phases. The choice of the thermodynamic property

calculation method depends on the components in the fluid and the

prevailing temperatures and pressures. PIPEPHASE also provides a

number of methods that can rigorously calculate vapor-liquid-liquid

equilibrium.

Table 1-4 gives recommendations for the commonly found pipeline

systems.

Table 1-3: Summary of Other Component Property Options

Synthetic Components

You may characterize a component as a synfuel of a specific type or as a mixture of different petroleum types.

Chapter 1

Other fixed property requirements

Rackett parameter is required for the Rackett method for liquid densities.Dipole moment and Radius of gyration are required for the Hayden-OConnell method for vapor properties.Hildebrand solubility parameter and liquid molar volume are required for various generalized and liquid activity thermodynamic correlations. Van der Waals area and volume are required for UNIFAC and UNIQUAC liquid activity thermodynamic correlations.

Chapter 1

Properties from Structure

You may define the structure of non-library components for use with the UNIFAC thermodynamic method.

Chapter 1

Table 1-4: Recommended Methods for Thermodynamic Properties

Method

Property Heavy Hydrocarbon Systems

Light HydrocarbonSystems

Natural GasSystems

K-value Braun K10 (


Transport Properties

The SIMSCI databank contains pure component data for the

thermal conductivity, surface tension, and viscosity of liquids and

vapors as functions of temperature. You can choose to use these

data and simple mixing rules to predict the flowing properties of the

fluid.

Alternatively you can choose to use the API Data Book property

prediction methods and mixing rules for mixed hydrocarbons.


K-values, enthalpy, density

You must select a thermodynamic method for calculating the vapor-liquid equilibrium and mixture properties from component properties. Either select a system with a predefined method for each property, or select an individual method for each property.

Thermodynamic Methods

Vapor-liquid-liquid equilibria

You can specify a VLLE thermodynamic system or K-value method or specify a second LLE K-value method.


Different enthalpy methods for liquid and vapor

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


Different density methods for liquid and vapor

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


Aqueous phase enthalpy

If you have water in a hydrocarbon system, you may select a method for calculating aqueous liquid and vapor enthalpies either by a simplified method which assumes that the steam is at its saturation point or by a rigorous method which takes into account the degree of superheat of the vapor, if any.


Binary interaction parameters

For some systems, notably close-boiling mixtures, the standard equations do not adequately reproduce experimental phase equilibria data. You may improve the predictability of many of the equations of state, or liquid activity coefficient methods by inputting your own binary interaction parameter values. For example, you can tune the PR, SRK, BWRS and LKP equations.



Some 60 of the bank components have data for viscosity and

thermal conductivity from the GPA TRAPP program. If you choose

to use the TRAPP data, all of your components must be TRAPP

components and you cannot have any pseudocomponents or assay

data.

Using Multiple Methods

In most cases, a single set of thermodynamic and transport methods

is adequate for calculating properties of all sources. However, your

flowsheet may contain sources with widely varying compositions or

conditions such that they cannot be simulated accurately using just

one set. For this, you may define more than one set of methods

(there is no limit) and apply different sets to different sources.


Prediction methods

You may choose a method for calculating bulk transport properties from component properties. Select a system with predefined methods for each property, or select an individual method for each property.


Overriding viscosity

To override the mixture liquid viscosity predictions, you may supply a liquid viscosity curve for either the hydrocarbon liquid phase, the water phase or the total liquid. A different viscosity curve may be supplied for each source.

Thermodynamic Methods, User Viscosity Data


More than one thermodynamic set

For each set use a separate METHOD statement. Name the set using the SET keyword.

Fluid Property Data, Thermodynamic Methods

The set used by a source

Link the source to the thermodynamic set using the SET keyword.

Compositional Source

A default thermodynamic set

When a single set is present, all sources use that set. If you do not link the source to a thermodynamic set, it will use the default set. Normally this is the first set that appears in the input. You can stipulate that another set is the default, by setting that set as the default.



Additional Thermodynamic Capabilities

All of SIMSCIs industry-standard thermophysical property

calculation methods have been incorporated into PIPEPHASE.

These are summarized in Table 1-5. For details of these methods

and their applicability, please consult Chapter 2 in the SIMSCI

Component and Thermodynamic Data Input Manual.

Defining Properties for Non-compositional Fluids

A non-compositional fluid model must be defined as blackoil, gas

condensate, liquid, gas, or steam. Blackoil and gas condensate are

two-phase, with one phase dominant. Gas and liquid fluid models

are single-phase. Steam may be single- or two-phase.

Table 1-5: Summary of Other Thermodynamic Options

Generalized Correlations

Grayson-StreedImproved-Grayson-StreedGrayson-Streed-ErbarBraun-K10

Chao-SeaderChao-Seader-ErbarIdeal

Equations of State

Soave-Redlich-KwongSRK-Kabadi-DannerSRK-Huron-VidalSRK-Panagiotopoulos-ReidSRK-ModifiedSRK-SIMSCISRK-Hexamer

Panagiotopoulos-ReidPeng-RobinsonPR-Huron-VidalPR-Panagiotopoulos-ReidBWRSUniwaals

Liquid Activity Methods

Non-random Two-liquid EquationUniversal Quasi-chemical (UNIQUAC)van LaarWilsonMargulesRegular Solution TheoryFlory-Huggins Theory

Universal Functional Activity Coefficient (UNIFAC)Lyngby-modified UNIFACDortmund-modified UNIFACModified UNIFAC methodFree volume modification to UNIFACIdeal

Special Packages

GlycolSourGPA Sour Water

AmineAlcohol

Other Features

Heat of MixingPoynting Correction

Henrys LawAmine Residence TimeCorrection

To... See...

Define the fluid You must tell PIPEPHASE the type of fluid you have; blackoil, gas condensate, liquid, gas, or steam.

Simulation Definition

Supply different data for different sources

You may supply specific gravities for each source.

Source


Liquid

All properties of a non-compositional liquid are calculated by

PIPEPHASE from the specific gravity and built-in correlations.

Gas

All properties of a non-compositional gas are calculated by

PIPEPHASE from the specific gravity and the built-in correlations.

To... See...

Define the liquid You must define the liquid as water or hydrocarbon, and supply its gravity. If the liquid is water, the specific gravity must be 1.0 or greater. For liquid hydrocarbon, the specific gravity must be less than 1.0.

Single Phase Liquid PVT Data

Specify the viscosity method

You may define the method that PIPEPHASE uses to predict non-compositional liquid viscosity.


Override viscosity data

You may supply liquid viscosity data to override the internally predicted data. You may define the viscosity as a single value or as a two-point viscosity curve.


Specify the specific heat

You may supply a single constant value for liquid specific heat to override the internally predicted data.


To... See...

Define the gas A non-compositional gas is defined in terms of its gravity, and PIPEPHASE will use the appropriate correlations to predict its properties.

Single Phase Gas PVT Data


You may define the method that PIPEPHASE uses to predict non-compositional gas viscosity.


Define the Cp/Cv ratio

A gas specific heat ratio may be defined to override the internal value used as default.


Define a contaminant

One or more of the following gas contaminants may also be defined: nitrogen, carbon dioxide, or hydrogen sulfide.


Supply the gasZ-factor

The method that PIPEPHASE uses to predict a non-compositional compressibility factor may also be defined.



Steam

Steam is a non-compositional fluid that is allowed to exist in two

phases. You cannot override the steam table data contained within

PIPEPHASEs data libraries. However, all pressure drop

correlations which are available to compositional fluids are also

available to the steam model.

Gas Condensate

Gas condensate is a multiphase non-compositional fluid with gas

predominating. All properties of gas condensate are calculated by

PIPEPHASE from the specific gravity and the built-in correlations.

Blackoil

Blackoil is a multiphase fluid model which predicts properties from

the gas gravity, oil gravity, and the standard volume of gas per

standard unit volume of oil.

To... See...

Use the steam tables

If the fluid is steam, use PIPEPHASE s internal steam tables. You may specify that the gravity of the condensed water is more than 1.0 to take into account dissolved solids.

Stream PVT Data

Specify saturated steam

You may specify steam quality if the steam is saturated. Specify the temperature and quality if the steam is superheated or the water is subcooled.

Source

To... See...

Define the condensate

A gas condensate is defined in terms of its gravity, and PIPEPHASE will use the appropriate correlations to predict its properties.

Gas Condensate PVT Data

Define the specific gravity

You must supply specific gravity data for gas, liquid and water phases, even if you do not expect them all to be present.





To... See...

Define the Blackoil

Blackoil is defined in terms of the gravity of its oil and gas and the Gas to Oil ratio. PIPEPHASE will use the appropriate correlations to predict its properties.

Blackoil PVT Data

Define the specific gravity

You must supply specific gravity data for gas, liquid, and water phases, even if you do not expect them all to be present.

Blackoil PVT Data


Defining Properties for Mixed Compositional/Non-Compositional Fluids

PIPEPHASE offers the user the ability to define blackoil models

that combine data from:

sources that are in the standard black oil format (see description of blackoil inputs),

with

sources that are in the standard compositional format (see description of compositional inputs).

PIPEPHASE treats the combined fluid model as a blackoil model;

flash calculations are used to define the appropriate blackoil

properties for the compositional sources. The inputs to the

compositional blackoil model are thus a combination of the inputs

to separate compositional and blackoil models.

Define the viscosity

You may optionally enter liquid viscosity data in the form of a two-point Antoine curve.

Blackoil PVT Data



Blackoil PVT Data

Adjust properties You may adjust the properties that PIPEPHASE calculates from its built-in correlations so that they more closely fit measured laboratory data.

Blackoil PVT Data

Define Lift Gas When you have a GLVALVE in the simulation, you need to define the lift gas in terms of Gravity and (optionally) contaminants.

Blackoil Liftgas Data

Tabular Data If laboratory data are available, you may input them and override the PIPEPHASE internally generated data. If you use tabular data, you must input all data: Formation Volume Factor, Solution Gas Oil Ratio, Live Viscosity, and Gravity.

Blackoil PVT Data

Supply the gas Z-factor

The method that PIPEPHASE uses to predict a non-compositional compressibility factor may be defined.

Blackoil PVT Correlations Data


You may define the method that PIPEPHASE uses to predict viscosities and blending rules.


Specify formation volume factor and solution gas oil ratio methods

You may define the methods that PIPEPHASE uses to calculate formation volume factor and solution gas oil ratio.


To... See...


Generating and Using Tables of Properties

For large scale compositional or blackoil simulations, a table of

fluid properties can be built and used. This will reduce the

computation time by phase separation calculations during the

solution procedure. This method is applicable if all the sources in

the network have the same composition or Blackoil properties.

Sources

A source is a point at which fluid enters the piping system. You

define a source by supplying parameters such as composition,

temperature, pressure, and flowrate. You can have more than one

source in a network.

Compositional Sources

To... See...

Build and use a table

You can have PIPEPHASE build the table and use it in the same run.

Generate PVT Table

Retrieve a table

Alternatively, you can have PIPEPHASE build the table, store it in a file, and then use it in a subsequent run. PIPEPHASE will not build a table for use in the same run while also storing it for a subsequent run.

Fluid Property Data


Defined components

You must define the total flowrate and composition of the source stream. Components can be either from the PIPEPHASE component library or defined as pseudocomponents.


Assay data A source fluid may be defined by an assay curve. You can combine library components and/or petroleum pseudocomponents with an assay curve by supplying a lightend analysis.


Viscosity data

To override the internally generated fluid viscosity data, you may specify a viscosity curve in the PVT data section.


Similar sources

To reduce redundant data entry, you may refer to a predefined source. Parameters may be specified to override the parameters that are different.



Non-compositional Sources

Structure of Network Systems

Flow devices such as pipes, risers, fittings, and other process

equipment are connected together in a Link. Each Link starts at a

Node (a Source or a Junction) and ends at another Node (a Junction

or a Sink).

PIPEPHASE can calculate either single link or network problems.

A single link is defined as a series of pipes, fittings, and process

equipment that has one source, one sink, and no junctions. A

network may have one or more sources and one or more sinks.

PIPEPHASE calculates the flowrates and pressure drops. In a

network configuration, you must either define these parameters or

provide an estimate at each node.


Steam sources

You must define the pressure and quality of a saturated steam source. The temperature must be specified only if the steam is superheated (Quality=100%) or subcooled (Quality=0%).

Steam Source

Gas, liquid, blackoil or condensate sources

One or more sets of fluid property data are defined in the PVT data section. You must assign a unique set number to each data set. Each source must be referred to the appropriate data set number.

Blackoil Source

Well In-flow Performance

You may specify the IPR of a well source for a single link with gas, liquid, blackoil or condensate. The IPR Model is treated as a device and is available from the Link window. You may also supply well test data.

Link Device Data, Inflow Performance Relationship, IPR-Advanced Options

Similar sources

If one source is the same as or similar to another, you may refer it to the other source. PIPEPHASE will copy all the data from one source to the other. You may then override the parameters that are different.

Reference Source


Network solution algorithm

There are two solution algorithms available for Networks. For the vast majority of networks, you would use the default PBAL method. If your fluid is a single-phase liquid or gas, you may find that the MBAL method (with simple estimates) gives a faster solution.

Network Calculation Methods


Controlling Convergence of Networks

PIPEPHASE solves networks iteratively. Whichever algorithm you

use, PIPEPHASE starts with an initial estimate of flowrates in all

links and pressures at all nodes and it adjusts these values until it

has reached a converged solution within a predefined tolerance.

Because of the complex nature of some networks, PIPEPHASE

allows you to make adjustments to several parameters that helps to

modify the iteration steps and stabilize the convergence.


Automatic generation of Initial estimates

PBAL has a choice of methods for generating initial estimates. By default, PBAL generates flowrate estimates by considering the diameters of the first pipe in each link. An alternative method uses the frictional resistances of the pipes in each link. A third method solves the first iteration with MBAL before going into PBAL. Finally, if you have solved this network before and just changed some of the conditions, you may instruct the program to use your previous solution as its initial estimate.


User-supplied initial estimates

You may also provide individual estimates for junction pressures and link flowrates.

Junction,Link Data

Maximum and minimum flows

For any link, you may specify the maximum and minimum flows that are to be allowed.

Link Data

Controlling convergence

In some difficult networks, convergence of the base case can be improved by adjusting various convergence parameters: for example, damping, relaxation, internal tolerances, etc. Refer to Chapter 6, Technical Reference in the PIPEPHASE Keyword Manual, for details.


Direction of flow If you know the flow direction in all links, you can specify that PIPEPHASE not try to reverse them from iteration to iteration.


Solution tolerance

The network calculation converges when the error is within a given tolerance. You may optionally change this tolerance.


Controlling optimization

You can adjust a number of optimization options: for example, the fractional change in the objective function or decision variables, damping, or error tolerances.

Optimization Options

Calculation time If PIPEPHASE does not converge within a certain number of iterations, it will stop and report the results of the last iteration. You may reduce or increase the maximum number of iterations. To reduce calculation time in large compositional runs, you may control the number of fluid property evaluations that are performed in each link for the PBAL initialization procedure.

Network Calculation Options


Single links

A single link has one source, one sink, and no junctions. There are

three variables:

The source flowrate (which is also the sink flowrate),

The source pressure, and

The sink pressure.

You must specify two of these, and PIPEPHASE will calculate the

third.

Closed loops If you have inadvertently specified your network so that closed loops are formed, PIPEPHASE will report these and, optionally, take remedial action.

Network Convergence Data

Pipe segments Pipes, tubing, risers, and annuli are divided into segments for pressure drop and heat transfer calculations. You can change either the number of segments or the length of segments for greater calculational accuracy. Alternatively, you can select PIPEPHASEs autosegmentation feature to automatically select the best segmentation options for your network.

Network Segmentation Data

Check valves You may allow regulators (unidirectional check valves) to pass a small backward flow.


Critical flow in chokes

Critical flow in chokes can cause difficulties for convergence algorithms. To help PIPEPHASE solve such networks, you can allow or a linear broadening of the critical flow regime.

Network Convergence Data

Wells You can prevent well flows from falling below the minimum required to transport fluid in a two-phase system.



Sources You must have only one source. Source

Sinks If the source pressure and rate are known, a sink pressure and rate need not be defined.

Sink, Source

Links You do not need to specify the flowrate or pressure drop in a link; all you need to define are the pipes, fittings, and equipment. Enter the link device data in the sequence in which the fluid flows through them. You can have any combination of pipes, fittings, and process equipment items, in any order.

Link Device Data



Networks

A network generally has more than one link and one or more

junctions. The variables are the pressure and flowrate at each source

and sink. You specify the values of the variables that are known,

and PIPEPHASE will calculate the unknowns. In order not to

under- or over-specify the system, simple rules must be followed in

constructing the problem:

You must specify a number of knowns equal to the total num-ber of sources and sinks.

You must specify at least one pressure.

If any source or sink flowrate is an unknown, you must supply an estimate.

If you do not know a pressure at a source, sink, or junction, you do not need to supply an estimate. You may specify estimates

to speed up convergence.

PIPEPHASE Flow Devices

A piping system is made up of links which join sources, sinks, and

junctions. Each link consists of a series of flow devices: pipes,

fittings, and process equipment and unit operations.

Sources and sinks must be named.


Sources and sinks

You must have at least one source and at least one sink.

Source, Sink

Junctions You must have a junction at the point where two or more links meet. If your network is complex, you may speed up the solution by supplying estimates for the junction pressures.

Junction

Links You must supply a unique name for each link. If your network is complex, you may speed up the solution by supplying estimates for flowrates through each link.

Link Device Data

Steam networks

PIPEPHASE can model preferential splitting at Tee junctions in pure distribution networks. These junctions can have only two outgoing and one incoming link.

Junction

Subnetworks PIPEPHASE has a number of devices that invoke a special algorithm. You may specify the inlet conditions; PIPEPHASE breaks the flowsheet at the inlet and solves the resulting subnetworks simultaneously and sizes the device.

Mcompressor, Mchoke Mregulator


The devices in the link must be added in the order in which they

occur in the link as you move from the From node to the To

node.

The flow devices that PIPEPHASE can handle are given in

Table 1-6.

Table 1-6: Flow Devices and Equipment Available in PIPEPHASE

Device Description

Flow Devices - have length

Pipe Horizontal, vertical or inclined. May be surrounded by air, water, or soil; insulated or bare.

Riser Vertical or near-vertical with flow in an upward direction. Heat loss is simulated using an overall heat transfer coefficient between the fluid and ambient conditions.

Annulus Well annulus. Heat loss is simulated using an overall heat transfer coefficient and geothermal gradient.

Tubing Well tubing. Heat loss is simulated using an overall heat transfer coefficient and geothermal gradient.

Inflow Performance Relationship

Models the relationship between flowrate and reservoir pressure draw-down or pressure drop at the sand face in a well.

Point Devices - have no length

Completion Bottomhole completion, the interface between the reservoir and a well. There are two types of completion: gravel-packed and open-perforated.

Fittings

Bend A standard mitred bend or non-standard bend with defined angle and radius.

Check valve Device that allows flow in only one direction.

Choke valve Restricts fluid flow. MCHOKE, a variant of CHOKE, introduces a discontinuity into a network which is solved using a special sub-networking method.

Contraction Reduction in diameter from larger to smaller pipe. Variable angle.

Entrance Entrance into a pipe from a larger volume such as a vessel.

Exit Exit from a pipe to a larger volume such as a vessel.

Expansion Increase in diameter from smaller to larger pipe. Variable angle.

Nozzle Flow restriction used in metering.

Orifice Orifice meter. Orifice plate can use thick or thin calculation formulae.

Tee Tee piece. Flow may be straight on or through the branch.


Pressure Drop Calculations

PIPEPHASE calculates pressure drops for pipes, risers, annuli and

tubings. There are many methods for calculating pressure drops.

You can define one method globally for use throughout the

simulation, or you can use different methods in different pipes.

Valve Any type of valve, e.g., gate, globe, angle, ball, butterfly, plug, cock.

Venturimeter Venturi flow meter.

Process Equipment

Compressor Simple single or multistage gas compressor.

MultistageCompressor

Rigorous single or multistage gas compressor with optional inlet pressure calculation. Uses a special sub-networking method.

Cooler Removes heat from a stream.

DPDT Any device that changes pressure and/or temperature with flowrate.

Expander Steam expander.

Gaslift Valve Well gaslift valve.

Heater Adds heat to a stream.

Injection Re-introduces a stream from a compositional separator back into a link.

Pump Single or multistage liquid pump. An electric submersible pump may be modeled.

Regulator Means of fixing maximum pressure at any point in the structure. MREGULATOR, a variant of REGULATOR, introduces a discontinuity into a network which is solved using a special sub-networking method.

Separator Splits some or all of one of the fluid phases from a link.

Unit Operations

Hydrates Predicts the temperature/pressure regime under which hydrates are prone to form.

Calculator A utility that allows you to compute results from flowsheet parameters. These results can then be used as optimizer constraints or objective parameters.


Pressure drop method

Choose a method appropriate to the type of fluid and piping topology you have. If you do not choose a method, PIPEPHASE will use Beggs & Brill-Moody for compositional, blackoil, condensate, or steam and Moody for non-compositional fluids.

Pressure Drop Flow Correlations

Table 1-6: Flow Devices and Equipment Available in PIPEPHASE

Device Description


Table 1-7 lists the pressure drop methods recommended for

multiphase flow in horizontal and inclined pipes.

You may choose a different method for an individual device. If you do not choose a method for a device, PIPEPHASE will use the method you selected globally.

Pressure Drop Flow Correlations

Table 1-7: Applicability of Multiphase Flow Correlations

Pipe

Method Horizontal and Inclines


Pressure Drop in Flow Devices

The pressure drop in a flow device (Pipe, Riser, Tubing or Annulus)

of length L consists of three components: friction, elevation, and

acceleration.

In general, the frictional pressure gradient may be expressed as:

where:

The friction factor, f, is inversely proportional to the Reynolds

number for laminar flow. For turbulent flow, f is a non-linear

function of the Reynolds number and the pipe roughness.

In general, the elevation pressure gradient may be expressed as:

where:

The acceleration pressure gradient is generally small, except when

the fluid is compressible, and the velocity and velocity gradients in

the pipe are high. In general, the acceleration pressure gradient may

be expressed as:

where:

1. In general, this method is recommended because it performs reasonably well for the widest range of flow condition.

2. This method is recommended for pipelines with low liquid holdup in hilly terrain.3. These non-standard hybrid models should be used only after matching measured data.4. These models are available as add-ons through your SIMSCI representative.

Legend: X Correlation recommended for the applicationX Correlation allowed but not recommended for the application

= fluid density

q = volumetric flux

d = equivalent diameter

(= actual diameter in the case of pipes, risers and tubing)

r = fluid density = inclination angle

v = fluid velocity

Table 1-7: Applicability of Multiphase Flow Correlations

dP

dL-------

f

fq2d5

-----------

l

dP

dL-------

e

( )sin

dP

dL-------

a

ddx------


Nominal Diameter and Pipe Schedule

As an alternative to entering a pipe (or riser or tubing) inside

diameter you can specify a nominal diameter and a schedule.

PIPEPHASE has an internal database of standard nominal pipe

sizes and pipe schedules; the allowed combinations of nominal

diameter and schedule in this database are detailed in Table 1-8.

You may supply your own database which PIPEPHASE will use

instead of its own.


Inside diameter and roughness

If the majority of your devices have the same inside diameter, you can specify a global inside diameter at the start of the simulation. Then you can override this value for those devices which do not conform to the default. Roughness can be specified also as a global parameter or for each device.

Diameter Defaults

Inclined pipes You can specify an elevation change or depth for each device If the elevation change equals the length, the device is vertical. If you do not specify an elevation change, PIPEPHASE assumes that pipes are horizontal and that risers, annuli, and tubings are vertical.

Pipe Riser Annulus Tubing

Acceleration terms

You may instruct PIPEPHASE to ignore the acceleration term in pressure drop calculations, if desired.

Calculation Speedup Options

To specify nominal diameter and schedule for... See...

All devices as a global value

You may supply a nominal diameter and schedule that will be used for all the fittings in this table, unless overridden by data in the input to the fitting itself.

Flow Devices Database Definition

Your pipes and fittings

You may create a database of nominal diameters and pipe schedules and have PIPEPHASE use it instead of its own internal database

Flow Devices Database Definition

Pipe You may supply a nominal diameter and schedule. Pipe

Riser You may supply a nominal diameter and schedule. Riser

Tubing You may supply a nominal diameter and schedule. Tubing

Bend You may supply a nominal diameter and schedule. Bend

Entrance You may supply a nominal diameter and schedule for the downstream pipe.

Entrance

Exit You may supply a nominal diameter and schedule for the upstream pipe.

Exit

Nozzle You may supply a nominal diameter and schedule for the upstream pipe.

Nozzle

Orifice You may supply a nominal diameter and schedule for the upstream pipe.

Orifice


Allowable Pipe Nominal Diameters and Schedules

Tee You may supply a nominal diameter and schedule for the upstream pipe.

Tee

Valve You may supply a nominal diameter and schedule for the upstream pipe.

Valve

Venturi You may supply a nominal diameter and schedule for the upstream pipe.

Venturi

Contraction You may supply a nominal diameter and schedule for the inlet and outlet pipes.

Contraction

Expansion You may supply a nominal diameter and schedule for the inlet and outlet pipes.

Expansion

Table 1-8: Allowable Pipe Nominal Diameters and Schedules

Nominal Diameter (Inches)

Valid Pipe Schedule Numbers

0.125 40 80

0.250 40 80

0.375 40 80

0.5 40 80 160

0.75 40 80 160

1.00 40 80 160

1.25 40 80 160

1.5 40 80 160

2.0 40 80 160

2.5 40 80 160

3.0 40 80 160

3.5 40 80

4.0 40 80 120 160

4.5 40

5.0 40 80 120 160

6.0 40 80 120 160

8.0 20 30 40 60 80 100 120 140 160

10.0 20 30 40 60 80 100 120 140 160

12.0 20 30 40 60 80 100 120 140 160

14.0 10 20 30 40 60 80 100 120 140 160

16.0 10 20 40 60 80 100 120 140 160

18.0 10 20 30 40 60 80 100 120 140 160

20.0 10 20 30 40 60 80 100 120 140 160

To specify nominal diameter and schedule for... See...


Pressure Drop in Completions

Bottomhole completion describes the interface between a reservoir

and a well. There are two types of completion: gravel packed and

open perforated. The pressure drop through a completion is

calculated from permeability and other data you input.

PIPEPHASE uses the Jones model for gravel-packed completion

and the McLeod model for open-perforated completions.

Pressure Drop in Fittings

The general form of the pressure drop equation is:

24.0 10 20 30 40 60 80 100 120 140 160

30.0 10 20 30

Figure 1-9: Jones Model Figure 1-10: McLeod Model


Completion You may define a completion as being gravel packed (Jones) or open perforated (McLeod).

Gravel Packed Completion,

Open Perforated Completion

Dual Completion

You may model dual completions, both concentric and parallel.

Link Data

Table 1-8: Allowable Pipe Nominal Diameters and Schedules

Nominal Diameter (Inches)

Valid Pipe Schedule Numbers

P KG22g----------------=


where:P = pressure drop across the fittingK = resistance coefficient/ K-factor

G = mass velocity (mass flowrate/flow area) = two-phase pressure drop multiplierg = acceleration due to gravity = fluid density (equal to liquid density for two-phase flows)


Bend, Tee,Valve

PIPEPHASE uses the generalized pressure drop equation with a resistance coefficient. For bends, tees, and valves, you can either supply the resistance coefficient directly or supply an equivalent length and have PIPEPHASE calculate the resistance coefficient as a function of the friction factor.

Bend,Tee,Valve

Entrance Exit

For entrances and exits you can supply the resistance coefficient or use the default value.

Entrance,Exit

Contraction, Expansion, Nozzle, Orifice, Venturi

For contractions, expansions, nozzles, orifices, and Venturimeters, you can supply the resistance coefficient or use the value that PIPEPHASE calculates from its built-in correlations. These correlations relate the resistance coefficient to the Reynolds number and specific fitting parameters such as orifice diameter, Venturi throat diameter, contraction and expansion angles, and nozzle diameter. For gas flow in nozzles, orifices, and Venturimeters, the specific heat ratio is also used in the calculation of the resistance coefficient.

Nozzle, Expansion, Venturi, Contraction, Orifice

Choke The pressure drop for a choke is calculated by the orifice method for a single-phase fluid or by the Fortunati method for a two-phase fluid. You can supply a discharge coefficient or use the default value. MCHOKE, a variant of CHOKE which introduces a discontinuity into a network, uses the Fortunati model only.

Choke Mchoke

Check Valve A valve that permits flow in one direction only. You can supply a resistance coefficient or use the default value.

Check

Two-phase correction in fittings

The pressure drops for fittings are corrected for two-phase flow by using either the Homogeneous flow model or the Chisholm model. If you do not make a selection, PIPEPHASE will use the default method. You may supply values for the Chisholm parameters.

Bend, Exit, Entrance, Valve, Tee, Contraction, Expansion, Nozzle, orifice, Venturi


Equipment Items

PIPEPHASE simulates the change in fluid conditions across items

of process equipment that typically appears in pipeline systems.


Compressor A compressor imparts work to a gas. You supply either a known power or a known outlet pressure, and PIPEPHASE calculates the unknown parameter. You may impose a maximum value on the unknown parameter, and PIPEPHASE will constrain the calculations according to whichever parameter is limiting. Alternatively, you can supply a curve of flowrate against head. You may also supply an adiabatic efficiency as either a constant or a curve against head. The exit temperature is then determined by energy balance. If you specify more than one stage, PIPEPHASE interprets the curve to be for each stage; any maximum power you specify is over all of the stages rather than for each individual stage.

Compressor

You can also reference the compressor curve to a previously defined performance curve.

Compressor Curve Data, Compressor Performance Curves

Multispeed Compressor

You can specify different compressor curves for up to five compressor speeds.

Compressor Curve Data

Multistage Compressor

In a multistage compressor you may specify different parameters curves, efficiencies, etc. for different stages. You may have multiple compressor trains, each train with multiple stages. You may have interstage scrubbers with downstream re-injection and interstage coolers and piping losses. You may specify the compressors inlet pressure. When you do this, PIPEPHASE invokes a special algorithm which breaks the flowsheet at the compressor inlet and solves the resulting subnetworks so that the pressures match at the interface.

Mcompressor

Cooler The cooler removes heat from the system. You supply either a known exit temperature or known duty of the unit, and PIPEPHASE will calculate the unknown parameter. You may impose a maximum (for duty) or minimum (for temperature) value on the unknown parameter, and PIPEPHASE will constrain calculations according to whichever parameter is limiting.

Cooler

Steam Expander

The expander models the expansion of steam from a high pressure to a low pressure. You may specify the power required, or the pressure drop or the pressure ratio. If the unit is in a spur link, you may alternatively specify the outlet pressure.

Expander

Gaslift Valve This unit simulates the presence of a gaslift valve as part of a well link. You must define the PVT properties of the lift gas.

Gaslift Valve, Fluid Property Data


General purpose DP and DT unit

The DPDT unit is a general purpose unit for defining a pressure and/or temperature difference at a point in the piping structure. You can use this unit to model any equipment device where the pressure difference and temperature difference characteristics can be represented as curves against flowrate. You may also specify the flow versus pressure drop equation for the curve.

DPDT

Heater The heater adds heat to the system. You supply either a known exit temperature or known duty of the unit, and PIPEPHASE will calculate the unknown. You may impose a maximum value on the unknown parameter, and PIPEPHASE will constrain the calculations according to whichever parameter is limiting.

Heater

Injector The injector introduces a stream into a link. The stream comes from a separator (see the entry below). You may fix the pressure and temperature of the injected stream. The injector must be downstream of the separator and in the same link.

Injector

Pump A pump imparts work to a liquid. You supply either a known power or a known outlet pressure, and PIPEPHASE calculates the unknown. You may impose a maximum value on the unknown parameter, and PIPEPHASE will constrain the calculations according to whichever parameter is limiting. Alternatively, you can supply a curve of flowrate against head. You may also supply an efficiency as a constant or as a curve against head. The exit temperature is determined by energy balance. If you specify more than one stage, PIPEPHASE interprets the curve to be for each stage; any maximum power you specify is over all of the stages rather than for each individual stage.You can also reference the pump curve to a previously defined performance curve.

Pump

Multispeed Pump

You can specify different pump curves for up to five pump speeds.

Pump Curve Data, Pump Performance Curves

Electric Submersible Pump

An extension of the PUMP item allows you to model an electric submersible pump. In addition to all the features mentioned above, you may supply motor horsepower as a curve, either in tabular form or as coefficients of an equation. You may specify auxilliary power to be supplied to the pump. You may specify head degradation as a function of gas ingestion percentage, plus minimum submergence, casing head pressure, and vertical pressure gradient in the casing-tubing annulus due to the gas column. Refer also to Separator, below.

Electric Submersible Pump

You can also reference the electric submersible pump curve to a previously defined ESP performance curve.

Electric Submersible Pump Curve



Regulator The regulator is used to set the maximum pressure at some point in the pipeline structure. It allows flow in only one direction and can be used to prevent flow reversal within selected links in a network. As an extension to the regulator allows you to specify the inlet pressure, you may specify the compressors inlet pressure. When you do this, PIPEPHASE invokes a special algorithm which breaks the flowsheet at the compressor inlet and solves the resulting subnetworks so that the pressures match at the interface.

Regulator

Multi-network Regulator

You may specify the inlet pressure of this item. When you do this, PIPEPHASE invokes a special algorithm which breaks the flowsheet at the inlet and solves the resulting subnetworks so that the pressures match at the interface. You may also specify the flowrate through the regulator.

Regulator

Separator The separator splits out all or part of the gas or liquid phase of a multiphase fluid. In the case of a hydrocarbon system with water, you can select the hydrocarbon or aqueous phase instead of the total liquid phase. You specify the amount separated as an absolute flowrate or as a percentage of the phase. You can separate more than one phase in one separator. You can then reinject the separated streams at points downstream in the link using the Injector. You cannot impose a pressure drop on the separator.

Separator

Bottomhole Separator

If a separator is positioned at the bottomhole below an electric submersible pump, you may either specify gas injection percentage or supply pump dimensions and have PIPEPHASE calculate it.

Separator

Hydrates Hydrates are solid mixtures of water and other small molecules. Under certain process conditions, particularly in the gas processing industry, hydrate formation may clog lines and foul process equipment. The HYDRATE unit operation predicts the pressure and temperature regime in which the process is vulnerable to hydrate formation. Calculations performed assume the presence of free water for hydrates to form. Possible hydrate formers include: methane through isobutane, carbon dioxide, hydrogen sulfide, nitrogen, ethylene, propylene, argon, krypton, xenon, cyclopropane, and sulfur hexafluoride. The effect of sodium chloride, methanol, ethylene glycol, di-ethylene glycol, and tri-ethylene glycol hydrate inhibitors can also be studied.

Hydrate Unit Operation

Calculator The Calculator allows you to perform calculations on flowsheet information using FORTRAN-like syntax. The Calculator results can be transfered back to the Optimizer for use as an optimization objective parameter or constraint.

Calculator



Heat Transfer Calculations

PIPEPHASE performs an energy balance on pipes, risers, tubing,

and annuli. The heat transfer depends on the fluid temperature,

properties, and flowrate, the temperature and properties of the

surrounding medium, and the heat transfer coefficient between the

fluid and the medium. PIPEPHASE does not model heat transfer to

the surroundings for fittings and equipment devices (point devices).

The general equation for heat transfer from a flow device is:

where:

The overall heat transfer coefficient either is input or may be

calculated from the constituent film coefficients and geometries.

For risers and annuli you must specify an overall heat transfer

coefficient.

For a pipe or tubing you may supply an overall coefficient or you

may request detailed heat transfer calculations. Detailed heat

transfer calculations are invoked when you input any one of the

parameters required to carry out the calculations.

Detailed Heat Transfer in Pipes and Tubing

For a pipe surrounded by soil, water, or air, you define the medium

properties (and velocity

Pipephase UG Libre

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