Introduction to VMGSim
Block Week
Fall 2009
University of Calgary
August 31 .... September 3
Table of Contents
PFD Hotkeys
Propane Loop Summary
Propane Loop Example
Dewpoint Plant Summary
Dewpoint Plant Example
Import Propane Loop
IVIDEA Summary
Import Claus
Crude Tower Summary
Excel Unit Operation Summary
Excel Unit Operation Example
Gunther Summary
Gunter Example
Hydrate Inhibition 1
Hydrate Inhibition 2
Hydrate Inhibition 3
Butyl Acetate Summary
Butyl Acetate Example
IVIDEA Reporting Example
Hydrodealkylation Summary
Hydrodealkylation Example
1. GeneralF4Reload stencilsF5Enter connection connector mode (drag to connect)Ctrl+FFind an object (unit or stream)Ctrl+BReturn to parent flowsheet in one stepCTRL+SHIFT+NShow stream name on PFDCTRL+SHIFT+TShow stream temperature on PFDCTRL+SHIFT+PShow stream pressure on PFDCTRL+SHIFT+FShow stream mole flow rate on PFDCTRL+SHIFT+MShow stream mass flow rate on PFD
VMGSim PFD Hot Keys
2. Zooming:
Zoom outCTRL+SHIFT+right-c1ickZoom inCTRL+SHIFT+left-c1ickZoom to Page SizeCTRL+WZoom out to single page viewCTRL+SHIFT+drag a rectangleZoom in on a selected areaCTRL+SHIFT, right-click, and drag the pagePan
4. TextEditing
CTRL+IItalicCTRL+UUnderlineCTRL+SHIFT+0Double underlineCTRL+SHIFT+AAll capsCTRL+SHIFT+KSmall capsCTRL+SHIFT+,Decrease font sizeCTRL+SHIFT+.Increase font sizeCTRL+=SubscriptCTRL+SHIFT+=Superscript
3. Icon Appearance
CTRL+HFlip HorizontalCTRL+JFlip VerticalCTRL+LRotate LeftCTRL+RRotate Right
5. Miscellanous
CTRL+1pointer ToolCTRL+2Text ToolF7Spelling checkerF6Browse the Palletes
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Propane Refrigeration Loop Summary
Property PackageAdvanced Peng Robinson
ComponentsPropane
Stream InformationStream Name 51 53
VapFrac 0 1
T (F) 100 0
Propane 1
Unit Operation Sumnlary
Chiller (Heater)InO - 3000000 Btu/hr
Delta P - 0.5 psi
CP1 (Comperssor)Adiabatic Efficency - 75%
Condenser (Cooler)Delta P - 5psi
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81
V182 83
Chiller
Compressor_Duty CP1
Contienser_Duty
Condenser
84
Propane Refrigeration Loop
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Propane Refrigeration LoopIn this tutorial we will create a simple Propane Refrigeration Loop.
Start a new VMGSim case by pressing the Cl button. Select the AdvancedPeng-Robinson property package.
Show Selection helper
r Add Solid Support
Canc-e1
Now navigate to the Components tab and we will add propane to the compoundlist.
family j;llC;;;;;;';~;;~;;~------ ----.......... - -.. :3 r' D,!a;I!'a.,.Iy'Gm"p,
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Type propane into the Compound textbox:
Eure Compound Search 'j .!ivpothetical Compound ICompoynd
.Eamily lAULCc;~;;;;:;t;~~~=~=-----~ r Detail Family Groups
l~ NamesP' formula
CA2N
Add Selected
PROPAr~E
propane, 1,1'-[ethylidenebls(oxy)}bispropane, 2-(2-chloro-1, l,2-trifluoroethoxy}propane I 1-(2-chloro-1, 1,2-trifluoroethoxy)propane, 2-chloro-2-fluoro-propane, 2-chloro-1, 1, 1,3,3, 3~lexafluoro-
This will bring up a list of compounds with propane being first in the list. To selectand add propane to the property package press the Enter key twice.
After pressing enter the first time PROPANE will be selected.
E.ure Compound Seardl
Compoynd jpropane.Eamily .~~---~~"~==--~""""~~~'4
P NamesR formular~N
propaner 1, l'-[ethylidenebis(oxy)]bispropane, 2-(2-chloro-1, 1, 2-trifluoroethoxy)propane, 1-(2-chloro-1,1,2-trifluoroethoxy)propane, 2-chloro-2-fluoro-propane, 2-ehloro-1, 1.lJ3,3r3~exafluoro-
Detail Family Groups
Pressing Enter a second time will add propane to the selected Compound(s) list.
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Properties of: RootThe,mo
Delete
DeleteAJI
The <New> to the right of PROPANE indicates that this component has not beenadded to the property package. You can do this by clicking the Apply button(which will allow you to make further modifications to the property package) or byclicking the OK button which is equivalent to clicking Apply but will also bring youto the model building environment. Your screen should appear similar to thefollowing screen shot:
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Start building the model by dragging and dropping a Material Stream from thePFD2 stencil.
Selecting the Material Stream
Dragging it onto the PFD.
The Material Stream after it has been dropped on the PFD.
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We now need to enter process information into this Material Stream. In order todo so the Material Stream form must be opened. A Material Stream/UnitOperation form can be opened in one of three ways: the icon in the PFD can bedouble clicked, the icon can be selected and then have the enter button pressedor the icon can be selected and then Open Form can be selected from the rightclick menu.
Ignore
Hi4e Label
Hide
Show DataSheet
Toggle Stream/Connector
Refresh Tables
Create NeW~'I'laterial Balance Table...
Save PaqeAs...
Once the Material Stream form is opened enter in the following values.
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Summary IEquilibrium Results Iune Sizing I
Dbmole;h]1.00
Db/h][ft3l's]
0.0010G.O189,06
[Fraction][Fraction]
Detail View
Exclude From Summary
Description:
Spec from
Connected to [In lOut]VapFracT[F]P [psia]MoleFlo'N Dbmole~l]
f"1assFlolN Db/h]VolumeFlow [ft3/s]StdLiqVolumeFlow [ft3Is]StdGasVolumeFlow [f<Ifv1SCFD1L±:i F'roperties
.:':"j f"lolePROPANE
if} r'1assLfi StdLiqVolume
Print Create Port !gnored
Notice that once the Vapor Fraction, Temperature and Composition are enteredthe stream will flash and the pressure of the stream will be calculated.
Now drag and drop a Valve to the right of 81,
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Valve
Drag and drop onto the dravofingpage.
More...
Connect S1 to the Valve by selecting the stream. Click on the green square onthe arrow head and hold the left mouse button down
--------------
/SI
Material StreaznT *100.0 fF1P 189.06 [psia}Mass Flow ~::Unknown> [1b/h]Volume Flow <unknown:> (ft3/S]
And then dragging it so that it falls on top of the connection point on the left handside of the Valve. A red square will appear when the Material Stream and theValve are aligned and a connection can be made, at this point release the leftmouse button.
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eJ*V1
\l1
Open the Valve form and expand the Properties node in the Material frame:
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174.1
100.0189.06
32.55944.10
29.633232.3050.0503
8.5490E~2
1.488
T[f]P [psia]Moleflo'l>l [lbmole.lh]r·lassflo'N Dbjh]\'/olumeflow [ft3js]StdUqVolumeflow [ft3/s]StdGasVolumeflo'N V'<lr"'lSCfD]r=: Properties (Alt+R)
Energy [Btujhr]H [Btu..1bmol]S [Btu~bmol-F]
r"lolecular'ilVeightr"'lassDensity Db/ft3]Cp [Btu!lbmol-f]ThermalConductivity [Btujhr-ft-f]Viscosity [cp]molarV [ft3~bmoO
Summary Equilibrium Results >!
f'1a in Data ,.. 1 1 Adva Illce~d:::::::::::::::::::::::::::::::::: :::.::::::::::: ::::::::::::;
f\Jame I>h'alue.................. ( •.•...........•.
Delta P [psi] IevCharacteristic linear% Opening [1%] 100.000
Notice how the enthalpy of the inlet of the Valve is passed to the outlet this isbecause the Valve Unit Operation represents an isenthalpic valve.
Add a new Material Stream and connect it to the outlet of the Valve.
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S2
Now add a Heater to the outlet of S2.
51
Lets rename this Heater to "Chiller" since it will represent the cold side of theChiller in the refrigeration loop. To do this open the Heater form and type Chillerin the Name text box.
INumberofsegmen~
Specify a pressure drop of 0.5 psi in the Main Data frame of the Chiller form.
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Fi~~b~~~fs~g~~~~T ... 'ilSummary fprofilel Plot IEquilibrium Results
~""'~~~"'''''''''.'''''''''~'''''''''''''''''')~ Ad~lanced!:.:.:::.:.::::.:::.:::::::.:::.:.:::::::::.::::....::.::::::.':.::::::::.:':'':)~=~==
L::::::::::::::::::::~~~9.)
Now connect a new Material Stream to the outlet of the Chiller and specify avapor fraction of 1 and a temperature of 0 F.
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Detail Vie'N
Exclude From Summary
Ignored
Objh][ft3/s]
1.00
38.37
ChiUer.Out
1..00
iII[Fraction] Obmole;,h]
I[Fraction]
IIFractionl
Connected to [In lOut]VapFracT [F).P [psia]MoleFlow Dbmolejh]r<lassFlow ~blh]
VolumeFlo\<\' [ft3/s1StdUqVolumeFlo'N [ft3Is]StdGas\>'olumeF[ow ~"1f'1SCFD]
L±I Properties1:::1 rv10le
PROPANE
Summary IEquilibrium Results I Line Sizing
"fateria I ' ~ , ~ ~ ,
Now connect a Compressor to 83 and set its adiabatic efficiency to be 75%.
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El
Description:
1.000.0
38.37
Is Recycle PortConnected Stream/Unit OpVapFracT[F]P [psia]fl"loleFlow Dbmole/h]1V1assFlov\' Db,Al]VolumeFlow Ift3/s]StdLlqVolumeFlow [ft3/s]StdGasVolumeFlov\' If.lf.1SCFD]
Summary Icurves!Plot i=.1 Nilin Data [t] AlIvaIlce,d::::::::::.:=::::=:::::::::::::::::::::::::.::::::::::.::==::::::=
~~I11E:_. ..... __. __._lI\,I:31~_. _InQ [HorsePower]Delta P [psi}Pressure Ratio
Ii,diabatic Efficiency [%] L:::::::::::::::!~~~:QiPolytropic Effidency [%]Speed (rpm]Adiabatic Head IfflPolytropic Head Ift]
Add a Cooler named "Condenser" and connect it's inlet to the outlet of theCompressor with a new Material Stream.
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::~:
S1V1
S2Chiller
Condenser
CP1
.......
S f'1ain Data·
Name >J ValueOutQ [Btul'hr]Delta P [psi] 5.00DeltaT [f]
Specify a pressure drop of 5 psi in the Condenser.
INumber of Segments 1 rSummary !profilEd Plot IEquilibrium Results
!±,l Ad'J'anc:ed:::::::::::·=:::.::::::=:::::::::::::J
Now connect the unconnected end of S1 to the Condenser.
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Group, Inc.. Simulating with VMGSim
,,:
V152 83
Chiller
CP1
81
Condenser
Notice how the information specified in S1 has been propagated into theCondenser.
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0.00100.0
189.06
1.00
1.00135.7
194.06
S4.0ut
In
iT
5.0035.73
Value
r'1ateria 1···_··,··__···········································································-c··················· _ _ _ __.._......................... .....j
PorttlameIs Recycle PortConnected StreamjUnit OpVapFracTIF]P[psia]r·lo[eFlow Dbmole.lh]f"lassFlow Dbjh]Volumeflow [ft3/s]StdLiqVolumeFlo,,\! [ft3/s]StdGasVolumeFlow [r.1r.1SCFD]a·j Properties (Alt+R)E:J Fraction [Fraction]
PROPANEEtJ r·lassFraction [Fraction]EB Sb:JLiqVc,IFraction [Fraction]
Summary Profile J Plot 1EquJlibrium Results Ifll'llr"l ._ , _- ., !tI Advanced: ::::::::::::::::::::::.. :::::::1
Also notice that throughout the process there is enough information for eachMaterial Stream to flash, and only an extensive property remains to be specifiedin order for the flow sheet to solve completely. In this case we will specify a dutyof 3000000 Btu/hr in the Chiller.
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1,00
0,0
38.37
630.4327799,29
20,951
0.245
0,36897- 0.7
38,87
630.43
27799.297,777
0,245
5.7417E+O
S2.0ut
InPortName......-., .._- ' ----_..- •..•.•.•._._..~_ _ __ -
Is Recyde PortConnected StreamjUnit OpVapFracT IF]Pfpsia]
MoleFlo'N Dbmolelh]r"'lassFlow DblhlVolumeFlmv Ift3ls]StdLiqVolumeFlow [ft3Is]stdGasVolumeFlow [MfvlSCFC~
ttl Properties (Alt+R)Fraction [Fraction]
If] l·lassFraction [Fraction]I±I StdUqVolFraction [Fraction]if] IvloleFlow .Dbmoleth]
i["lumber ofSegments'" 11summarv~profilelploti Equilibrium Results i
n~j~B .__ ,"',.,_., _ ,., !tJ Adva Il·ced::::;;:::..::::.=::::::::::=:::::::::::::::::::::::!t~~=~=~
1:::1
With this duty available the flow rate of propane through the refrigeration loop willbe determined as will the Compressor and Condenser duties. Note that dutiescan be viewed/specified directly from the Unit Operation form, Energy Streamscan also be connected to the energy port of Unit Operations as shown below.
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Compressocputy CP1
A summary of the Material and Energy Streams can easily be created usingSummary Sets. Select Summary Sets under the Reporting Menu:
~.;1aterial Stream Summary
Energy Stream Summary
co; fRep.orting] l~~in..~.ow Help
J-I Project Report
Summary Sets
PFDView PFDInse
Report Header
Report Settings
Create a Summary Set by clicking the Add button.
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Summar9 Sets 'I
By default a Summary of Material Streams will be selected, click the OK button tocreate the Material Stream Summary.
Stream, I Unit Operation:> Selection , .. :-, .>?" Iii
IiUnit Op TypeF' .. ","" ..
"~I IIStreamj\1aterial P IndudeAII
.....
Available Items Selected Items
/S1
~jS2
IS3/S4
Move!Up
r·1ove -lDown
=idJI' i! Cancel I
, ". '"
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SummariesStream Haterial
6:9J.4] 630,'13
27799,29 27.799.29 27799.2:."0,261 ;,777 20.951
An Energy Stream Summary can be created by clicking the Add SummaryButton. Selecting the Stream Energy from the Unit Op Type and then clicking theOK button.
Shearns I Unit Operations Selection
The simulation of the propane refrigeration loop is complete with an easy way tolook at each of the Material and Energy Streams in a centralized location.
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................. ;l{JiI! S10
88
Ovhd]eed
87
Vi
V2
M1
S3
Dewpoint Gas Plant
DeW_POinj~T...c;h~,
Ba11
Inlet_Gas
Stabilizer
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Dewpoint Gas Plant Summary
Property PackageAPR (Advanced Peng Robinson) for Natural Gas
ComponentsNitrogen, Carbon Dioxide, Methane, Ethane, Propane, IsoButane, n-Butane,IsoPentane, n-Pentane, n-Hexane, C7+ (Hypothetical compound NBP 215 F)Water, Ethylene Glycol (EG)
Stream InformationStream Name Inlet Gas EG Recycle
T (F) 140 165 -140
P (psia) 1060I
1060 -1060I
Mole Flow (Ibmollhr) --- --- -200
Mass Flow (Ib/hr) --- 50 ---StdGasVolumeFlow (MMSCFD) 2.0 --- ---
Nitrogen .057 a aCarbon Dioxide 0.010 a a
Methane 0.600 a 0.6
Ethane 0.100 a 0.4
Propane 0.120 a aIsoButane 0.030 a an-Butane 0.040 a a
IsoPentane 0.010 a an-Pentane 0.010 a an-Hexane 0.010 a I a
C7+ 0.010 a aWater 0.003 0.2 (mass frac) a
Ethylene Glycol 0.000 0.8 (mass frac) aAll compositions in mole fraction unless noted otherwise
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Unit Operation SUlTlmary
Hx1Tube DP - 5 psi
Shell DP - 5 psi
Approach T =15 F
Hx2Tube DP - 5 psi
Shell DP - 5 psi
ChillerDelta P - 5psia
To LTST -10 F
HX2 Shell OutletT-88 F
Ovhd FeedP - 440 psia
V2Delta P - 575 psi
Stabilizer (Reboiled Absorber)12 Stages
Connect Ovhd Feed as Feed to Stage 1
Connect Stage 3 Feed as Feed to Stage 3
Top Stage Pressure - 435 psia
Reboiler Pressure - 440 psia
Specification: Mol Ratio of Ethane to Propane in Bottoms Product of 0.045
CP1Adiabatic Efficiency - 80%
AC1Delta P - 2 psi
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Out T -140 F
Out P - 1060 psia
Dew Point T CheckVF -1
P - 800 psia
Simulating with VMGSim
Dew Point T Controller
Manipulated Variable (OP)
Connected Object - To LTS - Temperature
Process Variable (PV)
Connected Object - Dew Point T Check
Settings
StepSize - 10 F
OP Min - -100 F
OP Max -100 F
SP Value
Value - 15 F
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Dewpoint Gas PlantIn the following tutorial, a dewpoint gas plant will be developed. To start, theproperty package needs to be selected. For this example the "Advanced PengRobinson (APR) for Natural Gas" will be used.
Properties of: RootThermo
Property Package SelectionAdvanced SeJection r Natural Ga~ Processng
RefinervAdd Ga!> Treatillg Chem:cal solventAcid Gas-Treating Physical Soho'entSulfur treatinaPetrochemicals
Apply
The next step is to add the components necessary to the property package. Thefirst components that need to be added are: Nitrogen, Carbon Dioxide, Methane,Ethane, Propane, IsoButane, n-Butane, IsoPentane, n-Pentane, n-Hexane.
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1
Delete All
Camp Group •••
C{)mpare Comp ...
Apply
IALC~;;;PP~;;~;;;"""-'---'-"""""'-""""""" =:J I"'·' Detail F.alllil~' Groups:
CARBON DIOXIDE <Nev1>fv1ETl1ANE <New>ETHAl>:E <New>PROPA!',[E <New>ISOBUTAhlE <Ne'/>'>n-ELfTANE <Ne'N>ISOPENTA,;\lE -<NE'.N >n-PENTANE <New>n-HEXANE <New~
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A hypothetical compound to model the heavier hydrocarbons (C7+) in the systemneeds to be added. In order to add a hypothetical compound, the propertypackage must be applied first. Therefore, press "Apply" and then go to the"Hypothetical Compound" tab at the top of the form.
I.' <reate!!Iank
(' Clone from~isting:
Add tlewHJ/po
Cancel
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To add a hypothetical compound, either a normal boiling point (NBP) or amolecular weight and a liquid density are needed. For this case, a normal boilingpoint of 215 F is known. First, click the "Add New Hypo" button and enter thename to be "C7+".
OK I_~--l Structure lIuilder_ I cancel···'!___...l.
Then go to the "Basic Properties" tab and enter a normal boiling point of 215 F.
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Pressing "OK" will add C7+ as a new compound. Returning to the "PureCompound Search" tab, water and ethylene glycol need to be added as the lasttwo compounds present in the property package.
,'-Created PropertyPkg
E.ufe Compound Seorch 1 tlvpothetical Compound j
Cnmpo!!nd IIfamily ,[ALLcomponen;---"----
r,1ETHANEETHANEPROPANEISOBlJTANEn-6UTAJ\/EISOPENTAN=n-FENTANEn+iEXANEC7+*WATERETHYLENE GLYCOL
~ j~ Detail FamIly G~OL..JPS
Sort ...
Delete
Oe!eleAlI
Cancel
Pressing "OK" will add the property packages and all of the includedcomponents. The first stream that needs to be added is the "Inlet Gas" stream,as below.
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4
r-" Detail View
r Exclude From Summary
Summary IEquilibrium Resufts j line Sizing 1 tlotes I
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Solved
2.202.202.202.20
0.660.00
6.598.78
26,35
12.522.20
131.76
21.96
r Ignored
Envl.In0.93148
14lW1060.00
219.606015.74
0.2690.067
2.00HO
: [Fraction]
1
!IFraction]i[Fra.0i0n]
Create Port
connected to [In (OutlVapFracT [F]P [psia]~1c,leFlow ObmoleihlMassFlow Dbih]VolumeFlow [ft3fs]StdLiqVolumeFlow Ift3!s]StdGasVolumeFlow [M~'SCFD]
EE Properties':;:; '.10Ie
NITROGENCARBON DIOXIDEMETHANEETHANEPROPANEISOBlJTANEn-BlJT"NEISOPENT.<\NEn-PENTANEn+iEXANEC7+:$WATERETHYLENE GLYCOL
ill ~'itass
lfl StdLiQVoluo:_e _
To see the vapor liquid equilibrium relationship a phase envelope needs to beadded. The PT diagram can be seen on the "Table" tab of the phase envelope.
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Summary:! Controls Table Ir;:-.---- C--------jPTDiagr.sm ~ Curve: IQl ~
14000
12000
ro10000 .u;
2,
BOOO ~(f)(f)
6000 ~0...
Table (. Plot
--Jr--- Q1 IFr =1)Q1 IFr = 0)
....•._.. Port
.••.•••• Critical
-400 -300 -200 -100
Print Hydrate
Temperature [FJ
4000
10G 200
Right dick to .how plotmenu
.r.; Dry Basis r Ignored
The inlet gas must then be sent through a separator to remove the liquid from thesales gas. To do this, add a stream out of the phase envelope and add a verticaltwo phase separator to the end of this stream as below. Then connect a streamto each outlet of the separator.
82
The gas stream will then enter a mixer, where the ethylene glycol and the recyclestream will be mixed with the gas. To do this, add a mixer to the flowsheet. Amixer comes with 2 inlet ports by default, but our case requires that 3 inlet portsbe in the mixer. There are two ways to add an extra port to the mixer. The firstway is to right click on the mixer on the PFD and select "Create Port". This willadd the required port.
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o
Open Form
Ignore
Hi>!e Label
Hide
Show DataSheet
Create Port
Delete Port
Switch Icon To...
Refresh Tables
Create New fvlaterial Balance Table...
Save Page As, ..
.:itream Display Option ...
.Q.rawing Explorer
Align Shapes......................................................··············1
Paste ~pecial..,
,Ji, Cut
The second way is to open the mixer form and change the number of inlets from2 to 3 in the upper left hand corner of the form.
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r IgnoredPrint I Create Port
i I M"I~FI,-".", UbmoleJhJ
Db,lh]: l'lc,lumeFlo'N [ft3/sJiISt,jLiq\,.'olunneFI"'N [ft3/s]
Std(;asVolurf,eFlc,w U-1~lSCFDJ
Properties (l\lt+R)Fraction [FraCTIon]NITROGENCARBON DIOXIDE
,.,'ETHANEETHl\/iEPROPANEISOBUT,/i,NE
Portj ICcnnected StreamjlJnit Op
?8F=--==~= ~ rP-....• . ••")+
"'",?ummary Equilibrium R~!JJt(1 Notesl
Etr~iafiillata---'~'-:'~~'-
i§pr,}ode lOW~!PlnOutletI
Now the recycle and ethylene glycol streams must be created, They should bespecified as below. Make sure that the In port of the recycle stream is made arecycle port. This is done by placing a "-" before the specifications entered intothe In port of the recycle stream. Also, note that the composition of the ethyleneglycol stream is on a mass basis.
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
8
Virtual MaterialsGroup, Inc. Simulating with VMGSim
Solved
Spec From
r Detail Vie'/.,!
r ExcJude From Summary
Summary 'I Equilibrium Results line Sizing 'I Notes
r Ignored
0.00
0.00120.00
80.000.000.000.000.00
0.00
0.000.000.0f)
0.00
1.00
140.01060.00
200.004330.6Z
0.Z70
0.059
1.8Z15.E+O
toVapFracT[F]P [psia]MoleFiow Ubmolelh]l"1assFlow OblhIVolumeFlow [ft3!s]StdLiq'lolumeFlow [ft3ls]StdGasVolumeFlow IMlvlSCFD]FP Properties!,,! ly10le
NITROGEN
CARBON DIOXIDEr~ETHANE
ETHANEPROPANEISOBUTANEn-BllTANEISOPENTANEn-PENTANEn-HEXANEC7+"
HYDROGENETHYLENE GLYCOL
i±! Massit) Sb:lUqVolume
© 2009, Virtual Materials Group, Inc. 00 not copy unless authorized in writing by VirtualMaterials Group.
9
l~~ Detail View
ir E.xclude From Summary
Snmmary 1Equilibrium Results lineS-amg INotes ~
r'Jaterial
Virtual MaterialsGroup, Inc.
Spec From
to [InjOut]
Simulating with VMGSim
VapFracT[F]P [psia]r~oleFlo\N Dbmole/h]tvlassFlow Db/h]VolumeFlow [fi3/S]StdUqVolumeFlow [fi3/s]StdGasVolumeFlow [MMSCFD].±' Pr,:,peruesc'i') Mole
i:::i tvlassNITROGENCARBON DIOXIDEr'1ETHiI.NEETHANEPROPANEIS08UTANEn-BUTANEISOPENTANEn-PENTANEn-HE:(ANEC7+"VoJATERETHYLHJE GLYCOL
.ti StdUqVolume
0.00165.0
1060.601.20
50.0U0,000
0,000
1.0925E-2
Dbmole!h][Fraction] OiJ;hj
6.600.600.006.60'11.00
0.006.600.000.000.006.60
n.lO0.80
[Fraction] [fi3I's]
0.000,00
o.no0.00o.no6.00(WO
0.000.00n.oo0.00
1(}.(l0
40.00
r Ignored
Now connect these streams to the mixer created previously.
The outlet of the mixer must then be sent through 2 shell and tube heatexchangers. This should be setup as below,
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
10
Virtual MaterialsGroup, Inc. Simulating with VMGSim
s~;#P~--S-4--f'~tSH;~'··tM1
85Hx2
S6
----Il.I1JU-----,-----f'Inlel."Gas It'c.······1J
£lw1
The first heat exchanger is specified with an approach temperature 15 F. Bothheat exchangers are specified with a pressure drop of 5 psi on each side of theexchanger. The first exchanger is specified as below.
r Ignored
1055.00405,75
9651,55
0.12.0
3.695'IE+O
IIn5bell :OutTu!>., iOutshelltr ··FJ---------"i:J55.ln
0.99698HJ.O
1060.00405.75
9651.550.5330,120
3,695'IE+O
111 Counter Current j &'! I
InTu!>e---IT-----54.0ut
Add Energy Signai .". I PSF File ,., "1 Schematic
PortflameIs Recyde PortConnected Stream/Unit OJ)
VapFracT[FJP [psiaJMoleFlo'N Obmole,q,JMassFlow ObthJVolumeFlow Ift3!s]StdLiqVolumeFiow Ift3!s]StdGasVolumeFlow f!'1fvlSCFDl
Summary Settings I Profile IPlot Report I Notes IINumberofSegmenw
Similar pressure drop specifications will be made in the second heat exchanger.
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
11
Summary lsetlings I Profile IPlot Report flotes I?J Hain Data ::J Data- .... --------,------------- -------.-.--,
r,jame '>f Value Name !>; ValueTube DP [psi] 5.00 In Tub~:Si;-eii-DT[F] r----Shell DP [psi] 5.00 OutTube-Shell DT[FJ
UA [Btuihr-FJ,1 '1 Tube Delta T [FJApproach T [F] Shell Delta T [FJEnergy LostTube [Btu,11fl LJ:==========±:=========[l=================J,I±l[tl Detailed Rating ::::-----
1050.00405.75
9651.55
0.1203.6954E+O
1055.00-105.75
9651.55
0.1203.6954E+O
Virtual MaterialsGroup, Inc.
connected Stream;1Jnit OpVapFracT[F]P [psia]r'loleFlow Dbmaleth]~1assFlaw Db/hlValumeFlaw [ft3/s]StdLiqVolumeFlow [m/s]StdGasVolumeFlow U'1MSCFD]
EJ
__P_ri_nt_-, __A_d_dEn~e..::rg.:..y ...;Sig:..n_al_,,_.-J _~PS_F_F_ile_.'_"_I Schematic _I
The outlet of the heat exchanger goes through the chiller next, which will berepresented as a cooler. The chiller will cause a pressure drop of 5 psi to occur.Add the cooler and rename it "Chiller".
© 2009, Virlual Materials Group, Inc. Do not copy unless authorized in writing by VirlualMaterials Group.
12
1045,00405,75
9651,55
0.1203,6954E+O
with VMGSim
[]iOut
1050.00405.75
9651.55
0,1203.6954E+0
s.oo
11plot I Equilibrium Results I Notes 'I
0"1""·""""..·"""""""""""""""",,,,,,,,,,,,, [tl Advanced:::':
S6
Virtual MaterialsGroup, Inc.
Porl1'lame 'In.... . -.-._- _--. . __.__ _-~
Is Re(:yde Port iLlConne(:ted Stream/Unit Op :-'-"'5.;:::6.:.::;0.::;ut::.- --1llapFra(:T [F]P [PsiaJr<1oleF!ow Dbmole/h]~lassFiow Db/h]VolumeFlo'N [ft3/s]StdLiqVolumeFlo'N [fts/s1StdGasVolumeFlo'N I.MMSCFD]it) Properties (fi.lt+R);,,) Fra(:Jion [Fradion1
NITROGEN
EJ
Add a stream to the exit of the chiller and name it "To LTS". The temperature ofthis stream should be set to be 10 F.
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
13
Virtual MaterialsGroup, Inc.
5pecfrom
Simulating with VMGSim
50lved
Detail View
r' o
Exclude From Summary
Summary '1 Equilibrium Results I line Sizing I tlotesj
0.64082
5.4123.25
12.342.11
148.29100.54
_ r Ignored
1045.00405.75
9651.550.1530.120
3.69541:+0
[Fraction] DbmolelhI0.030420.005190.611940.247780.0573
0.01333
..............................;1,.0..,.0..
Print I. Create Port i Del<:te Port I
VolumeFlow [ft3ts]StdLiqVolumeFlow [ft3isIStdGasVolumeFlow [HlvlSCFD]
PropertiesHoleNITROGEN
CARBON DIOXIDEr"ETI-iANEETI-iANEPROPANEISOBLITANE
By going to the "Equilibrium Results" tab, it can be seen that there are threephases present in the stream exiting the chiller. The vapor stream consists of thesales gas, while one of the liquid streams contains the ethylene glycol. The otherliquid stream will be sent to a reboiled absorber for further processing.Therefore, to separate these phases, a three phase separator will be needed.
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
14
Solved
'LiquidO Ij9[jid1
0.6408 0.3547 0.0045
10.0 10,0 10.0
1045.00 1045.00 1045,00 I2551,0 37,0 -18751,234,710 ]O~-364 22.599
2.244 2.855 1,162 0.4770.4683 0,5989 0,2369 0.1142
23.79 20,84 28.99 33,48
10.6000 7,2986 24.9-396 70.155221.601 20,027 24.3'10 29,946
2830lE-2 1.4196E·2 6,493lE-2 2.3722E+l0,0379 0.0245 0.0531 0,1962
1.063 1.004 1.177 0.5030.5614 1.00 0.00 0.00'105.75 260.01 143.91 1.82
9651.55 5418,13 4172.35 61,070.253 0.206 0,046 0.0000.120 0,073 0.0-\7 0,000
0.03042 0.04044 0.01269 0.000050.00519 0,00513 0.00535 0.000560.61194 0.71346 0.43622 0.003770.24778 0.19885 0,33932 0.00057
0.0573 0,03019 0.10701 0.000.01333 0.00475 0,02899 0.000.01719 0,00538 0.03876 0.000.00382 0,00076 0,00941 0.00
0.0037 0.00067 0.00923 0.000.00282 0.00024 0.00751 0.00
0.002 0.0001 0.00546 0.000.00292 0.00002 0.00002 0.644370,00159 0.00 0,00003 0.35067.................._.._....- ..•.•.•..•...•..••••........•.•-- ............._...._-_.....
r Ignored
Description:
Print LCreate portj Delete Port I
~1QI~f'lo\\'D~I11()I~1.h.L ',fYlassFl""vUblhlVolumeFlowJft~Ls)
SldLiqVolumeFlow [fU/sl
Summary LE.~i.~~ji~.r.i~·~~:~~~j~JIUne Sizing INotes IPort
Virtual Materials
Group, Inc. Simulatin
Detall View
r~ Exdude From Summary
Spec From
Fra~~()~~til:lB()(3E:t~[F.~a.~~,,~]....Fraeti0I1,l::~~ON[)~O)(I[)E .. [Fr"cti()n]
Fr.oejj"r0.:.lI::r.H..I\I\lI:.!f!"c,U_°0.JFractic,n.~AJ'JE[Fr:.action] ..Fraetio~,l'.fl.9!'~~tJE: [Fra~ti()t1]
Fraeti0I1d§QBLrr.A.f'JE. IFrClctionJ ,.. .
~;:~~~is6~~ii~r~~~~1~~11F.ra.~ti()~~I1£.E_NIl\r'JE...IF.!acti()r11JFracti()n, f!±iEXANEJFractionJ .Fraetion.C7+' [Fraction] iF;acti~;;.i;'AiERIF;~~ti~~f-"--'i
,~r.!'~().~.;~:!y:f"S.~~:(.s.9UEr~<:!1"'::L....
Now add a three phase separator (SeparatorLLV), which will be our lowtemperature separator (LTS). Add material streams to each of the material portsand label them as below.
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
15
Virtual MaterialsGroup, Inc. Simulating with VMGSim
87
Hx286
Chiller
68
The cooled separated streams will now be connected to the shell and tube heatexchangers to provide the additional cooling required to efficiently cool theproduct streams. The vapor stream will be connected to the first exchanger, withthe liquid product stream connected to the second exchanger.
Note that since the approach temperature is specified in the first exchangeralready, that it will solve once the vapor stream is connected to it.
Hx185
Chliler
The stream out of the heat exchanger should be labeled "HX2 Shell Outlet". Thisstream will have a temperature of 88 F.
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
16
Virtual MaterialsGroup, Inc.
Spec from
Solved
with VMGSim
r Detail\liew
r Exclude From Summary
Summary Equilibrium Results IUneSizing 'I Notes)
0.005350.436220.339320,10701
0.02899
1.830,77
62,78
48.3315,404,17
0.62734
88.01040,00
143,91
4172.350,108
0,0471,3107E+0
Connected to [In lOut]VapFrac
,T[F]!p [psia]
I~~:;~\:' ~~~~leMiVolumeFlow [ft3/s]!StdLiq'VolumeFlo'N [ft3/s]!StdGasVolumeFlow U.1MSCFD]Ii+; Properties
IH ~::'OGENI CARBON DIOXIDE
METHANEETHANEPROPANE
IS0BUTANE
-r Ignored
By looking at the PFD, it can be seen that Hx2 is shown in red. Opening the heatexchanger form, it can be seen that there is a temperature cross in the heatexchanger.
Chiller
This can be seen by opening the "Plot" tab of the heat exchanger and seeing thetemperature profile.
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
17
......_"........• Tube··)Shell<··
1.0
Description:
Temperature cross (-5.83367917.149301) il1/Hx2
fHX2_Shell_Outiet
Number of Segments
·10+-------+------'&,0.0
Virtual Materials
Group, Inc. Simulatin with VMGSim
Print I Add Energy Signal... j PSF File... I---c------c----'
70
&0",.",,-------------,
.Summary I settings I profjler~.Ii:l!:.JI Report INotes IX Axis ISegment G'J Y Axis r---------,
Properties fAil Properties. -------a
Name: !Hx2
Once the recycle is closed, the temperature profile in the heat exchanger will beadjusted. Until that point, the process specifications do not need to be adjusted.
The next step is to prepare the two liquid streams that will be fed to the reboiledabsorber. Both the LTS liquid stream and the inlet separator streams must besent to the reboiled absorber. First, each of these streams must be sent througha valve to decrease the pressure of each stream.
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
18
ChillerHx2
Virtual Materials
Group, Inc. Simulating with VMGSim
s~lg~fSt--S-4-----,l.'~·'iHX1········~~·-"""5"""5--+
M1
The pressure of "Ovhd Feed" is setto be 440 psia, while the pressure dropacross V2 is set to be 575 psi.
r Ignored
44.9
143.914172.35
0.3080.047
1.3107E+D
[Fraction]0.012690.005350.436220.339320.107010.02899
toVapFracT{F]P [psia]r~oleFIO'N DbmoleihIMassFlo'N Dbih]volumeFlow [ft3!sIstdLiqVolumeFlow Ift3!s]StdGasVolumeFlow [r~MSCFD]
if: PropertiesZ:'1 r'1ole
NITROGENCARBON DIOXIDE",lETHANEETHANEPROPANEISOBUTA~IE
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
19
Virtual MateriafsGroup, Inc.
0.011560.006030.230320.094460.20622
0.0061.3704£'1
0.011560.006030.230320.094460.20622n n7Qil.1
0.00l'iD.O
1060.0015.05
744.800.0070.006
13704£·1
575.00................................l...Q,.Q??J!
Unear100.000
NameDella P [psITCvCharacteristic~~. Opening [%]
IsConnected Stream/Unit OpVapFracT[F]P [psia]r~oleFlow Dbmole;h]~lassflow Ob,lh]VolumeFlow [ft3is]StdLiqVolumeFlo'N [Mis]StdGasVolumeFlow U~I'4SCFD]
if! Properties (Alt-tR)[3 Fraction [Fraction]
NTIROGB'JCARBON DIOXIDEfvlETHANEETHANEPROPANE
---+r:x:J---+ r5~g~=3Y;~d··· ~~
Summary ICurves I Equilibrium Results [ notes IO"I,,,~· - _ _ , ItJ Advanced
EJ
A reboiled absorber must be now be added to the PFD. It should be renamed"Stabilizer". The stabilizer should have 12 stages. By default, the reboiledabsorber has 2 stages, one tray and the reboiler. To add the additional 10stages, press the "Add/Remove Stages" button.
These stages should be added below the first stage.
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
20
Virtual MaterialsGroup, Inc. Simulating with VMGSim
Add I Remove .~ stage(s)
below stage 1
overheadfeed <Jolew>1 .
!,...-~~~--....,
The feeds must now be connected. The overhead feed stream can beconnected to the pre-created feed connection by using the "Connected Obj"dropdown.
FEEDStageConnected Obj
e;::;D~~",:"e:,,:,::-ils ------{;~:~n';aj{~~!~XTI1~~;J~~2&;lert
Stage Stage.--'3_Feed.•Out j
T<Browse•••>
ype '0 , rawr:nnnp,tpd Ohi
A new feed must be added to allow for the second feed stream. This feed willenter at stage 3. To add this stream press the "<New>" cell in the feed section ofthe form.
Now connect the "Stage 3 Feed" stream to this connection.j
.... _ _ _ ._.__.._~_ _.._ _ _.._ __.__ 1. _._..
,overheadFeed feed <J
. 1 3i IOvhdJeed.O... !5tage_3Jee... c:::
loverheadV reboilerl <I
The last step is to specify the pressure and take care of the one necessarydegree of freedom. To do this, go to the "Spec/Estimates" tab. The pressure ofthe top stage will be set to be 435 psia, while the reboiler pressure will be 440psia.
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
21
with VMGSimVirtual Materials
Group, Inc.
~ /$tilhiliIf:<r (R>:,:b(lih::-d:~b~('fhf.f): 12 51<'19':::< n~,~,~~,~,'~',:::::,o::::,:'::':'-:":-:":: __,_. ._.__--,=~:':::.'::~.c=':Name: fStabil~ Description:
I_"Add/Re.mov-e.Stages ~~ I
Configuration Spec/Estimates Efficiencies] Profile; Convergence 1Notes I ~ ------.--jSpe<:ification Required = 1 (0 supplied). Delete ~name' to remove. Ddele 'Value' to tum Into viewed spec.
Viewed Specifications. Delete "lame' to remove. Enter a value to turn :jnto an active specification
12 EnergyIn reboflerQ<tlew>
Estimates
<flew>
r Ignored
Lastly, a bottoms product component ratio specification will be made. This ratiowill be a draw component ratio of ethane to propane of 0.045. To do this, press"<New>" under the "Specifications Required" section of the form. It will bring upthe following form.
The type of specification should be changed in the drop down menu andchanged to the "Draw Comp Ratio Spec".
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
22
Virtual MaterialsGroup, Inc.
Type Camp Ratio Spec
Stage Stage SpecDuty Spec
Value Duty to feed Ratio Spec-----1 Draw Property Spec
OK Draw Special Prop SpecDraw Component Spec
.1...- -1 ,"\.."'.,..
The draw used should be changed to be the reboiler product.
tlITROGHI
CARBON_DIOXIDENETHAtIEETHANE
nnOOA"II:
..'-NITROGEN
CARBON_DIOXIDEMETHANEETHANE
j,:t~I~R.~ti~s~~~~~~~~~-~-~------'_iJ
<New>Nume~t nqroneul nentUse the <Shift> ilnd <Control> keys for multiple selections
Ethane and propane need to be selected as the components used in the ratio,with the value of the ratio being set to 0.045.
OK
_-:II"loleRilitioSpec._~~~_. ······8
Cancel I
By pressing "OK" and then pressing the "Solve" button, the tower will now solve.
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
23
Schematic .... !
- - r Ignored
De~rlptlon:
Virtual MaterialsGroup, Inc.
W. Atways: Restart from Last Convi=="'?==-;
Restartl . l.astCo~
Configuration 1 Spec/Estimates 'j Iffkiencies 'j Profile: Convergence IHotes 1
InltiarlZation r-t-ethodrRi;;;;~~--~~"-'-----3 ~ tcb[l;~;lierat;;;:;-i-o~'~;'E~;'~;'(;:'048946--"--'- .....-----.---.---------------
tcbilizer kner Error 0,451:68tabllizer Imer Error 0,053443
Parameters ,tabilizer Ir.ner Error 0,025971
L~;fj-~~~~~~ffi~,,,~Il'1axouterErroy 0.0001 IlStabililer Inner Error 0,063362
l~~;~~~~_~L O.fi~:~ IS~~~!~ E~~[iig~~fii!ITriggerSo.fve 0 tabilizer Inner Error 0.000233TrvlastConverged 0 Inner Error 0,000112TtyToRest~rt 0 ImerErrar 0,000020
TryTo5otve 1. i:~?~~-~. ~~~~~~r 0,002926-y.~.p..f..~~~.~!~_q_~.~y.~......... 0 tabilizer Inner Ermr 0,007516
tabilizer Inner Error 0.-001443tcbiher Inner Error Q,0004Jltcbilli:er Irner Error 0,000111rebllizer Ironer Error I}. 000041
!Stabilizer Heraton 4 Outer Error 0,000555''stabilizer Inner Error 0.003359,'Stcbilirer Imer Errcor 0,001S$7'stebilirer Inner Error 0,000277Steblliler Inner Error 0,000054Stabilizer Iteraton 5 Outer Error 0,000084/Stabilizer Iener Error 0.000303lStabihzer Imer Error 0,000242i'Srebilizer Inner Error 0,000062
Now name the outlet streams as below.
The vapor stream from the stabilizer will be recompressed and used as therecycle. This stream needs to be connected to a compressor.
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
24
,~ Virtual MaterialsGroup, Inc.
CP1
Simulating with VMGSim
An adiabatic efficiency of 80% should be specified in the compressor.
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
25
Virtual Materials
Group, Inc. . Simulating with VMGSim
Plot INotes I
r Ignored
134,63
3413.85
0.042
1.2Z61E+0
1.00
55.1435,00
134.633413.85
0,:379
0,042
1.Z261E+O
Data - , Lt.J Advanced :::::::::::::::::::::::::::::::::::::::::::::::::::::::ecce::::::::::::
Name......................_- .
InQ [HorsePower]Delta P [psi]Pressure RatioAdiabatic Effidency [%] 80,00Polytropic Effidency [%]Speed [rpm]Adiabatic Head [ft]Polytropic Head [ft]
Portf IC'lflnected StreamjUnitOp
dM"leFI"w Dbmc<leihJDblh]
d VolumeFlow [ft3/s]IStdl-iqVe,lume:Flow [ft3/s]
f lSt,JGasVolurneFIc,w IMI~SCFD]
An air cooler will follow the compressor. It will have a pressure drop of 2 psi andan outlet temperature of 140 F and an outlet pressure of 1060 psia, With theoutlet conditions fully specified, and the pressure drop specified, the backwardpropagation of information allows the compressor to solve.
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
26
with VMGSim
1.00140.0
1060.00
........p.7.&~.:3413.85
0,1640,042
L2261E+0
1,00173,0
1062,00134,63'
34B.S50,1860,042
1,2261E+O
Solved
In lOutU . ·----TT
: S10.0ut
Description:
Virtual MaterialsGroup, Inc.
p"rttlame-- .._----------.-------
Is Recycle PortConnected Streamj1Jnit Op
VapFracT [F]P [psia]~lol.Flo'N Obmol.jh]f~assFlow ObIl-iJVolum.Flow [ft3/s]5tdUq'iolumeFlo"i [ft3!s]StdGasVolum.Flo'N [t'U~SCFD]
FE Properties {Alt+R)
[C) FracDon [FraCDon]NITROGENCARBON DIOXIDEf~ETrlANE
ETHANE
~INumber of 5eg,;,-nts,------1C11
Summary Profile1Plot INotes I~c!lcai~•...~~.~.~...••.•. :.::;:::.::::::.::::;. i±J Aclvanced=··.·::=··=
The "Recycle" stream can now be connected to the outlet of the air cooler. Thiswill allow the system to iterate and find a converged solution.
Lastly, the "Sales Gas" stream must be added out of the first heat exchanger.
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
27
,~ Virtual MaterialsGroup, Inc.
62
Simulating with VMGSinl
It is required for transmission that at 800 psia, the dewpoint of the sales gas mustbe 15 F. To do this, a balance unit operation can be used. This will allow thematerial balance to be transmitted across the unit operation, allowing for thetemperature and pressure of the stream to be specified. Therefore, once thebalance unit operation is created and connected to the "Sales Gas" stream itshould be checked that the balance type in it is set to "Mole".
© 2009, Vit1ual Materials Group, Inc. Do not copy unless authorized in writing by Vit1ualMaterials Group.
28
Virtual MaterialsGroup, Inc.
To calculate the dewpoint temperature, specify a pressure of 800 psia and avapor fraction of 1.
© 2009, Virtual Materials Grqup, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
29
Virtual MaterialsGroup, Inc.
flame: IBall
with VMGSim
0.070.0123
1.0014.2
1040.00 800.00178.82 ,····::jz§:;:@
3722.570.2320.049
1.6286E+O
3722.57
0.070.0123
0.73696
0.118550.05039n fHlli1;~
0.2550.049
1. 6286E+O
Solved
.........._....~."--- --_._~.._-...,
CDnnected StreamJ1Jnit OpVapfracT [F]P [psia]r>lloleFJow Dbmolefh]~'assFlow Dbjh]volumeFJow [ft3/s]StdLiqVolumeFlow [ft3!s]stdGasVolumeFlow I~1"'sCFD]
':j.! Properties· (A1t+R)'.C) Fraction [Fraction]
NITROGENCARBON DIO)(lDENETHANEETHANEPROPANET~nRI fTJlNF
As can be seen, at these current conditions, the dew point at 800 psia is 14.2 F.To adjust this, the temperature out of the chiller needs to be adjusted. This canbe done by using a controller. First, create a stream out of the balance unitoperation called "Dewpoint T Check". Now create a controller. The OP of thecontroller will be the temperature of the "Dewpoint T Check" stream. To add this,open the controller form, and in the OP drop down menu, select "<New>".
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
30
r Ignored
AC 1.Air Cooler AltitudeAC1,Air Cooler Cost
~AClAir Face Velodty
Settings' AC1.Air InletTA -ti ' ... , ...., .. AC1,Air I·lass Rate
L \,e AC1,Air OulletT~e:'JJ..l:fi!;ilJr, AC1..o.ir Relative HumidityI'lax Error ] AC l"i1.ir Side Delta PI'lax Absolut AC1,Air Std Volume RateI'lax controlll AC1.Air Volume Rate .
.. -: ,-.. ,.". AC1.Alrslde dp I'luitiplierAction AC1.Airside Film CoefficientUse Direction
Simulating with VMGSimVirtual Materials
Group, Inc.
Summary IPerformance -.-..------.-.-
r'·-'.·.·~ -..' -,.-- ' -.-.' -' ':'..' '........ -'-'~." i: Name I>! Value .. i
IPVfrarg~fv'a~ '. r··-- i,sp/rargetVal '
OP/I"1anVar
EJr-~------
With this new form, select "To LTS" as the connected unit operation and "!\Jew T"as the signal variable type.
Connected Unit Operation:
.signal varjabLeTypez
Cancel
Pressing "OK" will create a temperature signal port in "To LTS" and connect it tothe PV port of the controller. Repeat these steps to connect the temperature of"Dewpoint T Check" to PV.
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group,
31
r Ignored
I\"}[]
1.00E-040.02
60Direct
o
, Error. Absolute Error [F]Controller Iterations
ActionUse Direction
Virtual MaterialsGroup, Inc.
I:;]
r?\TJQ~;;P.:?!:~CT.:~h;'~!;::T.G
The set point of Dew Point T Check should be set to 15 F. Also, the OP Max andMin should be set to 100 F and -100 F respectively, with a step size of 10 F. Thisadjusts the temperature out of the chiller to be 10.9 F.
Direct
oUse Direction-100.0100.010.00
Summary 1
:=J perforD1al'lce--····_·· ...... ~···1 ~~~~===~=;.;.==c1Name__ ._._. . l~JYllllJ~__. I RIPV/Targetvar [F} ... 15.0 I' []SP/Targetval [F] 15.0 IJM~~:F;~~;;;:·:············:···..···_· j' -;i.orli:iJtd:1
OP/}<1anVar [F] .. , L::::::::::::::::::::i.iJ.::~j I
The last step is to check that hydrates are not formed in the stream exiting thechiller. To do this, the Out port of "To LTS" must be cloned, so that it can beconnected to the Hydrate unit operation. To clone a material port, open the "ToLTS" stream and press the "Create Port" button. This will bring up the formbelow.
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
32
Virtual MaterialsGroup, Inc.
Type:
Clone
with VMGSim
Since an Out port will be connected to the In port of the Hydrate unit operation,the type of port to be created should be switched to "Out".
Pressing OK will clone this port. Now create a Hydrate unit operation to connectthis newly created port to it. Opening the form, the cloned port can be connectedto the unit operation. In the "Connected Stream/Unit Op" dropdown, the clonedport can be found. It is named "To_LTS.Out_1" since it is the cloned version of"To_LTS.Out" port.
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
33
Dewpolnt_T_check.OutEG_to_Regen.OutStabilized Condesate.out:*J:el{*kl2d)~ITJ0ftl.%IP••£ffi~1l!0tl<Browse•••>
Is PortConnected Stream{Unlt OpVapFracT [F]P [psia]r'loleFlow Obmole/h]r'lassFlow Oblh]VolumeFIO'I\' Ift3!s]5tdLiqVolumeFlc,w [ft3Is]StdGasVolumeFlow [r~~15CFD]
[tl Properties (Il,lt+R)Fraction [Fraction]NITROGENCARBON DIOXIDEt'lETHANEETHANEPROPANEISOBUTANEn-BLrrANE
Virtual MaterialsGroup, Inc.
EJ~i~ff>--+ f~~~~~~~~<
t'V'i.'l.
Summary '[ settings 1Equilibrium Results 1Notes ~
EJ Data'-" I±l Activate Data '----:---.-....-- .::::l
I~I~'···-
Once connected, it can be seen that a hydrate is not formed at these currentconditions. Also, it shows the formation temperature at the current pressure andthe formation pressure at the current pressure, as well as the approachtemperature to the formation temperature.
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
34
Virtual MaterialsGroup, Inc. Simulating with VMGSim
Is PortConnected Stream;\Jnit Op\lapFracT [F]P [psia]~1oleFlow Dbmolelhlr·lassFlow Db/Ill\lolumeFlo'N [ft3/slS!dLiqVolumeFlow [ft3!slStdGas\!olumeFlow [r4~1SCFDl
if! Properties (Alt+R)!::::' Fra,:tion [Fraction]
NITROG8~
CARBON DIOXIDEf4ETHANEETHANEPROPANEISOBUTANEn-BLrrANE
0.-5221210.9
1045.00342.55
8895.730.2080.103
3. 1198E+0
0.045250.012520.580880.163670.127380.022060.02678
0.5221210.9
1045.00342.55
8895.730.2080.103
3.1198E+0
0.045250.012520.580880.163670.127380.022060.02678
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
35
Virtual MaterialsGroup, Inc. Simulating with VMGSim
Import Propane LoopNow that the dewpoint gas plant has been created, this can be combined with thepreviously developed propane loop to create an integrated project. The propaneloop will be used to accompany the chiller. The chiller created in the propaneloop will be one side of the chiller heat exchanger, being connected to the chillerin the dewpoint gas plant.
The first step in connecting the propane loop to the dewpoint gas plant is to openthe dewpoint gas plant case.. Next, under "File", select "Import". This will allowthe propane loop case to be imported into this project.
Tools Assistants
NEW Project
Open Project..
Import,,,
Report Export ...
Save Project
Save ProjedAs".
Exit
C:\Users\Carl Landra\Documents\.Block VVeek\DEwpointGasPlantvmp
C:\Users\Carl Landra\Documents\.BlockWeE;k\MDEAReporting.vmp
C:\.Users\Carl Landra\Documents\.Blockl>VEek\DewpointGasPlantDeveloping.vmp
C:\Users\Carl Landra\Documents\Block Week\reactor2UNIQUACdefaultsE'luil.vmp
C,\Users\,(arl Landra\Documents\Block Week\reactor2UNIQUACdefault,.vmp
C,\Users\Carl Landra\Documents\Block Week\reador2UNIQUACdefaultsSideRxns.vmp
This will open up the file form below. Select "propaneloop.vmp", or whichever fileis the propane loop case created previously.
File name' propaneloap.vmp
FoldEr!; A
,....J ~~•• t''"''.'a ....~......... ,'~••• ,.t"
LJ DE~vpointGa~PlantDe:veloping,bk5,vrnp
L.J DewpointGasPlantDe'.'elop-ing.vmp
LJ ExcdUnitOp.vmp
U GuntherR.ec.ydeMixer.vnlp
U GuntherRecycle-5treal11s,vmp
L~: MDEAExamplesmp
U MOElIP,epolting.bkl,'.mp
L..J r..,1DE,G.Reporting,vmp
Lj OilEx~mple,bkLvmpL..'j OitExample,':.'mp
:....J propane:laop.bkl.vmp
I?-i iJ prcpanelooF·vmp
LJ Teadorl.bld.vmp
LJ feactcrLvmp
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
1
,~ Virtual MaterialsGroup, Inc. Simulating with VMGSim
This will now add the propane loop as a second flowsheet within the dewpointgas plant case. The separate flowsheets can be seen as different tabs at thebottom of the PFD.
In order to connect the flowsheets, the duty in the propane loop chiller duty mustbe removed. This is specified in the "Chiller" unit operation itself. With this valueremoved, the propane loop will no longer be solved, as the extensive variablerequired has been removed. .
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
2
Virtual MaterialsGroup, Inc. Simulating with VMGSim
flame: fChiii;;~~-~-~---
E
1.00
38,37
n !gnored
1.00
INumber of Segments 11Summary IProfile IPlot. 1Equilibrium Results Notes I
Datia ------------- -----------.. --------, (tj Advanced::::
--------.--....----------------------------..-T=-------~·------·,,·--·--~-:-=----~--------------------'1-'-------------Porl1lame.__..._-_..~_. __ .. -. ..---_ ...-I. Recyde PortConnected Stream/Unll Op'v'apFracT [F]P [psia]'-loleFlow Dbmole/h]NassAo'N Db/h]
nVelumeFlow [ft3!s]1l~:~~:'~~~:;,~:~;:::vl[ft3!S]iIi [NNSCFD]
Properties (Alt+R)Fraction [Fracti',n]PROPANE
~CI\ilI;rjjlJt~
~ODDl:J00
SZ DonC~erVl
51
The "Chiller Duty" energy stream must now be disconnected from the chiller anddeleted on the propane loop flowsheet. The duty for the chiller will now bespecified by the chiller in the dewpoint gas plant. Therefore, an energy streammust be connected to the "Chiller" in the dewpoint gas plant.
To connect this stream across flowsheets, open up the "01" form. For the Outenergy port, in the "Connection" cell, press "<Browse>".
© 2009, Virtual Materials Group, Inc_ Do not copy unless authorized in writing by VirtualMaterials Group.
3
Virtual MaterialsGroup, Inc.
Name: fQl
Exclude From Summary
4.502E+5
E:;) Energy InIn [Btuillr]Energy Out
Out [Btuillr]
CP1.InQ-"~===-=1 Hxl.Energy Lost Tube
Hx2.Energy Lost TubeStabilizer.Enerql·Feed 11 reboiler
To connect to the In port of the propane loop chiller, select the "Chiller" under the"propaneloop" flowsheet.
~ancelR 5how Short listW 5how free PQrts onlyE.rintr",;"y,
i") i:,,: EnergyStreams
QiCompressors
CPi·H Re~oiledAbsorbers
Stabilizer, '.=i flowsheets
propaneloop
-l';: CompressorsCPi
Heaters
l¢.h..i.ii.~d
Once this is done, press "OK". As can be seen on the PFD, the energy streamon the dewpoint side of the chiller is now connected to the propane loopflowsheet.
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
4
,!I Virtual MaterialsGroup, Inc. Simulating with VMGSim
propaneloop
82EO
01
83
H
On the propane loop side ofthe project, there is also now an energy stream thathas been created and is connected to the chiller. This chiller duty specificationnow allows for the propane flowrate through the loop to be specified based onthe chiller duty in the gas plant. This connection will update any time a changehas been made to the dewpoint plant.
Since the propane loop and the dewpoint gas plant each used different propertypackages, these can be seen by opening the thermodynamic model form can beseen by pressing the toolbar button indicated below.
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5
~ Virtual Materials
Group, Inc. . Simulating with VMGSimAs can be seen in this form, a different property package is used for the mainflowsheet than for the propane loop flowsheet. This can be seen below.
Since only an energy stream is being transferred between the flowsheets, thedifference between property packages is not significant. However, this is a veryimportant aspect to take into consideration when transferring material streamsacross property packages. This will be shown in another example where theClaus plant is imported into a created MDEA case.
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
6
Virtual MaterialsGroup, Inc. Simulating with VMGSim
Gas SweeteningExample Using
MDEA~ _ ~ _ ~o ~ _, "00" 00 , .., , .. __ ,.., ..m ~ ~ "m ,,, .., .. m'''_o ..o_,~m,_.., ..,......,_,~_,,.... _.,_,..
Water_Balance_Calculator
, .. '.... 0'" ,oM .." .., ..,8", -, ~ -.... 'wi
!Rich_Amine_Loading_Contm,ller
l:5i¥"&:"lIilli;:j
~~~~1
Make:_up_w_at_e_r__i'-'"
Mi I1 1~ To_Coole,~ ,
Cooler Pi
R ..w~~
Sales_Gas
From_Crqss_ExchangeAcid_Gas
Flash_Tank_Vent
Rich_Amine_tcLCross_Exchange
Regenerator
d_Rich_Amine
Flash! Tank
Rich_From_AIT' • To Flash Tank'ADi Vi
Rich AmineContactor -
iGas_to_Abs
~Inlet_Separator Regenerated_Amine
© 2008, Virtual Materials Group, Inc. Do not copy unless authorized in writing by Virtual Materials Group.
,j Virtual MaterialsGroup, Inc. Simulating with VMGSim
Gas Sweetening Using MDEA Summary
Property PackageAmines Property Package
ComponentsNitrogen, Hydrogen Sulfide, Carbon Dioxide, Methane, Ethane, Propane,IsoButane, n-Butane, IsoPentane, n-Pentane, C6+ (Hypothetical compound NBP248 F) Water, Methyl Diethanolamine (MDEA)
Stream InformationStream Sour Gas Lean Amine Make Up Water
T (F) 90 -100 77
I P (psia) I1000 1010 ---
StdLiqVolumeFlow --- 1.782 (800 ---(ft3/s) gal(US)/min)
-
StdGasVolumeFlow 40 --- ---(MMSCFD)
Nitrogen 0.0279 0 0
I Hydrogen Sulfide 0.094 0 0
Carbon Dioxide 0.0493 0 I 0 I
I Methane II 0.7437 I 0 0
Ethane 0.0318 0 0
Propane 0.0167 0 0
IsoButane 0.0035 0 0
n-Butane 0.0089 0 0
IsoPentane 0.0033 0 0
n-Pentane 0.0035 0 0
C6+ 0.0166 0 0
Water 0.0008 0.55 (mass fraction) 1
Methyl 0 0.45 (mass fraction) 0Diethanolamine
All compositions in mole fraction unless noted otherwise
© 2008, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
,Ii Virtual MaterialsGroup, Inc. Simulating with VMGSin1
Unit Operation Summary
Contactor
Absorber
25 Stages
Top stage pressure 995 psia
Bottom stage pressure 1000 psia
Tray dimensions - GPSA Estimate
Efficiency Model - Auto Calculate
Rich Lean Cross ExchangeTube DP - 5 psi
Shell DP- 5 psi
InTube - Rich Amine to Cross Exchange
OutTube T - 200 F
OutTube P - 60 psia
RegeneratorDistillation Column
22 Stages
Feed Stage - Stage 4
Condenser Pressure - 19.5 psia
Top Stage Pressure - 21.5 psia
Reboiler Pressure - 24.5 psia
Stage 1 Temperature Specification - 120 F
Draw Flow Spec - condenser liquid 0 Ibmol/hr
Duty to Feed Ratio Spec (StdLiqVol) Stage4 Feed / ReboilerQ - 900 Btu/gal(US)
Tray dimensions - GPSA Estimate
Efficiency Model - Auto Calculate
Mi
Parameters
CalcPressureMode - AIlPEqual
PiEfficiency - 75%
© 2008, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
,~ Virtual MaterialsGroup, Inc.
CoolerDeltaP - 5psi
Out T -100 F
Out P - 1000 psia
Simulating with VMGSim
Water Balance Calculator (ExceIOp)
Import
Component Molar flow Water Gas to Abs (water in)
Component Molar flow Water Sales Gas (water out)
Component Molar flow Water Flash Tank Vent (water out)
Component Molar flow Water Acid Gas (water out)
Export
Sum water out and subtract water in and Export the value to Molar Flow Rate ofMake Up Water
Rich Amine Loading Controller
Manipulated Variable
Connected Object - Lean Amine.StdLiqVol
Target Variable
Connected Object - AD1.AcidGas/Amine_(mol)
Settings
StepSize - 0.25
Target Value
Value - 0.40
© 2008, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
Virtual MaterialsGroup, Inc. Simulating with VMGSim
Import Claus PlantThis example will demonstrate how integrated flowsheet models can be builtusing existing case by importing and then connecting it to a MDEA gas treatingplant.
Begin by opening the MDEAExample.vmp created previously.
Open the File Menu bar and select Import.
New Project
Report Export .. :
Save Project
Save Project As",
Exit
c: "Program Files\Vf'lG \Vr.1GSimPkg3_1Ipoeumentation"f'janual Examples¥'lDEAExample, \Imp
C:\Program Files \Vr-1GWMGSimPkg3_1Ipocumentation¥'lanual Examples\IntroductiontoVMGSimto'Ners, vmp
C: \Program Files\\1v1G wr-1GSimPkg3_1'poeumentation\Manual Examples \ol,mmoniaRefrigeration, vmp
C:'.program FilesWr'lGWr'1GSimPkg28DREALReleaseIpocumentation\Tutorials\f>1anual-TutoriaI1, "ImpC: "program FilesWrvlG\Vr'lGSimPkg2SDREALRelease\Documentationl)'v1anuaIExamples\Atmospheric Crude Tower,vmp
C:\Documents and Settings\James van der Leel)'vly Documents\Quench Compare,vmp
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
1
Virtual MaterialsGroup, Inc. Simulating with VMGSim
Once Import is chosen a file selection form will open. Select theGPSAClausPlantExample.vmp under the Manual Examples folder and thenpress the "Open" button.
Xrf' Heater, vmp
'xl HTRI_case_tutoriaI1_a,vmp
\;/' HTRU:ase_tutoriall_b. vmp
f'1l HTRI_case_tutoriaI3. vmp
'I' Hydrate, vmp
-- ---~-- -- - -- '---.-~-"~'--"~' .._-.. ~'~'-,-'~.'-~"-~.~.~ -···-··~~1
f\)if' ExcelUnitOp. 'Imp
'rj' expander. vmpExtractor. vmp
't{l FlowSheeting, 'Imp
\;,;:> GasOrilke, vmp
\Y'
r\lcs-rn;:.~~;;'~~ ..1'1!'~ CSTR2, vmp
I'tDepressuring1.vmp1"';7' Depl'essuring ExamplE Input FirE,vmp
itt DeprEssurino Example r··J2. BlowDo'l'.'n,bkl,vmp
I\lDEPressurin; Example N2 Blo'/,:Do'/'!n, vmp
lv' DistCurve. vmp
1'i;/ EjectorDEsign,'imp
1\/EjedorRating.vmp
1\')" envelope,vmp
I"X;/ eqReactor. vmp
I\D" Event Scheduler Example,vmp
1\:,.''' examplel.vmp
Recent
Desktop
'--~)My Documents
Filename: Open
My Network Files oftype:Places
Case Files r,vmp}
Open as read-on~'
Cancel
Once the "Open" button is pressed, this will begin the importing process. Afterthe Case is imported the GPSAClausPlantExample flowsheet will be the activesheet in the PFD.
Open the form for the Sour Feed stream.
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
2
Virtual MaterialsGroup, Inc.
Solved
Spec From
l~ Detail View
r Exclude from Summary
L~.~·~.~l~~:ry,;Jl Equilibrium Results I line SiZing J Sulfur Detaill
Properties
f"'loleHYDROGEN SULfIDECARBON DIOXIDE
W.lITERf"'lETHANESULfURSULfUR2SULFUR6
SULFURSOXYGENNITROGEN
SULfUR DIOXIDE
r ;Ignored
GPSAClausPl...
Obmole/hI0.60649 291.060.32171 154.390.06199 29.750.00981 4.71
0.,00 0.000,00 {),OO
0.00 0.000.00 0.000.00 0.000.00 0.000.00 0.00
Db!hl[ft3/s]
0.99959110.0
20.70479.91
17326.0139.355
0.0964. 3708E+0
IFractiQnl[Fraction]
to
Remove all of the specified information in Sour Feed. This will cause the Clausplant to become unsolved, and will allow Sour Feed to be specified by connectingit to the Acid Gas stream of the MDEA plant via a cross connector.
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
3
Virtual MaterialsGroup, Inc.
r Detail View
r Exdude From Summary
Equilibrium Results Iline Sizing ISulfur Detaill
GP5ACIausPI...VapFrac
(F]P [psia]
MoleFlow ~bmole!hJ
f¥lassFlow ~b!h]
VolumeFlow [ft3/sJStdLiqVolumeFlow [ft3/s]StdGasVolumeFlow ~"1r"'SCFDJ
Properties
r·loleHYDROGEN SULFIDECARBON DIOXIDE
"'\lATERf'4ETJ-1,Il,NE
SULFURSULFUR2SULFUR6SULFURSOXYGENNITROGENSULFUR DIOXIDE
Navigate to the Main Flowsheet.
Ublh][ill/sJ
r Ignored
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
4
4 Virtual MaterialsGroup, Inc. Simulating with ~~~~il!1~
Create a cross connector and connect it to the Acid Gas stream.
Open the form for the cross connector.
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
5
EI
Virtual MaterialsGroup, Inc.
Summary I
;IC(lnflected StreamjUnit Op
i 1~:~~~'~~~~i~~:~::}[ft3iS]if U-1r'lSCFD]ProPerties (Alt+R)Fraction [Fraction]NITROGENCARBON DIOXIDEHI'DROGEN SULFIDEMETHANEETHANEPROPANEIS08UTANEn.£LrrANEISOP8'iTANEn-PENTANEC6+"V...'ATERr'IETHYL DlETHANOLAMINEr·jassFraction [Fraction]StdVolFraction [Fraction]
; if:j:;' MoI'eFJc,w gbmc<!elh]
Properties (Alt+R)Fraction [Fraction]NITROGENCARBON DIOXIDEHYDROGEN SULFlDE14ETHANEETHANEPROPANEISOBLrrANEn-BLrrANEISOPENTANEn-PENTANEC6+"
METHYL DIETHANOLAl"1INENassFraction [Fraction]StdVdFraction [Fraction]NoleFlow [Ibmolelh]
Highlight the Connected Stream/Unit Op cell for the Outlet and select browsefrom the pull down menu.
532,8820169.96
Use the Navigation form and select Sour Feed in the GPSAClausPlantExampleflowsheet.
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
6
Virtual MaterialsGroup, Inc.
j" Showfree ports only
Click OK. This will cause the stream information for the Acid Gas stream to bepassed to Sour Feed.
HYDROGEN SULFIDE~1ElHANE
EJ}'ANE
PROPANE
ISOilUTAlifn'BUTANEISOPENTA1'~E
ri-f>ENTANE
Note that the difference in the components available in the Main andGPSAClausPlantExample flowsheets.
Move to the GPSAClausPlantExample flowsheet, notice that after the streaminformation from Acid Gas has been passed to Sour Feed there is enoughinformation for the Claus plant to solve.
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
7
.~ Virtual MaterialsGroup, Inc. Simulating with VMGSim
Notice that with the temperature and pressure specified to be transferred in thecross-connector, which is the default, that the acid gas is no longer entirelyvapor.
Air
'."""-".-:'~""-"~"-.
Air"Jet"Sat
Therefore, it should be seen what happens when different properties aretransferred in the cross connector. Return to the main flowsheet and open thecross connector's form. If the temperature intensive variable is ,replaced with thevapor fraction instead, it can be seen that the temperature is actually still 120.0 F.Therefore, this will provide more accurate results for the work done with theClaus plant.
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
8
/lame: rxl---~ Description: r-~-_..--.-----------5<>lved
with VMGSimVirtual Materials
Group, Inc.
[Add"]i;-------- ----..fl::::!:.~.3--.... r;GPs,ll,CJausPlantExam, ,~~
Summary INotes "I
S Intensive Variables B Advanced
iIIntensive Var 1 VapFrac j r;:;;;:;;:;;;:;;;::;;;:;;;;;;---;o;;;;;;;:;;:]illntensiveVar2 pI
r Ignored
0,378380,5319
0,08689
0.00280,000,000,00
-5,549E+7
-102115.35,23537,92
0.11898,698
0,01021.4623E-2
319.0181.0000
Dbmole;h][!b/h]
:t VollumeFio'''' [ft3/s]
II~:~~~:~\~~'~~:I~~~:,;[ft3fS]II: [f'<l~lSCFD]
Properties (Alt+R)Energy [Btu/hr]H [BtuilbmoilS [Btu,1bmol-F]f'1olecul.rWeight~1.ssDen,ity [!b!ft3]Cp [Btu!1bmol-f'jTherm.ICc,nductivity [Btu!hr-ft-F]VIscosity [ep]malarV [ft3fibmoilZFactorFraction [Fraction]HYDROG8' SULFIDECARBON DIOXIDE'li'VATERf£HANESULFURSUlFUR2SULFUR6
0,000020,531690,37823
0'
0028
10.000250,00007
0.00
-5,551E+7
-102117,341,8-373-7,92
0.11978.772
0.01031,4326E-2
316,6540,9926
19,50543,71
20515,90
47.8250.113
4,9519E+oProperties (.<\It+R)Energy [Btu.ihr]H [BtufibmailS [Btufibmol-F]r-iolecularWeightMa5sDensity Dbfft3]Cp [Btu,1bmol-F] •ThermalConductivity [Btu,hr-ft-F]V~CQsity [ep]molarV [ft3/1bmol]ZFactorFraction [Fracton]NITROG8'1CARBON DIOXIDEHYDROG8, SULFIDEMETHANEETHANEPROPANEISOBlJfANE
One other area where different property packages can be used is with individualunit operations and streams. This will be shown by comparing the results for theamount of steam produced by the waste heat boiler. Currently, the steam isproduced using the properties obtained from the Claus property package, Thisproduces 250 psia steam with the following properties and flow rate.
© 2009, Virtual Materials Group, Inc, Do not copy unless authorized in writing by VirtualMaterials Group.
9
Virtual Materials
Group, Inc. Simulatin with VMGSim
B Name: :1250 psi~wsl:ear" Description:
.solved
Spec from
0.000.00
581.12
r Ignored
11 lIn
Obmolelh]0.000.001.00
-5.891E+7-101394.8
-12.45318,02
0.48758.360
0.01991,6470E-2
36,9511.0000
1.00401.1,.······························,················,1
250.00581.12
10469,065.9650.047
5.2926E+OPropertiesEnergy D3tu/hr)H [B1JJflbmol]5 [B1JJ}1bmol-F]r.1olecularWelghtMassDensity Ob/ft31Cp [Btu.,~bmol-FJ
ThermalConductivity [Btu/hr-ft-F]Viscosity Tcp]molarV [ft3flbmol1ZFactorr,jole
HYDROGEN SULFIDECARBON DIOXIDEWATER
Connected to [In IOut)VapFracT [F]P [psia]r~oleFlow Dbmole/hIMassFlow Db/h]VolumeFlow [ft3!s]StdLiqllc,lumeFlow [ft3/s]iStdlGasVolLlmeF'low l.MMSCFDI
r- Detail View
r Exclude From Summary
Summary IEquilibrium Results IDne Sizing I Sulfur Detail I Notes I
Next, we will perform this same procedure, except with Steam 95 as the propertypackage. To do this, open the thermodynamic model window. Currently, it looksas below, with only the Amine and Claus property packages included.
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10
Virtual MaterialsGroup, Inc.
ChemJcal Soh;entPhysi.-:al Solvent
f""' Add Solid Support
In order to use the Steam 95 package, press the u<Add New Package>" underthe "Created Property Package" section. This will create a "VMGThermo"package, which needs to be specified. The thermodynamic model of thispackage should be changed to "Steam 95".
Components; Settings! BoilerPlate
Then add water as the only component in this system.
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11
" Virtual MaterialsGroup, Inc.
Add selected! ISimulating with VMGSim
Property Package Componenm ISettings] Boiler Plate J
Now press "Apply" to add this property package to the case.
Opening the "VMGThermo" property package node, it can be seen that there isthe option to add a new link to the property package. This property packagemust be linked to both the water and steam streams, as well as the heater. Todo this, select "<Browse>" under the "<Add New Link>" drop down menu.
Under the GPSAClausPlantExample, select the two streams that are needed,"250 psig steam" and "250 psig water", as well as the heater, H1. These musteach be done separately.
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12
~ancel J
Simulating with VMGSimVirtual Materials
Group, Inc.
1-c;-D~~~:~~:~~~~m5I', H Absorbersj Contactor
i"i ValvesV1
,,'=, Flowsheets
'.,' GPSAClausPlan!Example:C) HaterialStreams
!~?~'~?=e'~.;.~.~~~~~:~~~]250...psig":NaterAirAir_ToJurnac.eAir_to_5atFl'Om_Bed-lFfom_Bed-2Fron1_'tlHBFurn&ceyeedSaturation_WaterSour_FeedSQur_Gas_TQ_FurnaceS~""}eep_Gas
ToReheater-1
ToSulfurPit-l
To_Bed-lTo_Bed-:?To_IndneratorTo_ReHeater'2
To_SulfurPit-2To_SulfurPit-3Tc,_WHB
EnergyStreams
Ql!;,;., rl;::uu:_~.p.:=IlrtionFlu·n;::lr~~
OKL::--=-
After each of these links has been made, press "OK" in the thermodynamicmodel form.
The steam out of the heater will now look as below. Note that the temperature isalmost identical to the previous temperature of 401.1 F. However, the flow rateof the Steam 95 steam is 0.047 MMSCFD larger than when the Claus propertypackage was used. These results are now more appropriate and will provide amore accurate design.
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13
with VMGSim
1.00401,0
250.00586,30
10562,34
5.410
PrcopertiesEnergy [Bbu/hr]H [BlulQbmollS [Bbu}1bmol-F]MolecularWeightMassDensity Db/ill]Cp [Bbu,llbmol-F]mermaICondu,:tivity [Bbu/hr,ft-F]Viscosity [ep]molarV [ft3jQbme,1jZfacborf¥1oleWAlER
Virtual MaterialsGroup, Inc.
1 Detail View"I Exclude From Summary
Summary I£quilibrium Results !lineSizjng I Notes'l
iI r'loleF'lo'", Ubmole/h]i! M21ssfl(m Db/h]iI Vt.llurrleFlclw [ft3is]II SbdLiq'iiolurneFII)'N [ill/5]IStljGa,sVoJ'umf~Flow [r.lf'1SCFD]
B !'Iame:f2~Q' ste;~ Description:
.solved
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14
Virtual MaterialsGroup, Inc. Simulating with VMGSim
Crude TowerExample
Crude Feed
M1
Crude Furnace
Crude_Feed_1
Crude_Steam
Ven~Gas
-------~~ Condenser_Water
Kerosene
DieselDieselSS-Steam
Gas Oil
AGOSS:Steam
ResidueCrude_Tower
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,~ Virtual MaterialsGroup, Inc. Simulating with VMGSim
Crude Tower Summary
Property PackageAdvanced Peng-Robinson Property Package
ComponentsMethane, Ethane, Propane, IsoButane, n-Butane, Water, "Oil Pseudo-Comps"
Stream InformationI
Stream Crude_Feed AGOSS- DieselSS- Crude-Steam Steam Steam
T (F) 450 300 300 375
P (psia) 75 va 50 150
Mass Flow (Ib/hr)I --- 3000 3000 7500
StdLiqVolumeFlow 100000 --- --- ---(bbllday)
StdGasVolumeFlow --- --- --- ---(MMSCFD)
ut::::lilled oil" 0.0 0.0 0.0ane
Ethane "Defined oil" 0.0I
0.0 0.0
Propane "Defined oil" I 0.0 I 0.0 0.0
IsoButane "Defined oil" 0.0 0.0 0.0
n-Butane "Defined oil" 0.0 0.0 0.0
Water "Defined oil" 1.0 1.0 1.0
Oil Psudeo-Comps I "Defined oil" I 0.0 0,0 0.0
All compositions in mole fraction unless noted otherwise
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,~ Virtual MaterialsGroup, Inc. Simulating with VMGSim
Oil Assay Summary
AtmCrudeTowerFeedBulk LD60 [API (60/60F)] = 29.0
Light Ends (Volume Percent): Methane = 0.0065
Propane = 0.32
n-Butane = 0.82
TBP Curve (Volume Percent): 0.0 = 15 F
4.5 = 90 F
9.0=165F
14.5 = 240 F
20.0 = 310 F
30.0 = 435 F
40.0 = 524 F
50.0 = 620 F
60.0 = 740 F
70.0 = 885 F
76.0 = 969 F
80.0=1015F
85.0 = 1059 F
Unit Operation Summary
Crude HeaterDeltaP = 10 psi
Out T = 650 F
Ethane = 0.0225
IsoButane = 0.24
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.", Virtual MaterialsGroup, Inc. Simulating with VMGSim
Crude Tower (RefluxedAbsorber)30 Stages
Add water draw to Stage 1
Connect Crude_Feed_1 as Feed to Stage 29
Connect Crude_Steam as Feed to Stage 30
15t Stage Pressure - 19.7 psia
2nd Stage Pressure - 28.7 psia
30th Stage Pressue - 32.7 psla
Pump Around1 from Stage 3 to Stage 2
Pump Around2 from Stage 18 to Stage 17
Pump Around3 from Stage 23 to Stage 22
3 Stage Side Stripper1 from Stage 10 to Stage 9 with Energy Input
3 Stage Side Stripper2 from Stage 18 to Stage 17 with Steam Input
3 Stage Side Stripper3 from Stage 23 to Stage 22 with Steam Input
Connect DieselSS-Steam as feed to Side Stripper2
Connect AGOSS-Steam as feed to Side Stripper3
Add Trim Energy In to Stage 29
Add Overflash internal liquid stream on stage 28
Tower Specifications: Condenser liquid standard liquid flow rate =23000 bbl/day
Condenser vapor flow rate = 0 Ibmole/hr
Side Stripper1 standard liquid flow rate =9300 bbl/day
Side Stripper1 energy = 7.5 E+6 Btu/hr
Side Stripper2 standard liquid flow rate = 19250 bbl/day
Side Stripper3 standard liquid flow rate = 4500 bbl/day
Pump Around1 standard liquid flow rate = 50000 bbl/day
Pump Around2 standard liquid flow rate =30000 bbl/day
Pump Around3 standard liquid flow rate =30000 bbl/day
Pump Around1 energy = 5.5 E+7 Btu/hr
Pump Around2 energy =3.5 E+7 Btu/hr
Pump Around3 energy = 3.5 E+7 Btu/hr
Overflash standard liquid flow rate = 3500 bbl/day
Tower Estimates: Stage 1 Temperature =100 F
Stage 2 Temperature = 250 F
Stage 30 Temperature = 600 F
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Virtual MaterialsGroup, Inc. Simulating with VMGSim
){L1
52
Excel Unit OperationExample
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Virtual MaterialsGroup, Inc. Simulating with VMGSim
Summary
Property PackageNRTL
ComponentsEthanol, Water
Stream InformationStream Name 81 82
VF 1 aT (F) - -P (psia) 15 -
Mole Flow 76.8 -(Ibmol/hr)
Ethanol 0.5 -Water 0.5 -
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Virtual MaterialsGroup, Inc. Simulating with VMGSim
Unit Operation Summary
C1DeltaP - 20 kPa
XL1Import
Mass density 81 (Mass Density)
Export
Mass Flow 81
Specify
Pitot Coefficient - 0.95
Pipe Diameter - 0.3m
Pitot Delta p.:... 0.05 kPa
Calculate
Velocity
Volumetric Flow
Mass Flow
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.,~ Virtual MaterialsGroup, Inc. Simulating with VMGSim
ExcelUnitOp ExampleIn this example we will create an ExcelUnitOp to calculate the mass flowmeasurement provided by a Pitot tube. This unit operation will determine the flowof a vapor stream feeding a condenser using the pressure difference measuredby a Pitot tUbe and the inner diameter of the pipe feeding the condenser. Thebasic working equation for a Pitot tube is shown below.
Vo =C~2~Va is the velocity of the fluid at the tip of the Pitot Tube, C is a calibrationconstant, in this case assumed to be 0.95, M is the pressure differential read bya manometer connected to the Pitot tube, and p is the density of the fluid at thetip of the Pitot tube. In this case, we know the composition of the fluid as well asthe fact that it is a saturated vapor coming from the first tray of an industrialethanol production tower, as well as the M read at the plant. Our task is tocalculate the necessary amount of cooling water to cool this vapor from the dewpoint to the bubble point. We also know that the internal diameter of the vaporpipe is 0.3 m.
Start a new VMGSim Case and use the recommended property package with theNRTL property package selected and add Ethanol and Water as components.Define a material stream as described below.
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1
Virtual MaterialsGroup, Inc.
~ecFrom
Detail View
Exclude From Summ,:lt'y'
[~~.~~~~.~~.iJl Line Sizing IEquilibrium Resultsj
Material --~._-..-_ _- : -..--.----.- -...----- ------- ---------..-'---~c_.---- .---...............-.------c_--.,
Connected to [In lOut]VapFracT[C]P [f'-Pa][\'loleFlow [kgmole/h]fYlassFlow [kg/h]VolumeFlow [m3jhr]StdLiqVolumeFlow [m3jhr]stdGasVolumeFlow [SCMD]i£ F'ropertiesI::::: rYlole
ETHANOLWATER.
If! ~~ass
FE StdLiqVolume
1.00
79.3105.00
[Fraction][Fraction]
Print Create Port Delete Port Ignored
Note that the thermodynamic state of the material stream is defined, but the flowrate is not known. Add an ExcelUnitOp to the flowsheet, click the enable macrobutton on any dialog boxes that popup. The ExcelUnitOp will appear as follows.
Click the Show Spreadsheet button to show the Excel spreadsheet. It will appearsimilar to the worksheet below.
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2
-A
,$ Virtual MaterialsGroup, Inc.
I~ ~
Ready
The Instructi.ons worksheet contains instructions for working with theExcelUnitOp. The Connections worksheet contains the necessary connectionsbetween Excel and other VMGSim unit operations. This worksheet is protectedand you should not modify its contents manually. Finally, the UnitOp worksheetis your work area for the definition of your unit operation.
Your work area can be multiple worksheets and you can create new worksheetsas your work area.
Let's start by defining our work area as suggested below.
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3
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There are two ways of connecting the Excel unit operation with VMGSim. Firstwe will connect the Molecular Weight of S1 to the cell 83 using Copy/PasteConnection.
Click on the Properties node in S1, select the MolecularWeight cell and right clickon it. You will see the following pop up menu.
r' Detail View
Exclude From Summary
Summary ILine Sizing I Equilibrium Results 1
Copy Whole Table
Copy Columns with Heading
Copy
Print Portrait
Print Landscape
Properties
Energ~'[W]
H [kJ/kmol]S [kJ/hnol-K]MolecularWeightrJ1assDensit~1 [kg/m3]Cp· [kJ/kmol-K]ThermaIConductivit~' [WIm-K]Viscosit~' [Pa-s]molarV [m3/hnol]ZFactor
~;;;;;;;.;~;;;;;;;.;=~=~ __ .Spec 'In' As ,.,
Select Copy Connection.
Now select the Excel unit operation and go to the 83 cell. Right click on the 83cell and the following pop up dialog will appear.
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4
Virtual MaterialsGroup, Inc. with VMGSim
db cut~ ~opy
~ Easte
Paste 2Pecial ...
Insert. ..
Qelete•..
Clear Contents
Import/Export Obiect; •.
Set IJnit...
Show Object Data ."
Update All Object Data
Select Paste Connection by clicking it or by pressing Ctrl+Shift+V.
Note that the molecular weight of material stream S1 is now connected to Excel's83 cell. This is a live connection and any changes happening in the VMGSimproject will be automatically reflected on cell 83.
A useful feature of VMGSim's Excel unit operation is the use of tool tips toidentify the connection between VMGSim and Excel. Just place the mousepointer over the 83 cell and the following tool tip will appear.
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5
UnitType: r"l'Jlecular\',VeightUnit:Imported from: /S1,r'lolecular"Neight, f'.'lolecular',Neight
Virtual Materials
Group, Inc. Simulatin\/MG Values
We will now connect the 84 cell to 81's mass density in a different way using theObject Inspector.
Right click on the cell 84 and select Import I Export object.
Insert",
Q.elete•••
Clear Contents
Ed Insert Comment
Eormat Cells".
Pich From List .. ,
Set Unit...
CQP'i Connection Ctd+shift+C
Paste Connection Ctrl+Shift+V
Show Object Data .•..
UpdC\te All Object Data
The Object inspection form will appear as shown below.
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
6
79,307600169" ,105 * kPaNoneNoneNoneNoneNoneNone17055,004286" .212,81213537",41.8604661.4998785213" .68.261673028" ,2.1939996367, "1.0639379320" ,27,909237583, ,,
1
0,85 *0,15 *
'Data
, 51.In
Variable
TPMoleFlowfvlassFlow
·VolumeFlow
IIStduqvolumeFJow
•StdGasVolumeFlow,EnergyiH -isIMolecularWeighti ~1assDensjty
CpThermalConductivityViscositymolarV
IZFactor,Fraction.ETHANOL,
IFraction.WATER· MassFraction.ETHANOL
Material5treams
Virtual MaterialsGroup, Inc.
I--=..mport 'I Export
Select Mass Density and press the Import button
179,307600169" ,
105 *' kPa
NoneNoneNoneNone~,one
None17055,004286. "212,81213537...
41.860466
68.261673028., ,
2.1939996367...1.0639379320" ,
27.909237583. "10.85*0.15 *
0,9354452480" ,
,cancell
VapFracTPMoleFlowMassFlowVolumeFlowStdUqVolumeFlowStdGasVolumeFlowEnergyH5MolecularWeight
cpThermaJConductivityViscositymolarVZFactorFradion.ETHANOLFraction, WATERMassFraction.ETHANOL
IS1.In
ExportImport
i::-j /
:::::: Material5treamsI±: 51
The mass density is now connected to cell 84.
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7
Virtual MaterialsGroup, Inc. Simulatingvvith VMGSim
Now specify the constant values as below.
The velocity of the fluid can be calculated using the Pitot tube formula,
l';, ~ C~2 ~ . Note the 1000 factor to convert the pressure from kPa to N/m2.
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8
Simulatin with VMGSim=BEi*SGlRT(2*·1 000*B8/B4)B11
J Virtual MaterialsGroup, Inc.
Next we assume that the flow is completely developed and the volumetric flowcan be calculated by.multiplying the veloc:ity by the pipe area.·············Bi2··;J·····---~~I~~IQ:(@f(2j.~?*B1 -1.. .
ABC..................................._--_....... , --.- - _ .
:VMG \!'allll:1s
The mass flow in kg/s can now be calculated by multiplying the volumetric flowby the mass density.
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
9
813 ....
VMG \!alll€!§A C
Virtual MaterialsGroup, Inc.
And finally the mole flow in kmol/h can be calculated using the mass flow and themolecular weight.
814
AVMG Vailles
I~--·· -, .
c
Now the mole flow is going to be exported back to S1. Right click on the cell 814.Select copy connection.
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10
Virtual MaterialsGroup, Inc.
db cut............. - ..
~ kOP~l.......................................... ..' _ -.-
; _ _ et E:aste
Paste 2iJecial."
Insert" •
Q.eJete."
Clear Contents
'til Insert Comment
Eormat Cells".
Pief:; From List. i •
Show Object Data.,.
Update All
Now go to material stream 81 and right click on the MoleFlow cell. Finally selectPaste Connection.
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11
Virtual MaterialsGroup, Inc.
1.499941.86
NameMassDensit~l [kglm3]rvlolecularWeight
Detail View
Exclude From Summar~1
Summary 'I Line Sizing IEquilibrium Results 1Signal Ports -,- »,-- --,,,,,,,,,,.,,,,•• ,,,,,,,,,,,,.,, ""."""",,.,,---.,
. - ...-.~._~ ..._._...-..-Connected to [InI0ut]VapFracT[C]P[kPa]MoleFlow [kgmole/h]MassFlow [I<,glh]VolumeFlow [m3lhr]StdLiqVolumeFlow [m3lhr]StdGasVolumeFlow [SCMD]±, Properties::, rvlole
ETHANOLWATER
Create Port
1.0079.3
105.00
Print Portrait
Print Landscape
Copy INhole Table
Copy Columns with Heading
Copy
Paste
Cop';!' Connection
Note that the stream is now completely specified.
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12
Virtual MaterialsGroup, Inc.
Detail View
r Exclude From Summary
Summary ILine Sizing IEquilibrium Results
Signal Ports . ..._..~ .._-_...._.
1.499970.7341.86
60.12
r !gnored
79,31.00
[kgmole/h]0.850.15
[kg/h][m3/hr]
105.0070.73
2960.641973.922
3.6714.0213E+4
:[Fraction]
Delete Port I•• :%
lD=raction]I[Fraction]
Create PortJ
....~ _-- + _ , ············_······1
Connected to [InIOut]VapFracT[C]P [I1'a]MoleFlol-'.1 [kgmole/h]~~assFlo\", [kg/h]VolumeFlow [m3/hr]StdLiqVolumeFlow [mS/hr]StdGasVolumeFlow [SCMD]
Properties
"'loleETHANOLWATER
'f,ll'1ass
Now we have created an Excel unit operation with some connections. Click onthe Connections page we can inspect the information all the import/exportconnections.
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13
Ready
Virtual MaterialsGroup, Inc.
The worksheet correctly shows two imports and one export. In the case that thispage doesn't show the correct information, you can press "Refresh Connections"button to refresh this page.
Create a material stream (82) and specify it's vapor fraction to be O. Nowcomplete the problem by creating a cooler with a pressure drop of 20 kPa andconnect it's In material port to 81 and it's Out material port to 82 as shownbelow. The solved cooler and condenser duty are shown below in the figurebelow.
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14
Virtual MaterialsGroup, Inc. Simulating with VMGSim
SolvedB
IJ Mc,leF!c)w [kgmole/h], j ~lalssFlcJW [kg/h],I Vc,lumeFlclW [m3/hr]
qStdUQIVoILJrnel=low [m3/hr]IStdGasVollumeFlow [SCMD]
Properties (Alt+R)Fraction [Fraction]ETHANOLWATERMassFl-action [Fraction]
1.0079.3
105.0070.73
2960.651973.924
3.6714,0213E+4
0.0073.8
85.0070.73
2960.653.9433.671
4.0213E+4
Note that if the pressure of stream S1 changes the flow of S1 will now change asshown below.
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15
Virtual MaterialsGroup, Inc.
ID>ec From
r' Detail Viewr- Exclude From Summary
A'
Ignored
3,946E+517584.8
4.5934E+4
..........................._ _- -Connected to [InjOut]VapFracT [C]P [!<Pa]MoleFlow [kgrnolelh]fvl.~ssFlow [kglh]VolumeFlow [m3lhr]StdLiqVolurneFlow [m3Ihr]StdGasVolumeFlow [SCMD];':'; Properties
Energ\' [W]H [kJll:mol]
Summary' 'j Line Sizing !Equilibrium Results
Ports .' -.- -... ························---·0 -...•..,
Naturally, if values on the Excel unit operation are changed, a new flow will alsobe calculated. Assume that the calibration factor was recalculated to be 0.98.The flow will be immediately recalculated as shown below.
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16
Virtual MaterialsGroup, Inc. Simulating with VMGSim
r !gnDred
68.6712.12
r' Detail View
r Exclude From Summary
1.0087.0
140.0080,79
3381.861728.068
4,1934.5934E+4,
'[Fraction]
VapFracT[Clp [YPa]MoleFlow [kgmole/h]MassFlow [kg/h]VolumeFlow [m3/hr1StdLiqVolumeFlow[m3jhr]StdGasVolumeFlow [SCMD]
Properties~'ole
ETHANOLWATER
it} r~ass
if] StdLiqVolume
5ummary IEquilibrium Results 1Line 5izing IMain Data
The flow rate can also have been specified as a mass flow rate. To change this,the molar flow rate must be disconnected. Go to the spreadsheet and right clickon the connected molar flow rate cell. Press Disconnect Import/Export Object.
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17
Virtual MaterialsGroup, Inc.
~ Eot'mat Cells .. ,
Pic!!, Fmm List ...
Show Object Data.. ,
Update All Object Data
Returning to VMGSim, it can be seen that the flow rate is no longer connected to81, and the stream is no longer solved.
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
18
Virtual MaterialsGroup, Inc. Simulating with VMGSim
Detail View
Exclude From Summary
summaryl Equilibrium Results! Line Sizing IMain Data
CUn
1.957041.86
17584,8211.907
41.861.957069,1400,0228
1.0848E-521.3901.0000
I[Fraction] [kgmolelh]0.850.15
II' [Fraction] [kglh],[Fraction] [m3/ht·]
ValueNameMassDel1sity [kglm3]lvlolecularWelght
Connected to [InIOut]VapFracT[C]P [l<I'a]IvJoleFlo\'i [kgmolelh]IvJassFlow [kglh]VolumeFlow [m3Ihr]StdLiqVolumeFlow [m3/hr]StdGasVolumeFlow [SCIvlD]',,! Properties
Energy [W]H [kJlhnol]S IkJ/kmol-K]~1oletularWelght
MassDenslty [kglm3]Cp [kJlhnol-K]ThermalConductivity [Wlm-K]Viscosity [Pa-s]molarV [m3/hnol]ZFactorMoleETHANOLWATERMassStdLiqvolume
The formula for molar flow rate can now be removed from the spreadsheet. Also,the molecular weight can be disconnected, as it is no longer needed. Notice howwhen disconnected imported cells return a value of '#NULL!'.
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19
,ll Virtual MaterialsGroup, Inc.
Simulatil"lg... ""i!I~YJVlGSim
Now connect the mass flow value to 81 by right clicking on the mass flow celland selecting 'Copy Connection'.
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20
with VMGSimVirtual Materials
Group, Inc.
jb Cut" , , ,.. - ' ~ kOPy
~ e.aste
Paste 2,pecial ...
Insert .
Qelete .
Clear Contents
d.(.r:::a Insert Com.ment
Import/Export Obiect, ..
Set Unit",
P§.ste Connection ctrl+Shift+v
Show Object Data, ..
Update Object Data
Then chose to paste the connection in the mass flow cell in 81.
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21
Virtual MaterialsGroup, Inc. Simulating with VMGSim
r' Detail View
r- Exclude From Summary
T[C]P(I'Pa]MoleFlow [kgmolelh]
iiVolumeFlow [m3Ihr]StdLiqlJolumeFlow [m3Ihr]5tdGasVolumeFI,)w rSC~1D]
J: Properties"': Ivlole
ETHANOLWATERI'lass
t: StdLiq\lolume
Print PortraitPrint Landscape
Connection
rXgnored
Notice that the value of the flow rate is much less than the previous value whenthe molar flow rate yvas used.
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22
Virtual MaterialsGroup, Inc. Simulating with VMGSim
r Detail View
r·o
Exclude From Summary
Summary IEquilibrium Results I· Line Sizing IMain 0"1·,, ,.,...........................•.,
Connected to [InIOut]VapFracTIC]P [!<Pa]MoleFlow [kgmole/h]MassFJow [kglh]VolumeFlow [m3/hr]StdLiqVoJumeFJow [m3!hr]StdGasVolumeFlow [SCMD]if: PropertiesE:! r10le
ETHANOLWATER
l±.l Massif) StdLiq"'olume
{[LIn
1.0087.0
140.000.020,94
0,4800.001
1.2759E+1
[Fraction] [kgmoJe!h]0.85 0.020.15 0.00
i[Fraction] [kg/h]I[Fraction] [m3/hr]
r· Ignored
This is because the mass flow is in kgIs in Excel, but in kg/h in S1. Therefore,the units must be converted. This can be changed by editing the formula formass rate, or by specifying the units of the flow rate. To do this, right click on813 and select 'Set Units'.
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23
J Virtual MaterialsGroup, Inc.
O.H3H4f1hr:;RI-;'M,CU!;
........................................ -- - .
I§l§l ~.oP~·
~ E:aste
Paste ;2pecial" ,
CQP~' Connection Ctrl+Shift+C
Pgste Connection Ctrl+Shift+V
Show Object Data."
Update All Object Data
Set the unit type as 'MassFlow' and the unit as 'kg/s'.
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24
,~ Virtual MaterialsGroup, Inc.
Unit Type:
Unit:
Simulating with VMGSim
OKIbl'hkgl'h
L.....""::"':"'''''::''':'''''''::''':'''''''::''':'''"'''1 Ibl's....... kgidIbidton(metric)/d
. . ················Ie-=ton""{s=h=ort::E.:::...d ---,-- ---,-- "..J -...........
By moving over the mass flow cell you can see that the unit has been changed tokg/so
VMG Values
UnitT~'pe: MassFlowUnit: kg/sExported to: 151. r'1assFlow.r""assFlow
Returning to 81, the mass flow rate has now been adjusted to be in kg/h, givingthe same results as when the molar flow was used.
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25
Virtual MaterialsGroup, Inc. Simulating with VMGSim
Spec From
r Detail I'iewr" Exclude From Summary
Summary '1 Equilibrium Results/line Sizing IEI Main Data _ ~.., _.... ...~_ _ .
JName
II ~:::~1::~~~~~1~;3],"'Material
[Fraction],. [Fraction]
• 1
68.67
12.12
[kgmolejh]0.850.15
[kg/h][m3/hr]
1.0087,0
140.0080,79
3381.86
1728.0684.193
4.5934E+4!:[Fraction]
.........-.----l-..-.---Connected to [In/Out]l'apFrac
1T [C]JP [~Pa]
, 'I.' MoleFlow [kgmolelh]!•rvlassFlow [kg/h]; j l'olumeF!ow [m3/hr]'I Stdliql'olumeFlow [m3/hr]!,. ~tdGaSl'olumeFlow [SCMD]~ ttl Properties
'Ii=] Mole! ETHANOl
.1 WATER
'I' it: Mass,:FE StdliqVolume
__~rint ~I Create Port
Another way to obtain information in Excel is by using 'Show Object Data'. If itwas desired to create a phase envelope for S2 that can be used in Excel, 'ShowObject Data' can be used to do this.
First, create a phase envelope and attach it to S2. Since only water and ethanolare present, the dry basis must be turned off.
xu
Now, to important the phase envelope profile, go to the Excel spreadsheet andright click on an empty cell. Select 'Show Object Data'.
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26
Virtual Materials
Group, Inc. Simulating with VMGSinlC=C"~r"~F~-]~G···•.•.·••.••••• !~~
dI:, Cui;
~ C;;OPY
mE'.aste
Paste ;apecial",
!nsert" ,
Q.elete".
Cleat Contents
til Insert Comment
~EotmatCells".
Piel From List".
Impott!EXpottObiect" .
Set lJ.nit".
CQPY Connection Cttl+Shift+C
Pgste Connection Ctt'i+Shift+V
This will bring up the following form in VMGSim.
I
QK .1 Cancel
To get the phase envelope profile, select 'Env1', then 'Profile' and select 'OK'.
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27
Virtual MaterialsGroup, Inc. Simulating with VMGSinl
IC::::::::i1r::::::::J1 Cancel I
This will import the phase envelope's data profile into Excel. This informationcan be gathered into a plot.
l... series1 I
200150100
T
50
500
2000
·1000 +---
·1500
This plot can be edited as desired.
'Show Object Data' does not update until the case is fully solved. However, oncethe case is solved, it will be updated.
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28
Virtual MaterialsGroup, Inc. Simulating with VMGSim
To see this, change the composition in 81 to be equimolar. The change can beseen in the plot in Excel.
7000
6000
5000
4000Q.
3000
2000
1000
00 50 100 150 200 250 300
T
I. Series'1 1
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29
Virtua~ MaterialsGroup, ~nc. Simulating with VMGSim
t II!! DSs~c,'"CPI
8p2
V1
Feed
Cavett Recycle Loop ExampleGunther, US Patent 3,575,077, April 13th , 1971
a
815
8111__ ~ c>,,,J[) .1
87
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Virtual MaterialsGroup, Inc. Simulating with VMGSim
Gunther Summary
Property PackageAdvanced Peng-Robinson
ComponentsNitrogen, carbon dioxide, hydrogen sulfide, methane, ethane, propane,isobutene, n-butane, isopentane, n-pentane, n-hexane, n-heptane, n-octane, nnonane, n-decane, n-dodecane
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
,j Virtual MateriaJsGroup, Inc. Simulating with VMGSim
Streanl InformationStream Feed 82 83 810 813Name
T (F) 120 -60 -60 -60 -60
P (psia) 287.7 -287.7 -287.7 -63.7 -27.7
Mole Flow - -0 -0 -0 -0(Ibmol/hr)
Nitrogen 358.2 1 1 1 1(Ibmole/h)
Carbon 4965.6 0 0 0 0Dioxide
Hydrogen 339.4 0 0 0 0Sulfide
Methane 2995.5 0 0 0 0
Ethane 2395.5 0 0 0 0
Propane 2291.0 0 0 0 0
Isobutane 604.1 0 0 0 0
n-Butane 1539.9 0 0 0 0
Isopentane 790.4 0 0 0 0
n-Pentane 1129.9 0 0 0 0
n-Hexane 1764.7 0 0 0 0
n-Heptane 2606.7 0 0 0 0
n-Octane 1844.5 0 0 0 0
n-Nonane 1869.0 0 0 0 0
n-Decane 831.7 0 0 0 0
n-Dodecane 1214.5 0 0 0 0
Unit Operation Summary
CP1Adiabatic Efficiency - 75%
OutP - 814.7
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.~ Virtual MaterialsGroup, Inc.
C1GutT - 100 F
DeltaP - 0 psia
V2GutP - 63.7
V3GutP - 27.7
CP2
Simulating with VMGSim
Adiabatic Efficiency - 75%
GutP - 63.7
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Virtual MaterialsGroup, Inc. Simulating with VMGSim
Recycles in VMGSimVMGSim handles recycles in a rather intuitive, but quite different way whencompared to other process simulators. In this section we will simulate anisothermal distillation arrangement and examine how recycles can be used indetail.
Problem statementHenley and Seader (1998) present a delightful problem that was formulated byCavett and extensively used to test tearing, sequencing and convergenceprocedures for steady state process simulators. The flowsheet is equivalent to a4 stage, near isothermal distillation tower instead of the common near isobarictype. It is desired to determine the flowrates.
Problem SetupStart up VMGSim, choose Advanced Peng-Robinson as the property package ofchoice and add N2, C02, H2S, C1, C2, C3, iC4, nC4, iC5, nC5, C6, Cl, C8, C9,C10, C12.
Create a material stream called feed and specify it as shown below.
CA1=tE()N DIOXIDEHyDROGEN SUlFIDEf>lETliANEEntANEPROPANElSOBUTAHEn-BUTANErSOPENTft.HEh-PENTAhEn-HEXANEn-HEPTAf".E
n-GerANEn-NONAl'iE
n-DECANEn-DPOECANE
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1
Virtual MaterialsGroup, Inc. Simulating with VMGSim
Creating the Tower Feed StageIn a separation stage we have as feeds the liquid from the stage above and thevapor from the tray below. In a feed stage we will also have the feed we want toprocess. Therefore we can model a feed stage as a mixer with the In ports and aseparator.
1. Create a Mixer unit operation
2. Open the Mixer form. You will have the following:
'I Mc)leFI(lW Dbmole;h],I r'lclSsFI(JW DbirQ" Voluf1le,Flow [ft3/s]: j 5tdLiql/olurneFI,ow [ft3/s]'l Sl1JGasVolurneFlllw [MMSCFD]
Properbes (Alt+R)HoleFractionf'1assFracbonStdvolFractionHoleFlow Dbmole/h]r,jassFlow Db/h]
±StdLiqVolumeFlow [ft3/s]
peletePort J Ignored
3. Press the Create Port button to add a new port.
4. Connect the material stream Feed to the mixer M1 middle port.
5. Now connect a two phase separator to the Out port of M1 using a materialconnector
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2
Virtual MaterialsGroup, Inc.
~~~~...........~.:;;.: ~.Feed
M1
Simulating with VMGSim
81
8ep1
6. Note that for the time being we have no additional information. To proceedwe have to estimate the values that are fed to M1. This is done by addingtwo new streams to the In ports of M1.
7. Estimate values for S2 and S3 In ports. Since we have nothing better we willestimate the flows as zero and set an arbitrary composition.
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3
Virtual MaterialsGroup, Inc. Simulating with VMGSim
Spec From
I'm Detail View
r Exclude From Summary
Summary Equilibrium Results I Line Sizing I
[Ibmole/h]il ~1a;ssFIc)w [lb/h]q VolumeFlow [Ft3/s]ijStIJLiqllolwrneFI,)w [ft3/s]:IStdGclsVo,lum,eFlow [r,IMSCFD]
Propertiesf'loleNITROGENCARBON DIOXIDEHYDROGEN SULFIDEfvlETHANEETHANEPROPANE
1.00liO.O
287.700.000.00
0.0000.000
2.0079E-42
[Ibmole/h]1.00 0.000.00 0.000.00 0.000.00 0.000.00 0.000.00 0.00nnn
r Detail View
j~ Exclude From Summary
1.00liO.O
287.700.000.00
0.0000.000
2.0079E-42
r Ignored
[Ibmole/h]1.00 0.000.00 0.000.00 0.000.00 0.000.00 0.000.00 0.00"nil
\!"pFracT[F]P[psia]fvloleFlow [Ibmole/h]MassFlow [Ib/h]VolumeFlow [ft3/s]StdLiqVolumeFlow [ft3/s]StdG"sVolumeFloV'.' If~M5CFD]
Properties[':'Mole
NITROGENCARBON DIOXIDEHYDROGEN SULFIDEMETHANEETHANEPROPANE
Summar!( Equilibrium Results I Line Sizing I
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4
Virtual MaterialsGroup, Inc. Simulating with VMGSim
Partial Condenser SetupThe top stage is comprised of a compressor and a condenser. The compressorwill raise the pressure to 814.7 psia and the condenser will drop the temperatureto 100 F. For the sake of simplicity we will assume that the adiabatic efficiency ofthe compressor is 75 % and that the condenser has no pressure drop.
1.00
272.5
814.70
9079.28
314931.82
21. 714
2.630
56.lnL.J
1.00120.0
287.70
9079.28
314931.82
49.514
2.630
8.269E+1
Summary ICurves 'I Plot IB Main Dal:a --"'-c---"c...------ ...·--.,.-.-:-..• .. ·-·. !tl Adllanlced ::::::::::::::::,':::C::::::',C::::C::::;::-:::::·::.:C:::::::
: ~'Ja;"'e . 1>1 ValueIli~Q iH~;~~Po,~;~;j-"----j-56i2: 3-6II Delta P [psi]. 527,00
IIPre55ure Ratio • 2,83i Adiabatic Efficiency [%] I 15.00
I!Polytropic Efficiency [%] 77,23
11 Speed [rpm]
iI Adiabatic Head eft] 26511.14
.1 Polytropic Head eft] 27298,71
:- Material _..._._._-_._---_._.._--_.__ ... _-_._,-..... --------._.._... ,_.,"_.-._..,-.-._---......._.,'_.. ,',." ..,-,..,-._----,
'! PortName :In .... . .._.i~:~.t.. .__: iI5R~cy~I~Po;i: ..... ..... .....--------.C-;IConnected Stream/Unit Op
~ IVapFrac!'T[F]lip [p5ia]
II ~1oleFlow [Ibmole/h]
II ~lassFlow [Ib/h]
.IVolumeFlow [ft3/5]
: i'StdLiQVOIUmeFlow [ft3/5]SldGasVollJmeFlo~~[MMSCFD]±: Properties (AlttR)
!,,~: fraction [Fraction] .
" NITROGENII CARBON DIOXIDE• ! HYDROGEN SULFIDE
II r~ETHANEH
© 2009, Vittual Materials Group, Inc. Do not copy unless authorized in writing by VittualMaterials Group.
5
Virtual MaterialsGroup, Inc. Simulating with VMGSim
EJ
*:onrlected Stream/Unit Op
nrvlolei=low [Ibmole/h]!i. f'la,ssFJc)W [Ib/h]
n5tdLiclVohJme'FJow [ft3/s]HStdGasVol'umeiFlow [MM5CFD]
Properties (Alt+R)Fraction [Fraction]NITROGENCARBON DIOXIDEHYDROGEN SULFIDEMETHANEETHANE
1.00272.5
814.709079.28
314931.8221.7142.630
8.269E+1
0.96037100.0
814.709079.28
314931.8212.7762.630
8.269E+1
The arrangement is show in the picture below.
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6
,4 Virtual MaterialsGroup, Inc. Simulating with VMGSim
64 fJCP-1
85
Sep2
V1
Let's now create our first recycle, Attach the stream S2 to the LiqO Out port ofSep2. Note that VMGSim immediately starts to solve, and converges in 3iterations. This step is shown below.
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7
Virtual MaterialsGroup, Inc. Simulating with VMGSim
Lower StageWe can now create the lower stage just below Sep1. Recall that it will receivetwo feeds, one a saturated liquid from Sep1 and the other will be a saturatedvapor from the reboiler. Therefore we will need to set a mixer with the saturatedvapor estimated. As before we will set it to have a zero flow and an arbitrary molefraction. Note that this stage operates at 63.7 psia, thus we will have to add avalve between Sep 1 and Sep3.
5ummarvj Equilibrium Results I
0,00
Linear100.000
Dal.a·······_················ !tl Advanced •••••..............................
CvCftaracteristic% Opening [»/0]
B
0,00
78.363.70
15373,511485686,38
9,7649,738
1.4001E+2
/58.ln0,0078,3
63.7015373,51
1485686,389,7649,738
1.4001E+2
:~~I~~===========J1I~n======= lOutIs Recycle Port Er- []Connected Stream/Unit Op '57.0utlJapFrac
[f][psia]
MoleFlow [Ibmole/ft]MassFlow [Ib/ft]VolumeFlow [ft3/s]StdLiqlJolumeflow [ft3/s]StdGaslJolumeFlow [MMSCFD]
Properties (Alt+R)Fraction [Fraction]
ft) MassFraction [Fraction]Stdl.ialJ,JIFri3cti(Jn [Fraction]MoleFlow [Ibmole/ft]
This is illustrated below.
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8
85
Virtual MaterialsGroup, Inc. Simulating with VMGSim
.f.~~:lI;--!r-56--i>:.'Ir"~:"]···01 """10''''
_,--.,.----'- ~P2
Vi
Note that we can now connect the vapor outlet from 8ep3 to the Mixer M1. Justconnect the ports using the stream 83. The entire system converges in 11iterations.
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9
'" Virtual MaterialsGroup, Inc. Simulating with VMGSim
Feed
Partial Reboiler
84
C"Akt.·/.J..~""'~"".-'.•.~"•."'-.""-"'.-' d'.>......•.•• '.•....•..........•. " . .,.'.,0-'-..W " .... ·S8V*----Sg--"f'tV211DM2
*...-Sep3
We can now develop the partial reboiler, which operates at 27.7 psia. Note thatwe will need another valve between the liquid outlet from Sep3 and the mixer thatwill feed the reboiler. This is shown in the figure below.
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10
Virtual MaterialsGroup, Inc. Simulating with VMGSim
Summary Equilibrium Results 1
Characteristic% Opening [%]
36.00601.27Linear
100.000
0,05555
71.827.70
15373,511485686.38
57,1539,738
1.4001E+2
lOuti:JSI2.In
0.0078,3
63.7015373.51
1485686,389,764
9.7381.4001E+2
"Sl1.0ut
PortNameIs Recycle PortConnected Stream/Unit OpVapFracT[F]P[psia]fvloleFlow [ibmole/h]MassFlow [Ib/h]VolumeFlow [ft3/s]StdLiqVolumeFlow [ft3/s]StdGasVolumeFlow [~1r~SCFD]
Properties (Alt+R)::fJ Fraction [Fraction]':F MassFraction [Fraction]+ StdLiqVolFraction [Fraction]£ r'loleFlow [Ibmole/h]'±1 fvlassFlow [ib/h]
5tdLiqVolumeFIow [ft3/s]
© 2009, Virlual Materials Group, Inc. 00 not copy unless authorized in writing by VirlualMaterials Group.
11
,~ Virtual MaterialsGroup, Inc. Simulating with VMGSim
V1
5554 9: so '0
.__~ ~-"",e=-'"f':c'P"P'1._---'-_~----=Sep2
We are almost done. Now we need to add a compressor to compress the topvapor from Sep4 and finally we can connect it to the mixer M2. Make sure thatthe output pressure of CP2 is the same pressure as that of S8.
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12
Virtual MaterialsGroup, Inc. Simulating with VMGSim
EI
r Ignored
Summary ICurves 1Plot
Main Data
NameInQ [HorsePower]Delta P[psi] .Pressure RatioAdiabatic Efficiency ["!o]Polytropic Efficiency I"!oJSpeed [rpm]Adiabatic Head [ft]Polytropic Head [ft]
Vaiue543,23
36.002,30
75.0076.22
15753.4016010,29
1.0074,5
27.701152,34
51207,62
64.5440,419
1.0495E+l
1.00150,0
63.701152.34
51207,62
31.5330.419
1.0495E+1
The final system is shown below. Note that it converges in 11 iterations.
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13
Virtual MaterialsGroup, Inc. Simulating with VMGSim
~~F~aa~~~l~~>. 51
M1
V1
Cavell Recycle Loop ExampleGunther, US Patent 3,575,077, April 1311
', 1971
This recycle loop could also have been accomplished by placing the recycles inthe mixer as well.
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14
.Jt Virtual MaterialsGroup, Inc. Simulating with VMGSim
Hydrate Inhibition withMethanol Injection
8aturatfd
~=t:.'''''''''~,
M-e-th-a-n.......o.......I .......F"'--ett1
P1
81
HY1~*'t1
:.:",',f'iJ"',:'",/'
HY2
© 2009, Virtual Materials Group, Inc. 00 not copy unless authorized in writing by Virtual Materials Group.
~ Virtual MaterialsGroup, Inc. Simulating with VMGSim
Hydrate Inhibition 1 Summary
Property PackageAdvanced Peng-Robinson for Natural Gas
ComponentsMethane, ethane, propane, isobutane, water, methanol
Stream InformationStream Name Total Wells Saturation Methanol
Water Feed
T (F) 60 - 77
P (psia) 614.7 - 14.7
Mass Flow (Ib/hr) - - 41.67
StdGasVolumeFlow 6.78 - -(MMSCFD)
Methane 0.9800 0 0
Ethane 0.0100 0 0
Propane 0.0008 0 0
Isobutane 0.0092 0 0
Water 0.0000 1 0
Methanol 0.0000 0 1
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~ Virtual MaterialsGroup, Inc. Simulating with VMGSim
Unit Operation Summary
M1AIiPEqual
P1Efficiency - 75%
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Virtual MaterialsGroup, Inc. Simulating with VMGSim
Saturatidn·········Wat·e.r
*"'
HY2H1
Hydrate Inhibition with LineHeating
r····~···.···..•... -."J
Totl:il..;.wellS\.J ....~....
Sat1
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Virtual MaterialsGroup, Inc. Simulating with VMGSim
Hydrate Inhibition 2 Summary
Property PackageAdvanced Peng-Robinson for I\latural Gas
ComponentsMethane, ethane, propane, isobutane, water, methanol
Stream InformationStream Name Total Wells Saturation
Water
T (F) 60 -P (psia) 614.7 -Mass Flow (Ib/hr) - -
StdGasVolumeFlow 6.78 -(MMSCFD)
Methane 0.9800 0
Ethane 0.0100 0
Propane 0.0008 0
Isobutane 0.0092 0
Water 0.0000 1
Methanol 0.0000 0
Unit Operation Summary
H1DeltaP - 5 psi
OutT -140 F
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Virtual MaterialsGroup, Inc. Simulating with VMGSim
:~::
Sf 1
l;Ij-lmSRi
Hydrate Inhibition withTEG Dehydration
© 2009, Virlual Materials Group, Inc. Do not copy unless author' 'n writing by Virlua( Materials Group.
. .1 Virtual MaterialsGroup, Inc. Simulating with VMGSim
Hydrate Inhibition 3 Summary
Property PackageAdvanced Peng-Robinson for Natural Gas
ComponentsMethane, ethane, propane, isobutane, water, triethylene glycol
Stream InformationStream Name Total Wells Saturation Lean TEG TEG
Water Makeup
T (F) 60 - 70 77
P (psia) 614.7 - 810 14.7
Mass Flow (Ib/hr) - - - -
Volume flow (fe/s) - - 0.002 -StdGasVolumeFlow 6.78 - - -(MMSCFD)
Methane 0.9800 a 0.0 aEthane 0.0100 a 0.0 aPropane 0.0008 a 0.0 aIsobutane 0.0092 a 0.0 aWater 0.0000 1 0.1 aTriethylene Glycol 0.0000 a 0.9 1
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# Virtual MaterialsGroup, Inc. Simulating with VMGSim
Unit Operation Summary
T1 (Absorber)3 Stages
Connect Lean TEG as Feed to Stage 1
Connect S1 as Feed to Stage 3
Top Stage Pressure - 587 psia
Bottom Stage Pressure - 590 psia
Hx1Tube DP - 2 psi
Shell DP - 2 psi
OutTubeT - 300 F
OutTubeP - 60 psia
T2 (Distillation Column)3 Stages
Connect S1 0 as Feed to Stage 2
Top Stage Pressure - 15 psia
Bottom Stage Pressure - 21 psia
Specification: Reboiler duty of 14,4675,333 BTU/hr
Stage 3 temperature of 404.6 F
Condenser liquid volume flow of 0 Ibmollh
P1Efficiency - 75%
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,~ Virtual MaterialsGroup, Inc.
Hx2Tube DP - 5 psi
Shell DP - 5 psi
OutTubeT -70 F
OutTubeP - 810 psia
SEL1
Simulating with VMGSim
Input
S11 Moleflow Triethylene glycol
Sales Gas Moleflow Triethylene glycol
Flash Gas Moleflow Triethylene glycol
Output
TEG Makeup mole flow
Selector Mode
Sum
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Virtua~ MaterialsGroup, Inc. Simulating with VMGSim
-MeACU:~:ecYJ1:le
},--~*...
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4 Virtual MaterialsGroup, Inc. Simulating with VMGSim
Butyl Acetate Production Summary
Property PackageUNIQUAC
Componentsn-Butanol, n-Butyl Acetate, Methyl Acetate, Methanol
Stream InformationStream Name BuOH Feed MeAC MeOH Butanol MeAC
Feed Recycle Recycle
T (F) 77 77 - 316.5 - 130
P (psia) 15 15 - 50 - 15
Mole Flow 76.8 128.3 - 215 - 593(Ibmol/hr)
n-Butanol 1 a 0.83 an-Butyl a 10 0.17 aAcetate
Methyl a 0.6 a 0.65Acetate
Methanol a 0.4 a 0.35
Unit Operation Summary
M2LowestPlnOutlet
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.~ Virtual MaterialsGroup, Inc.
CSTR
Simulating with VMGSim
OutT - 200 F
OutP - 100 psia
Volume - 200 fe
Reaction: n-butanol + methyl acetate -7 n-butyl acetate + methanol
~. ard .... e
A 7,000,000 9,467,000
E [kJ/kmolJ 71,960 72,670
Reaction Order
In-Butanol 1 0
n-Butyl Acetate 0 I 1 IMethyl Acetate 1 10 I
Methanol 0 1
T1 (Distillation Column)32 Stages
Connect S1 as Feed to Stage 17
Top Stage Pressure - 15 psia
Bottom Stage Pressure - 18 psia
Specification: Mole fraction of n-butyl acetate in top product of 0.000002
Mole fraction of methanol in bottom product of 0.0001
T2 (Distillation Column)32 Stages
Connect S2 as Feed to Stage 17
Top Stage Pressure - 15 psia
Bottom Stage Pressure - 21 psia
Specification: Reflux ratio of 1.00
lVIole fraction of methyl acetate in bottom product of 0.01
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'" Virtual MaterialsGroup, Inc. Simulating with VMGSim
T3 (Distillation Column)52 Stages
Connect S3 as Feed to Stage 27
Top Stage Pressure - 50 psia
Bottom Stage Pressure - 55 psia
Specification: Reflux ratio of 2.00
Reboiler duty of 11,100,000 BTU/hr
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Virtual MaterialsGroup, Inc. Simulating with VMGSim
Butyl Acetate Production ExampleIn the following tutorial, a model for a butyl acetate production process will becreated. To start, a property package needs to be created. For this example theUNIQUAC Thermodynamic Model will be used.
Property Pat:kag~5e:lf'.CtlooAdvanced 5efecUon r
L: Add SoUd Support
e;yGi'lS Treating Chem~:a) sot·;entG~sTreating F'hY5'cal501ventif b·eati:lgochem,c..'ll£Pressure Non Associating Cb.::mica!s/Me&.Jm F'reSSt;re Associatlllg S'r':;te~
Pressure c:hEmkalsalty Pa:kages
Next, add the components necessary to the property package. The componentsthat need to be added are: n-butanol; n-butyl acetate; methyl acetate; methanol.
2.jj:e Cornpo:Jrd Sear&! I tlvpothetJ.ca1 Compound1Compoynd
family fmc;;';;;;;;;;-~~::':"':':'~=~3r DetafFamaj.i Groups
DeleteAU
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1
Virtual MaterialsGroup, Inc. Simulating with VMGSim
Press "OK" to add these components to the property package and start buildingthe case. Make sure that the "Field" unit set has been selected. There are twofeed streams for this process. The will be specified as below.
76.800.00
0.000.00
r Ignored
77.0
15.0076.80
5692.540,031
0,031
6,9946E-1
[Fraction] Dbmcoleih]1.000.000.000.00
ObfhlIft3/s]
r Detail View
r" Exclude From Summary
£quinbrium Results Iune Sizing i Notes j
5pecfrom
MoleFlo'!>! DbmolefhIf'<1assFlo'i\' Dbjh]VolumeFJow [ft3{sIStdLiqVolumeFlow [ft3{s]StdGas'llolumeFIQw I:r~r~SCFDJ
[f) Propertiesl:::! Iclole
n-llUTANOLn-llUTYL ACETATEr'IETHYL ACETATEI'·'IETHANOL
ICo!nne,:ted to [IniOut]
© 2009, Virlual Materials Group, Inc. Do not copy unless authorized in writing by VirlualMaterials Group.
2
Description:
Virtual MaterialsGroup, Inc.
Spec from
r~ Detail View
r Exclude From Summary
0.00{).OO
76.9851.32
r Ignored
Dbmoleih]0.00
0.00
0.60·0.4{l
Dbihl[ft3/s]
0.0077.0
15.00128.3073%.95
0.0370.036
1.1685E+O
![Fraction]
iI[Fraction]I[Fraction]
VapFracT[F]P [psia]MoleFlow Dbmoleih]MassFlow Db/h]VolumeFlo'N [fiJ/s]StdUqVolumeFlow [ft3/s]StdGasVolumeFlow [MMSCFD]±' Properties:3 Hole
n-BUTANOLn-BUWL ACETATEr",ETHYL ACEr.oI.TEr",ETHANOL
Summary Equilibrium Results I line Sizing
These will now be sent to a mixer, with a stream named "Combined Feed" exitingit.
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3
Virtual MaterialsGroup, Inc. Simulating with VMGsim
The total feed will then be sent to another mixer which will allow the total recyclestream to be combined with the feed. The recycle stream will be combined bytwo specified recycle streams.
Note that you will need to use have a - presiding at least one of the valuesentered to turn the stream into a recycle stream. For example you would type-316.5 in the temperature value in the Butanol Recycle stream.
These streams are below.
__print] Create ._Dele~e ?()rt_J ,r Ignored
Dbmoleih)IO;S3 179.28iO;D 36.7210.00 D.Oill0.00 0.00;
lfbfrtJIft3~~L,-:-_-,
0.00316.550.00
216.0017553,35
0.1130,094
1.9672E+D
I[Fraction)
lITFractionI. --'-'1[O-Fraction]
r Detaill/iewr Exdude From Summary
Summary ~ Equilibrium Results I Line SIZing 1Notesl
[Naterial --------~-- - .------ ..
l..... ii. Con~~cted to [IniOL;tr~--" ·jr- -'"/f~.i3;:,:;.I:;::·~~i_··--_··.--.-i...,
j VapFracj TTFIi P IPsiaIi ~1oleFlow Dbmole~-uj, ~1assFlow Db/h]•• VolumeFlow [ft3islI' StdLiq'....c,'umeFlow [ft3ls]• StdGasVolumeFlow U"llvlSCFD];·"F Properties;'i'" Hole
n-BUTANOLn-BUTYL ACETATEf.1ETH'il ACETATE~1ETHANOL
[: l.fi f·1ass-Iv. StdLiqVolume
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4
Virtual MaterialsGroup, Inc.
El flame: rr~J;;AC";>R~~i~*T Description:
Solved
Spec From
with VMGSim
Detail View
f" Exclude From Summary
Summary "I Equilibrium Results I line Sizing I flotes l
Hr~c)leFklW DbmoleJhl:I Mc,ssF!ll'N [Ibih]: JVolumeFlo\',! [ft3ts]:IStdLiqlVolLlmeF'low [ft3/5]
•: ~ SLdGa,sVol'umei=low [r"r'lSCFD]PropertiesMoleh-BUTANOLn-BUTiL ACETATEr~ETHYL ACETATEr<1ETHANOLf'lass5tdUqVolume
0.96437130.{j
15.DfJfi9S.0fJ
35322..5967.233
0.1735A19E+0
I[Fraction]
,[Fraction]I[Fraction]
H3.InO
O.OIJO.DfJ
386.75
2fJ8.25
r Ignored
These streams will then be combined and sent to the reactor.
ReactQCFeed
The reactor which will be used is a CSTR. Add a CSTR to the flowsheet andconnect it to the reactor feed stream.
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5
Virtual MaterialsGroup, Inc.
M2
Simulating with VMGSim
CSTR1
The reaction must now be specified within the CSTR. To add the reaction to thereactor, go to the "Reactions" tab and press the "Add/Edit" button.
The reaction that will be added is:
MeAc + SuOH -7 MeOH + SuAc
!OOI!CSTPJ (eSTR)Name:kr-.sQ- R""';l-"""":"- Description:
Summary &EadiOnsl Kinetics KineticVariables! Notes I n SCbematic
xn NamE
n-BUTANOL..._ _-,._.,_ _ _.._..-n-BUTl'L ACETATE.-._ __ ._ _ _ __._._ __ .
METHYL ACETATE........_..__...._._-_....._.-_ ...._.
r·1ETHANOLBalanCE.__._.._.._._.__.__.._.....I:i.Rx'n(15.."(;)lfltu11brnoU.
Print n Ignored
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6
Virtual MaterialsGroup, Inc. Simulating with VMGSim
This will bring up the following form.
To add a new reaction, type "Rxn1" into the "<New>" cell. Then specify thereaction stoichiometry as below.
, -- selection reaction: RxnO
J8alance-- iHi1~';:'(2S;c)fs;;;i1bmol} ,
I__..•.I~?;~~=== __-..-._.-...-+~C"":' "··J-<:ttew>
O,n-BUTANOL i__~I D:Jl',n:i~A;:~~~ :_:_:2rJV1ETHYL ACETATE .. _.. ;31NETHANOL
Now press "OK" to add the reaction to the reactor. To specify the reactionkinetics, go to the "Kinetics" tab and press "Edit".
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7
Virtual MaterialsGroup, Inc.
Summary IReactions L::0.:;;:~~p'::jl Kinetic Variables I Notes I r- Schematic
Parameters
Cust:'}IIlE91l11l:it>lllJllitset , sim4ll)illllpil1!Jf'llct~r ,1FreijJacobianl-'S!! :10,.taxError . !I}.OOOOl
l-taxNumlterations .. :,' 12011inimizeError
HonitorConverge:n<:e 10ReactionPbase !OVerall
r IgnoredUser VariablesPrint
Kinetics Reaction Unit5et = sim42
17
Notes
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8
Virtual MaterialsGroup, Inc. Simulating with VMGSim
The kinetics should be specified as below.
~-;;~;;tfrom reactor (sim42) 3Advanced Kinetics
7.0000e+06 9.4670e+067.1960e+04 7.2670e+04
RxnOrder1.00 0.000.00 1.001.00 0.00
0.00 C:::::::::::::::::::::::i:Qq)
1-- --..--..--- -.- +.c c: c..:.cc c... _... :..:R.:.e::I/.:.e:.:r..sc:.e.c .......... .._ '1
!:ancel
The units for these values are in the 81 unit set, so change the unit setaccordingly.
Notes
1.000.001.000.00
~ancel ••1
Pressing "OK" adds the reaction kinetics. The last set of specifications is theoutlet pressure and temperature, as well as the volume. Once these are addedas below, the reactor will solve.
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9
Virtual MaterialsGroup, Inc. with VMGSim
Solved
, ~~iQ;!~i:;::Jj Reactions I Kinetics I Kinetic Variable" I Note" I r-- Schematic
Nain Data -...". - - - - -
Namei,,' Energy Out
OutQ [Btulhr]i=:.i Signal
Deita P [psi}Volume [ft3]
7.022E+6
--85,00200.000
0.178060.1101
0.382420.32942
0.00200.0
100.00
1016.1065915.94
0.3720.335
9.2542E+0
0.252020.036140.456380.25546
0.58653168.615,00
1016.1065915.94
74,5310.334
9.2542E+0
Reactor Fee•••
Pori:l'lameIs Recyde PortConnected Stream/Unit OpVapFracT [F]P [psia]MoleFlo'N Dbmoleih]r'lassFlow DbJh]VolumeFlow [ft3Is]StdLiqVolumeFlow [fU/sJStdGasV"lumeFlow [~'I~SCFD]
[+i Properties (AIHR)Ie Fraction [Fraction]
n-BUTANOLn-BlJTYL ACETATEMETHYL .4CErATEr'IETHANOL
if: r'lassFractioll [Fraction]'+ StdUqVolFractiol1 [FractiorJd" HoleFlow Dbme-Ielh]
1.,' ...... ,......1::1..... "., nhtt... l
__Erint J User Variables n Ignored
This stream will now be sent to a distillation column to help separate themethanol and methyl acetate from the butanol and butyl acetate.
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10
Virtual MaterialsGroup, Inc. Simulating with VMGSim
Add a distillation column to the flowsheet, and we will now modify the tower tosuite our needs. The first step is to change the condenser from the default partialcondenser to a total condenser, thus removing the vapor product from the top.
r 5fmpleTowe.r Form
<New>
<New><New>
, IS1.0ut
i condenserl condenserV reboilerL <New>1 3
: UquidDra~.\' VapourDra'N UquidDraw
icondenserQ reooilerq <New>1 3
;EnergyOut Energyln
Configuration I Spec/Estimates ~ Efficiencies I Profile :1 Convergence 1 Notes
Condenser. Degree. Subcool [f}: ~
~~~ing.~ I_~~~zW---_·_---_·__·__··_----,---,----·---1
'feed <flew>
Next, by pressing the "Add/Remove Stages" button, 29 stages will be addedbelow the condenser.
Add I Remoy,e 1291-- stage{:s}
below stage 11{~~fld~Ils~~j
R~lnoYel
The feed stage must then be changed to enter at stage 17.
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11
Add/Removestages ... I Schematic .... !~._~,·_, ·_~~,_·~.· __,.•_._~_.c_._••~._~ ~__:,: ·_·__'~~·~CC·_·,_ _'_'_~_""_"""_'."._ ..'_.'_'_'.' '_""'_'.'_', .•_,_.~..
t W
SimpleTower Form
<New>
,12 ';"'-=-:"""-'<"'"lIe"'w":"">"""'
32ergyln
2223
i<Hew>
I~i1
272329
Virtual MaterialsGroup, Inc.
EHERGYStageType
Connected ObjValue [Btu{hr]
3 INTERllAl VAP/LIQSt3ge
Type
Connected Obj'.~+j Deta,fs
Configuration I 5pec/btilUate:sl EfficiendlS 1 Profile Convergence 'I Uotes 1
Cond-enser. Degree SUbcool [f]~
±j SIDE STRIPPER
,,' PUNP AROUND
<New>i<New>
The last step is to enter the pressure and other specifications on the"Spec/Estimates" tab. The top pressure will be set to be 15 psia, with the bottompressure being 18 psia. The specifications made will be a top and bottom molefraction. The top fraction of butyl acetate will be set to 0.000002. To enter this,press "<!\Jew>" and complete the specification form as below.
ComponentUse the <shift> and <Control> keys for multiple selections
r[)r~';;c~~;;~~tS;~ ..ISt~~~~i~~~d~~~rl
2.00E-06
3 .1~1~I~f;~~ti~;5;~
g
Repeat this for a bottom mole fraction of 0.0001 in methanol. This will notautomatically solve the tower. By pressing the "Solve" button, it can be seen thatthe column will not solve.
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12
CQn\j~rgence. I.NQtes I
101
0.000150
0.00012.00
0.0001oooo1o
Description:
Virtual Materials
Group, Inc. Simulati
Print I j;i Alway. Solve
Solve f.RestartJ last Cony I
Configuration I Spe.c/Estimates! Efficiencies 1 Profile
Inftiarrzation fo1.ethod
~OroU5 ~I <Run>...~-. Cakulaong Jccobian fOl IT1
In Iteration 1 Outer ErrQr 0,389283
~pa~r~a~n~,e~te~r:'~;~-===:::T~:~~:;::!! Calculating J.acobian for ,tn111 Inner Error 3,365042(.._.......•.......•,,' /Tl Inner Error 3.861964
ITl Inner Error 3,860684.In Inner Error 3,360137/r1 Iten~tion 2 Outer Error 0,211601Calculating Jambian for In{TIInnef Error 3.764294/TllnnEr Error 3.763922,rn Iteration 3 Outer Error 0,053552CalOJJating Jacoblan for ,iT1
~9::J~~~~_~_!:~~p..
!~i.~~.e.~~!_~~..f'~a_>Qn_rl~~~~~~r
r-1_a~r1~er~£?p_~ _f·1axOuterError.........".,,, .NaxouterLoopsI· .. ... .. __.._ .....---~:1mlnn~~5~~p .ThreeP'ha-seHodelTriggerSolveT;'l.~sti:;;;,ve"!led...TryToRestartTryToSolve
ifapf~~~t;;!i~~ve_
In order to help the column solve, change the "DampingFactor" to 0.7 in the lefthand column. After changing this, trying to solve the column will allow thecolumn to converge.
, IIllotes IConvergence
.3 lrrlInner Error 0.0'10656VT11nnerError 0,004108~;~1 Inner Error 0,000122~lTl1nnerError 0,000006
":::,::::r::·:·::-::,,'::..:::·-:,,::::::::..'!' Yrl1t€.ration 10 Outer ErrQr 0.010623..j ll-7 !/r1lnner Error 0.008422
. 10:~11nnerErroro.002233
1. Ilf1lnner Error 0.000016O.OOtU: 1/Tl1teration 11 Outer Error 0.005052
50 )/f11nne.1" Error 0,001524v.!:11nner Error 0,000161
-0.0001, *!T11nner Error 0.000002200: j{r11teration 12 Outer Error 0.. 001822
-U-.OO01: Y111nner Error 0,000165f/fl1nner Error 0.000015
0; 'rrf! Iteraoon 13 Outer Error O.ODQ4700; ~:rf11nner Error 0,0002080: ~rrllnnerError 0.DOOOD80.:. llteration 14Outer Error 0,0003571 1 Inner Error 0.000105
lfrllnner Error 0.000008o Ifrllteration 15 Oi..lter Error 0.000341
Un Inner Error 0.000059ifrt Iteration 16 Outer Error 0.000254
r.~i i~~r~b~~O{700°.J~~~~rorO,~J015~1~~i i~~~ti~~o;8°o~~;~~~or0,000076~'Tl ]nner Error 0.000051
I'
Conftgl.uation I Spec/Estimates I £ffkiencies J -Profile:
Initialization r·lethad
[Ri!;rous
Print - r-W',' Always Restart from Last Cony
Solve ·1 :,w.>:~~~.~.~J Last Cony
Parameters
1
·,····'·'·····:·,,'··"·"'·············'··.··:··-.........•:•..:.'.:..'.._:.'..:DanlpingFador·FreqJ~~obian!<t~_~InitKPower.....---,_ __ ..•.__._.._ __.~ .
.~,.~~'=.~E~?r.~~~~rl~~~~p~NaxOuterErrorM"axOute
r'1inInner5"JT
!!X~~~~~~~~~~_...~Try"JaRe.tartT,:vl";;S;;~""-~-
.Y.~E~~~~!~!~~!~~~e_.
Now connect streams to the two outlets of this column. Then connect a secondcolumn to each of these streams.
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13
Virtual MaterialsGroup, Inc. Simulating with VMGSim
Column T2 will have 32 stages, with the feed entering at stage 17. This columnwill also have a total condenser.
I
j condenserQ rebol(erQ <flew>j 1 32]EnergyOut Energyln
icondenserL reboilerL <Hew>
jUquidDraw 1 LiqUjdDra,!~2
i
1feed <New>
I/S2.0ut 17
!<Uew>
ISpec/Estimates J Efficiencies i Profile: 1Convergence:] Notes
DegreeSubcool[F]: ro.o~
Tower Sizing .... I
TypeConnected ObjValue [Btu,ihr]INTI'RfIAL YAP/LIQStage
Type
Connec.ted Obj~+F: Det.a!lsIt SIDE STRIPPER "<New>',i PUHP AROUND '<Hew>fi VAPOUR SLIP i<New:>
Priut Ir Always Restart
__Solve '" I Restart I _last Cony j
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14
Virtual MaterialsGroup, Inc. Simulating with VMGSim
This column will have a condenser pressure of 15 psia and a reboiler pressure of21 psia. Also, it will have a reflux ratio of 1. Reflux ratio is already added as aviewed specification in the "Viewed Specifications" panel. This allows thespecification to be added directly into its value cell.
Description~
I 1 Add/RemoveStages .....1 Schematic ..Spec!Estimatesl [tt....de-ndes "I Profile t Convergence I fiOt5
Specification Requtred :; 2 (0 supplied). Delete ·Name~ to remove. Delete 'Value' to tum mto viewed spec.
Name-- IStage - jType TA~odstecfDra';;_··T~_~if- [~~f!i~~t~~.qJ~t:·j~~~-t ---fvai~e~'" --~~-~.<New><Uew>
Viewed Specificatklns. Dclete 'Name' to remove. Enter a value to turn into an active spectfication
1'~~~>:Rati~····~ .~_~~~~.~~9_!?!.~~',; ....:.p~~!1 l.S~!].~~~~~ ..9.'?}. iUfit -·-'-3r~--···
1 EnergyOut condenserQ Energy Btulhr32 EnergyIn rebollerQ Energy Btu,lhr
r Ignored
The other specification that will be made a reboiler is a product fraction of methylacetate of 0.01. This will be made in a similar way as the other draw componentspec.
-~hematic .~.Jspec/Estimate, Iffflciem:"" Profile I. Convergence I flote. I
Specmcation Required:;:; 2 {2supptted}. Delete 'tlame' to remove. Delete 'Value' to tum into Viewed spec.
Viewed 5pedfications~ Delete 'name' to -remove. Enter a value to turn into an active specification
" j~~g~._. jTIP~_.. AssodatedDra!i;J JDetail !CQ~m:LU!dObj \Unjt Value1 EnergyOut ~onden$erQ···"········"~E;;"~~gY-··-'-·······-·---·--B·tulhr
32. Energ1rn reboHerQ Energ"'1' BhJ/hr
Always Restart
~tart "f "l~st ConY" I r!!lnored
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15
Virtual MaterialsGroup, Inc. Simulating with VMGSim
Pressing solve will allow the tower to converge. Add the product streams asbelow. The MeAC recycle stream will be connected up to this tower as below.
!/Slll .... ¥b'-
l~~:3
"'''' ""The third tower is the last unit operation that needs to be solved. This tower has52 stages with the feed entering at stage 27.
r Ignored
i~" SimpleTower-form
<New><New><New::.
[-condens-ert condenserV reboHerl <New>1 1 52
iUqLlidDrav,' VapourDraw UqujdD~aw
'<New>
condens.erQ reboiterQ <New>1 52
lEnergyOut EnergyIn
Description:
ltnERlIAL VAP/UQstage
..C: £flERGYStageTvpeConnecte.d DbjValue [Bru/hr]
Configuration ISpec/Estimates j Efficiencies "I Profile Convergence Illotes iCondenser: Degree: Suhcoo! fF]~
c'DRAW
I ~tagF.=ypeConnected Obj
Details
Harne;
The condenser pressure will be 50 psia, with a reboiler pressure of 55 psia. Bothspecifications are already created in the viewed specifications panel. A refluxratio of 2 and a reboiler duty of 1,100,000 BTU/hr will be specified. Beforesolving, return to the "Configuration" tab and make sure that the condenser is atotal condenser again. Much like with the first tower, without changing thedamping factor, the tower will not solve. By going to the "Convergence" tab andchanging the damping factor to 0.3 and pressing "Solve", the tower will solve.Add the product streams as below.
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16
," Virtual MaterialsGroup, Inc. Simulating with VMGSim
This will now allow the case to solve, as the recycles are continually updated untilthe recycles converge.
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17
Virtual MaterialsGroup, Inc. Simulating with VMGSim
MDEA Reporting/Case Study ExampleThis example will go through the components required to perform reporting andcase studies relating to the MDEA example created previously. For starters,open the MDEA example.
The first step will be to create a "Project Report". To do this, go under"Reporting" and select "Project Report".
Ready
ShapesmUtility
Claus
Project R.eport
Sum ma r:\<' Set:;
~."Taterial Stream Summarj
Energy Stream SummarJ
Report Header
Report Settings
This will open the following form.
,
;
, ,
, --
I
'- ,
I ~aPF'"
: ~'oleF1owI '''''"AowI ,",,"e'~w
Excel·Ind:Jde: P,~'1br,g s::ttings
Reference Flo\.<;sl;eetooooooooooooo
fi:::'"--: ,--- ",'- -""""",'~A"" """'''',,',m,,,:o,,,'-,--V,; Ls2IJfuli';';;:J] loo~ ISaveI::7: ~;:~aton;'~,0:;trea'T'"
, 0r'1aterial Streamsr::~ L'rtitOperaiions
~Abo;orber:.;
o Arnir.e Uelails0Contrcilers~coo!ers
~Djsti§ation Cournns- IilHeatEx01&1!,"Crs
0MixEf5. 0Pumrs
0Sep.arator5. 0V"J"es
I~necgy
5
r"ctecuIa:"Wei!~ht
r.1;,,;sDer:sityI Cp
TherrnalCond'Jctillity"~:;::osity
molarV
ZFactor
1-- -I
i
Clos,
By default, all of the unit operations are selected and will be included in thereport. Also, the vapor fraction, temperature, pressure, molar flow, mass flowand molar composition are the default variables which will be displayed for
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
1
Virtual MaterialsGroup, Inc. Simulating with VMGSim
material streams. Each unit operation has its own individual report format,showing all pertinent information for the unit operations. If you wish to only addselected unit operations to the report, the check boxes should be checkedappropriately.
These reports can be created in Microsoft Excel or Word. In Excel, the differentunit operations can be seen on separate tabs. These can be linked to on themain report page.
MDEAReportingVirtual Materials Group
August-11-09Field
File Name:Company:Customer:Project:Job No:Prepared By:Report Date:Unit Set:
Main F10wsheet
Flle: C:\Users\Cari Landra\Documenh\B1ock Vieek\MDEARepor1ing.vrnp
Material Stream (161Absorber 11\Amine Detail iT!Controller i1lCooler (1)
Distillation Column (1lHeat Exchanger i11Mixer (1)
.B.!.nllilllSeoarator 12\Valve 11\
VMGSimv5.1l
Below is the report cover created in Word for a project report, with a table ofcontents included.
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2
.~ VirtuallV1aterialsGroup, Inc. Simulating with VMGSinl
Main Flowsheet. 1Material Streams 2Absorbers 18Amine Oem ils """ """ 20Controllers 22Coolers 23Distillation COlumns __ _ __ _ _._ _ _ 24Heat Exchangers _ _.._ _ _ _ .27Mixers _ _ __ .._.._.. __ ._ _ _ __.._ 28Pumps _ _ _ _ _ 29Separators _ __ _ _ _ _ _ _ .30Valves _ .32
Next, we will add a summary set to the case. These are found in the same"Reporting" drop down as the "Project Report" form was found. This will open thefollowing form below.
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3
Virtual MaterialsGroup, Inc. Simulating with VMGSim
To create a summary set, press the "Add" button. Now double-click on thecreated summary set to open up the following form.
As can be seen from the "Unit Op Type" dropdown, a different summary set canbe created for each unit operation within the project.· Also, not all of the streamsor unit operations need to be included in the summary set. For this example, usethe arrow buttons to include only the inlet and outlet streams in the project in thesummary set.
/Acid3as,IFrom_Cross_Exchange
tMab'_Up-',ValerISales_Gas/Sour_Gas
Items
Pressing "OK" will bring up the summary set below.
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4
Virtual Materials
Group, Inc. Simulati
To choose which variables are shown press the "Select Variables" button. Thiswill bring up the following form.
0.0
<>.000.000.000.000
GISTor·1
Several material properties can be selected, with information available in both theIn and the Out port. As well, the properties of each phase can be accessed aswell, with the separate liquid phases, the vapour phase, the bulk liquid phase andthe overall bulk phase being accessible. For this case we will add the bulk, vapordensity and the bulk liquid properties for the following variables: mass density,Cpand viscosity. The "Variable Selection" form will now look as below.
MassFracti.:.>l;
StdVofhtctior':
,"'ole'lo',\"s
M"ssflows- StduqVourr.eFlows
-E FiuidBulkVapLiqDUqlUqEl:!k
" :~OutFradian
r"assFraclk·nStdvolFra:t:on
0.00
0.00MO0.000CUSTOH
f",..', ""n>itv Ib/lt:3 0.0000tltu/lbmO"f-F 0.000t:p O.OOOOE+O
'I'''' "",,,,.tv Ib/It:3 0,0000Dtu/lbmol-F 0,000cp 0.0000£+0
f ....,l),,,""'" 1b/ft3 0,0000
© 2009, Virtual Materials Group, Inc, 00 not copy unless authorized in writing by VirtualMaterials Group.
5
Virtual MaterialsGroup, Inc. Simulating with VMGSim
Pressing "OK" will now create the summary set as below.
Add Sum""v
';'i' ..•....... 't ; .;...,..... ...... ... ;,tS'_il3 !I~I
Summaty·-·····
I i1
i 'n"'"arne !Add Go; 'FI,,,, Tank Ven' Mate Lb W8tec
I:,pFrac 1.0000 1.00 0,00 0,9984 0.9668120,0 135,8 77.0 lOLO 90,0
Ip [ps~l 19,50 65,00 19,50 995.00 1000.flO
r<1ole Flo:,\; [bmole;hJ 543,71 25,36 SO,H 3727,26 4391.97
fAa!;,; Row Ub/h] 20615,90 534.69 905,04 72090,.33 102203.68Volume Flo',,' [ft3!:;] 47.825 0,635 0,004 5,356 5.792-+: hFracli::on
r·\ass Density Pb/ft3] 0.1197 0,2168 62.2420 3,7]91 4.9013
Cp [BtuJl00:c~-FJ 8,772 9,551 16.045 11.792 12,947
¥isCCtsi':y lcp] lA326E-2 1,27041:-2. 3.90()7E·j 1,H20E'2 1.6'J70E-2 ~
r.,i'l~S Density Pbjft3) 1,),1197 0.2.168 0.0623 3.7215 4.4821 ~
Cp L8tu,lbmci-fJ 8.772 9.651 S,131 11.755 12.192 ~
Vlscosit'i [ep] 1.4326E-2 1.270q:-2 9.84S6E·} l.JJ15E·2 1.4Q76E-2
Mass Density DbjftJ] 61.6430 67,2602: 62.2420 39,8257 39.2197"
Cp llltuibmoi-f] 17,852 23.22'(. 18,046 34.537 34,911 ,VIscosity rep] 5.5613E-l 1. 7105E+O 8,9')07E'1 3.2094E-l 2,,31S9E-l i
Conflguratiull - -- ---'- ---,,-----
PrintAJI
This summary set can now be used in one of three ways: 1) Copied to theclipboard, 2) Exported to Excel or 3) Exported to Word.
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
6
Virtual MaterialsGroup, Inc. Simulating with VMGSim
When copying to the clipboard, a table similar to below is created.
Name Acid_Gas Flash_Tank Make_Up Sales_Gas I Sour_GasVent Water
VapFrac 1.0000 1.00 0.00 0.9984 0.9668
T [F] 120.0 135.8 77.0 101.0 190.0 IP [psia] 19.50 1165.00 1 19.50 995.00 111000.00 1
Mole Flow [Ibmole/hl 543.71 25.36 50.24 3727.26 114391.97 IMass Flow rib/h) II ".,. t:>n 905.04 172090.33 1 102203.68 .
Volume Flow [ft3/sl 47.8?<; n RR<; 0.004 5.356 5.792
In.Fraction
Fraction NITROGEN [Fraction] 2.42E-05 0.0150 0.00 0.0327 O.O"'7Q
Fraction CARBON DIOXIDE 0.5317 0.0972 0.00 0.0302[Fractiorii
Fraction_HYDROGEN SULFIDE 0.3782 0.0308 0.00 3.63E-07 0.0493[Fraction]
Fraction METHANE [Fraction] 0.0028 0.7596 0.00 0.8625 0.7437
I Fraction ETH ..- ') l';,)l:::_nA 0.0397 0.00 0.0359 0.0318
I Fraction PROPANE [Fractionl ,- 0.0133 0.00 0.0179 0.0167
Fraction ISOBUTANE [Fract ".."., .... n6 0.0011 0.0,~
Fraction n-BUTANE [Fractionl 3.50E-05 0.0058 0.00 0.0
Fraction ISOPENTANE [fraction] 3.82E-06 9.94E-04 O.OOE+OO 0.0027 0.0033
I Fraction n-PENTANE [Fraction] 115.85E-06 0.0012 0.00 0.0026 0.0035
Fraction C6+* [Fraction] 1 2.69E-05 0.0019 0.00 1 0.0028 1 0.0166
Fraction WATER [Fraction] 0.0869 0.0334 1.00 8.76E-04 8.00E-04
Fraction_METHYL 1.78E-17 3.55E-07 O.OOE+OO 3.42E-09 O.OOE+OODIETHANOLAMINE [Fraction]
Mass Density [Ib/ft3] 0.1197 0.2168 62.2420 3.7391 4.9013
Cp [Btullbmol-F] 8.772 1 9.651 1 18.046 11.792 12.947
Viscosity [cp] 1.4826E-2 1.2704E-2 8.9007E-1 1.3420E-2 1.6070E-2
Mass Density [Ib/ft3] II 0.1197 0.2168 0.0623 3.7215 4.4821
Cp [Btullbmol-F] ~ 8.772 9.651 8.181 11.755 12.192
Viscosity [cpl I 1.4826E-2 1.2704E-2 n 1.3315E-2 1.4076E-2
Mass Densitv [lb/ft3] I 61 67.2602 0 39.8257 .,n "'n.."
CP [Btu/lbmol-F] 17.952 23.222 18.046 34.537 34.911
1Viscosity [cp] 115.5613E-1 1.7105E+0 8.9007E-1 3.2094E-1 2.3159E-1
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
7
Virtual MaterialsGroup, Inc. Simulating with VMGSim
If the summary set is exported to Word, it will look as below.
Equipment Summary: Stream Material
rtF]
11... flow Pbihj
Volume-flow [ftYsI
fr"'lio~.PR()PANEtF"",l1on]
"'",lio11. n-BUTANE [fracioll]
U.,.;tion.),.pENlAIIE tFlactiol1]
FrattiDfl C6+' IFr-Ktion}
ft",l!rm3,uJ1fl\ OIETllAIIOl.AMINE [Fratiool
Cp [Bl.1~m,1-f]
Mm o"",;ty [IOifiJ]
Cp [Bt.1@pl-F]
tM,.n""oityIllJftJI
Cp [BM~""I.-FI
Vi.",.i", I'P]
2.421:..1:/5 O,Oi5';} UO ;JG327
053U 0,0872 0.00 i 0.0~02
0..31::2 O.O~~ 0.00 S,63E·C'
0.0018 O.7S-6 0.00 iJ.e'325>
2..5-:ZE-04 0.0317 0.00 0,05'?
e'.E2E·05 O.OB$ UO {',CfT?
2.13::...-:>6 o.o-:n 0.00 0.C(i3~·
3..5tE-O.5 O.C\.~·8 0.00 0.C{>t4
~.f::'J:"(>6 8.94EJ:>4 O.OOE+OO 0.0:'21
5.65E-O& O.0Jt: UO 0.0n~·
2.fSt-0S O.CC~S 0.00 O.W2e
O.t-&09 0,03':4 un O.T5E->,."4
tTaE-t? 3.55E-07 D.OOE~O 3A2E-:':S
(I.tiS7 0.2108 52.242(, 3,nSt
E../fl S55~ 'i&.04S ~~.i82
~.4c2~E~ t2704E·2 &£'\.-(=f;:;_~ U420E·2
O.1t9! O.2EB G.G~·23 3.n~5
t.r!2 B.SS~ s. ~Et 11.755
iAE25E--2 '.Z794E~ S.,~4:.E-E--1 !J~·~5E-2
8tM3C' 57 2~2 c2.242~ 2S.OZ'"'
~7~E2 232.n 't~·.C'4f. 14.537
S.561aE-~ ~.7jC'5E+-O ,!LSO~f:E-t J..20:24E·t0
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
8
Virtual MaterialsGroup, Inc. Simulating with VMGSim
Meanwhile, if the summary set is exported to Excel, it will look as follows.
......., .9 fraction_NITROGEN [fraettonI-·1· · · ..10· Fri!:ttlon_CARBON DIOXIDE Ifriu:t1QO]
·tfl:~i~~jii.~;~x~~0.i.~t.i::~y.:~i.!~~:ii.i~~ii~·~i.12 IFrattion_MEIHANE IFriit!ion] NN·;13]:f.i~~jii.~;.E.T.~~~~::[~:~~~!i~~i.::::::::::::::· F
2·.:5:.·2'·E:::.(··..4..· ,:.: :.:.: :.:.:.: ::.:.:.:.: ,.: : :.: (
14 .F.E~c.ti.~~.""P.!':?~:':~.~..IF..r~;;:i.?!!L F6.:-'.3:2.E"..'•.>5:: :.:.:..:.::' :.:.: .
F.:.~;;t!~n..""I~?~~!.~~~JF.:.~;;t!~~.l.......................... 1..273..E.(5 : ..~:.~;;t.i~.n..""n.:~.~.!~~~ ..[.F.:~;;!i.~~J....... r3..50..E-..O..5: : :.:.. :.: : : ..
fratlion_lSOPENTM1E Ifraclinn] 132EoO,"
r.,:~I~ ..F..'.?'~·.. [.I.~'!i.~.I.~!~.I. .~:a.:S...F.I.~:~:.!I.~!~.l... ..Vctlu me Flcw Ilt3le]
.F..r.~;;t!~.~.""n.:p.~~~.~~.!F..r.~tl~.n.J.... ...:.:3..0..::"..':"' :.: :.:.: : : , ( .fraction_Cll+' [fra>Clionj 1..25..>..·E-..(..': : ; , 1 .
L~g f6~~jii.~:>~~~~::i.f.i~~~!i~~i.:::::::::::::::::::::::::::::::::::::::::: ..::1(·· ..O359 : : +I 21 Ifractinn_MEIHYl DlEIHANOlAMlNE [Frattion] l.78E·17r22..J..r,i;;~D~~~itY·iiblft:;j · · ''''''0':.:\··..E:::T..·..: ·..:·:·:·:·:::··:: · · ·· ..:·:·:.:.:i" ::.: ,.::..:.~::: ..:.: ;.::..:.:.::: :.:: ( ......_ ·1 · ··: · · · ·..•..: : , , (
23 IGp [BtuJlbmol-F] 3.77224lvi;~~;i;y[~pi · · · · · · · ·1·:·::..·:·: ·..·:..:·:·:·:..: · · · ·..:.:.::.:..: :.•:.:.:: ::: ::::::.: : (
-25·rr;i~;·~·o~~~iiY·ii~lfi:;i ..· · F0.:..1:..1';::7: ,.:.:.: :..: :.:.:.:.:: ,.:
·2..6TG~[·Bj~:;i·b~;~i:~ ·::::::::::::::::::::::::::::::::::::::::::::::::::::::::::1..';·.7..72 , , I .
,~~~t{~~~::::::·:::::::::::::I ..i.;..i..~:.~:'..~ '..:;.:.:.c.: ,..:.;; :.: :.: ;.:.:.:.: : +
Additional summaries can be added within the summary set, up to 10 summariescan be created. Extra summary sets can be created, without a limit to how manysummary sets can be created.
The next process that we will go through is developing a case study. The casestudy can be used to find the effect that changing a variable will have on a varietyof properties or flowrates being studied. For our case study, we will adjust theinlet gas temperature, as well as the rich amine loading and see the effects on
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
9
Virtual MaterialsGroup, Inc. Simulating with VMGSim
the sales gas and acid gas flow rates, as well as the H2S and CO2 flowrates ineach of these streams and the lean amine flowrate.
To start this, open "Case Study" under the "Tools" dropdown.
Refre5h All \IVind ow's Ctrl+A
Cl05e All, Except Current, Unit Op Forms
Check PFD
Check Unit Op.Hierarchy Tree
Unit Sets .
Options ..
Hardware Key Info
Ctrl+Z
This will open the following case study form.
~dd ...•.·.·.1
Delete]
Add J... Custo~ ....
foUssing Independent Variable
Name:
Set Up '1 Results I Plot I StatusIR' Run All Combinations Number ofPoints:
Independent Variables···········_·.·········j [""Dependent Variables .,......~-,.....-,i!
.~~:.....ljj
I 'I .~ .;[)eete· I I
.' Add 111~H.~...~~_! L.__....
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
10
Virtual MaterialsGroup, Inc. Simulating with VMGSim
There are two different ways to add variables to a case study. Both ways will beshown in this example. First, we will add the inlet temperature as anindependent variable. In order to select something as an independent variable, itmust be a specified value. To do this, press "Add" next to the "IndependentVariable" table. This will bring up the following navigation form.
To change the inlet temperature, go to the "Sour Gas" and select the In port,since this is where the temperature is specified. Now select the temperature asthe independent variable and press "OK".
Haterja(Streams'J.: Add_Gas
-{+.1 Flash~Tar.k~Vent
;:f! From_Cross_Exchange
+±'i Gas_to_Absj±1 Heated_Rich_AmrnE
d-) LeanJ\mine
i±-' Make_Up-'''''Job=rFf,: Reger,erated_An"lneft:i Rich_Amir:e
i:+i Rich_Amine_to_Cross_Excha.. ,'·F Ridl_frOll1_AD
'+1 Sa!eELGasSour_Gas
[n
Out;.+.i To~Cooler
\:t' To_Flash_Tank':j:: To_Pump
'....;-"::: <:ontrollersRlCh_loaclnQ_Controlier
"'l:;:~ £xce:IUnitOps_. V"later_Bdance_Ca!cuIatQf
P Show Short list
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
11
Virtual MaterialsGroup, Inc.
Copy Connection
Simulating with VMGSimThe sour gas temperature is now available as an independent variable. Next, therich amine loading will be entered as an independent variable. Since the loadingis set using the controller, the set point of the controller must be added as anindependent variable. This will be done by opening up the controller form. Byright-clicking on the SP value cell, it can be added to the case study.
~_-_ Lean=~ine.Std Uq v...
Summary INotes IEl Performance·- ....: El SettinQs··
11~!~~:?f~~~,~;l-j~¥;'·~?~~~~···~···.-:~=.~····••···~••~·••~=r;~:::1' J.. . : ,'-•........1 60
E1 OP/f'lan Var Range .._ _....! Print Landscape
. .... !~IV~'u~~~1 Copy Whole Table
Copy
0.2' Pastel---'----~---'---"---'----___,_j
Convert 'Target' to arecyde port
Add to Case Study; CaseStudyl
This will open the following form which allows the variable to be added as anindependent or dependent variable. Select this as an independent variable andpress "OK".
p.dd Variable to Case Stud}.; CaseStudy1IRich_LoadinfLController.SP
Add variable as , _ ,
f+- Independent Variable
(' Dependent Variable
The case study form now looks as below.
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
12
Virtual MaterialsGroup, Inc.
Selected Case:
tlame:
Set Up IResults] Plot] Status I
with VMGSim
IV' Run All Combinations Number of Points: 121
Independent Variables i~~~~~'a~'''~aa='=-.:'=.········.-.. ·· I
/Sour_Gas.ln.T '--AdIJ Add .1
IRidl Loading contrOJler.T'Delete=! Delete IAdd:1 Add I
Custom I Custom
I-!i.sing Dependent VariableRun
11
Unear
11
linear
close
The dependent variables can be added using either of the two methods shownpreviously. After adding the variables mentioned before, the case study will lookas below.
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
13
Virtual MaterialsGroup, Inc.
FrCi':_CARBOfCDIOXIDEl UAad_Gcs,I!'Vo!-=-Fkr.';,CARBOf.,_DIOXIDE)FrCi':--,..,m;tOGBCSUl.FlDEl (iAdd_G~s.I".r"'.oIeAQ\\,.K fDROGE.:'U;utFIDE)ft.ean_Amrfle.In,StdJq'.'o.'lrneF[O'il
.3
11
linear
11
Unear
111!t5iJJg HinValue in /Sour_Gas.ln.T
Frac_CARBOr'CDIOXIDEUSales_Gas.lnJ""oleFlow.CARBON_DIOXIDE)Frac_HYDROGEN_SULFIDE USales_Gas,In. r'1oleFlow. HYDROGEN_SULFIDE)/Sales_Gas.In. fvJoleFlow!A,jd_Gas.In. r·loJeFlo~\'Frac_C.4RBOf'·CDIOXIDE1UAdd_Gas,In.IV'oleFlow.CARBOf\J_DIOXIDE)Frac_HYDROGEN_SULFIDE1UMd_Gas.In.f\'10IeFlo'i\' .HYDROGEt'J_SULFIDE)lLean Amine.In.StdLiqVolumeFlow
Add ·1
. D~letel
Add 1Custom
The case study data must now be specified. For both independent variables, 5data points will be used. The minimum and maximum temperature will be set to50 F and 130 F respectively. The range ofrich amine loading will vary between0.2 mol/mol and 0.8 mol/mol, as suggested by the GPSA. The case study willautomatically calculate the points which will be used for the trails. With the "RunAll Combinations" box checked, each temperature will be run with each richamine loading, resulting in 25 different tests. To perform these tests, press"Run".
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
14
Virtual Materials
Group, Inc. Simulatin
N3me~
SetUp IResults I Plot I Status!
f\;i Run All Combinations Number of POints: 25
:/c~~,,=,~~~~12,=-~I::': .::....===......:........................ ,... DependentVariables--
n~:~~~~~~,~~~: ~ !rF;:;'C_CARB6iij)iQXI-[JE-C-isa-les-'_G;;;:i~:MoleFI;-;;;:t~ Iile _. I jlFrac.HYDROGEN.SUlFIDE V$ales.Gas.ln.MoleFlo'li Delete Ii
DeJe!:...J 1 !Sales_Gas,In,r'1oJeFlo'N --- j
. cuA,d.todm I i {Add Gas,In,T'!QleFlow Add I:, I FracSARBON.D10XIDEl (fAdd_G... Ir,,~loleFlow.C~ I
I Frac.HYDROGEN.5UlFIDE 1 (fAdd_Gas,lnJ'1oleFlo,\l'IILean Amine.ln,S!dLiqVolumeFlo',\'
50.0 0.2000130.0 0.800051::::::::....5120.00 0.1500
linear LinearSO,O 0.200070.0 0.350090.0 0.5000
110.0 0.6S00130.0
Ready
The results of these tests are displayed in a number of ways. The first can beseen in the "Results" tab. This tab, by default, shows all of the results in onetable.
By checking the "XYZ Table" box each variable can be seen in its own separatetable that can more easily show the effects of the independent variables on thedependent variables.
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
15
Virtual MaterialsGroup, Inc. Sim ulating with VMGSim
NewI_.:J
CaseStudyl
Run
I
II
Name:
Set Up Results J plot Status I
f';; XYZ Table X: r.lSo~~:G;;'I~ ,T
Selected Case~ !caseStudYl
The results can also be seen in the "Plot" tab. With 2 different independentvariables, one variable will be shown on the X axis, with the other beingdisplayed as the series. Once this has been decided, which variable is desired tobe studied can be looked at by selecting it under "Y". To see the acid gas flowrate with the inlet temperature on the x axis, the plot looks as below.
---.ir-- 0.2 [lbmolJlbfj)ol]0.35 [IbrnolJlbmol]0. 5 {Ibmol/lbmol]0.65 [IbmolJlbmol]0.8 [IbmoJ/lbmoij
•
!Sou,_GaslnT [Fj
1:1=-- -:-~--:--LL~:O. 4~oo:f'.:: :::::::~:. --. ·~ " ........+.......... .•
~ -----0, ---------~TI'3:00 ~.~-~~
~ ------
By changing the "Plot Type" to "Density" with the radio buttons, this sameinformation can be shown using a color density plot. The lighter that the color is,the lower the value is, as shown by the legend on the right hand side. Leaving
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
16
Virtual MaterialsGroup, Inc. Simulating with VMGSim
the acid gas flowrate as the dependent variable, it can be seen that the sour gastemperature is on the x-axis and amine loading is on the y-axis. Changing theplot color to green, the density plot looks as follows.
The last plot type that should be looked at is the 3D plot, which can be seen bychanging the "Plot Type" radio button again. By switching the "Y Type" between"IVloleFlow" and "StdLiqVoIFlow", the dependent variable which will be looked atcan be selected with the check boxes. By checked the acid gas flow ratecheckbox and changing the radio buttons surrounding "View Angle", the following3D plot can be developed.
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
17
Virtual Materials
Group, Inc. Simulatin with VMGSim
-SetUp; Results Fiot I status]
P!otlype- I,~;:~~:;f,~~]~~==::~2D sene,,-, Densityi. 3DPlDt
IAnD_Gas.Tn. !-lc~eFlo;NFrac_CARSm-,_DlOXIDEl (jAoo_Gas.Tn.r-loleflu\:I.CARBOr-CDIO\1DE)
/Acid_Gas.ln.MoleFlow 3D BAR PLOT [Ibmole/h]
130,00 50.00
{" Black
" Blue(. Red
/". Orange
,-' YeUow
c", purple-
50.00
f;BC~CARBOfCDIOXIDEl (i;'.dd_Gas~Tn,t>1o;e90w.CARBorCDlOXIDE)
,"c__ ....,.......,...,.,,.-1=,., "'" ""rY:;' U~.>,.l r __ ._ ~>_I~_l;l_ .. , ~,,,,,,.,r::->.' "'. ";'r'.l;'
130.00
/Acid_Gas,In.MoleFlow 3D BAR PLOT [Ibmole/h]
set Up t Results Plot Istatusl
r' DenSIty
[t' 3DP!ot
By changing the variables displayed for each of these three different plotmethods mentioned, the information obtained by the case study can be seenvisually.
One other type of case study that can be run is a case study based on thefraction of H2S in the inlet sour gas. When adjusting the mole fraction of a
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
18
Virtual Materials
Group, Inc. . Simulating with VMGSimcomponent, the other components will be normalized to allow for a constant ratioof those components. To create another case study press the "New" button atthe top of the case study form. This will create a "CaseStudy2".
'u ••uu.~.
Add ! Add IDelete I Delete I
~Add!
_Custom. Custom
Selected Case: rc~~~sh;d'j~i-'I··m~~__.:.__
Name: CaseStudy2
Set UP! Results ~ Plot I StatusIj;;l Run All Combinations Number c,f Points:
'·tissing Independent Variable Close
To add the mole fraction of H2S, press "Add" next to the independent variablesection. It will bring up the same form as previously. By opening "Sour Gas" andselection the In port and then opening the "Fraction" node, the hydrogen sulfidemole fraction can be accessed.
© 2009, Virtual Materials Group, Inc. Do not copy unless authorized in writing by VirtualMaterials Group.
19
Virtual Materials
.............~r~.~~,I~~:__ . __§J~_~~_~_!!_~9 ....~_i._!I.~_.'!~§~i.~_
i0,9666 i
90,oi
1:~~::~1102203.68 j
~:~~~I4A10E+1 i
-2,ODSE+Sj
lMl279'1.0940
R Show Short List
VapFrac
T[F]P [psla]Mole Flow [bmolejh]1'1M' Flow Dbih]Volume Flo'if [mi']Std liq Volcme Flow [ft3i']Std Gas Vobme Flow u~r,lSCFD]
Energy [lltuthr]J:i Propernes(:-.' Fraction
NITROGEN [Fraction]CARBON DIOXIDE [Fraction]HYDROC,fN SULFIDE [Fraction]r'lETHANE [Fraction]ETH.o,NE [Fraction]PROPANE [Fraction]I£.QBLrTANE [Fraction]r.-llUTAhE [Fraction]
In
':E Flash_Tonk_VentT.: From_Crass_Exchange
+ Gas_to_Abs
±! Heated_Rlch_Amnef! Lean_Amine
''If) Make_Up_~;r;;ater
!t' Rege.nerated_.o.\mine
i+ Rich....;Arnine'+: Rich_4.mine_to_Cross_Excha. ,.
."..: Rich_fron1_AD
±: Sales_Gas
Out
f:E To_Coolerltj TO_f13sh_Tank
Of: Toyump
Controller.sRjch_Loading_CantrQlh~f
(j fxce:IUnitOpsWater_Balance_CafQJlatQf
By clicking on "Hydrogen Sulfide [Fraction]" and then pressing "OK" the molefraction of H2S will be added as an independent variable. It should vary between0.0 and 0.2 with 21 points in between this range. For dependent variables, selectthe molar flowrate of the lean amine, sales gas and sour gas, as well as thehydrogen sulfide mole fraction in the last two streams. Once added, press "Run"to perform the case study.
flame:
Set u? ) Reiults I Nat! 5b:lh.l'i!
j;t- RllfI AJt CQnminab:)f;S t"umQer .ofPoints-:, 11
r~~~:;fit~~~~~is;:;3;;J~·:·F~~~~~~~QOG~0!1S.L~.CFll:~E'~):.- 'A;9;:';.-....,ii iil!~~~~."~'~"f:,.h~''"'~";::::;~::::~~:::::::·. ~~~~Jj,llDO'''' J "*'" I
_~~~~J Cslom
Going to the "Plot" tab, it can be seen that the plotted results are displayeddifferently with one independent variable than they were for two independentvariables. With one independent variable, the Y axis is defined by the type ofvariable that will be shown (mole fraction, flowrate, etc.). Once the variable typehas been selected, the check boxes can be chosen to show whichever variables
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20
Virtual MaterialsGroup, Inc. Simulating with VMGSim
of that type are desired to be shown. With "MoleFlow" as the Y variable type andall 3 stream options selected, the plot will look as follows.
2400(;
22f.l011
Oeletl!
ft'Qhldi:ktomowP'otme,-;
..-------&----- lle::..,jl.rnine,ln Mol-=F1ow,,~ !JaI",~_Gas.In.Mo!enow
....•.. IAcj·:tGadn.Hol.:Fkrw
,,-~'OOl;'-------------------:i
~.JK'l,1:\_'4.'
.<:tOOG
~lBO(lD
~ H~!}OC
g HOOG
~ 12001}IT:(I) toDOl)-0:2. IWOC,
600C
400C
200C
:i.1O 020
cO-C.1""'-C'."""C-"'·'--"'<---".--'.'--....'O-.'--._'--.i--_.-.-._._.~---._.. -.-.•-'--.-._.E),DB
ac_HYDROGEN_SULRDE qSou,_Gas.ln.Fraciion HYDROGEN SULFiDE)
Meanwhile, the plot looks as below with air of the mole fractions shown.
',7,------------------,.".' ....-..u.s
Frae_HYDRO GErc5ULFlDEFrac_HYDROGHCSULFIDEl
....•--.. Frac_HYDROGHUULFlDE2 Rlghtd:cktoSY.l'NpiotlIlenJ
1)2 .•
_HYDROGEN_SULFIDE (ISou,_Gas in Frachon HYDROGEN SULFiDE)
Also, the dependent variables can be displayed on the x-axis. For example, ifthe sales gas flowrate is chosen as the x-axis variable, with the mole fractions set
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21
Virtual MaterialsGroup, Inc. Simulating with VMGSim
to be on the y-axis, the plot will look as below. This provides for many possibledisplay options.
~Iected(a$e';
II<lme:
SetUp! Results ;>:ot l Status I
0.7,-:------------,.'...'. "...
ISaies_Gas.hMoleFlow [lbmole,'h]
------.------. FI5CHYDAOGEtCSULFlDEFrac_HYDROGHUUlFlDEl
- • Ftac~H'TDROGEtCSULFlDE2R"J'lt dr:k 1D sh'JY,' p'olrr.ef:U
As well as the plots displayed, the results tab will also display the gatheredinformation, as was the case with two independent variables.
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;}.....~~~.....,>i<,l\
Hydrodealkylation Reactors
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J Virtual MaterialsGroup, Inc. Simulating with VMGSim
Summary
Property PackageAdvanced Peng-Robinson
ComponentsHydrogen, Methane, Benzene, Toluene, Biphenyl
Stream Information
Stream Name Feed
T (K) 894.3
P (psia) 503
Mole Flow 4382.5(Ibmole/hr)
Hydrogen 0.4291
Methane 0.4800
Benzene 0.0053
Toluene 0.0856
Biphenyl 0.0000
Unit Operation Summary
PFR1Diameter - 9.57 feet
Length - 57 feet
OutT - 957.2 K
OutP - 486 psia
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Reactions
Simulating with VMGSim
Reaction Name r1 r2
HydroQen -1 1
Methane 1
Benzene 1 -2
Toluene -1
Biphenyl 1
Reaction Kinetics
r1
X1 =rxnCmp['HYDROGEN'].Fraction
X2 = rxnCmp['METHAI\IE'].Fraction
X3 = rxnCmp['BENZENE'].Fraction
X4 =rxnCmp['TOLUENE'].Fraction
X5 =rxnCmp['BIPHENYL'].Fraction
r = 61430*exp(-25616/T)*(X4*P)*(X1*P)**O.5 # Ibmol/s-ft3
r2
X1 = rxnCmp['HYDROGEN'].Fraction
X2 = rxnCmp['METHAI\IE'].Fraction
X3 =rxnCmp['BENZENE'].Fraction
X4 = rxnCmp['TOLUENE'].Fraction
X5 = rxnCmp['BIPHENYL'].Fraction
r =998*exp(-25616/T)*(X3*P)**2-4255*exp(-25616/T)*(X5*P)*(X1*P)
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~ Virtual MaterialsGroup, Inc. Simulating with VMGSim
CSTR1Volume - 4065.842 feee
OutT - 957.2 K
OutP - 486 psia
Reactions
Reaction Name r1 r2
Hydrogen -1 1
Methane 1
Benzene 1 -2
Toluene -1
Biphenyl 1
Reaction Kinetics
r1
X1 = rxnCmp['HYDROGEN'].Fraction
X2 = rxnCmp['METHANE'].Fraction
X3 =rxnCmp['BENZENE'].Fraction
X4 = rxnCmp[TOLUENE'].Fraction
X5 =rxnCmp['BIPHENYL'].Fraction
r = 61430*exp(-25616/T)*(X4*P)*(X1*P)**0.5 # Ibmol/s-ft3
r2
X1 = rxnCmp['HYDROGEN'].Fraction
X2 = rxnCmp['METHANE'].Fraction
X3 =rxnCmp['BENZENE'].Fraction
X4 =rxnCmp['TOLUENE'].Fraction
X5 = rxnCmp['BIPHENYL'].Fraction
r = 998*exp(-25616/T)*(X3*P)**2-4255*exp(-25616/T)*(X5*P)*(X1 *P)
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Virtual MaterialsGroup, Inc. Simulating with VMGSim
Hydrodealkylation ExampleIn the following tutorial, two reactors will be created which will performhydrodealkylation of toluene. One reactor will be a PFR, with the other being aCSTR. For this case, Advanced Peng Robinson (APR) will be used as theproperty package.
Show Sekxtioll helper
~hetnlodyn~~~~~~ .•!Ad-"O!1::ed PengAwbinson
eryGas Treating Chem~a! SolvE:ntGa~Tfeatin9 Physocc! Solventcr treatingoche.m'calsPressure no:') Associating ChemiC5istT'lediuT: Pfes~lire: Assodatina SystemsPressure C!:em;:<ils -
Cancel
Hydrogen, methane, benzene, toluene and biphenyl will be the componentsadded to the property package.
~Ute (om;:>ound Secrch IHypothetical Compound 1
<:ompoynd ffamify rmo;;.;;;;;;~= - __~ i~- DetatFamuy Groups
Delete
Delete AU
Apply
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Once these have been added to the case, the reactor feed stream should becreated. This stream is shown below.
r Detail View
r Exdude From Summary
Summary IEquilibrium Results I tine Sizing I
connected to (In lOut]VapFracT[F]P [psialfYlc,leFlow Obmc,le;h]MassFlow Ob;h]VolumeFlm'l [ft3,1s]StdUqVolumeFlow Ift3,1s]StdGasVolumeFlow UYlfYlSCFDJ+, PropertiesH·j Hole
··f StdUqVolume
1.001150,0
503.004382.5073917.16
42.1661.2D9
3,9914E+1
PFR1Jn
[rbmolefriJUb/q,][ftS/s]
Print I Creatie Port I.' Deletie Port I r Ignored
The first reactor that will be created is the PFR. Create the reactor and connect itto the feed stream.
PFR1
There are two reactions that take place within the PFR. They are as below.
Tolune + H 2 ~ Benzene + CH4
2Benzene ~ Biphenyl + H 2
The kinetics for each of these reactions are expressed based on the partialpressures of the components. These are shown below.
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If?1'1 =61430exp(-25616/T)PTPH -
1'2 =998exp(-25616/T)PB 2 -4255exp(-25616/T)PDPH
The units for rate of reaction for these equations is Ibmol/(ft3s), with thetemperature in Kelvin and the pressure in psia.
The first step in solving the reactor is to specify the reactions. To do this, openthe PFR form and go to the "Reactions" tab. Press the "Add/Edit" button to bringup the form below. Fill it out with the required reactions, as shown below.
Enter data 011 the <New> column' to add a reactioJl, <Delete> key to delete a reaction
0.00 0.00tu~bn101] 1-17973.8562 3568.9714
r~~~~re~a~ct~ion: Rxn1 _ - - _ ,
lr2:HyDR.6GEf~+BlpHE~jyL~2~lBEr'JZEi;JE
IF..: : :..:..:.::.:.:.:..: ! r1 <New>HYDROGEN BENZENE
Since the reaction rate uses a combination of imperial and metric units, a newunit set should be created. Since all of the units used are Field units, except forthe temperature, this will be used as the basis for the new unit set. To do this,select "Unit Sets" under the "Tools" menu.
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R.efresh All W'indows
Close All, Except Current,. Unit Op Forms
Frle Viewftoo!s} Assist.~~~t.~,_.?{~at::I::__R.eporting
R.e-solve the case
Check PFD
Check Unit Op. Hierarchy Tree
Unit Sets...
Options".
Hardware Key Info
Case Study."
r 100 PFD2
Now press the "Clone Unit Set" button and select "Field" as the unit set to becloned. Name this new unit set "FieldHDA".
Clone Unit Set
as
By scrolling to the right the created unit set can be seen.
cpbbljday
Bt"Brurib-P(BbJ{ft3)1{2psta-ft311bmQI-R,Btu,furBbJ•.1bBtJi'1bmol-FfI.':!Ah.........1
···················--····l~
}r' Unlt Sets __._ -._..... . _-_..__ - _.- __.- _._ -
<~<~~A~cti~ve~u~r;~~~e=·~:=_·~·~~"ildHD~_-iAI·_· ~..-m·-m..~··1..I-i:;Ji·~'[~;=>'::tro:din"'··i··:'"'oirm""·i'··;;;'~=:;CCt~·~:u=-i··CCl·~~'!i~<i""~iJ·i~·~~c=lJn~:J;!'~et~.....=..=I=~••iU~••~~~~~~f===;~j!L ......._.._..._...._..._....J4iftg...5..hs dd9, (i ME SImgscm _..__J94 E4 "kI,4 HetdHDA ...~~~_~ .....
j Pa pSla kPa kPc ip;;·_·--· kPa f:".Pa psia ~I:··.~·.<...<... ·l,.,: :,:.
';K F eKe K K F :
J~9~'3 :;ft3 ;~~m3 :~1n3 ~:m3 :~m3 ~g~m3:fD L ":! 1,1
..............................!m2 acre m2 m2 m2 m2 m2 acre............ . j N Ib-force kg-fon::e kg·fufl::e kg:4orce kg~furce kg-force Ib-furce
ft m m m m ftIb kg kg kg kg '.g Ibday s s day
Pa-s Pa-s Pa~.s Pa-s cpm3jhr m3/hr m3jbr m3/l-! ft3fsJ J J J BtuIUlkg-K 1U/kg,K kJ/kg·K kJft:g-K Btu/lb·f(J{m3)ljZ (J/m3)1{2 {J/m3)1/2 (Jjm3)lj2 (Btu/ft3••JikmoJ-K, lUikmoHC J/kmt>H<. kJ;,kmoJ-K. psia·ft3_Vi W JeW IN Btujhrr~!~J rJAg kJ{kg kJ,~41 Btu/lbkJ/krnol-K kJ,Ikrnol-K kJllcmQ]-K Btu/Ibm....
The temperature of this unit set should be changed from F to K. To do this,select the temperature unit set drop down and change the unit set.
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4
,~ Virtual MaterialsGroup, Inc.
• Fi'eldHDA <~psia
~-~
RCf
'"TU
ft
Simulating with VMGSim
Now press "OK" and then select "Yes" in both of the following pop-ups to use thenewly created unit set.
Do you want to install/Modify the unit set FieldHDA?Empty units ....vill use VfvlGSim defaults:
Yes
Change active unit sette FieldHDA7
No
Yes
Returning to the PFR form and going to the "Kinetic Variables" tab and switch thereaction to "r1".
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Virtual MaterialsGroup, Inc.
Summary1Reactions Kinetics I Kinetic Variables I Profile IC:lIst().I1l~I:III.a.t:i_()111!l1i'?lO~; sim42
[)iJml'in!l:FiJcl:J>.f. i 1parametersl'r.~I:IJac()bia_l1t:f~ :10
NaxError i0.00001
"laxtlum~t~r<l.ti()I1~_~~::::!20NinimizeError i 1
" , -~_._.~-_..;
HonitorConve!!l:ell'<:~___ :0Number5ections 110
Kinetics
=0
Print User Variables· .,
To enter the reaction kinetics, now press the "Edit". When the kinetics formopens, check the "Using Advanced Kinetics" box. Replace the
X1 = rxnCmp['HYDROGEN'].Fraction
X2 = rxnCmp['METHANE'].Fraction
X3 = rxnCmp['BENZENE'].Fraction
X4 = rxnCmp['TOLUENE'].Fraction
X5 = rxnCmp['BIPHENYL'].Fraction
r = 61430*exp(-25616/T)*(X4*P)*(X1*P)**O.5 # Ibmol/s-ft3
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6
0,00
0,00
0,00
0,00
# Ibmol/s-ft3
Virtual Materials
Group, Inc. Simulatin
/"rll"~i'J~E:~;:,a~"~~i'~~~'~t"t"_"""""'T"""'" _. :~i~:~:E~:i~~R~ii.:~j:.F.;~cti.~.~ .X2 = f)(nCmp['f>1ITHAflE'].fractionX3 :::: rxnCrnp['BEtllEliE'].FractKmX4 := rxnCmp['TOlUENE'}.FractionX5 :::: rxnCmp['BIPHEJ'Nl'].fractionr ~ 61430*""p(-25616/TJ*{X4*P)'(Xl·Pj'·O.S
Make sure to change the reaction unit set to the created FieldHDA.
Unlt5etofKinetics Reaction
; Kinetics
Notes
QK !;;ancel
Pressing "OK" will allow this to be added to the reaction kinetics. Repeat thesesteps for the other reaction by selecting it and then pressing "Edit" again. Enterthe kinetics below for this reaction.
X1 = rxnCmp['HYDROGEN'].Fraction
X2 =rxnCmp['I\/IETHANE'].Fraction
X3 = rxnCmp['BENZENE'].Fraction
X4 = rxnCmp['TOLUENE'].Fraction
X5 = rxnCmp['BIPHENYL'].Fraction
r = 998*exp(-25616/T)*(X3*P)**2-4255*exp(-25616/T)*(X5*P)*(X1 *P) #Ibmol/s-ft3
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Virtual Materials
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[;7 Using Advanced Kinetics'"""~'"~"""'""••'.':'.:~.".~'"~"'~.~"••""""~T"~."~."'""".~.ix:i·;··~c;:;~;'6iYDROGEWr.r;;ct;;;:;"·_-···~·~~~"·~~
\
'X2 = rxnCmp['f-lITHAliE'].FractionX3 = rxnCmp['BENZHlE'].FractionX4 = rXTlCmp['TOLUEtIE'].FradionX5 = rxnCmp['BIPHEllYl'].Fractionr, 0 "-'_="m'(""')'W""~ # .""".",
QK
Pressing "OK" allows both of these reaction kinetics to now be specified. Returnto the "Summary" tab to finish specifying the reactor. The outlet temperature andpressure will be 957.2K and 486 psia. Lastly, the reactor diameter will be 9.53feet and the length will be 57 feet. Entering these specifications will allow thereactor to solve.
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Summary)
j Reactions
solved
Kinetics'j Kinetic Variables 1 Profile Notes I
3.9914E+1
0.42910.48
0.00530.0856
0.00
1.00894.3
503.004382.50
73917.1642.166
1.2093.9914E+l
17,009.53
298.257.00-1,03
4D65.842
-1.987E+6
User Variables
Delta P [psi]Diameter [ft]External T [k.1Length [ft]U [Btujhr-ft2-f]Volume
Is Recycle PortConnected Stream/Unit OpVapFracT [K]
JP [psia] ••r-1oleFlo'N Dbmole/h]fvlassFlow Db/h]VolumeFlo'N [ft3/s]StdLiqVolumeFlow [ft3/s]StdGasVolumeFIc,w [MMSCFD]EH Properties (.C\lt+R);::i Fraction [Fraction]
IfVDROGEN
rVJETHANEBENZENETOLUENEBIPHENYL
Naterial ·..· ·..· ·..·· ··· · , "I
The CSTR can now be created. So that the same feed is sent to both reactors,the Out port of the "Feed" stream will be cloned and connected to the CSTR. Todo this, open the "Feed" material stream form. Press the "Create Port" button.
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9
... 'Feed (SifeamJAaterial)
EJ flame: Description:
Simulating with VMGSimVirtual Materials
Group, Inc.
Spe<:from
r- Detail View'r Exdude From Summary
Summary 'I Equilibrium ResultEi tine Sizing I
Print 1[creat.ePortl ... DeleiePort I r Ignored
PFRl.ln1.00
894.3503.00
4382.5073917.16
42.1661.209
3.9914E+1
![l'raction]![l'ractionli [Fraction]
toVapFracT[K]P [psia]MoleFlow Obmoletru~lassFlow ObthlVolumeFlo'/'l [ft3/s]StdLiqVolumeFlow [ft3/s]StdGasVolumeFlow [Mr"SCFD]it: PropertiesFE Hole'f' f4assif: StdLiqVolume
This opens the following form.
Change the port type to "Out" and press "Clone". This will clone the port,although it cannot be seen on the PFD. Now create a CSTR and connect thecloned "Feed.Out" port, which will be named "Feed.Out_1 ", to the CSTR.
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10
f' Schematic
r Ignored
Virtual MaterialsGroup, Inc.
Nain Data
Summary 1Reactions I Kinetics 'I Kinetic Variables I
Portl'iameIis-R~~y~i~~p~~t .. -- -----~- ..-...-~--.-j Connected Stream/Unit OpIVapFracIT [K}
IP [psia}
:. r'IoleFlow Qbmoleih}r'1assFlow Qbih]Volumeflo'N [ft3js]StdLiqVolumeFlow [ft3is]StdGasVolumeFIDw U'Ir'ISCFD}
Properties (,"Ilt+R)Fraction [Fraction]HYDROGEN~1E11-J,4NE
BB~ZENE
TOLUENEBIPHENYL
if) l"lassFraction [Fraction][±; SroLiqVolFraction [Fraction]
This will now send the same feed stream information to both created reactors, incase changes are made to the inlet feed.
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Virtual MaterialsGroup, Inc.
Summary "j Reactions I Kinetics Kinetic Variables:1 r Schematic
l'lain Data
0.42910.48
0.00530.0856
0.00
1.00894.3
503.004382.50
73917.16 73917.1642..166
1,2.093.9914E+1
Feed.Out 1
User VariablesPrint
Dbmole.lh]Dblh]
I VoliumeFlow [ft3/s]I StdLiqVolun1eFI(lW [ft3/s]iStclGasVolLlmeF:low {I'lr'lSCFD]
Properties (Alt+R)Fraction [Fraetie'n]HYDROGENI;JETIiANEBENZENETOLUENEBIPHB~YL
MassFraction [Fracbon]StdUqVolFraction [Fraction]r.1l ....1....c:I""", nh ............L.., ,l-.T
The reactions and reaction kinetics should now be specified in the CSTR usingthe same methods used to specify the information in the PFR.
Once this is done, the same outlet temperature will be specified for the CSTR aswell. The same volume, 4065.842 feet3, will be used as well. It can be seen thatquite similar results are obtained with the CSTR as are with the PFR. There arehowever slight differences, which are due to the fundam~ntal differencesbetween a CSTR and a PFR.
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Virtual MaterialsGroup, Inc.
Solved
r:::§~i~i~~~;,:::J] .!!,eactionsl Kinetics I Kinetic Varia bles I rM
Schematic
f-1ain Data
0,3661
0.54509
0.06620.02051
0.00209
0.42910.48
0.0053
0.08560.00
17,00
4065.842
User variables!
r:------~:-r:--;-----,_------------
r'lateria!-
~;;:':::--I..'~.:..};::.eed=.o=ut::-::9'-\_~I_;_-t_r_.---9-5-,,-~..,r:1 P [psia] 503.00 486.00lr"loleFJo\\' Dbmole/h] 4382.50 '1382.50IMassFlo'N Dblh] 73917.16 73917.16
IVolumeFlow [ft3/s] 42.166 46.692"StdUqVolumeFlow [ft3/!>] 1.209 1.178
.StdGasVolumeFlow D-1r'lSCFD] 3.9914E+1 3.9914E+1
'I' fE Pro~perties (.l\lt+R). i=::J Fraction [Fraction]
j ~:::J
IBENZENETOLUENEBIPHENYL
1
','" IVlassFraction [FI'action]:Ef' StdLiqVolFraction [Fraction],',-, '"i.-.l ....cl .....,.,, nh ...... ,.,J"..., ,\-.1
CSTR1
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