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IPEPHASE, INPLANT, and SimSci-Esscor are trademarks of Invensys plc, its
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Table of Contents
Introduction
About this Manual . . . v-iii
Example Simulation Features . . . v-iv
Chapter 1 PIPEPHASE EXAMPLE
Example 1 - Liquid - Pump . . . .1-1
Simulation Model . . . .1-1
Simulation Model . . . .1-1
Input Data . . . .1-4
Case Execution . . . .1-5
Results . . . .1-6
Example 2 -Blackoil Well . . . .1-9
Simulation Objective. . . .1-9
Simulation Model . . . .1-9
Input Data . . . .1-12
Case Execution and Results . . . .1-14
Nodal Analysis Calculations . . . .1-15
Example 3 - Distillation Curve . . . .1-18
Simulation Objective. . . .1-18
Simulation Model . . . .1-18
Input Data . . . .1-20
Case Execution . . . .1-22
Results . . . .1-22
Example 4 - Gas Pipeline . . . .1-24
Simulation Objective. . . .1-24
Simulation Model . . . .1-24
Input Data . . . .1-28
Case Execution and Results . . . .1-29
Example 5 - Compositional Sub Sea Riser . . . .1-30
Simulation Objective. . . .1-30
Simulation Model . . . .1-30
Input Data . . . .1-35
Case Execution . . . .1-37
Results . . . .1-37
Example 6 - Pigging Pipeline . . . .1-39
Simulation Objective . . . 1-39
Simulation Model . . . 1-39
Input Data . . . 1-41
Case Execution and Results . . . 1-43
Example 7 - Well Test Data . . . 1-44
Simulation Objective . . . 1-44
Simulation Model . . . 1-44
Input Data . . . 1-47
Case Execution . . . 1-48
Results. . . 1-48
Example 8 - Blackoil Gathering Network . . . 1-49
Simulation Objective . . . 1-49
Simulation Model . . . 1-49
Input Data . . . 1-51
Case Execution . . . 1-55
Results. . . 1-55
Example 9 - Gas Condensate Network . . . 1-57
Simulation Objective . . . 1-57
Simulation Model . . . 1-57
Input Data . . . 1-59
Case Execution - Calculation Segment. . . 1-63
Results. . . 1-66
Example 10 - Steam Line Sizing . . . 1-67
Simulation Objective . . . 1-67
Simulation Model . . . 1-67
Input Data . . . 1-69
Case Execution . . . 1-70
Results. . . 1-70
Example 11 - Gas - Lift Manifold . . . 1-72
Simulation Objective . . . 1-72
Simulation Model . . . 1-72
Input Data . . . 1-73
Case Execution . . . 1-76
Results. . . 1-77
Example 11A - Link Groups for Subsurface Junctions . . . 1-78
Simulation Objective . . . 1-78
Input Data . . . 1-78
Results. . . 1-79
Example 12 - Nodal Analysis . . . 1-82
Simulation Model . . . .1-82
Simulation Model . . . .1-82
Input Data . . . .1-84
Case Execution . . . .1-86
Results . . . .1-86
Example 13 - Hydrate Analysis for Compositional Fluids . . . . .1-89
Simulation Objective. . . .1-89
Simulation Model . . . .1-89
Input Data . . . .1-91
Case Execution . . . .1-93
Example 14 - Choke Sizing and MChokes in PIPEPHASE . . . .1-97
Simulation Objective. . . .1-97
Simulation Model . . . .1-97
Input Data . . . .1-99
Case Execution . . . .1-100
Results . . . .1-100
Example 15 - The Gilbert Choke Model in PIPEPHASE . . . . .1-103
Simulation Objective. . . .1-103
Simulation Model . . . .1-103
Input Data . . . .1-105
Case Execution . . . .1-107
Results . . . .1-107
Example 16 - The New DPDT Device - Can be used to Model
Compressors. . . .1-108
Simulation Objective. . . .1-108
Simulation Model . . . .1-108
Input Data . . . 1-111
Case Execution . . . .1-112
Results . . . .1-112
Example 17 - Generate a Vertical Flow Performance (VFP) Table to
Represent a Well . . . .1-113
Simulation Objective. . . .1-113
Simulation Model . . . .1-113
Input Data . . . .1-115
Case Execution . . . .1-117
Results . . . .1-119
Example 18 - Using the Vertical Flow Performance (VFP) Table to
Represent a Well . . . .1-120
Simulation Objective. . . .1-120
Simulation Model . . . .1-120
Input Data . . . 1-121
Case Execution . . . 1-122
Results. . . 1-124
Example 19 - Generate PVT Data using PIPEPHASE . . . 1-126
Simulation Objective . . . 1-126
Simulation Model . . . 1-126
Input Data . . . 1-130
Case Execution and Results . . . 1-132
Example 20 - Generating Output Reports in Excel . . . 1-138
Simulation Objective . . . 1-138
Simulation Model . . . 1-138
Input Data . . . 1-140
Case Execution . . . 1-142
Results. . . 1-142
Example 21A - Manifold Junction Unit . . . 1-147
Simulation Objective . . . 1-147
Simulation Model . . . 1-147
Input Data . . . 1-153
Case Execution . . . 1-159
Results & Discussion . . . 1-160
Example 21B - Network Change Utilities. . . 1-163
Simulation Objective . . . 1-163
Simulation Model . . . 1-163
Input Data . . . 1-164
Results & Discussion . . . 1-171
Example 22 - PIPEPHASE-GEM Integration . . . 1-176
Simulation Objective . . . 1-176
Simulation Model . . . 1-176
Input Data . . . 1-179
Results & Discussion . . . 1-182
Example 23 – Long pipeline using a Drag Reduction Agent . . 1-192
Simulation Objective . . . 1-192
Simulation Model . . . 1-192
Input Data . . . 1-193
Results and Discussion . . . 1-194
Introduction
About this Manual
This manual contains examples of the use of PIPEPHASE and
illustrates many of the features of the program. It is not possible to
include every program option in the examples and a list of the
features which appear in each example is given in an easy-to-read
tabular format in Table 1-1, Table 1-2 and Table 1-3. This is where
to look if you are looking for an example which contains a specific
feature.The user is urged to read and become familiar with the
Pipephase, Netopt, Tacite User’s manual and obtain adequate
training before attempting to these examples.
The manual then details the example simulations. Each example is
comprised of five sections:
■
Simulation Objective - This section outlines the goals of the
simulation, as well as presenting some of the important
problem parameters.
■
Simulation Model - This section describes how the example is
translated into the PIPEPHASE input data.
■
Input Data - The full keyword input data file is listed in this
section.
■
Case Execution - This section describes how the example is
executed keeping the goals specified in the simulation
objective.
■
Results - For clarity, the full excel output reports are not
presented here. Instead, the link and node summaries are shown
along with selected reports which are particularly relevant to
the simulation goals given in the Simulation Objective.
Example Simulation Features
Table 1-1: Features Used in Example (1-10) Simulations
Statement
Feature
Example Number
1 2 3 4 5 6 7 8 9 10
General Data Category of Input
Pipeline
• • • • • •
• • •
Well
•
• •
CALCULATIONNetwork
•
• •
Single Link
• •
• • • •
•
Gas lift
•
PVT generation
•
Compositional
•
• •
Blackoil
•
• •
Condensate
•
Liquid
•
Gas
•
Steam
•
Isothermal
•
•
Sphering
•
FCODE
Correlations for flow
device
• •
•
• • • • •
Liquid holdup corrections
•
DEFAULT
Medium and its
parameters
•
•
•
Flow device details
•
• • • • •
•
Conductivities, insulation
thickness
•
•
SEGMENT
Horizontal and vertical
•
• • • • • •
OUTDIMENSION
Alternative output
•
•
Output options
• • • • • • • •
Plot
•
Methods Data Category of Input
SOLUTION
Pbalance method
•
• •
No flow reversals
•
TOLERANCE
Convergence tolerance
•
Individual enthalpy,
density
•
TRANSPORT
System
•
• •
Component Data Category of Input
LIBID
Library components
•
• •
PETROLEUM
Petro components
• •
CHARACTERIZE
Property method
•
•
PVT Data Category of Input
SET
Gravity
• •
•
• • •
Viscosity
•
Contaminants
•
Specific heat
•
LIFTGAS
Gravity
•
GENERATE
Property tables
•
Structure Data Category of Input
SOURCE
Set number, pressure/rate
• • • • • • • • • •
Pressure estimate
•
Ref. source
•
Temperature
• • • • • • • • •
Quality (steam)
•
Composition
• •
TBP
Assay curve
•
LIGHTENDS
Defined components in
assay
•
WTEST
Well inflow performance
relationship
•
SINK
Rate estimate
•
• •
Fixed pressure
•
•
• • •
JUNCTION
Pressure estimates
•
• •
PIPE
Length/ID
• • • • • •
• • •
Elevation change
• •
• •
•
•
Heat transfer parameters
• •
Pipe data – thickness,
conductivity
•
Sphere diameter
•
Table 1-1: Features Used in Example (1-10) Simulations
Statement
Feature
Example Number
RISER
Length/Elevation
•
ANNULUS
Depth
•
TUBING
Length, depth
•
• •
Structure Data Category of Input, continued
Detailed heat transfer
•
BEND
K or KMUL
•
•
2-phase flow model -
Chisholm or
Homogeneous
•
Non-standard
•
PUMP
Fixed power
•
CHOKE
•
COMPRESSOR Fixed pressure
•
CONTRACTION
Angle
•
COOLER
Tout
•
DPDT
Curve
•
EXIT
•
ENTRANCE
•
ORIFICE
•
TEE
•
VALVE
•
VENTURIMET
ER
CPCV
•
EXPANSION
Angle
•
COMPLETION
Gravel packed
•
MANIFOLD
Gas Lift Data Category of Input
GASLIFT
Capacity calculated
•
Sizing Data Category of Input
DEVICE
All devices
•
Casestudy Data Category of Input
CHANGE
Global
•
•
Individual
•
Sensitivity Analysis Data Category of Input
Table 1-1: Features Used in Example (1-10) Simulations
Statement
Feature
Example Number
Table 1-2: Features Used in Example (11 -20) Simulations
SENSITIVITY
Inflow
•
Outflow
•
Statement
Feature
Example Number
11 12 13 14 15 16 17 18 19 20
General Data Category of Input
Pipeline
•
•
Well
•
•
•
•
CALCULA- TIONNetwork
•
•
•
•
•
•
•
•
Single Link
•
Gas lift
PVT generation
•
Compositional
•
•
Blackoil
•
•
•
•
•
•
•
Condensate
Liquid
Gas
•
Steam
Isothermal
Sphering
FCODECorrelations for
flow device
•
•
•
•
•
•
Liquid holdup
corrections
DEFAULTMedium and its
parameters
•
•
•
•
Flow device
details
•
•
•
•
•
•
•
•
•
Conductivities,
insulation
thickness
•
•
•
•
SEGMENT
Horizontal and
vertical
•
•
•
•
•
•
•
•
•
•
OUTDIME-
NSION
Alternative
output
•
Output options
•
•
•
•
•
•
•
•
•
Table 1-1: Features Used in Example (1-10) Simulations
Statement
Feature
Example Number
Plot
•
•
•
•
•
•
•
•
•
Methods Data Category of Input
SOLUTION
Pbalance
method
•
•
•
•
•
•
•
•
•
•
No flow
reversals
TOLERAN-CEConvergence
tolerance
•
•
•
•
•
•
•
•
•
•
THERMOSystem
•
•
Individual
enthalpy,
density
•
TRANSPOR TSystem
Component Data Category of Input
LIBID
Library
components
•
•
PETROLEU
M
Petro
components
CHARACTERIZE
Property
method
PVT Data Category of Input
SET
Gravity
•
•
•
•
•
•
•
•
Viscosity
Contaminants
•
•
Specific heat
LIFTGAS
Gravity
•
•
•
GENERATE
Property tables
•
Structure Data Category of Input
SOURCE
Set number,
pressure/rate
•
•
•
•
•
•
•
•
•
•
Pressure
estimate
•
•
Ref. source
Temperature
•
•
•
•
•
•
•
•
•
•
Quality (steam)
Composition
TBPAssay curve
Statement
Feature
Example Number
LIGHTEND
S
Defined
components in
assay
WTEST
Well inflow
performance
relationship
SINK
Rate estimate
•
•
•
•
•
•
•
•
•
•
Fixed pressure
•
•
•
•
•
•
•
•
JUNCTIONPressure
estimates
PIPELength/ID
•
•
•
•
•
•
•
•
Elevation
change
•
•
•
•
•
•
•
•
•
Heat transfer
parameters
•
•
•
•
•
•
Pipe data –
thickness,
conductivity
Sphere
diameter
RISERLength/
Elevation
ANNULUSDepth
•
TUBING
Length, depth
•
•
•
•
•
•
Structure Data Category of Input, continued
Detailed heat
transfer
•
BENDK or KMUL
2-phase flow
model -
Chisholm or
Homogeneous
Non-standard
PUMP
Fixed power
CHOKE
•
•
•
•
•
COMPRE-SSOR
Fixed pressure
CONTRA-CTION
Angle
COOLER
Tout
DPDT
Curve
•
EXIT
Statement
Feature
Example Number
ENTRAN-CE ORIFICE TEE VALVE VENTURI-METER
CPCV
EXPANSI-ONAngle
COMPLE-TION
Gravel packed
•
•
MANIFOLD
Gas Lift Data Category of Input
GASLIFT
Capacity
calculated
Sizing Data Category of Input
DEVICE
All devices
Casestudy Data Category of Input
CHANGE
Global
Individual
Sensitivity Analysis Data Category of Input
SENSITIVIT
Y
Inflow
•
•
•
Outflow
Statement
Feature
Example Number
Table 1-3: Features Used in Example (21 A & 21B) Simulations
Statement
Feature
Example
Number
21 A
21B
General Data Category of Input
Pipeline
•
•
Well
•
•
CALCULATIONNetwork
•
•
Single Link
Gas lift
PVT generation
Compositional
•
•
Blackoil
Condensate
Liquid
Gas
Steam
Isothermal
Sphering
FCODE
Correlations for flow
device
•
•
Liquid holdup corrections
DEFAULT
Medium and its
parameters
Flow device details
•
•
Conductivities, insulation
thickness
SEGMENT
Horizontal and vertical
OUTDIMENSION
Alternative output
•
•
Output options
•
•
Plot
•
•
Methods Data Category of Input
SOLUTION
Pbalance method
•
•
No flow reversals
TOLERANCE
Convergence tolerance
•
•
THERMO
System
•
•
Individual enthalpy,
density
Component Data Category of Input
LIBID
Library components
•
•
PETROLEUM
Petro components
•
•
CHARACTERIZE
Property method
PVT Data Category of Input
SET
Gravity
•
•
Viscosity
•
Contaminants
Specific heat
•
LIFTGAS
Gravity
GENERATE
Property tables
Structure Data Category of Input
SOURCE
Set number, pressure/rate
•
•
Pressure estimate
Ref. source
Temperature
•
•
Quality (steam)
Composition
TBP
Assay curve
LIGHTENDS
Defined components in
assay
WTEST
Well inflow performance
relationship
SINK
Rate estimate
•
•
Fixed pressure
•
•
JUNCTION
Pressure estimates
PIPE
Length/ID
•
•
Elevation change
•
•
Heat transfer parameters
Pipe data – thickness,
conductivity
Sphere diameter
RISER
Length/Elevation
ANNULUS
Depth
TUBING
Length, depth
•
•
Statement
Feature
Example
Number
Structure Data Category of Input, continued
Detailed heat transfer
BEND
K or KMUL
2-phase flow model -
Chisholm or
Homogeneous
Non-standard
PUMP
Fixed power
CHOKE
•
•
COMPRESSOR Fixed pressure
CONTRACTION
Angle
COOLER
Tout
DPDT
Curve
EXIT
ENTRANCE
ORIFICE
TEE
VALVE
•
•
VENTURIMET
ER
CPCV
EXPANSION
Angle
COMPLETION
Gravel packed
MANIFOLD
•
•
Gas Lift Data Category of Input
GASLIFT
Capacity calculated
Sizing Data Category of Input
DEVICE
All devices
Casestudy Data Category of Input
CHANGE
Global
Individual
Sensitivity Analysis Data Category of Input
SENSITIVITY
Inflow
Outflow
Statement
Feature
Example
Number
Chapter 1 PIPEPHASE EXAMPLE
Example 1 - Liquid - Pump
Simulation Model
In this simulation, PIPEPHASE calculates the pressure drop
through the system to ensure that the pump is adequately sized.
Simulation Model
In this example (see Figure 1-2), PIPEPHASE is used to simulate
the transfer of solvent from an atmospheric storage tank to an
elevated header tank at a rate of 100 gpm. The pump is rated at 10
HP but its discharge pressure is limited to 30 psig. The user needs to
calculates the pressure drop through the system to ensure that the
pump is adequately sized. Any temperature changes along the
piping can be ignored (i.e. assume isothermal heat transfer).
Figure 1-2: Schematic representation of Liquid - Pump
The inside diameter of the pipe and elbows are 3.068" and 3"
respectively. All elbows are 90º with a friction factor multiplier
(Kmul) of 30. The Kmul for the gate valve is 13.
The solvent is defined as a single-phase liquid and its physical
properties are entered into the Single Phase Liquid PVT Data dialog
box.
1. Fluid Property Data dialog box is opened by selecting PVT
Data from General menu or by clicking the PVT Data icon
.
2. Click Edit in Fluid Property Data dialog box to display Single
Phase Liquid PVT Data dialog box (see Figure 1-3 ).
The gravity is the only mandatory property required but viscosity
and/or specific heat data should always be supplied if available.
Otherwise these properties will be estimated from the gravity.
Input Data
$General Data Section $
TITLE PROBLEM=EXAMPLE1, USER=SIMSCI, DATE=10/01/97 $
DESCRIPTION PUMP LIQUID SOLVENT FROM A STOCK TANK TO A HEADER TANK $
DIMENSION English, PRESSURE=PSIG, RATE(LV)=GPM $
OUTDIMENSION SI, ADD $
CALCULATION NETWORK, Liquid $
FCODE PIPE=HW $
DEFAULT IDPIPE=4.026, IDTUBING=4.026, IDANNULUS=6.065, * THKPIPE=0.2, THKINS=0, 0, *
0, 0, 0, *
CONPIPE=29, CONINS=0.015, 0.015, * 0.015, 0.015, 0.015, *
HINSIDE=0, HOUTSIDE=0, HRADIANT=0 $
PRINT INPUT=FULL, DEVICE=PART, PLOT=FULL, * PROPERTY=FULL, FLASH=FULL, MAP=TAITEL, * CONNECT=NONE, SUMMARY=BOTH, DATABASE=FULL, * SIMULATOR=PART
$
SEGMENT AUTO=ON, DLHORIZ(FT)=2000, DLVERT(FT)=500 $
$Network Data Section $
NETWORK DATA $
SOLUTION PBALANCE, FLOWAL=1 $ TOLERANCE PRESSURE=2 $ $PVT Data Section $ PVT PROPERTY DATA $
SET SETNO=1, GRAV(LIQUID, API)=46.062, CP=0.525, * VISC=32, 0.395/ 122, 0.246
$
$Structure Data Section $
STRUCTURE DATA $
SOURCE NAME=FEED, IDNAME=FEED, PRIORITY=0, * SETNO=1, PRES=0, TEMP=104, *
RATE=100, XCORD=0, YCORD=-125 $
SINK NAME=SINK, IDNAME=SINK, PRES(ESTI)=1, * RATE(ESTI)=1, XCORD=1000, YCORD=-125 $
$ $
LINK NAME=LINK, FROM=FEED, TO=SINK, * IDNAME=LINK, IDFROM=FEED, IDTO=SINK, * PRINT
ENTRANCE NAME=EN1 , IDPIPE=3.068 PIPE NAME=PIP0, LENGTH=4, ID=3.068, * ISOTHERMAL
PUMP NAME=PMP1, POWER=4.1, PRES(MAX)=30, * EFF=90
PIPE NAME=PIP1, LENGTH=30, ID=3.068, * ISOTHERMAL
VALVE NAME=GAT1, IDIN=3.068, IDOUT=3, * KMUL=13
ROUGH(REL)=4.471e-004
PIPE NAME=PIP2, LENGTH=10, ECHG=10, * ID=3.068, ISOTHERMAL
BEND NAME=BEN2, ID=3, KMUL=30, * ROUGH(REL)=4.471e-004
PIPE NAME=PIP3, LENGTH=70, ID=3.068, * ISOTHERMAL
BEND NAME=BEN3, ID=3, KMUL=30, * ROUGH(REL)=4.471e-004
PIPE NAME=PIP4, LENGTH=30, ECHG=30, * ID=3.068, ISOTHERMAL
BEND NAME=BEN4, ID=3, KMUL=30, * ROUGH(REL)=4.471e-004
EXIT NAME=EX1 , IDPIPE=3.068 $
$ End of keyword file... $
END
Case Execution
If alternate output dimensions (SI) are requested in addition to those
used for the input data, select Output Units of Measure from
General menu to specify the output units (see Figure 1-4). When
the simulation is run the resulting output file displays results in both
the original user specified Unit of Measurements (UOMs) and SI.
It is important to note that if the user generates an Excel report, only
the Output UOMs will be displayed. Excel reports unlike the ASCII
Output reports only support a single UOM set. Normally, the UOM
set corresponds to the UOM set defined in the PIPEPHASE
simulation. If the user specifies an Output UOM set, the Excel
report will automatically use the output UOM set and ignore the
original UOM set.
Figure 1-4: Output Units of Measurement Dialog Box
Results
1. Select File/Run.. or click
to display Run Simulation and
View Results dialog box. Click Run to solve the network.
Figure 1-5: Run Simulation and View Results Dialog Box
Note:
The generation of Excel output reports does take some time
solved and converged before generating complex output reports.
2. Click Excel present in the top right-hand corner of this dialog
box. This displays the Excel Reports dialog box.
3. The user can select the reports that are to be displayed in Excel.
By default, everything is selected. The user should judiciously
select the reports to be displayed as large simulation models
contain numerous nodes and links. The Links Reports in
partic-ular can take several minutes to generate.
4. In the Excel Reports dialog box, the user also needs to select
Run Options located at the top right- hand corner of the dialog
box (see Figure 1-5).
■
Run Simulation - Simply runs and solves the simulation.
■Create Database - Creates a Microsoft Access database with
all the data to be displayed in the Excel Reports. The user must
select this option to generate an Excel Report.
■
Create Excel Report - Creates a detailed Excel Report.
5. After selecting the options in the Excel Reports dialog box, the
user has to click Run Current Network. In the above case, it
skips running and converging the network model (it assumes
that the user has previously converged the simulation), creates
the Access database, and subsequently creates the Excel
Report.
The output report shows that the discharge pressure from the pipe is
15 psig or 205 kPa, which means that the pump is adequate for the
intended application.
Figure 1-6: Excel Output
Excel report displays results in one set of units only. In this case the
output UOM set.
Surface Pressure Plot for Link LINK - Base Case
0 50 100 150 200 250 300 350 0 10 20 30 40 50
Distance from Inlet, M
P re ssu re , K P A Fluid
Example 2 -Blackoil Well
Simulation Objective
In this simulation, EX2_BLACKOIL-WELL, the user needs to
determine the production rate for an oil well with a separator
pressure of 25 Bar. In addition to determining the production rate,
the user is asked to determine the degradation in performance as the
reservoir pressure declines and to investigate the effect of
increasing the flow line diameter.
Simulation Model
In the simulation model, EX2_BLACKOIL-WELL, recent
reservoir data including a Vogel coefficient for the well is provided.
The well tubing is deviated from the vertical and the flow line from
the wellhead increases in elevation by 15m along its length. A 1.0"
choke is placed at the wellhead (See Figure 1-7).
Figure 1-8: Schematic Representation of Blackoil Well
The well completion is gravel-packed with data as shown in Figure
1-9.
Figure 1-9: Gravel Packed Completion Dialog Box
The well tubing is surrounded by a layer of insulation held in place
by a metal sheet. The annulus between this metal sheet and the
outer casing contains gas. The user must consider the heat transfer
throughout the well bore and the flow line as shown in Figure 1-10.
Figure 1-10: Tubing Detailed Heat transfer Data
The well is simulated as a single link. The pressure boundary is
fixed at each end and the flow rate is estimated. The fluid is
modeled as a Blackoil where the Gravity, Gas/Oil Ratio, and Water
Cut are defined. The Hagedorn-Brown (HB) pressure drop
correlation is selected for the tubing device and the
Beggs-Brill-Moody (BBM) correlation is used to calculate the pressure drop in
the flow line.
The SOURCE node temperature and pressure correspond to the
reservoir conditions. The inflow performance relationship is
modeled using the Vogel IPR model. An estimate for the flow rate
is also supplied. The tunnel length for the COMPLETION is the
difference between the screen and the borehole radii (i.e. 105mm -
60mm), which is 45mm. The default permeability is suitable for this
gravel size.
Input Data
$General Data Section $
TITLE PROBLEM=EXAMPLE2, USER=SIMSCI, DATE=10/01/97 $
DESCRIPTION BLACKOIL WELL SENSITIVITY ANALYSIS $
DIMENSION Metric, RATE(LV)=CMHR, LENGTH=M,IN, * DENSITY=SPGR
$
OUTDIMENSION Metric, ADD $
CALCULATION NETWORK, Blackoil $
FCODE TUBING=HB $
DEFAULT IDPIPE=102.26, IDTUBING=102.26, IDANNULUS=154.05099 $
PRINT INPUT=FULL, DEVICE=FULL, PLOT=FULL, * PROPERTY=FULL, FLASH=FULL, MAP=TAITEL, * CONNECT=NONE, SUMMARY=BOTH, DATABASE=FULL, * SIMULATOR=PART
$
SEGMENT AUTO=OFF, NHOR=10, NVER=10 $
$Network Data Section $
NETWORK DATA $
SOLUTION PBALANCE, FLOWAL=1 $ TOLERANCE PRESSURE=6.895e-003 $ $PVT Data Section $ PVT PROPERTY DATA $
SET SETNO=1, GRAV(OIL,SPGR)=0.876, GRAV(GAS,SPGR)=0.71, * GRAV(WATER,SPGR)=1.05
$
$Structure Data Section $
STRUCTURE DATA $
SOURCE NAME=RES, IDNAME=RES, PRIORITY=0, * SETNO=1, PRES=400, TEMP=110, *
RATE(ESTI)=50, GOR=320, WCUT=5, * XCORD=0, YCORD=-125
$
SINK NAME=SEPR, IDNAME=SEPR, PRES=25, * RATE(ESTI)=1, XCORD=1000, YCORD=-125 $
$ $
LINK NAME=LINK, FROM=RES, TO=SEPR, * IDNAME=LINK, IDFROM=RES, IDTO=SEPR, * PRINT
IPR NAME=IPR , TYPE=VOGEL, * IVAL=BASIS, 2, *
RVAL=QMAX, 100 / VOGCON, 0.2 / VOGEXP, 1 / * UPTIME,1 / OPEN,1
COMPLETION NAME=Z001, JONES, TUNNEL=45, * PERFD=10, SHOTS=25, LENGTH=10
TUBING NAME=TUB1, LENGTH=1830, DEPTH=1710, * ID=3.873, U=4.882
CHOKE NAME=CHK1, FN, ID=1
PIPE NAME=LINE, LENGTH=1250, ECHG=15, * ID=3.5, ROUGH(IN)=0.18, U=4.882 $
$ END $
$Sensitivity Analysis Data Section $
GSENSITIVITY ANALYSIS LINK DATA $
LINK NAME=LINK NODE NAME=CHK1
FLOW RATE=40, 50, 60, * 70
DESCRIPTION INFLOW= 450 BAR, 400 BAR, * 350 BAR
DESCRIPTION OUTFLOW= 3 1/2 IN DIA, 4 IN DIA, * 4 1/2 IN DIA, 5 IN DIA INFLOW NAME=RES, * PRES=450, 400, 350 OUTFLOW NAME=LINE, * ID=3.5, 4, 4.5, 5 $
Case Execution and Results
To generate and view the calculated Pressure and Temperature
profiles for the well bore:
1. Click
on the main toolbar. The Run Simulation and View
Results dialog box.
2. Select Network as the simulation Type and click the Run
but-ton. The simulation solves and converges successfully.
3. To view the results in MS-Excel, select Excel from the
drop-down list in the Report menu.
4. To view the results in MS-Excel,Click the Excel button to
dis-play the results. The results are disdis-played in the Link worksheet
and appear as shown in Figure 1-11.
Nodal Analysis Calculations
To study the flow rates at different reservoir pressures and flow line
diameter perform a Nodal Analysis. The wellhead choke is to be
specified as the NODE. Flow rates at the choke will be reported for
the combinations of pressure and diameter. The reservoir pressure is
investigated between 300 and 450 bar with flow line diameters of
3.5", 4", 4.5" and 5". The expected range of flow rates in the study
is between 40 & 70 m3/h.
1. Double click on the link to display the Link <LINK> Device
Data dialog box. Click on the Nodal button to display the
Nodal Analysis dialog box. Enter the details in the Nodal
Analysis Parameters dialog box as shown in Figure 1-12 -
Nodal Analysis Parameters.
Figure 1-12: Nodal Analysis Parameters
2. Click
on the main toolbar. The Run Simulation and View
Figure 1-13: Run Simulation and View Results
3. Select Nodal Analysis as the simulation Type and click the
Run button. The Nodal Analysis simulation converges
successfully.
4. To analyze the results, click the RAS button to display the
PIPEPHASE Result Access System window.
5. Click File/New and load the Nodal plot stored in the same
loca-tion as the simulaloca-tion.
6. Click Special Plots button in the PIPEPHASE Result Access
System window to display the RSA Special Plots dialog box.
Enter the details and click the View Plot button.
7. The RAS Nodal plots can be generated in Excel (see Figure
1-14), by clicking on the General menu in PIPEPHASE Result
Example 3 - Distillation Curve
Simulation Objective
In this simulation, PIPEPHASE determines the pressure losses
through the network and also investigates the effect of raising the
inlet pressure and of using larger diameter pipes in the network
Simulation Model
Crude oil is heated before entering refinery distillation columns for
separation into various petroleum products. The user is required to
determine the pressure losses through the network. The user must
also investigates the effect of raising the inlet pressure and of using
larger diameter pipes.
Figure 1-15: Distillation Curve
This is a compositional network model. Since the direction of flow
must be from left to right, the No Reverse Flow option can be
specified in the Network Convergence Data dialog box (see Figure
1-17 ).
Figure 1-17: Network Convergence Data Dialog Box
The crude oil is defined using a TBP (True Boiling Point)
distillation curve and an average API gravity. PIPEPHASE
automatically characterizes the oil by generating a number of
petroleum fractions with associated physical properties. Lightend
components are defined in addition to the crude oil distillation
curve, all properties for which are stored in internal component
databanks. Grayson-Streed K-values are used with Lee-Kesler
enthalpies and vapor density. Liquid density is calculated using the
API method.
Input Data
$General Data Section $
TITLE PROBLEM=EXAMPLE3, USER=SIMSCI, DATE=10/01/97 $
DESCRIPTION CRUDE OIL HEAT EXCHANGER NETWORK $
DIMENSION RATE(LV)=BPH $
CALCULATION NETWORK, Compositional $
DEFAULT IDPIPE=4.026, IDTUBING=4.026, IDANNULUS=6.065 $
PRINT INPUT=FULL, DEVICE=FULL, PLOT=FULL, * PROPERTY=FULL, FLASH=FULL, MAP=TAITEL, * CONNECT=NONE, SUMMARY=BOTH, DATABASE=FULL, * SIMULATOR=PART
$
SEGMENT AUTO=ON, DLHORIZ(FT)=2000, DLVERT(FT)=500 $
$Component Data Section $ COMPONENT DATA $ LIBID 1, C2 / * 2, C3 / * 3, IC4 / * 4, NC4 / * 5, IC5 / * 6, NC5 , BANK=PROCESS, SIMSCI $ PHASE VL=1,6 $
ASSAY CHARACTERIZE=LK, CONVERSION=API94, CURVEFIT=IMPR $
$Network Data Section $
NETWORK DATA $
SOLUTION PBALANCE, FLOWAL=1, NOFR $
TOLERANCE PRESSURE=1 $
$Thermodynamic Data Section $
THERMODYNAMIC DATA $
METHOD SET=SET01, SYSTEM=GS, ENTHALPY=LK, * DENSITY(V)=LK $ WATER PROPERTY=Super $ KVALUE BANK=SimSci $ $PVT Data Section $ PVT PROPERTY DATA $
GENERATE SETNO=1, SOURCE=FEED, TEMP=0, * DT=30, NT=16, PRES=10, *
DP=40, NP=4, PRINT=LDEN SET SETNO=1, SET=SET01 $
$Structure Data Section $
STRUCTURE DATA $
SOURCE NAME=FEED, IDNAME=FEED, PRIORITY=0, * SETNO=1, SET=SET01, PRES=114, *
TEMP=60, RATE(W)=1.5000e+006, ASSAY=LV, * XCORD=0, YCORD=245 TBP DATA=3, 97 / 5, 149 / 10, 208 / * 20, 330 / 30, 459 / 40, 590 / * 50, 690 / 60, 770 / 70, 865 / * 80, 980 / 100, 1100 API AVG=31
LIGHTENDS PERCENT(LV)=3, NORMALIZE, * COMPOSITION(LV)=1, 0.1 / 2, 0.2 / 3, 0.3 / * 4, 0.7 / 5, 0.5 / 6, 1.2
$
SINK NAME=PROD, IDNAME=PROD, PRES(ESTI)=1, * RATE(ESTI)=1.500e+006, XCORD=1210, YCORD=55 $
JUNCTION NAME=J1, IDNAME=J1, XCORD=455, * YCORD=185
JUNCTION NAME=J2, IDNAME=J2, XCORD=665, * YCORD=235
$ $
LINK NAME=1, FROM=FEED, TO=J1, * IDNAME=1, IDFROM=FEED, IDTO=J1, * PRINT
PIPE NAME=Z001, LENGTH=20, ID=12, * U=1
TEE NAME=Z002, IDPIPE=12, KMUL=20, * ROUGH(REL)=1.000e-004
PIPE NAME=Z003, LENGTH=20, ID=10, * U=1
DPDT NAME=E1, *
CURVE=5.0000e+005, -10, 50 / 1.5000e+006, -5, 40 PIPE NAME=Z005, LENGTH=20, ID=12, *
U=1
VENTURI NAME=Z006, IDPIPE=12, IDTHROAT=9.5, * CPCV=1.45
CONTRACTION NAME=Z007, IDIN=12, IDOUT=10, * ANGLE=135
PIPE NAME=Z008, LENGTH=5, ID=10, * U=1
$
LINK NAME=2, FROM=J1, TO=J2, * IDNAME=2, IDFROM=J1, IDTO=J2, * PRINT
PIPE NAME=Z009, LENGTH=10, ID=10, * U=1
BEND NAME=Z010, ID=10, KMUL=60, * ROUGH(REL)=4.471e-004
PIPE NAME=Z011, LENGTH=40, ID=10, * U=1
DPDT NAME=E2, *
CURVE=5.0000e+005, -10, 50 / 1.5000e+006, -5, 40 PIPE NAME=Z013, LENGTH=20, ID=10, *
U=1
ORIFICE NAME=Z014, Thick, IDPIPE=10, * IDORIFICE=6
PIPE NAME=Z015, LENGTH=20, ID=10, * U=1
BEND NAME=Z016, ID=10, KMUL=60, * ROUGH(REL)=4.471e-004, HOMOGENEOUS PIPE NAME=Z017, LENGTH=10, ID=10, * U=1
$
LINK NAME=3, FROM=J1, TO=J2, * IDNAME=3, IDFROM=J1, IDTO=J2, * PRINT
PIPE NAME=Z018, LENGTH=10, ID=10, * U=1
BEND NAME=Z019, ID=10, NONSTANDARD, * ANGLE=60, RADIUS=30, KMUL=50, * ROUGH(REL)=4.471e-004
PIPE NAME=Z020, LENGTH=40, ID=10, * U=1
DPDT NAME=E3, *
CURVE=5.0000e+005, -15, 40 / 1.5000e+006, -7, 35 PIPE NAME=Z022, LENGTH=40, ID=10, *
U=1
BEND NAME=Z023, ID=10, KMUL=60, * ROUGH(REL)=4.471e-004, LAMBDA=1.1, C2=4 PIPE NAME=Z024, LENGTH=10, ID=10, * U=1
$
LINK NAME=4, FROM=J2, TO=PROD, * IDNAME=4, IDFROM=J2, IDTO=PROD, * PRINT
PIPE NAME=Z025, LENGTH=5, ID=10, * U=1
EXPANSION NAME=Z026, IDIN=10, IDOUT=12, * ANGLE=135
PIPE NAME=Z027, LENGTH=40, ID=12, * U=1
DPDT NAME=E4, *
CURVE=5.0000e+005, -10, 50 / 1.5000e+006, -5, 40 PIPE NAME=Z029, LENGTH=40, ID=12, *
U=1 $
$Case Study Data Section $
CASE STUDY DATA
DESCRIPTION CASE STUDY 1 PARAMETER CCLASS=SOUR, CNAME=FEED , VARI=PRESSURE , *
Value=125 CASE STUDY DATA
DESCRIPTION CASE STUDY 2 PARAMETER CCLASS=SOUR, CNAME=FEED , VARI=PRESSURE , *
Value=114
PARAMETER CCLASS=PIPE , CNAME=GFROM, VARI=PIPE ID , * Value=10
PARAMETER CCLASS=PIPE , CNAME=GNETWORK, VARI=PIPE ID , * Value=12
$ End of keyword file... $
END
Case Execution
Heat exchanger in the simulation is modeled as a DPDT device,
where the temperature and pressure changes are entered as
functions of the mass flow rates.
Results
Click Run and solve the simulation.Two case studies are performed
after the base case to investigate the effect of the feed pressure and
pipe diameter. Each case study produces a completely separate
output report and a case study summary is generated at the end of
the report (see Figure 1-18).
Example 4 - Gas Pipeline
Simulation Objective
In this simulation, PIPEPHASE computes the heat loss to the
surroundings (i.e. soil) using built in correlations to determine the
buried pipeline heat transfer coefficients.
Simulation Model
An obsolete, cross - country oil pipeline is to be converted to gas
service. A five stage compressor is available and will be installed at
the inlet of the pipeline. The pipeline runs over rough terrain and is
buried 36 inches below the surface. Most of the pipeline has 1.5
inches of insulation with a thermal conductivity of 0.0116
BTU/hr-ft2-F. However, a portion of the pipeline is not insulated. Even
though the insulation is a liability for gas flow, it would be too
expensive to remove it.
Figure 1-19: Gas Pipeline
The user must establish the rate of gas which can be delivered at a
pressure of 600 psig. The maximum allowable operating pressure
for the pipeline must also be checked for the new service. Line and
route specifications are shown on the following page.
A simple single-phase GAS fluid model is used to characterize the
fluid. To minimize the amount of input data, the most commonly
used pipeline diameter, pipeline thickness and insulation thickness
are set as global defaults. User can select Global Defaults from the
General menu or click the Global Defaults icon
. The thermal
conductivities of the insulation and soil are also set as default values
(see Figure 1-21).
Figure 1-21: Pipe Heat Transfer Defaults Dialog Box
The compressor has a power and efficiency specification. The outlet
temperature of the cooler is defined subject to the maximum design
duty. If the required duty exceeds this value, it will be set to the
maximum value and the temperature will be higher than the
specified value.
The required delivery pressure is specified as a fixed sink pressure
boundary condition. PIPEPHASE computes the heat loss to the
surroundings (i.e. soil) using built in correlations to determine the
buried pipeline heat transfer coefficients.
The pipeline route and size data are shown in Table 1-1 below.
Pipeline profiles can be displayed by clicking View Profile (see
Figure 1-22) in the Link Device Data dialog box.
Table 1-1: Pipeline Data
Section
Length
(Miles)
Pipe ID
(in)
Elevation
Increase
(ft)
Pipe
Thickness
(in)
Insulation
Thickness
(in)
1
15.8
29.25
587
0.375
1.5
2
1.81
29.25
160
0.375
1.5
3
4.79
26.376
1041
0.312
1.5
4
0.8
29.062
681
0.469
1.5
5
1.7
29.376
1600
0.375
1.5
6
5.9
29.376 0.0
0.375
1.5
7
11.3
29.376
1020
0.375
1.5
8
10.4
29.376
-2220
0.375
1.5
9
10.4
29.25
-220
0.375
1.5
10
16.7
29.25
-230
0.375
-11
25.5
29.25
-70
0.375
-12
2.02
29.15
-
0.375
-13
21.78
29.312
-260
0.349
1.5
14
0.6
29.0
-
0.500
1.5
15
14.7
29.376
-170
0.375
1.5
16
5.8
29.376
150
0.375
1.5
17
16.9
29.376
400
0.375
1.5
18
10.4
29.376
-30
0.375
1.5
19
42.1
29.376
-1570
0.375
1.5
Input Data
$General Data Section $
TITLE PROBLEM=EXAMPLE4, USER=SIMSCI, DATE=10/01/97 $
DESCRIPTION BURIED CROSS COUNTRY GAS PIPELINE $
DIMENSION RATE(GV)=CFD $
OUTDIMENSION Metric, ADD $
CALCULATION NETWORK, Gas $
DEFAULT IDPIPE=29.376, IDTUBING=29.376, IDANNULUS=6.065, * ROUGH(IN)=6.0000e-004, TAMBIENT=50, *
THKPIPE=0.375, THKINS=1.5, 0, * 0, 0, 0, *
CONPIPE=29, CONINS=0.0116, 0.015, * 0.015, 0.015, 0.015, *
HINSIDE=0, HOUTSIDE=0, HRADIANT=0, * SOIL, COND=0.7, BDTOP=36
$
PRINT INPUT=FULL, DEVICE=FULL, PLOT=FULL, * PROPERTY=FULL, FLASH=FULL, MAP=TAITEL, * CONNECT=NONE, SUMMARY=BOTH, DATABASE=FULL, * SIMULATOR=PART
$
SEGMENT AUTO=OFF, DLHORIZ(FT)=1000, DLVERT(FT)=500 $
$Network Data Section $
NETWORK DATA $
SOLUTION PBALANCE, FLOWAL=1 $ TOLERANCE PRESSURE=2 $ $PVT Data Section $ PVT PROPERTY DATA $
SET SETNO=1, GRAV(SPGR)=0.93, CPRATIO=1.3, * CONT=0, 0.2, 0
$
$Structure Data Section $
STRUCTURE DATA $
SOURCE NAME=S1, IDNAME=S1, PRIORITY=0, * SETNO=1, PRES=375, TEMP=97, *
RATE(ESTI)=500, XCORD=0, YCORD=-125 $
SINK NAME=SINK, IDNAME=SINK, PRES=600, * RATE(ESTI)=1, XCORD=1000, YCORD=-125 $
$ $
LINK NAME=LINK, FROM=S1, TO=SINK, * IDNAME=LINK, IDFROM=S1, IDTO=SINK, * PRINT
MCOMPRESSOR NAME=Z001, STAGES=5, EQUALPR, * ADEFF=76, 100, 100, *
100, 100, POWER=27000
COOLER NAME=Z002, TOUT=100, DUTY(MAX)=500 PIPE NAME=Z003, LENGTH=83424, ECHG=587, * ID=29.25, SOIL
PIPE NAME=Z004, LENGTH=9556.7998, ECHG=160, * ID=29.25, SOIL
PIPE NAME=Z005, LENGTH=25291.20117, ECHG=1041, * SOIL, THKPIPE=0.312
PIPE NAME=Z006, LENGTH=4224, ECHG=681, * ID=29.062, SOIL, THKPIPE=0.469
PIPE NAME=Z007, LENGTH=8976, ECHG=1600, * SOIL
PIPE NAME=Z008, LENGTH=31152, ECHG=0, * SOIL
PIPE NAME=Z009, LENGTH=59664, ECHG=1020, * SOIL
PIPE NAME=Z010, LENGTH=54912, ECHG=-2220, * SOIL
PIPE NAME=Z011, LENGTH=54912, ECHG=-220, * ID=29.25, SOIL
PIPE NAME=Z012, LENGTH=88176, ECHG=-230, * ID=29.25, SOIL, THKINS=0, *
0, 0, 0, *
0, CONINS=0.0116, 0.015, * 0.015, 0.015, 0.015
PIPE NAME=Z013, LENGTH=1.346e+005, ECHG=-70, * ID=29.25, SOIL, THKINS=0, *
0, 0, 0, *
0, CONINS=0.0116, 0.015, * 0.015, 0.015, 0.015
PIPE NAME=Z014, LENGTH=10665.59961, ECHG=0, * ID=29.15, SOIL, THKINS=0, *
0, 0, 0, *
0, CONINS=0.0116, 0.015, * 0.015, 0.015, 0.015
PIPE NAME=Z015, LENGTH=1.150e+005, ECHG=-260, * ID=29.312, SOIL, THKPIPE=0.344
PIPE NAME=Z016, LENGTH=3168, ECHG=0, * ID=29, SOIL, THKPIPE=0.5
PIPE NAME=Z017, LENGTH=77616, ECHG=-170, * SOIL
PIPE NAME=Z018, LENGTH=30624, ECHG=150, * SOIL
PIPE NAME=Z019, LENGTH=89232, ECHG=400, * SOIL
PIPE NAME=Z020, LENGTH=54912, ECHG=-30, * SOIL
PIPE NAME=Z021, LENGTH=2.223e+005, ECHG=-1570, * SOIL
$
$ End of keyword file... $
END
Case Execution and Results
If metric units are selected as the output UOM, then the Excel
Reports will display all results in metric units.
Example 5 - Compositional Sub Sea Riser
Simulation Objective
In the simulation, EX5_COMPOSITIONAL-SUBSEA-RISER, the
user is required to:
1. Determine the onshore slug catcher size. To do this, the user
must calculate the onshore fluid temperature, pressure, liquid
and vapor rate, and the total liquid holdup.
2. Generate a fluid phase envelope and hydrate curves. Assuming
that the average seabed temperature is 10ºC, the user must
determine if hydrate will form in the line.
Simulation Model
Wet gas is produced offshore and subsequently transported to the
shore through a 32-inch pipeline. The wet gas passes through a
booster platform where the gas is separated and compressed. The
gas is then re-combined with the condensate and sent to the onshore
destination.
The pipeline is coated with concrete for negative buoyancy and the
heat transfer coefficient for heat loss to the sea-water is estimated at
0.16 BTU/hr-ft2-F. The risers and downcomers are bare and heat
transfer coefficients for heat loss to the water and air are computed
to be 1.60 and 0.25 BTU/hr-ft2-F, respectively.
Figure 1-24: Schematic Representation of Example - Compostional Sub Sea Riser
Table 1-2: Pipe Details
Section
Length (m)
Rise (m)
Notes
1
10
-10
Downcomer in air
2
155
-155
Downcomer in water
3
38000
-177
Main line
4
39000
22
5
30400
35
6
4400
11
7
2600
-21
8
24000
25
9
9300
-15
10
3600
13
11
4100
-18
12
12800
25
13
8700
-26
14
11500
191
15
200
160
Riser to booster platform
16
10
10
Riser in air
17
10
-10
Downcomer in air
18
160
-150
Downcomer in water
19
17000
-184
20
5500
27
21
24900
-26
22
7700
31
23
49100
-9
The compositional fluid is modeled using library components with
a petroleum pseudo-component to represent the heavy condensate.
All the required condensate properties are computed by
PIPEPHASE from the supplied values of molecular weight and
specific gravity. The Soave-Redlich-Kwong (SRK) equation of
state is used to compute the liquid-vapor phase splits.
A single link simulation is used to determine the outlet pressure
corresponding to the survey rate of 1,000 metric tons of production
with an inlet pressure of 143 bar. The temperature profile for the
pipeline is also computed via a heat balance over each calculation
segment.
■
Compositional runs provide flash reports at the inlet and outlet
of the pipeline. These reports show a detailed breakdown of gas
and condensate compositions and associated properties.
■
The node summary reports values at standard conditions (see
Figure 1-25). The link summary reports values at actual
conditions. It is important to differentiate between the two. In
this case the Link Summary reports an actual condensate flow
rate of 88.6 m3/hr at the sink whereas, under standard
conditions, no liquid exists.
24
900
6
25
19700
-10
26
6100
31
27
12600
-16
28
8700
18
29
3000
-19
30
15400
66
31
4600
42
32
20000
203
Shore
Table 1-2: Pipe Details
Figure 1-25: Node and Link Summary Report
■
The Taitel-Dukler-Barnea flow regime map (see Figure 1-26) is
used to accurately predict the flow pattern. The results indicate
single-phase and stratified flow through most of the pipeline.
The last vertical pipes are shown to be in annular flow.
Figure 1-26: Flow Regime Map
The temperature and pressure profiles for the pipeline can be
viewed in the output report. There is significant cooling of the gas
in the initial downcomer. This is reflected in the phase diagram for
the fluid (see Figure 1-27). The traverse traces the temperature and
pressure profile of the pipeline across the phase envelope. Initially a
single-phase fluid as the temperature and pressure drop the fluid
become two-phase as liquid condensate drops out of the gas.
Flow Regime Map for LINK - Base CaseOutlet
W I D A X 1.00E-02 1.00E-01 1.00E+00 1.00E+01 1.00E+02 0.1 1 10 100 1000
Superficial Gas Velocity, M/SEC
S up er fic ia l L iq u id V el o ci ty , M /S E C
Figure 1-27: Phase Envelope Map
Phase Envelope for LINK - Base Case
0 20 40 60 80 100 120 140 160 -200 -150 -100 -50 0 50 100 Temperature, DEG C P re ssu re , B A R
Input Data
$General Data Section $
TITLE PROBLEM=EXAMPLE5, USER=SIMSCI, DATE=10/01/97 $
DESCRIPTION OFFSHORE GAS AND CONDENSATE PIPELINE $
DIMENSION Metric, DENSITY=SPGR $
CALCULATION NETWORK, Compositional $
DEFAULT IDPIPE=774.70001, IDTUBING=300, IDANNULUS=354.05099, * ODTUBE=325.211, ROUGH(MM)=0.056, TAMBIENT=10, *
UPIPE=549.2383, UTUBING=3432.6694, UANNULUS=3432.6694, * THKPIPE=19.05, THKINS=45.72, 0, *
0, 0, 0, *
CONPIPE=43.15734, CONINS=7.1432, 0.0223, * 0.0223, 0.0223, 0.0223, *
HINSIDE=0, HOUTSIDE=0, HRADIANT=0, * WATER, COND=0.44645, VISC=1, * DENSITY(SPGR)=1, VELO=5 $
PRINT INPUT=FULL, DEVICE=FULL, PLOT=FULL, * PROPERTY=FULL, FLASH=FULL, MAP=TAITEL, * CONNECT=NONE, SUMMARY=BOTH, DATABASE=FULL, * SIMULATOR=PART, SLUG=BRILL
$
SEGMENT AUTO=OFF, DLHORIZ(M)=1500, DLVERT(M)=100 $
$Component Data Section $ COMPONENT DATA $ LIBID 1, H2O / * 2, N2 / * 3, CO2 / * 4, C1 / * 5, C2 / * 6, C3 / * 7, IC4 / * 8, NC4 / * 9, IC5 / * 10, NC5 / * 11, NC6 / * 12, NC7 , BANK=PROCESS, SIMSCI $ PHASE VL=1,12 $
$Network Data Section $
NETWORK DATA $
SOLUTION PBALANCE, FLOWAL=1 $
TOLERANCE PRESSURE=0.138 $
$Thermodynamic Data Section $
THERMODYNAMIC DATA $
METHOD SET=SET01, SYSTEM(VLE)=PRM $ KVALUE BANK=SimSci $ $PVT Data Section $ PVT PROPERTY DATA $
$
$Structure Data Section $
STRUCTURE DATA $
SOURCE NAME=1, IDNAME=1, PRIORITY=0, * SETNO=1, SET=SET01, PRES=143, *
TEMP=47, RATE(W)=1.0000e+006, XCORD=0, * YCORD=-125, * COMP(M)=1, 0.08 / 2, 0.19 / 3, 2.07 / * 4, 87.18 / 5, 4.93 / 6, 2.98 / * 7, 0.54 / 8, 0.69 / 9, 0.29 / * 10, 0.2 / 11, 0.3 / 12, 0.55 $
SINK NAME=SINK, IDNAME=SINK, PRES(ESTI)=40, * RATE(ESTI)=1.000e+006, XCORD=1000, YCORD=-125 $
$ $
LINK NAME=LINK, FROM=1, TO=SINK, * IDNAME=LINK, IDFROM=1, IDTO=SINK, * PRINT
PIPE NAME=Z001, LENGTH=10, ECHG=-10, * U=175.7675
PIPE NAME=Z002, LENGTH=155, ECHG=-155, * U=1124.9121
PIPE NAME=Z003, LENGTH=38000, ECHG=-177 PIPE NAME=Z004, LENGTH=39000, ECHG=22, * U=549.0978
PIPE NAME=Z005, LENGTH=30400, ECHG=-35 PIPE NAME=Z006, LENGTH=4400, ECHG=11 PIPE NAME=Z007, LENGTH=2600, ECHG=-21 PIPE NAME=Z008, LENGTH=24000, ECHG=25 PIPE NAME=Z009, LENGTH=9300, ECHG=-15 PIPE NAME=Z010, LENGTH=3600, ECHG=13 PIPE NAME=Z011, LENGTH=4100, ECHG=-18 PIPE NAME=Z012, LENGTH=12800, ECHG=25 PIPE NAME=Z013, LENGTH=8700, ECHG=-26 PIPE NAME=Z014, LENGTH=11500, ECHG=191 PIPE NAME=Z015, LENGTH=200, ECHG=160, * U=1124.9121
PIPE NAME=Z016, LENGTH=10, ECHG=10, * U=175.7675
SEPARATOR NAME=S001, PERCENT(WATER)=100, PERCENT(COND)=100 COMPRESSOR NAME=C002, PRES=120, EFF=85
INJECTION NAME=I003, FROM=S001, COND PIPE NAME=Z017, LENGTH=10, ECHG=-10, * U=175.7675
PIPE NAME=Z018, LENGTH=160, ECHG=-150, * U=1124.9121
PIPE NAME=Z019, LENGTH=17000, ECHG=-184 PIPE NAME=Z020, LENGTH=5500, ECHG=27 PIPE NAME=Z021, LENGTH=24900, ECHG=-26 PIPE NAME=Z022, LENGTH=7700, ECHG=31 PIPE NAME=Z023, LENGTH=49100, ECHG=-9 PIPE NAME=Z024, LENGTH=900, ECHG=6 PIPE NAME=Z025, LENGTH=19700, ECHG=-10 PIPE NAME=Z026, LENGTH=6100, ECHG=31 PIPE NAME=Z027, LENGTH=12600, ECHG=-16 PIPE NAME=Z028, LENGTH=8700, ECHG=18 PIPE NAME=Z029, LENGTH=3000, ECHG=-19 PIPE NAME=Z030, LENGTH=15400, ECHG=66 PIPE NAME=Z031, LENGTH=4600, ECHG=42 PIPE NAME=Z032, LENGTH=20000, ECHG=203 $
$UNIT OPERATION Data Section $
UNIT OPERATION DATA $
HYDRATE UID=H001, NAME=HYDRATE EVALUATION EVALUATE STREAM=SINK, POINTS=30, IPRES=40, * MAXPRES=160, TESTIMATE=50, INHIB(MEOH)=10
$
$ End of keyword file... $
END
Case Execution
For single link simulations, PIPEPHASE users can estimate the
slug catcher size by choosing from three statistical slugging models
■
Brill
■Scott
■Norris.
These models are not available for network simulations.
The slugging model is specified in the Print Options in the
General menu (see Figure 1-28).
Figure 1-28: Print Options Dialog Box
Results
The slug catcher size can be estimated by reviewing the data in the
In this case the mean slug length is calculated to be approximately
600 m. This is multiplied by the cross sectional area of the pipeline
to determine the volume of the slug.
Example 6 - Pigging Pipeline
Simulation Objective
In this simulation, the Sphering or Pigging feature is used to
increase the throughput of the pipeline.
Simulation Model
A cross-country pipeline, which transports a two-phase natural gas
mixture, is currently operating at maximum capacity. The delivery
pressure at the end of the pipeline will become too low if the flow
rate is increased. Hence additional compression will be required.
sphering or pigging, is to be performed in order to increase the
throughput of the pipeline. Pigs will be launched at the beginning of
the line and at two intermediate points along the line.
Figure 1-30: Pigging Pipeline
The user must determine the quantity of liquid, which will be
removed from the pipeline in order to size the slug catcher.
The source has compositional fluid with two, defined petroleum
components as the heavy ends. The Cavett 1980 method is specified
for characterizing the petro components. The SRK equation of state
and petroleum transport properties are selected as suitable for
simulating the behavior of the natural gas mixture.
Pigging or sphering calculations can only be specified for single
link simulations. The user activates the pigging calculations by
selecting Calculation Methods from the General menu, and
clicking the Sphering Analysis radio button (see Figure 1-32). The
user also needs to supply a time increment - this defines the rate for
successive steady state sphering calculations. It is important that an
appropriate time interval is selected in order to ensure that pipeline
transients are adequately simulated.
Figure 1-32: Network Calculation Methods Dialog Box
The user specifies the diameter and launch position for the sphere in
the Pipe dialog box. The pigging algorithm can simulate multiple
pigs launching for different locations along the pipeline. A pig is
automatically launched from an intermediate site when the previous
sphere reaches it.
In addition to activating the pigging calculations in the Network
Calculation dialog box (see Figure 1-32), the user must also specify
the size and location of the pig in the Pipe device dialog box (see
Figure 1-33). In this case, three Pigs are launched at the beginning
of pipes Z001, Z003 and Z006 respectively - each with different
diameters.
Figure 1-33: Pipe Dialog Box
Input Data
$General Data Section $
TITLE PROBLEM=EXAMPLE6, USER=SIMSCI, DATE=10/01/97 $
DESCRIPTION PIPELINE SPHERING EXAMPLE $
DIMENSION English $
CALCULATION NETWORK, Compositional, SPHERING $
DEFAULT IDPIPE=8, IDTUBING=8, IDANNULUS=6.065, * TAMBIENT=65, UPIPE=0.8, UTUBING=1, *
UANNULUS=1 $
PRINT INPUT=FULL, DEVICE=FULL, PLOT=FULL, * PROPERTY=FULL, FLASH=FULL, MAP=TAITEL, * CONNECT=NONE, SUMMARY=BOTH, DATABASE=FULL, * SIMULATOR=PART, SLUG=BRILL
$
SEGMENT AUTO=OFF, DLHORIZ(FT)=5000, DLVERT(FT)=500, * DTIM(SEC)=19
$
$Component Data Section $ COMPONENT DATA $ LIBID 1, C1 / * 2, C2 / * 3, C3 / *
