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Problem Statement: What are the names of the Aspen HYSYS unit operations to be used in VBA? | Solution: The following table presents the list of the names used by Aspen HYSYS to define the unit operations.
Visible Type Name
TypeName
Separator
flashtank
3 Phase Separator
sep3op
Tank
tankop
Cooler
coolerop
Heater
heaterop
LNG
lngop
Heat Exchanger
heatexop
Compressor
compressor
Expander
expandop
Pump
pumpop
Valve
valveop
Pipe Segment
pipeseg
Mixer
mixerop
Tee
teeop
Simple Solid Separator
simplesolidsepop
Cyclone
gascycloneop
Hydrocyclone
hydrocycloneop
Rotary Vacuum Filter
rotaryfilterop
Baghouse Filter
baghousefilterop
Cont. Stirred Tank Reactor
kineticreactorop
Plug Flow Reactor
pfreactorop
Gibbs Reactor
gibbsreactorop
Equilibrium Reactor
equilibriumreactorop
Conversion Reactor
conversionreactorop
Distillation
distillation
Refluxed Absorber
refluxedabsorber
Component Splitter
fractop
Absorber
absorber
Reboiled Absorber
reboiledabsorber
Shortcut Column
shdistop
Liquid-Liquid Extractor
liqliqextractor
Standard Sub-Flowsheet
templateop
Absorber
absorber
Adjust
adjust
Set
setop
Recycle
recycle
Spreadsheet
spreadsheetop
PID Controller
fbcontrolop
Selector Block
selectionop
Balance
balanceop
Digital Pt
digitalop
Transfer Function Block
signalop
Split Range Controller
fbcontrolspltop
Ratio Controller
fbcontrolratoop
MPC Controller
fbcontrolmpcop
Boolean Not
booleannotop
Boolean And
booleanandop
Boolean Or
booleanorop
Boolean XOr
booleanxorop
Boolean OffDly
booleanoffdlyop
Boolean OnDly
booleanondlyop
Boolean Latch
booleanlatchop
Boolean CountUp
booleancountupop
Boolean CountDown
booleancountdownop
External Data Linker
linkop
MASSBAL Sub-Flowsheet
massbalop
Relief valve
reliefvalveop
DMCplus Controller
fbcontroldmcop
Cause And Effect Matrix
causeandeffect
Lumper
lumperop
Delumper
delumperop
Black Oil Translator
blackoiltranslatorop
PIPESIM
pipesim
Compressible Gas Pipe
gaspipe
Yield Shift Reactor
yieldshift
ACM Oper
acmop
HYSYS-OLGA Link
olgapipeline.olga
Aspen Hydraulics Sub-Flowsheet
comhydraulicop
Liquid-liquid Hydrocyclone
llhydrocycloneop
Petroleum Experts GAP
petroleumexpertsgap
Fired Heater
firedheaterop
Partial Condenser
partialcondenser
Total Condenser
totalcondenser
3 Phase Condenser
condenser3op
Tray Section
traysection
Reboiler
bpreboiler
Transfer Function Block
signalop
Keywords: Unit Operations, Ops, Name, Visual Basic, VBA
References: None |
Problem Statement: How do I model a packed tower in Hysys? | Solution: The column solves using theoretical stages of separation. Therefore, you must use a HETP approach.
In the sizing utility (Tools | Utilities | Tray Sizing), you can size and rate packed towers and select packing types.
Keywords: HETP, tray sizing, packing
References: None |
Problem Statement: My environment is a Windows 7 machine and it is mandatory to use Aspen Engineering Suite V7.1 (AES) and older versions of the AES but after the installation we are encountering some runtime errors. | Solution: Windows 7 x86 support was introduced with AES v7.2 and Windows 7 x64 support has been introduced with version 7.3 of the AES v7.3. This means all the the defects related to the compatibility with new operating systems shown by older versions have been corrected in these newer versions of the Aspen Engineering Suite.
If the use of AES V7.1 or any older supported version of the AES applications is mandatory under Windows 7, we strongly suggest using Windows 7 XP Compatibility Mode, where the stability of the software can be guaranteed.
http://www.microsoft.com/windows/virtual-pc/download.aspx
Keywords: AspenTech Installer, operating system, Windows 7 compatibility
References: None |
Problem Statement: How do I create a copy of the 'customized materials streams tab' in the same workbook? | Solution: To create a copy of the customized material streams tab in the same workbook first you have to open the HYSYS workbook by clicking on the workbook icon (CTRL+W). In the menu bar go to Workbook | Export | Pages... and select the page of interest to export and save the file on the computer. Now import the saved file by going to Workbook | Import | Pages... This will create a new tab in the workbook with same customized page.
Keywords: export, import, page, tab, workbook, customized
References: None |
Problem Statement: The analysis of water samples from laboratory is given in cations and anions. Can cations and anions be used directly as input? | Solution: Currently cations and anions cannot be used to define electrolytes using HYSYS with OLI . While OLI electrolyte package has this capability, this is a limitation of HYSYS - OLI interface.
The user has to convert the cations and anions to apparent species.
Keywords: cation, anion, electrolyte
References: None |
Problem Statement: Can I link compressor speed to some property of the compressor inlet? | Solution: Yes it is relatively easy to do this via a User Variable. The enclosed user variable (code below) links compressor speed to inlet molecular weight - through a simple linear relationship - however this could be made more complicated or it could be linked to another property, for example feed molar density using InGas.MolarDensityValue.
Sub PreExecute()
'
'Description: Demonstration of how to link compressor speed to inlet gas MW
'
'Declare Variables
Keywords: None
References: None |
Problem Statement: How do I configure a surge controller for a single speed compressor? | Solution: A compressor with single speed motor has only one surge point. Therefore no regression is necessary to generate the surge line. The single surge point can be represented by the surge control parameters as shown in the following screenshot.
For a single speed compressor you only need to enter Parameter B and the values for the A, C, D should be zero. The Parameter B is calculated dividing the Head by the Actual Volume Flow converting the units of this last one from m3/h to m3/s.
Keywords: Single Speed Compressor, Surge Controller
References: None |
Problem Statement: How can I control compressor speed? | Solution: HYSYS vesions 2.2 to 3.2
A PID controller cannot directly manipulate Compressor Speed, but you can always use a spreadsheet in between. Here is what you need to do:
1- Connect your controller output to a dummy operation (selector block is a common choice, since it can handle multiple inlets)
2- Import the controller OP to the spreadsheet.
3- Input the min and max compressor RPM values (these are needed since the OP of a controller is in %, while the value the spreadsheet should send is in RPM)
4- Calculate the required RPM value based on the equation [(OP/100) * (PVmax - PVmin) + PVmin]
5- Export the calculated RPM value to the compressor speed.
Enclosed there is a simulation case created in HYSYS 3.2 that illustrates the above instructions (S109365_v32.hsc)
HYSYS versions 3.4 to current
A PID controller is set up to use the compressor speed as a manipulated variable. The enclosed simulation case created in HYSYS 3.4 illustrates the set up (S109365_v34.hsc).
Keywords: compressor speed
References: None |
Problem Statement: How can I export a HYSYS workbook to Excel? | Solution: You have a number of options here. The simplest one would be to use the Text To File option. This saves the data from the workbook in a comma delimited ascii text file which can then be opened and formatted in Excel. To do this, open the workbook and select File - Print from the main toolbar. When the print dialog appears, select the Text To File checkbox and then press the print button. You will then be prompted to name the file. The file will be given a .txt extension and can then be imported in Excel. (when opening the file in Excel you must specify All Files (.) or Text Files (*.txt) in order to see this file) Another option would be to use OLE to perform this task for you. This option can sometimes be a better idea since it allows you to set the formatting and only import the information you are interested in examining. There are a number of downloadable examples in the Macros and Extensions section of this website.
Sample OLE option: The Workbook Dump. Open your HYSYS case, open WorkbookDump.xls file, click on the Dump Workbook button. Each time the Stream Data changes in HYSYS, you will have to update the Excel workbook (ie. again click on Dump Workbook).
Keywords: workbook, datasheet, print, options, OLE, automation, Excel
References: None |
Problem Statement: What does the Maximum Iterations field affect? | Solution: Maximum Iterations: This sets the maximum number of iterations that the MASS solver is allowed to perform regardless if theSolution is converged or not when this number is hit.
Keywords: MASSBAL, maximum iterations
References: None |
Problem Statement: What does the value in the | Solution: Phase field mean?Solution
Setup - will be displayed during the initial formulation of the optimization problem and construction of the required matrices.
Following this, a feasible point search may be conducted if required, then once a feasible point is established, the optimizer enters an optimization phase within the feasible operating range.
FPS Gradients - gradients are being computed during the feasible point phase
FPS Visible - during the feasible point search, indicates that a feasible point is visible
FPS Invisible - during the feasible point search, indicates that a point in the feasible range is not visible based on the gradient information available at the current operating point.
OPT Gradients - the current operating point is feasible, the optimizer is in a
OPT Search - during the optimization phase, the optimizer is looking for an operating point which stays feasible and improves the objective function
Results - The optimizer has completed its run.
Keywords:
References: None |
Problem Statement: If my Hydrocarbon phase is heavier than my Aqueous phase, why is it still going to the Light liquid Phase connection on a 3 phase separator? What about Dynamics? | Solution: In Steady State HYSYS decides which phase to go which stream only using the phase type definition and doesn't consider the density, so an aqueous phase will always go to the heavy liquid phase stream, even if it has a lower density.
Dynamics on the other hand acts much like a real separator, where the stream is only dependant on the what phases are available for the nozzle to draw from. This means that the higher density liquid will go through the nozzle with the lowest elevation (be default this is the Heavy Liquid Nozzle). Since the nozzle elevations can be set by the user, the product phase can be controlled by the proper setup of the separator.
Keywords: separator; three phase
References: None |
Problem Statement: What are Script files and how do I use them? | Solution: If you do a repetitive task that you want to automate, the easiest way (particularly without programming knowledge required) is to record a script (Tools menu, Script manager, New). This will generate a file (Script file with extension .scp) that contains special Hysys Language instructions detailing what you did. You can then Run this file (Tools menu, Script Manager, Play) to repeat the steps you recorded.
Keywords:
References: None |
Problem Statement: How do I multiply the input variables such as flow rate in Aspen HYSYS? | Solution: To multiply the input (specified) variables, the spreadsheet is used in Aspen HYSYS. In a spreadsheet, you first need to specify the variables that the you want to multiply rather than specifying these variables directly in the streams initially. This is done to prevent consistency errors. Now from the spreadsheet you need to export the multiplied value cell in the spreadsheet back to the actual stream variable.
Note: The value in the stream is now in black color as it is coming as a calculated value from the spreadsheet instead of a specified value in the stream, which would be displayed in blue color.
Please see the attached file sample.hsc for the Temperature (F), Pressure (psia), Flow (lbmole/hr) for the SOUR GAS stream in the spreadsheet, which are linked back to the actual SOUR GAS stream.
Keywords: multiplier, double, increase, math operation
References: None |
Problem Statement: Can I Design/Rate a Heat Exchanger with in HYSYS using Aspen Tasc+? | Solution: New in Aspen HYSYS 2006.5 there is a new HYSYS utility called Tasc+ Design/Rating Utility under the Tools | Utilities (Ctrl+U), which is used to design, rate or evaluate maximum fouling for any existing exchanger in the Aspen HYSYS flowsheet.
? The new utility can use either the specified process conditions or copied process condition from the exchanger and do a design, rating, or maximum fouling calculation.
Design mode allows you to use the Tasc+ design optimization logic to find best exchanger geometry for the current process conditions.
Rating mode allows you to evaluate how much over or under surface the current exchanger geometry is for the current process conditions.
Maximum Fouling mode evaluates the fouling resistance that would be consistent with the current exchanger geometry and process conditions.
A Run button is provided to design, rate, or evaluate the maximum fouling for the selected exchanger independently from the HYSYS solver.
A Transfer geometry from exchanger button is provided to transfer geometry from an existing exchanger to perform a rating or maximum fouling calculation.
A Transfer geometry to exchanger button is provided to transfer the calculated geometry from design to the exchanger.
Keywords: design, rating, Tasc+, 2006.5, utility, enhancement
References: None |
Problem Statement: How do I add my own equation for HETP for my custom packing to HYSYS? | Solution: In HYSYS 2.4, functionality was introduced which allows you to export a value from the spreadsheet to the HETP value in the Design Tab/Specs page of the Tray Sizing utility. This means that you can create your own expression for HETP in the spreadsheet, and export that value to the tray sizing utility.
Keywords: custom packing HETP tray sizing
References: None |
Problem Statement: How do I change the Calculation Execution rate for a specific unit operation alone? | Solution: By default all unit operations follow the default calculation execution rate defined in the Integrator menu. Still the user can override that by adding a Workbook page for each operation type he desires, and including on it the following variables:
1- Use integrator period
2- Composition period
3- Energy period
Then you can un-check the box in the Use integrator period cell and change the energy and composition periods to whatever you want.
Keywords: Calculation Execution Rate, Integrator
References: None |
Problem Statement: How do I print the data as I see it on my screen? Print Datasheet does not give me the option. | Solution: For any operation, if you place your mouse over the blue bar (Window default colour) at the top of the window and right click, you'll get the option to Print Datasheet. If you do not see an option to print what you want, you can Print Window Snapshot. This is under the File menu. Printing a Window Snapshot will print the current active window on your screen.
If you find you cannot go the File menu while keeping the window open (you find you have to close it then you can access File), you have to turn off your modal views (HYSYS 2.2.2 and earlier). Go Tools Preferences and on the Simulation tab under General Options, uncheck the box for Use Modal Views. Now open the desired window again and go to File Print Window Snapshot
Or, for that window only, you can press on the 'pin' in the top right corner of the window to change it to non-modal, then you'll have access to the File menu. By default Modal views are turned off in HYSYS 2.3 and HYSYS 2.4 therefore this will not be a concern.
Keywords: Print Window Snapshot, active winow, print table, print operation, print data
References: None |
Problem Statement: Is it possible to change the results display units when using the HTFS Engines model in an Aspen HYSYS heat exchanger? | Solution: To change the units displayed on the HTFS-TASC results page, navigate to the HTFS-TASC | Methods pagetab and click on the OTHER radio button. A drop-down menu is provided on this form where the user can change the unit of output field.
Keywords: unit, measurement, HYSYS, HTFS, TASC
References: None |
Problem Statement: I am simulating a Distillation column with a total condenser. The distillate temperature is significantly different than what I expect. What could cause this? | Solution: The presence of non-condensable components (even at minute quantities) in the system can strongly influence the condenser temperature. If the upstream unit operations are 'slipping' non-condensable components to the distillation column, the distillation column condenser type should be changed from total condensation to partial condensation. When this change is made, an additional column specification will be required. A column specification of 100% non-condensable component(s) recovery on the condenser vapour stream can be used.
As an illustration, a simulation file is provided. It compares two distillation columns (total condenser vs. partial condenser). Both columns are splitting a n-hexane (C6) / n-heptane (C7) feed such that the top product contains 95% C6 whilst the bottoms product contains 95% C7. A case study has been run for Helium slip into the feed. The results are summarized below:
Helium content in column feed
[ppm]
Distillate temperature [deg.C]
Total Condensation
Partial Condensation
0
119.4
119.4
100
118.4
119.4
200
117.3
119.4
300
116.2
119.4
400
115.1
119.4
500
113.9
119.3
600
112.7
119.3
700
111.5
119.3
800
110.2
119.3
900
108.9
119.3
1000
107.5
119.3
Keywords: Distillation column, Total Condensation, Partial Condensation.
References: None |
Problem Statement: How do I use something like | Solution: The most straight forward way is to add a Balance operation with a Mole and Heat balance type to keep the flows and enthalpies the same. Then add a Set operation to set one of the conditions (such as pressure) of the mirror stream as the original one (The balance keeps the total energy the same, but not the conditions. Setting the pressure, for example, will give the stream enough information to perform a P-H flash).
Also see user variables for PRO II reference stream
Keywords: Pro2 Conversion
References: Streams of Pro2? |
Problem Statement: How do I know if my network key has different family codes? | Solution: You can run the Findnet.exe utility on the computer upon which the keys are stacked to determine if the keys have different family codes. If this utility shows that both keys are both C-CG, they're not stackable. The second one will need to be C-CF or something else other than C-CG.
Keywords: family code, network key
References: None |
Problem Statement: What does the compressor surge curve do? | Solution: The compressor surge curve is used by HYSYS to introduce disturbances in the compressor if the flow drops below the surge limit. This is not the curve used for predicting the Surge Flow for the Surge Controller.
For more information about how the Surge Controller works see the HYSYS Dynamic Modeling Manual, or the followingSolutions, found under the Process Controllers and Logical Ops category:
What is a Compressor Surge Controller? (Solution 109042)
How do I create a Surge Controller in HYSYS? (Solution 115317) What are the Surge Parameters of the Compressor Surge Controller? (Solution 109040)
Keywords: Compressor, Surge
References: None |
Problem Statement: Can I access Stream and Operation Object Notes via OLE Automation? | Solution: Object Notes are found on the Notes page of all streams and operations in HYSYS (on the Worksheet tab of streams and the Design tab of Operations). These notes can be entered with formatting (fonts, colours, etc.). HYSYS stores these notes in RTF (Rich Text Format) form. These notes can be accessed via OLE Automation, but the procedure is not straightforward for two reasons:
It requires use of backdoor variables since operation notes have not been wrapped for OLE access yet.
There is no built in way to get the notes in a plain text format.
The VBA code below will get the Object Note for a named stream and operation, however it will still be in raw RTF format.
Public Sub GetObjectNotes()
Dim hyApp As HYSYS.Application
Dim hyCase As HYSYS.SimulationCase
Dim hyStream As HYSYS.ProcessStream
Dim hyHeater As HYSYS.HeaterOp
Dim hyBD As HYSYS.BackDoor 'Must be of type Backdoor, Object is not good enough
Dim hyObjNote As HYSYS.TextVariable
Dim strObjNote As String
'Link to the currently active document within HYSYS
Set hyApp = GetObject(, HYSYS.Application)
Set hyCase = hyApp.ActiveDocument
'and a named stream and operation on the mainflowsheet
Set hyStream = hyCase.Flowsheet.MaterialStreams.Item(1)
Set hyHeater = hyCase.Flowsheet.Operations.Item(E-101)
Set hyBD = hyStream
Set hyObjNote = hyBD.BackDoorVariable(:Notes.400).Variable
strObjNote = hyObjNote.Value
MsgBox strObjNote
Set hyBD = hyHeater
Set hyObjNote = hyBD.BackDoorVariable(:Notes.400).Variable
strObjNote = hyObjNote.Value
MsgBox strObjNote
End Sub
The attached Excel spreadsheet includes code to convert the RTF format text into plain text and allows object notes (and stream descriptions) to be reported for all streams or operations in a given flowsheet.
See KnowledgebaseSolution #112700 for more information about accessing Stream descriptions via OLE Automation.
For troubleshooting advice on common HYSYS / OLE Automation errors seeSolution #112361.
Note
The Knowledge Base examples are provided for academic purposes only and as such are not subject to the quality and support procedures of officially released AspenTech products. Users are strongly encouraged to check performance and results carefully and, by downloading, agree to assume all risk related to the use these examples. We invite any feedback through the normal support channel at [email protected].
Keywords: OLE Automation, Stream and Operation notes, Backdoor variables
References: None |
Problem Statement: I get a warning that the Pipe angle out of range of pressure drop correlation - what does it mean? | Solution: The Gregory Aziz Mandhane correlation for two-phase flow can only be used up to an elevation change of half the length of the pipe (30 degree angle).
Keywords: pipe segment, angle out of range
References: None |
Problem Statement: How do I set up the RTI Server functionality (which is used for case collaboration) ? | Solution: The server machine can be any machine on your network. It will be the host for messages sent between instances of HYSYS. These messages will contain data published from cases which you wish to link.
Select a machine to act as a server. Set up the Server machine:
1. Share the RTISupport sub-directory located in the HYSYS installed root directory as RTISupport. (To do this, right click on the RTISupport directory in Windows Explorer and select Sharing.)
2. Start the msgserver.exe program located in the RTISupport directory. Once the view is up, press the Start Server button.
3. Ensure that the .xml files located in the RTISupport directory are read/writeable.
Set up the client machine to point to the RTI Server:
1. On the client machine (the machine which will be used to run one or more of the simulation cases to be linked), open HYSYS.
2. Under Tools | Preferences, the first tab is the Simulation Tab. On this tab, select RTI Server. Specify the following settings:
RTI Server Machine = machine name of PC with msgserver running.*
Port number = 2001
XML server IP or name = will be filled in by HYSYS. This is the machine name of PC with msgserver running
RTI User Login name = not required. This is only used to identify the user when using the messaging functionality of the message server.
To find the name of the server machine (ie. the machine on which the runtime server executable will be running), take the following steps. Go to the server machine, and:
From the Start Menu, open the Control Panel.
In WinNT 4.0, open Network and look on the Identification tab.
In Win2K, open System. The name of the machine will be found on the Network Identification tab, under Full Computer Name.
To find the IP Address of a machine:
trom the Start Menu, select Run
type cmd and press OK to open a command window
at the prompt, type ipconfig
This should be all that is required to configure the server and client machines. To find out how to link cases using the case collaboration, refer to the FAQ (ID 109667) How do I link cases/use the case collaboration feature in HYSYS?
Keywords: RTI Server setup case collaboration
References: None |
Problem Statement: Sample example for Unit Operation Extension in Visual Basic .NET | Solution: Unzip the attached files, load theSolution into Visual Studio 2005, build it. Then copy the EDF file to the same folder as the generated DLL file (should be in generated bin folder).
Now run Aspen HYSYS 2006, register the extension, close Aspen HYSYS, and open it up again, the extension should be ready for use.
Note: You need both Visual Studio 2005 and Aspen HYSYS 2006 installed on the same machine in order to compile and run the extension. However, to distribute it to other machines, only .Net run time is required with the dll and the edf files.
To learn how to register the extension, please seeSolution 120871
Note: Visual Basic extensions are supported from HYSYS 2006 and later.
Keywords: Unit Operation Extension, Extension, Visual Basic, VB, VB.NET, .NET, WellHead, WellHeadPlot.
References: None |
Problem Statement: Why I can not change blend name? If I type a new name, HYSYS changes it back to the original name. | Solution: The blend name has to be 12 characters or less. HYSYS gives this message in the trace window. If you give the name within this limit HYSYS will accept the blend new name.
Keywords: blend, name, can not change
References: None |
Problem Statement: When using the OLI package, why do I only see a few components in the component list in the Basis Environment, when I actually have a lot more in my simulation case? | Solution: What you see in component list view in the Basis Environment are the molecular species you selected from the pure component database. Once the Initialize Electrolytes Environment button is pressed, Aspen HYSYS will generate a group of additional components based on your selected components from OLI chemistry model. These additional components and your selected components will be displayed together in the stream composition view, however you will not see those additional components on the Selected tab of the component list view. If you wish, you can see the additional components on the Component by Type tab. The full list of components (selected + additional) can be viewed by clicking the Edit Properties... button at the Fluid Package level or the Stream level.
Keywords: OLI, components
References: None |
Problem Statement: How do I automate the adjustment of my valve size in HYSYS.Process or steady state? | Solution: The valve sizes are used in HYSYS.Plant (dynamic operation) to calculate the pressure-flow relationship for pressure drops. They do not have any bearing on calculations in Steady State. If you want to vary the size of a valve to achieve a certain pressure drop for a given flow in steady state, the adjust operation cannot be used on the valve itself. The valve equations must be set up in a HYSYS spreadsheet and the Cv can be back calculated. Details on the valve flow equations can be found in Chapter 5 of the HYSYS Operations Guide.
Keywords: adjust, valve size, steady state, dynamic
References: None |
Problem Statement: How can I change the Integrator Step Size via OLE Automation? | Solution: The Integrator object has a .StepSize property however this returns a read-only double. In order to set this value you need to use a Backdoor variable (see below). Note this will only work when the Integrator isn't running.
Paste the following code into Excel's VBA editor (or similar) and press the Run button.
Public Sub SetStepSize()
'Description: Use a Backdoor variable to set the Integrator step size
'
' NB Backdoor methods are only recommended when there is no other alternative, the internal
' HYSYS monikers may not remain constant between versions
' so care should be exercised when upgrading
'
'Declare Variables
Keywords: None
References: None |
Problem Statement: How much information do I need to provide to solve a heat exchanger using HTFS+ link in HYSYS?
I have putting data all day long. Still my heat exchanger has not converged? What is the minimum number of data I have to provide to make the heat exchanger to solve? | Solution: Six data/specifications. 5 data under Exchanger | Exchanger Data | Basics: (Shown in Figure 1)
u Shell Diameter
u Tube Outside Diameter
u Tube Length
u Hot Side (It means location of the hot fluid tube or shell side?)
u Number of Tube Passes
1 Data to set baffle type as unbaffled. Path: Bundle | Baffles | Baffle Type. (Shown in Figure 2).
u Baffle Type: Unbaffled
Unless there is an error or Tasc+ fails to converge, an exchanger should solve with these six minimum specifications. All other specifications are taken from default values/algorithm.
Please note that these six specifications are not enough to represent your actual heat exchanger. You should always provide as much information as possible. Major information for pressure drop calculations are (a) Everything in Figure 1, (b) Tube Pitch and Tube Pattern (c) Baffle Type, Number of Baffles, Baffle Spacing and (d) Nozzle Specifications.
In terms of heat transfer coefficient, specifications of fouling resistances are very important. Default values are zero.
Another Note: When it shows Unknown Delta P (as in Figure 1), it means Tasc+ is yet to calculate delta P. It is TASC or Tasc+?s job to calculate the delta Ps. You should not provide delta Ps (in HYSYS) when you are using HTFS (TASC) or HTFS+ (Tasc+) link.
Figure 1.
Figure 2
Keywords: HTFS+, HTFS+ link, Tasc+, data, specification, minimum
References: None |
Problem Statement: How can I add an expander or a reducer in a pipeline? Is there a way to specify its angle? | Solution: Append or insert a segment and select Swage: Abrupt or Swage 45 in Fitting/Pipe (the default type is Pipe, however you can change this via the associated drop down list). The inlet and outlet diameter of the Swage will be determined based on the upstream and downstream connections.
Note that the swage angle is blue, meaning that you can change this value if you want a different angle. If you modify the angle, the name of the fitting will change to Swage: User Specified.
Keywords: expander, reducer, pipe, fitting, swage, angle
References: None |
Problem Statement: I'm trying to import a HYSYS cooler into ACX but I can't see it in the list to select when I'm in ACX with the HYSYS case running in the background. | Solution: You probably need to re-register the acxhysys.dll. To do this:
Go to the DOS prompt and type in: regsvr32 <pathname><filename> (e.g. if you have ACX installed at C:\acx, you would type in: regsvr32 c:\acx\acxhysys.dll)
Once the dll has been registered successfully, shut down ACX and HYSYS (if you haven't already done so already).
You may want to reboot your computer.
Keywords: ACX import
References: None |
Problem Statement: Why does my pump curve display a different flow unit than was specified in the pump curve data? | Solution: On the Rating | Curves pagetab, click on the Plot Curve button to open the Pump Curves Profiles window. Right click on the plot and select Graph Control from the ensuing menu. In Graph Control window, click on the Axes tab and select Flow from the variable list on the left side of the frame. Next, deactivate the check box entitled Use Default Unit and choose the desired unit from the drop down list.
Keywords: pump, curve, unit
References: None |
Problem Statement: Mass isn't being conserved across my column, and some of the components seem to have disappeared altogether. Why might this be happening? | Solution: This is likely to be caused because the column is using a fluid package with different components to the fluid package for the main PFD.
Check which fluid package each flowsheet is using by looking at the Fluid Packages tab of the Simulation Basis Manager (Flask icon on the button bar, or Ctrl + B).
If the column sub-flowsheet fluid package has different components than the main flowsheet fluid package, HYSYS attempts to map one component to another when it transfers compositions across - to view and adjust this mapping go to the Component Maps tab of the Simulation Basis Manager or the Flowsheet tab, Mapping ply of the column runner. Clicking the Imbalance... buttons will show the components that aren't being transferred and should correspond with the loss of mass!
Keywords: Component Maps, Column, Fluid Package
References: None |
Problem Statement: The HYSYS Manual indicates the availability of external Exchanger Rating software like STX. Do I need something like that to do my rating, or can I use HYSYS alone? | Solution: HYSYS can do the rating based on its own internal models. The external software (eg STX) is a more rigorous option.
Keywords: Heat Exchanger
References: None |
Problem Statement: How the heat balance is calculated for a distillation column? I have a converged column. The column's heat is not balanced. | Solution: Heat balance is a default specification. For a converged column, the heat should be balanced.
Here is how it calculates.
Method 1:
Calculate how much heat difference between the outlet and inlet streams (Heat of outlet stream - heat of inlet streams). If it is positive, column feed materials have consumed heat overall. If it is negative, the feed materials have given up heat.
Calculate the difference between reboiler and condenser dutites (Reboiler heat-Condenser heat). This figure must be equal to the previous one(+/- error tolerance). Here, if it is positive, we have provided heat for the materials to heat up. If it is negative, we are taking out heat from the column, which is equal to heat given up by the feed materials.
Method 2:
Say, heat in = negative and heat out = positive.
Error = Sum(heat of outlet streams) - Sum (heat of inlet streams) + Condenser heat - Reboiler heat.
If these two methods show that heat is not balanced, ignore the column and then un-ignore. Recalculate the heat balance. If still the heat is not balanced (except a relatively small difference, which comes from tolerance), check your assay data if you are entered assay information for Oil Characterization.
Such problem we have observed with an assay enthalpy calculation. It happens if the user is not sure about the distillation curve includes light ends or not.
The check point in such a situation is to see the Assay initial boiling point for initial assay (say 1% assay). If the boiling point starts at very low temperature such as -70 F, then assay should have included light ends or else no. The user need to select ignore light ends if the initial boiling points are higher such as 100F.
Also make sure the assay is calculated by pressing the calculate all button in the assay environment to get all the properties recalculated and transferred to the simulation environment.
In simulation environment users are always recommended to create the phase envelop using the envelop utility, there may be some problem with phase envelop (such as only dew point is generated) and user need to work on the assay accuracy.
Keywords: Heat balance, heat imbalance, heat, balance, imbalance, distillation, column
References: None |
Problem Statement: What algorithm is used by the HYSYS SQP optimizer? | Solution: The Hyprotech SQP is a sequential quadratic programming (SQP) algorithm incorporating an L1-merit function and a BFGS (Broyden-Fletcher-Goldfarb-Shanno) approximation to the Hessian of the Lagrangian.
The algorithm features step size restriction, decision variable and objective function scaling, a basic watchdog method, and a problem-independent and scale-independent relative convergence test. The algorithm also ensures that the model is evaluated only at points feasible with respect to the variable bounds.
Keywords:
References: None |
Problem Statement: Can Aspen HYSYS provide reservoir inflow performance data to Petex IPM applications? | Solution: IPM is the whole suite of Petex applications; the experience we have with Petex is on GAP and Resolve. There is a link to GAP as part of Aspen HYSYS Upstream for steady state hydraulics calculations. Here GAP works as an Aspen HYSYS unit operation in the upstream palette.
Petex RESOLVE links into Aspen HYSYS using an ActiveX automation interface. This is useful for extracting information from Aspen HYSYS. However, since it is RESOLVE that is linking into Apsen HYSYS, this link is maintained by Petex and not by AspenTech.
Please direct queries to Petex (www.petex.com) asking specifically if the RESOLVE-HYSYS link can extract the required information.
Keywords: Petex, GAP, RESOLVE
References: None |
Problem Statement: How do I control the position of Inlet Guide Vane curves in a centrifugal compressor? | Solution: Inlet guide vanes have been used to change the capacity of centrifugal compressors. The Inlet guide vanes are pre-swirling the inlet stream to help minimize power consumption, increasing efficiency near maximum capacity.
The enclosed Aspen HYSYS dynamic simulation (S117509.hsc in HYSYS v3.4) illustrates the modeling of a centrifugal compressor using inlet guide vanes. Inlet Guide Vane curves are a built-in feature of Aspen HYSYS Dynamics; however, the position of the vanes is controlled through the use of a spreadsheet. The spreadsheet may be attached to a PID-controller, as is shown in the attached model.
Keywords: compressor, IGV
References: None |
Problem Statement: How are the Dynamics tray efficiencies related to the Steady State ones? | Solution: Steady State HYSYS uses modified Murphree Tray Efficiency, while in Dynamics HYSYS uses vapour bypass. Steady State tray efficiencies don't mathematically relate directly to Dynamic efficiencies. Of course they both have the same trend (reducing SS or Dynamic eff. will reduce the column performance), but for the same eff. value in both cases you will NOT get the same column performance.
For more details on how efficiencies are calculated in HYSYS please visit HYSYS Documentation andSolution number 112557 titled The Scoop on tray efficiency
Keywords: tray efficiency, column, dynamic, steady state
References: None |
Problem Statement: How is the volume for calculating of kinetic reaction is calculated for a packed and trayed column for Reactive Distillation? | Solution: liquid holdup volume = tray area*weir_height
vapor holdup volume = tray area *(tray spacing - weir height)
Note: The calculation is same for trayed and packed tower. To access the variable Go to the column environment ll Double click on the column ll Go to the rating Tab and Sizing page
Keywords: Kinetic reaction, volume, reaction
References: None |
Problem Statement: How do I know what the buttons on the Object Palette represent? | Solution: Move the mouse pointer over the desired button in the Palette. A fly-by description appears in the Status Bar at the bottom of the DeskTop. Note: This also works for buttons in the Button Bar.
Keywords:
References: None |
Problem Statement: What Valve Types does HYSYS have? | Solution: HYSYS has three different valve types:
Linear:
%Cv = OP
Quick Opening:
%Cv = [(OP/100)^0.5]*100
Equal Percentage:
%Cv = [(OP/100)^3]*100
Keywords: Valve
References: None |
Problem Statement: What is the diagnostic print level? Where can I find the diagnostic output file? | Solution: During the optimization calculations, detailed data can be continuously output to a text file, which can be used for diagnostic work with the optimizer. This file is written into the HYSYS installation directory.
The diagnostic print level controls the amount of detail which is written into this file.
When using the HYSYS.RTO+ optimizer, the file will be titled OptimDiag_dyymmdd_thhmmss.txt (where yymmdd is a date stamp and hhmmss a time stamp). Prior to HYSYS version 3.0, the file was titled optimdiagxxxx.txt (where xxxx was a four digit number incremented with each optimizer run).
The data which is recorded will vary depending on the chosen diagnostic level. It will generally include increasing degrees of diagnostic information, such as the optimizer tuning parameters, variable, constraint and objective function values, the Jacobian and Hessian for each gradient evaluation and optimization step, feasibility data, step size, goodness of fit, and optimizer status.
When using the Hyprotech SQP optimization algorithm, the diagnostic file will be named something like sqphp-20020227-121919.log where sqphp is followed by the date in format yyyymmdd and the time from your computer system clock when the run was initiated.
Tuning parameters and initial values of variables, constraints and objective function will be recorded. Updated values of the variables in the problem and additional diagnostic information will be provided with each optimizer iteration.
Keywords: diagnostic print level, optimizer
References: None |
Problem Statement: What options are there for linking Aspen HYSYS data to Microsoft Excel? An Overview | Solution: There are a number of options for transferring data from Aspen HYSYS into Excel. These options are described here. Our recommended option for plant operations and during conceptual design engineering is the Aspen Simulation Workbook. More information is found below and inSolution id#118330.
Copy/Paste (Link)
The simplest option would be to use Copy/Paste. In other words, use the 'Copy' function for any numeric data in Aspen HYSYS, either by using the shortcut Ctrl+C or from the Edit menu and then the 'Paste' function in Excel.
Alternatively, in Aspen HYSYS v3.x and beyond, the option to 'Copy with Labels'/Paste is available. Just like the 'Copy' function, use the 'Copy with Labels' function for any numeric data and its corresponding label in Aspen HYSYS, either by using the shortcut Ctrl+Shift+C or from the Edit menu and then the 'Paste' function in Excel.
An extension of this is to paste a link to the data. This gives a live link, when the data in HYSYS changes, it is automatically updated in Excel. In Excel use the Edit ... Paste Special menu command and then pick As Text in the listbox, and Paste Link on the radio buttons. Instead of pasting in the data, a special formula which links to the HYSYS data is written.
Printing to a Text file
Another simple method along the same lines is to use the 'Text To File' option. This saves the data from the Workbook, or any stream or unit operation, in a comma delimited ASCII text file which can then be opened and formatted in Excel. To do this, open the workbook or any stream or operation and select File ... Print from the main menu. When the print dialog appears, select the 'Text To File' checkbox and then press the Print button. You will then be prompted to name the file. The file will be given a '.txt' extension and can then be imported into Excel. (When opening the file in Excel you must specify 'All Files (.)' or 'Text Files (*.txt)' in order to see this file.)
Aspen Simulation Workbook
The Aspen Simulation Workbook product was developed, because our AspenTech simulation application users were frequently accessing the available HYSYS/Excel linking features. The Simulation Workbook will increase the value of your simulation investment with dramatically improved integration between AspenTech simulation applications and Microsoft? Excel - with no programming expertise required. Since the Aspen Simulation Workbook is an official AspenTech product, it does go through Quality Testing prior to being released. This is a huge improvement over the sample legacy HYSYS/Excel linking tools that are presently available on the AspenTech Support website. The sample legacy HYSYS/Excel linking tools will remain available on the website until AspenONE 2006 is released at the end of 2006.
More information about how to use the Aspen Simulation Workbook may be found in Knowledge Base ID# 118330 and by clicking this link Aspen Simulation Workbook information.
NOTE: The following legacy HYSYS/Excel linking tools will be phased-out with the release of Aspen HYSYS version 2006 (i.e. the examples will no longer be updated). Version 2006 is scheduled for release at the end of 2006 or early 2007.
Workbook Dump
The next option would be to use the Workbook Dump Excel spreadsheet; this can be found in Knowledge Base ID# 110051. Workbook Dump produces a copy in Excel of the data that is being displayed in the current Aspen HYSYS workbook. Each time the stream data changes in Aspen HYSYS, you will have to update the Excel workbook (i.e. click again on Dump Workbook). This option only transfers data from Aspen HYSYS to Excel.
HYSYS Stream Reporter (HSR)
A more flexible option is to use Aspen HYSYS Stream Reporter (HSR); this can be found in Knowledge Base ID# 110050. HSR is an Excel spreadsheet utility that allows material stream conditions, properties and compositions to be easily reported onto a spreadsheet, it also enables streams in different cases to be conveniently compared.
HSR can report properties from the following phases: Overall, Vapour, Light and Heavy (/Aqueous) Liquid, Combined Liquid and Solid. It also allows stream user variables and property correlations to be reported. It is also possible to create formulae in the output table. The user can save sets of properties or use one of the pre-built property sets. Streams from different Aspen HYSYS cases can be reported in the same stream table. Once a stream table has been generated it can be updated by pressing a single button. Stream tables can be moved to another Excel workbook whilst maintaining the ability to be updated.
HSR takes the form of an Excel spreadsheet file with embedded Visual Basic for Applications (VBA) code that demonstrates how Aspen HYSYS can be accessed programmatically. The VBA source code is freely accessible and users are encouraged to learn from it and adapt it to their own needs. Like Workbook Dump, HSR only transfers data from Aspen HYSYS to Excel.
HYSYS Stream Table Generator 3000
Another option is the Aspen HYSYS Stream Table Generator 3000; this can be found in Knowledge Base ID# 110056. When you transfer the stream information to Excel, you may choose the stream order, format, etc. You may also transfer phase information. Stream Table Generator 3000 is similar to HSR except that the VB code is written as a standalone program rather than within Excel. Again, this option only transfers data from Aspen HYSYS to Excel NOT the other way.
HYSYS Browser
The Aspen HYSYS Browser can be found in Knowledge Base ID# 110052. This allows special formulae to be written in Excel cells to create a live link to Aspen HYSYS. Values can be transferred both from Aspen HYSYS to Excel and from Excel back to Aspen HYSYS.
Custom Code
If none of the above prove suitable then it is possible to write custom VBA code within Excel to import any data from Aspen HYSYS that is required. Additionally VBA code can be used to 'drive' Aspen HYSYS; i.e. input data, add streams and operations, change connections, modify and settings and control the solver. There are many specific examples of this within the Programmability/Extensibility and Sample Macros and Extensions sections of the Knowledge Base. A good introductory example can be found in Knowledge Base ID# 110969. More details can be found in the Customization Guide manual and the Developing AutomationSolutions for Aspen HYSYS training course.
Keywords: Excel, Link, HSR, STG, HYSYS Browser, Workbook Dump, Simulation Workbook, Workbook
References: None |
Problem Statement: Is it possible to rotate three dimensional plots generated by a case study? | Solution: Right click on the plot and select the Graph Control option. Use the View Control arrows to rotate the plot.
Activating the Always Apply checkbox forces the plot to update automatically whenever the Angle or Aziumth are changed. If this checkbox is not active, the Apply button must be used in order to invoke any changes made to the Angle or Azimuth values.
Alternatively, a three dimensional graph can be rotated manually by right clicking on the plot and activating the Rotation option. The angle and degree of rotation are then controlled using the mouse via a click-and-drag approach (using the left mouse key).
Keywords: databook, case, study, rotate, rotation, plot, graph
References: None |
Problem Statement: Why does the liquid density remain unchanged when the calculation method is changed? | Solution: It is probably because you only have changed the calculation method for liquid density but not for liquid volume. For example, if you want to use the COSTALD method to represent liqiud density, you need to select this model for both MolarDensity AND MolarVolume for liquid phase.
Keywords: liqiud density, COMThermo, COSTALD
References: None |
Problem Statement: How is the Heat of Vapourization estimated for a Hypothetical Component? | Solution: Several methods are available to estimate the Heat of Vapourization of Hypothetical Components in HYSYS (Simulation Basis Manager Property View, Hypothetical tab, View Group, Estimation Methods button). These methods actually change how the Cavett Heat of Vapourization Coefficients are estimated for the Hypothetical Components Group.
The Cavett Heat of Vapourization Coefficients can be seen in the Component Property View, Point tab (Thermodynamic and Physical Props group).
How HYSYS uses the Cavett Heat of Vapourization Coefficients depends on which property package is used:
For Equations of State (EOS) such as Peng-Robinson, the liquid enthalpy is determined by the EOS directly and therefore the Cavett Heat of Vapourization Coefficients are not used.
For Activity Models (e.g. NRTL, Wilson, Unifac, etc.), the Cavett parameter is determined using an iterative method where the values of the A and B coefficients are hard coded into the program. The optimum Cavett parameter is found using the iterative procedure to optimize the Heat of Vapourization at the Normal Boiling Point (NBP).
The Cavett method in HYSYS is a single term representation, and as such it is difficult to match experimental data closely over a large temperature range. Although both A and B terms are displayed in HYSYS, only one parameter (Cavett A) is actually used in the program. Typically, the predicted data will match exactly at one point (the NBP) but the divergence increases as the temperature moves away from this point.
For more information, please refer to the Hypotheticals section of the Simulation Basis Guide.
Keywords: Hypothetical, components, heat of vapourization, vaporization
References: None |
Problem Statement: Is it possible to run a case study starting with the highest value? | Solution: A case study can be run in reverse order by activating the Step Downward option found on the Independent Variables Setup pagetab.
Keywords: databook, case, study, descending
References: None |
Problem Statement: What does the Calculate wax formation temperature checkbox do? | Solution: The Calculate wax formation temperature checkbox allows you to select whether the deposition model is used to calculate the initial wax formation temperature or the cloud point for each pipe element when performing the deposition calculations.
If activated, the results appear in the Profile page of the Deposition tab.
Keywords: wax, deposition, pipe, segment, ProFES
References: None |
Problem Statement: Is the holdup in the pipe in a valve before or after the valve ? | Solution: The holdup in the valve and pipe is defined as the holdup of whatever is activated in the operation. i.e. it could be pipe only or valve only or pipe and valve.
This then raises the question that if the valve is shut what happens to the holdup? The answer is that it does not change. So the hold up is AFTER the valve.
You can see this in the following case attached.
Start the integrator and go to Dynamics / Holdup / Advanced / compositions on VLV-100. You'll see the valve is closed and is a check valve to avoid backflow from the product block.
The valve holdup has different compositions to feed stream 1.
If you open the valve VLV-100 you will see the composition change to be the same as the feed stream.
Conclusion : The holdup in the valve (pipe and valve holdup if activated as in this case) is after the valve operation.
The pressure drop incidentally can be calculated using either the pipe only, the valve only, or the pipe and the valve together.
Keywords: holdup; pipe; valve
References: None |
Problem Statement: Can I change which tray section a tray sizing utility points to via OLE? | Solution: Yes although the way of doing this involves a 'backdoor method'.
N.B. Backdoor methods are only recommended when there is no other alternative, the internal HYSYS monikers used to access properties which have not been wrapped for access via normal OLE may not remain constant between versions so care should be exercised when upgrading.
The following code snippet illustrates how to create / access an existing tray sizing utility, then change which tray section it refers to, and then make the utility run. Here hyCase is a simulation case object reference to the R-1.hsc sample case.
Dim TSUtil As HYSYS.TraySizingUtility
Dim ATS As HYSYS.TraySection
Dim TSUtilBD As HYSYS.BackDoor
Dim BDTSObjectVar As HYSYS.InternalObjectVariable
'To add a utility use
'Set TSUtil = hyCase.UtilityObjects.Add(TSJM, traysizingutility) '
Keywords: Backdoor, Tray sizing utility, tray section, run, calculate
References: an already present TS util
Set TSUtil = hyCase.UtilityObjects.Item(Tray Sizing-1)
'Reference a tray section (this assumes the R-1 sample case) Set ATS = hyCase.Flowsheet.Operations.Item(T-100).ColumnFlowsheet.Operations.Item(Main TS)
'Get a backdoor variable
Set TSUtilBD = TSUtil
'Attach the tray section to the utility
Set BDTSObjectVar = TSUtilBD.BackDoorVariable(:TraySection.500).Variable BDTSObjectVar.Object = ATS
'Run the tray sizing utility - this goes with the defaults as setup in Preferences TSUtilBD.SendBackDoorMessage AutoSection
TSUtilBD.SendBackDoorMessage RunTraySizing |
Problem Statement: Under Tools | Preferences | RTI Server, what is the RTI Server Login Name? | Solution: This name is displayed in place of a GUID if you use the message window to discuss the case with your co-collaborators.
Keywords: RTI Server Login Name
References: None |
Problem Statement: Why will my column not solve with a subcooled condenser? | Solution: The error message that appears, the column cannot be solved completely with a subcooler condenser with a non-zero vapour stream flow indicates that you had implemented the subcooling option on a condenser which includes a vapour outlet. This feature will only allow the user to specify subcooling on a total condenser. Subcooling is not available using either a partial condenser or full reflux.
If you wish to subcool the liquid stream returning to the column, add a cooler on the reflux stream.
Keywords:
References: None |
Problem Statement: What is the 'Weeping Factor' in Aspen HYSYS and how do I use it? | Solution: In the column subflowsheet, open the Tray Section property view, go to Rating | Sizing | Weeping Factor.
The Weeping Factor is used to add the weeping effect adjusted term to the calculated liquid height over weir:
hghtOverWeir += weepFactor * 2.0 * weepDp * (1.0 - vapToAboveKAvg);
So, when the Weeping Factor is 0, the liquid height over weir will not be adjusted by the above right hand side weeping effect term; and when the Weeping Factor is 1, the liquid height over weir will be adjusted by the full weeping effect term.
As the head of liquid on the tray increases, it overcomes the opposing head generated by the vapour traffic, and you get more weeping (reference Henry Z. Kister's Distillation Design book). Essentially, all columns weep to some degree all the time, and the 'Weeping Factor' in Aspen HYSYS can be used as a calibration factor that helps to tune a dynamic model to match plant data.
Note that the weeping effect modeling has to be enabled by checking the 'Model Weeping' box in the Tray Section property view by going to Dynamics | Specs, and that the default value when you want to model weeping is 1.0 - i.e. full weeping is automatically turned on when the 'Model Weeping' box is checked. You can then adjust the amount of weeping to more accurately represent your real plant by adjusting the Weeping Factor to a value less than 1.0.
Keywords: Weeping, tray, sieve, valve, dynamic
References: None |
Problem Statement: Is the temperature predicted by the Hydrate Formation utility related to hydrate formation or dissociation? | Solution: The Hydrate Formation utility in Aspen HYSYS predicts hydrate formation temperature, not hydrate dissociation temperature.
Keywords: hydrate, utility, prediction, hydrate, formation temperature, dissociation temperature
References: None |
Problem Statement: How does the MASSBAL subflowsheet in HYSYS work? | Solution: A MASSBAL Object in HYSYS is a Flowsheet Object (much like a template object) that holds all streams/unit operations subjected to the equation based solver.
The MASSBAL application uses a graphical interface to create a DAT file. This is essentially a text file containing the streams, unit operations, connections, and any specifications the case may have. It is this DAT file which is used by the MASSBAL dlls to generate simulation results.
HYSYS is able to translate the following unit operations: Separator, Heat Exchanger, Valve, Heater, Cooler, Compressor, Expander, Pump, Mixer, Tee, Recycle Op, Adjust Op, and Set Op.
The concept of the Stream in HYSYS is different from that in MASSBAL. HYSYS streams are flowsheet objects with properties/characteristics (and can exist without unit operations) whereas MASSBAL streams are connections between unit operations. Special streams known as SOURCES feed into unit operations and are fully defined for VLE cases. Streams that exit the flowsheet are known as SINKS.
In MASSBAL, convention dictates that streams are defined as either feeds to a unit operation, or products of a unit operation. In generating identifiers for streams, HYSYS has associated each stream as the product of the immediate upstream unit operation. This works for all streams except SOURCE streams which, by definition, are fully defined.
Keywords: MASSBAL subflowsheet
References: None |
Problem Statement: I loaded my converged case in HYSYS v2.1.1 to v2.2 and now I get inconsistencies generated. Why? | Solution: There have been a number of changes to HYSYS v2.2 which required a v2.1.1 case to re-converge when loading it into HYSYS v2.2 eg stream Cp/Cv is now calculated rigorously. HYSYS v2.2 is now much more rigorous when checking for inconsistencies within a case. If you now get inconsistencies which were not present in HYSYS v2.1.1 there are a number of potential areas which could result in this poblem. Two common examples are explained below:
If the temperature, pressure and vapour fraction are specified for a saturated liquid or vapour stream and the calculated vapour fraction is the same as the specified value. HYSYS v2.1.1 will not display an inconsistency for this despite the vapour fraction being both specified and calculated. In HYSYS v2.2 an inconsistency will be generated. To correct this you need to remove the vapour fraction specification for the stream.
In HYSYS v2.1.1, a component splitter can be set up without an energy stream attached and converge without a complete energy balance over the component Splitter. In HYSYS v2.2, the energy balance must be satisfied so you will get an inconsistency. To correct this you need to add an energy stream to the component splitter.
Keywords: Inconsistency, Over-specified, Component Splitter
References: None |
Problem Statement: Is there a difference in the handling of Streams using the MASSBAL solver as compared to the HYSYS Sequential Modular solver? | Solution: The concept of the Stream in HYSYS is different from that in MASSBAL. HYSYS streams are flowsheet objects with properties/characteristics (and can exist without unit operations) whereas MASSBAL streams are connections between unit operations. Special streams known as SOURCES feed into unit operations and are fully defined for VLE cases. Streams that exit the flowsheet are known as SINKS.
In MASSBAL, convention dictates that streams are defined as either feeds to a unit operation, or products of a unit operation. In generating identifiers for streams, HYSYS has associated each stream as the product of the immediate upstream unit operation. This works for all streams except SOURCE streams which, by definition, are fully defined.
Keywords: MASSBAL, streams, sequential modular solver
References: None |
Problem Statement: What does the Restore File Associationsoption do? | Solution: Starting from version 2006, a standard installation of Aspen HYSYS or Aspen RefSYS will add an option called Restore File Associations to the Start menu on your computer, as shown in the attached image file. To understand what this option does requires a bit of background information.
For Aspen HYSYS to be recognized by your computer, it has to be registered in the computer's registry. This will allow for two things:
1. To start Aspen HYSYS from other programs/applications via OLE.
2. To associate .hsc files with Aspen HYSYS application, so that when you click the name of an .hsc file in Windows Explorer, you will open up the Aspen HYSYS application and have this file loaded.
In the older versions (v2004.2 and older), Aspen HYSYS has a built-in self-registration function, both at installation and at run time. It allows the application to remember the last version a user has used. For example, if you have multiple versions of Aspen HYSYS installed on your computer and double-click on the name of a simulation file, you will bring up the same version of HYSYS application you are currently using or last used if no Aspen HYSYS application is in use at the time.
From HYSYS 2006 onwards, Aspen HYSYS does not self register on start up like it used to do before. It will still do the registration at installation, but no longer at run time. So if you want to bring up Aspen HYSYS 2006 while clicking on the name of a simulation file, you need to select this Restore File Associationsoption to have your Aspen HYSYS registered. You will receive a message indicating that OLE Registration successful once the option is selected.
Keywords: Restore, File Association, Registration, start up, load, bring up, .hsc
References: None |
Problem Statement: Can I specify actuator fail position for a valve in dynamics? | Solution: Yes, This can be done on the Dynamics Tab, Actuator Page of the Valve. Note that using a Fail Open (air to close) valve reverses the action of the attached controller.
However, you must have the HYSYS Fidelity license enabled in order to modify these parameters. To enable this license, go to the Options tab of the Integrator and enable Access fidelity license options. The actuator parameters on the valve will now be shown in blue instead of black.
Keywords: Valve, Actuator
References: None |
Problem Statement: If I flash a stream through a valve, the outlet temperature is different to the case where I run the depressuring utility to the same final pressure. | Solution: The valve operation is assumed to be an isenthalpic process in HYSYS, so the temperature of the value outlet stream is obtained by doing P-H flash on the outlet stream.
However, for a dynamic depressuring, the final temperature will be different for each of the operation modes. It will be different under fire API 521 mode, or with the adiabatic mode. And it is also possible to differ with each heat loss model selected. This is because the heat absorbed by the vessel should be different under different operation modes and the heat loss model.
In addition, the value of the PV Work Contribution on the options page will also be affecting. It is a similar representative for the isentropic efficiency, and is commonly set as 87-98%. The higher value of this term, the lower value of the temperature and/or pressure you will get at the end, or in another words, it is more approach to the isentropic process as compared with the isenthalpic process across the valve operation.
An entirely isenthalpic process like the one in the valve would be represented with a 0%. If you run the utility with this value for the PV contribution, you will be getting more similar values to the ones achieved by the valve.
Keywords: Valve, Flash, Depressuring utility
References: None |
Problem Statement: What are the Calculation Execution Rates on the integrator window options tab? | Solution: The Calculation execution rate are the periods of different types of calculations. The smaller the number the slower the calculation. For example the defaults in the Integrator mean that the Pressure/Flow equations will be solved every time step, control and logic operations will solve every 2 time steps, energy calculations will solve every two time steps and compositions calculations are solved every 10 time steps. It is recommended to use the defaults.
Keywords: Integrator
References: None |
Problem Statement: The liquid level in my vessel is 3%, and I'm getting some vapor in bottom liquid stream, Why is that? | Solution: The nozzles in Hysys are side ways, which means that if the liquid level drops such that it becames less than the nozzle diameter, the product stream will be two phase.
Keywords: Separator, Level, Nozzle
References: None |
Problem Statement: What conditions cause the message Warning ... - Solid particles (e.g. ice pellets) have been detected inside pipe? | Solution: This warning is displayed when either:
The temperature somewhere in pipe segment is below 0C AND water is present in the stream
OR
The inlet stream has a solid phase
If hydrates are likely to be a problem in your system you should check that the pipe temperature profile always stays above the hydrate formation temperature as calculated by the Hydrate Utility (Tools|Utilities).
If you have already used the Hydrate Utility to account for hydrate formation in your stream, you may disregard the warning.
Keywords: Pipe Segment, warning, solid, ice pellets, hydrates
References: None |
Problem Statement: How to generate a plot of a variable or a property?
How to plot a variable (flow rate, composition etc) or a property (viscosity, density, enthalpy etc) with respect to pressure and /or temperature? | Solution: User can generate a property or a variable curve with respect to pressure and / or temperature using Property Table Utility.
Double click on a stream || Attachments || Utilities || Create || Property table || Add Utility
Specify temperature and pressure in state or incremental form
Under Design (left hand side box) select Dep. Prop (stands for dependent property) || Add || select the property you want.
Click on Calculate button.
The status bar will become green if the curve is ready. Use the Performance tab to view results in tabular or plot form.
Note: Like any other utility, property table utility can be accessed via Tools menu. The path is Tools || Utilities || select Property Table || Add utility.
Keywords: Plot, graph, variable, property
References: None |
Problem Statement: After changing anything in HYSYS through OLE, VBA waits for HYSYS to finish solving. Can I regain control in my VBA code and monitor HYSYS as it solves?
What do I do to gain back control over my VBA application while the HYSYS solver is running? | Solution: Generally VB/VBA will wait till HYSYS finishes solving before it starts executing the next line. However if the .CalculationTimeOut property of the HYSYS application object is set to a low number (eg 1) then control will return to the VB code straight away.
If multiple changes are being made to HYSYS using VB it is worth switching off the solver (using [Case Object].Solver.CanSolve = False), making all the changes, and then switching the solver back on again. This prevents the solver from starting after each individual change is made.
The Excel VBA code below illustrates the use of the .CalculationTimeOut property and shows how to monitor the status of the HYSYS Case as it solves. It is designed to work with the HYSYS case Excel Hysys Link - Wait to Solve.hsc (attached) and requires a named cell called HysysStatus. An Excel file containing this code is also attached.
'Require Explicit Variable Declaration
Option Explicit
'dll call declarations
Private Declare Sub Sleep Lib kernel32 (ByVal dwMilliseconds As Long)
Public Sub WaitToSolve()
'
'Description: Demonstration of how to start HYSYS solving, yet still retain
' execution of a VBA macro. Normally whenever you start the HYSYS
' solver VBA stops on the line that caused the solver to start.
' However you can get around this by using the CalculationTimeOut
' property of the HYSYS application object
'
'Declare Variables
Keywords: None
References: None |
Problem Statement: What does the Maximum Iterations field affect? | Solution: Maximum Iterations: This sets the maximum number of iterations that the MASS solver is allowed to perform regardless if theSolution is converged or not when this number is hit.
Keywords: MASSBAL, maximum iterations
References: None |
Problem Statement: What does the value in the | Solution: Phase field mean?Solution
Setup - will be displayed during the initial formulation of the optimization problem and construction of the required matrices.
Following this, a feasible point search may be conducted if required, then once a feasible point is established, the optimizer enters an optimization phase within the feasible operating range.
FPS Gradients - gradients are being computed during the feasible point phase
FPS Visible - during the feasible point search, indicates that a feasible point is visible
FPS Invisible - during the feasible point search, indicates that a point in the feasible range is not visible based on the gradient information available at the current operating point.
OPT Gradients - the current operating point is feasible, the optimizer is in a
OPT Search - during the optimization phase, the optimizer is looking for an operating point which stays feasible and improves the objective function
Results - The optimizer has completed its run.
Keywords:
References: None |
Problem Statement: If my Hydrocarbon phase is heavier than my Aqueous phase, why is it still going to the Light liquid Phase connection on a 3 phase separator? What about Dynamics? | Solution: In Steady State HYSYS decides which phase to go which stream only using the phase type definition and doesn't consider the density, so an aqueous phase will always go to the heavy liquid phase stream, even if it has a lower density.
Dynamics on the other hand acts much like a real separator, where the stream is only dependant on the what phases are available for the nozzle to draw from. This means that the higher density liquid will go through the nozzle with the lowest elevation (be default this is the Heavy Liquid Nozzle). Since the nozzle elevations can be set by the user, the product phase can be controlled by the proper setup of the separator.
Keywords: separator; three phase
References: None |
Problem Statement: What are Script files and how do I use them? | Solution: If you do a repetitive task that you want to automate, the easiest way (particularly without programming knowledge required) is to record a script (Tools menu, Script manager, New). This will generate a file (Script file with extension .scp) that contains special Hysys Language instructions detailing what you did. You can then Run this file (Tools menu, Script Manager, Play) to repeat the steps you recorded.
Keywords:
References: None |
Problem Statement: What is a split range controller? | Solution: A Split Range Controller allows you to split the Output from the Controller to two different valves. The Range of the Output dictates which Output device or valve receives the signal. The split ranges can overlap so that the OP may be going to both output devices at the same time.
Keywords: split range; controller
References: None |
Problem Statement: Can I use Fortran with Aspen HYSYS? | Solution: Aspen HYSYS uses an object model for communicating with extensions. Whether or not it is possible to call up Aspen HYSYS physical routines from a Fortran executable depends on the capabilities of the version of Fortran used (Object Linking and Embedding (OLE) or Component Object Model (COM) compliant or not).
There are currently two methods available for incorporating Fortran routines with Aspen HYSYS:
Use Visual Basic (VB) as an intermediate layer which can call the Fortran code from Aspen HYSYS. Enclosed is an example showing how to link HYSYS to Fortran code through a Unit Operation Extension wrapper written in Visual Basic. The files in MAY17GS1.ZIP can be extracted in a directory such as C:\HYSYS\SAMPLES\85 (for example) while the files in MAY17GS2.ZIP can be extracted in a directory such as C:\HYSYS\SAMPLES\85\85fort (for example). In MAY17GS1.zip, there is a file, readme.txt, which provides more details on the example.
Visual C++ (using MFC) also allows access to COM Automation objects, but it is much harder to achieve and we have very little information or examples for it.
Some versions of Fortran accommodate Automation (OLE or COM compliant). Visual Fortran, for example, provides a wizard to simplify the use of functionality available with COM and OLE. The wizard generates Fortran 90 modules that simplify calling COM and Automation services from Fortran programs, automatically generating Fortran source code that simplifies invoking routines in a Dynamic Link Library (DLL), methods of an Automation object and member functions of a COM object. The generated code includes derived-type data declarations for data structures, procedure interface block definitions, and procedure definitions (external jacket routines) that simplify calling conventions.
Courses are available on Aspen HYSYS Automation and Extensibility regularly throughout the year, at various locations. We can provide a current training schedule. If you require more information on these courses, please email [email protected] and ask for a course schedule or course outlines.
Keywords: Fortran, Visual, Basic, C++, programmability, extensibility, OLE, Object Linking and Embedding, automation, Dynamic Link Library, DLL, Component Object Model, COM, routine, sub-routine, integrate, integration, wizard, wrapper, wrapping, example.
References: None |
Problem Statement: How do I copy a stream between cases? | Solution: First ensure that both cases are using a Fluid package that has the same components. One way of doing this is to export the Fluid Package from the original case and import it into the new one.
Do this by using the Export / Import buttons on the Fluid Packages tab of the Simulation Basis Manager window (Access from the main environment by going to Simulation ... Enter Basis Environment)
Secondly, ensure that the stream in the original case has all the values you want to copy specified (blue) not calculated (black). For example if the stream is in the middle of a process its composition, T, P and flow are likely to be calculated by the upstream process. When you copy this stream all these calculated values will be lost. To get around this create a new stream in your original case, then press the Define from Other Stream button and choose your original stream. You'll see that now composition, T, P and flow appear blue (specified).
Now right click on the PFD icon of this new fully specified stream. Choose Cut/Paste Objects ... Copy Selected objects on the pop-up menu that appears. Go to your new case, right click on the PFD background choose Cut/Paste Objects ... Paste on the menu, the fully specified stream will be copied across. This copy / paste procedure can be used on multiple streams / operations by first selecting all of them by left clicking and dragging on the PFD to select them.
Note that if the two cases do not have the same components, any composition data for those present in the old case but not in the new case will be lost and the remaining compositions re-normalised. HYSYS will give you a warning message before doing this. If the new case contains components not in the old case then their compositions will be set to zero.
Keywords: Copy / Paste, Stream, Cases, Composition, Components, Renormalise
References: None |
Problem Statement: How do I get user variables from *.huv files into HYSYS and start using them? | Solution: Before a user variable can be used, it must first be imported into the case, this is done as follows:
Go to the menu option Simulation ... Import and Export User Variables
Press the Select File button and navigate to the .huv file on your computer (You may need to change the file filter, if it is currently set to .hvv)
Select it and press OK (or Save, if the dialogue box looks like a standard Windows one rather than a Hyprotech one)
The user variables in the selected file should now appear in the right-hand list box, select the user variables required, the Import button should become activated
Press the Import button - the selected user variables should now appear in the listboxes on the left-hand side. These show their names and the type of object they apply to
Press OK
Now go to the user variables page of an object that the user variable applies to...
Stream = User Variables Tab
Operations = Design Tab ... User Variables page
Flowsheet = Flowsheet Menu ... Flowsheet user variables option Simulation Case = Simulation Menu ... Simulation user variables option
The user variable may already appear in the list - if it doesn't, press the green tick button, it should now appear.
To enable the user variable check the checkbox next to its name. To see the code for the user variable, double click on its value, or press the cross and pencil button
Keywords: User Variables, Importing, Enabling
References: None |
Problem Statement: What's new in version 2006 for compressor simulation? | Solution: In the previous versions of Aspen HYSYS, the Inlet Guide Vane (IGV) control was only implemented for dynamic mode. If you have a compressor with a set of user specified IGV curves. If you change the current IGV position in steady state using Aspen HYSYS and previous versions, you will find that the actual operating point stays in one place and doesn't move at all as the current IGV position is changed. In version 2006, you can see that once the current IGV position changes, the operating point changes accordingly in stead state mode.
An enhancement in dynamics is in the area of controllers. In version 2006, you can use the current IGV position as an output target. It means that controllers can now be used to control the IGV position to control the compressor.
Attached with thisSolution is a recorded demo. The second half of this recording refers to the new compressor features, while the first half is for expanders (Solution #120487). For this reason, we have cross-referenced the twoSolutions. Please note that this file is over 13MB in size. If you are interested in download and play it, you are advised to check with your system administrator first to see if such a large file is allowed for your system.
Keywords: compressor, Inlet Guide Vane, IGV, controller
References: None |
Problem Statement: What does the Area values indicated in the LNG, Performance Tab, Summary (Dynamics) page represent? | Solution: It represents the area for each individual layer in the exchanger, multiplied by the number of sets in the zone.
Keywords: LNG Exchangers
References: None |
Problem Statement: Hysys starts but disappears after a few second. Hysys 2004 was working fine but stopped working after installing Hysys 2004.2. Neither version works at this time | Solution:
Keywords: Re-registering SLM client, STRGXI2.DLL, solves the problem
How to Reregister STRGXI2.dll
Log on to an account with Admin privileges
Open a command line or a DOS Prompt and change folder to:
'C:\Program Files\Common FIles\Hyprotech\Shared Folder' and register the file STRGXI2.dll:
1.) Click on Start | Run and type in cmd and click OK
2.) C:\> cd Program Files\Common FIles\Hyprotech\Shared Folder <enter>
3.) C:\Program Files\Common FIles\Hyprotech\Shared Folder >regsvr32 /u strgxi2.dll <enter>
The confirmation message DllRegisterServer in STRGXI2.dll succeeded should appear.
4.) C:\Program Files\Common FIles\Hyprotech\Shared Folder >regsvr32 strgxi2.dll <enter>
The confirmation message DllRegisterServer in STRGXI2.dll succeeded should appear
Keywords
Hysys
References: None |
Problem Statement: Can I perform equipment cost and operating cost studies using Aspen HYSYS? | Solution: Yes, a new costing feature has been added to HYSYS 2006 (this feature requires the installation of Aspen ICARUS). The new functionality allows you to perform a simple cost analysis on all or part of a flowsheet in order to evaluate relative costs as design parameters are changed.
Attached to thisSolution is a recorded demo that explains in detail how this feature can be used. Please note that this file is about 12.5MB in size. If you are interested in download and play it, you are advised to check with your system administrator first to see if such a large file is allowed for your system.
Keywords: costing feature, cost study, economics, ICARUS, equipment costs, operating costs, IPE Integration to Aspen HYSYS
References: None |
Problem Statement: How does one delete the variables in Depressizing utility strip chart? | Solution: You can not directly delete the variables via the Strip Charts page of the Depressuring utility. In order to delete the unwanted variables in the strip chart, you need to access the Databook from the Tools | Databook menu item (or press Ctrl+D).
Please follow the steps below for deleting the strip chart variables:
1. After entering the appropriate connections in the Depressuring utility, open the Databook from the Tools | Databook menu item (or press Ctrl + D).
2. On the Variables page of the Databook, you should be able to see all the current variables from the Depressuring utility. To delete a variable, select the variable and click on the Delete button. It is also possible to Edit and Add new variables from this same page using the corresponding buttons.
If you don't see any variables in the Databook ensure that you have connected a feed stream to the Depressuring utility.
Keywords: delete, variables, depressurring, databook, utility, unwanted, strip charts
References: None |
Problem Statement: What are cyclone, hydrocyclone (HC) and Liquid Liquid hydrocyclone (LLHC) in Aspen HYSYS and how do I use them? | Solution: The Cyclone is used to separate solids from a gas stream and is recommended only for particle sizes greater than 5 microns.
The Hydrocyclone (HC) is essentially the same as the cyclone, the primary difference being that this operation separates the solid from a liquid phase, rather than a gas phase. The solids being separated must be previously specified and installed as components in the stream attached to this operation.
Refer to the HYSYS Operations Guide for more information regarding the Cyclone.
The Liquid Liquid hydrocyclone (LLHC) predicts the performance of an oily water cleaning unit operation. The Liquid-liquid Hydrocyclone generates results based on the Migration Probability Theory. An oil droplet size distribution based on a sauter mean diameter is applied and the resulting volume of oil separated is calculated.
Cyclone & Hydrocyclone (HC)
The Sizing page contains two design modes, On and Off. The radio buttons enables to toggle between turning on or turning off the Design Mode option. When the Off radio button is selected, the Specify Number of Parallel Cyclones checkbox appears in the Sizing page. Activate the checkbox if you want to specify the number of parallel Cyclones in the flowsheet. The Cyclone / Hydrocyclone body diameter can also be entered when design mode is off. In design mode the body diameter is calculated.
For Hydrocyclone, the Mode 1 , Mode 2 and user specification can be selected on the Parameters page. The configuration about the mode is provided on the Rating | Sizing. Similarly for cyclone user has option to select High efficiency, High through output or user specified. The details can be entered on the Rating | Sizing option.
The hydrocyclone used in HYSYS is a narrow cone angle design (cone angle less than 25o ).Mode 1 and Mode 2 configurations are used for high efficiency and high output respectively. The sizing ratios for the two modes are listed below.
CONFIGURATION MODE 1 MODE 2
Inlet Diameter Ratio 0.143 0.333
Included Angle 9.0 20.0
Overflow Length Ratio 0.4 0.333
Overflow Diameter Ratio 0.125 0.435
Total Height Ratio 4.0 12.0
Underflow Diameter Ratio 0.1 0.2
User defined mode allows the user to customize the sizing ratios.
Overflow Length Ratio = Overflow length / Body diameter.
Total Height Ratio = Total height of the apparatus / Body diameter.
The Overflow Length Ratio and Total Height Ratio are only used in the calculation of Leith and Lappel Efficienceies. These efficiencies are relevant to cyclone not hydrocyclone. These ratios are irrelevant pertaining to Hydrocyclone calculations.
When the design mode is OFF (Rating Mode), the body diameter should be specified by the user and it is used in the calculations. When the design mode is ON, the body diameter cannot be specified by the user (it will be EMPTY). The body diameter will be calculated by HYSYS based on the inlet and outlet stream conditions.
If the user gets any error message for solving these unit operations, it is worth to check the constraint page under Rating.
Liquid Liquid hydrocyclone (LLHC)
Refer to the attached HydrocycloneHelp.chm file in the attached LLHC.zip file.
Keywords: Hydrocyclone, Cyclone, Mode 1, Mode, Liquid
References: None |
Problem Statement: For Aspen HYSYS users who are familiar with its application via OLE, please note the changes made in v2006 allow you to start different versions of Aspen HYSYS from other programs, such as Excel, via OLE. | Solution: Currently the following ProgIDs have been made available:
HYSYS.Application
This will start or activate the most current registered version of Aspen HYSYS.
If Aspen HYSYS 2006.5 is registered this will get returned.
If Aspen HYSYS 2004.2 is started up after Aspen HYSYS 2006.5 is installed, that is the one that will be returned.
It is important to keep in mind that Aspen HYSYS 2004.2, as well as older versions would register by itself every time one would run it.
HYSYS.Application.2006
This will return Aspen HYSYS 2006 as long as it is registered.
HYSYS.Application.2006.5
This will return Aspen HYSYS 2006.5 as long as it is registered.
HYSYS.Application.Latest
This will return the latest Aspen HYSYS that is registered. This is more for convenience of future updates. Therefore, for example, when Aspen HYSYS V7 is released, that is the one that will start up if this ProgID is used.
HYSYS.Application.3.0
This will return 2004.2 or earlier version, whichever is registered
HYSYS.Application.NewInstance
This will start a new instance of the most current registered version of Aspen HYSYS.
If Aspen HYSYS 2006.5 is registered this will get returned.
If Aspen HYSYS 2004.2 is started up after Aspen HYSYS 2006.5 is installed, that is the one that will be returned.
It is important to know that Aspen HYSYS 2004.2, as well as older versions would register itself every time one would run it.
HYSYS.Application.NewInstance.2006
This will start a new instance of Aspen HYSYS 2006 as long as it is registered.
HYSYS.Application.NewInstance.2006.5
This will start a new instance of Aspen HYSYS 2006.5 as long as it is registered.
HYSYS.Application.NewInstance.Latest
This will start a new instance of the latest HYSYS that is registered. This is more for convenience of future updates. Therefore, for example, when Aspen HYSYS V7 is released, that is the one that will start up if this ProgID is used.
HYSYS.Application.NewInstance3.0
This will start a new instance of version 2004.2 or earlier version, whichever was last run
Keywords: version, start up, register, instance, ProgID, Excel, OLE, access, automation
References: None |
Problem Statement: Can I see the contents of more than one tab for the same stream/operation at the same time? | Solution: Yes
If you right click on the title bar of the stream/operation window and choose Open Page... Hysys will bring up a new window showing just the contents of the current tab.
Keywords: Open Page, tabs
References: None |
Problem Statement: How do I create a custom tab in the workbook? | Solution: With the workbook view open, go to the Workbook menu, and select Setup.
In the Workbook Setup view, you can Add a new tab, rename it, and include the variables that you are interested in.
Keywords: Custom workbook tab
References: None |
Problem Statement: Does the Twu-Sim-Tassone property package also include the Twu EOS alpha function included in PR-Twu? | Solution: Yes the Twu-Sim-Tassone EOS does include the same Twu alpha function as in the PR-Twu EOS.
Keywords: Twu, alpha function
References: None |
Problem Statement: What is the difference between API and API_60? | Solution: API and API_60 both refer to the same measure, however, within HYSYS, API is used to refer to the actual density of the fluid at flowing conditions, whereas API_60 is used when representing standard ideal mass density. In general, API gravity is defined as follows:
API = (141.5/SG at 60 ?F) - 131.5,
where SG is the ratio of the fluid density divided by the density of water at 60 ?F (i.e. 998 kg/m3).
Note that if you want to change the datum for the specific gravity calculation (i.e. use a density other than 998 kg/m3), you will need to create a user variable, as demonstrated inSolution 115647.
Keywords: density, SG, API, API_60
References: None |
Problem Statement: How do I print tray wise composition at each stage of the column? | Solution: Tray phase composition can be displayed on the Performance | Plots page of the column. Go to the column property interface (Double click on the column) and go to Performance tab & Plots page. Highlight the Composition in the Tray by Tray Properties view. Click on View Table Command Button, a new window with Compositions and a Properties will be displayed. Click on the Properties to customize the information to be displayed. After customizing it can be printed for the composition by right clicking on the title bar (blue colored) of the active view property table.
Alternative way is to use Internal Streams (Go to Flowsheet / Internal Streams page). From there user can create streams containing same conditions and compositions as column trays. By clicking on Add button, user have to enter the name. After that a light blue stream will be created in the column sub-flowsheet. Using the Export option user can create the same stream in the main PFD. Then it can be printed from the workbook.
Keywords: print, composition, vapor, liquid, stage, tray, column
References: None |
Problem Statement: After running a Dynamic model for some time, can we go back to an earlier point in time? | Solution: Unfortunately, this is not possible within the current case. The recommended way to do that is save multiple copies of your model at significant and/or stable points such that you can return to them whenever needed.
This functionality is being considered for future versions of HYSYS.
Keywords:
References: None |
Problem Statement: How can I model a vertical pipe in HYSYS? | Solution: HYSYS contains correlations which can be applied for vertical pipes in certain situations. Below is a discussion of the options available for simulation of vertical pipes.
HYSYS uses the Darcy equation for single phase flow in pipe segments, which can be used for both horizontal or vertical pipes. The Beggs and Brill correlation for two-phase flow can effectively be used for vertical pipes, although it is not a true vertical pipe method - correction factors are added to the horizontal flow map to account for the pipe inclination. The Gregory Aziz Mandhane correlation for two-phase flow can only be used up to an elevation change of half the length of the pipe (30 degree angle), so it cannot be used for vertical pipes.
The OLGAS correlation, which can be purchased as an add-on to the basic HYSYS Pipe Segment, has been tested for all angles from horizontal to vertical flow but does have some limitations (contact Technical Support for more information).
There are several new correlations for use in the pipe segment as of HYSYS 2.4.1 that can be used to model a vertical pipe. Please refer toSolution 109435 for more information regarding these new correlations.
Finally, PIPESYS is a rigorous program specifically designed to model pipeline hydraulics which can also be purchased as an add-on to HYSYS. PIPESYS offers several correlations such as six methods for horizontal/inclined pipes, five methods for vertical upflow and three for vertical downflow. Generally in PIPESYS, the AGF correlation is recommended for vertical upflow while Beggs and Brill is recommended for vertical downflow.
Keywords: vertical, pipe, segment, angle, degree, elevation, pressure, drop, correlation, two-phase, flow
References: None |
Problem Statement: Can the tray section weeping calculations be disabled in Hysys? | Solution: In Hysys versions prior to 2.3 this was not possible. In Hysys version 2.3 this option was added as a check box on the Dynamic Tab of the Tray Section.
Keywords: Column, Tray Section, Weeping
References: None |
Problem Statement: Why is my liquid density different in HYSYS 3.0? | Solution: In Hysys 3.0, the Fluid Package view (Set Up page) has two new check boxes, one for using equation of state (EOS) for density calculation and the other for smoothing the liquid density. These two check boxes show up for and affect the PR, Sour-PR, SRK, and Sour-SRK property packages. The impact is as follows:
Before HYSYS 3.0:
These packages use the COSTALD liquid density model, which only applies when the pseudo-reduced temperature (Tr) is less then unity. When the pseudo-reduced temperature exceeds unity, the liquid density calculation switches to the EOS model. Hence at the switching point, there can be a sharp change (discontinuity) in the liquid density which can cause problems (especially in dynamics simulation).
As of HYSYS 3.0:
For new cases, the density smoothing option is turned on by default. For old cases (including HYSIM ones), this option is turned off. When turned on, HYSYS will interpolate the liquid densities from Tr=0.95 to Tr=1.0, thus giving a smooth transition (and different densities than without the option, especially in the temperature region close to Tr).
If the smoothing option and the EOS density option are both turned off, the behaviour and results will be the same as in the past.
The recommended option is to use the smoothing option and leave the EOS densities turned off. This is set by default in HYSYS version 3.0, based on the fact that the COSTALD model typically does give better liquid densities and smoothing near Tr=1 is common.
This means that liquid densities in cases using the smoothing option may be different from those reported in the older versions of HYSYS.
Keywords: liquid density, smooth density curve, EOS for liquid density, COSTALD method
References: None |
Problem Statement: How can I quickly locate a particular unit operation / stream in a large simulation case? | Solution: If you are looking for an item on a large PFD, functionality has been added since v 2.2 of HYSYS which will help to draw your attention to this item. Under the PFD menu, choose Select Objects, and select the object which you would like to find. A white box should blink around the object in question. You can then press the Home key on your keyboard and HYSYS will zoom into that object.
If you do not need to find the item on the PFD, but simply would like to open the property view, you can use the Object Navigator. You can use the Filter to display only Streams, Unit Operations, or Logicals, or use the Find button to search for the Object by name.
Keywords: lost; pfd
References: None |
Problem Statement: How does HYSYS handle the sizing of split feeds in columns? | Solution: If you have a feed and you mark on the column that it is split, HYSYS will send the vapour to the tray above the feed tray. This will give you the correct flow profile in the column itself but the column will not be sized properly in the utility.
With a feed split, the column is solved with the liquid going to tray 6 and the vapour going to tray 5. But tray 4 will be sized in the Tray Sizing utility with the feed vapour load, not tray 5. To get proper sizing results in HYSYS 2.1, 2.2 and 2.3, do not split the feed in the column itself prior to doing sizing calculations. Only size the column if the feeds are not split. And always answer Yes to the question of whether you wish to use the vapour to size.
(Note: The above description is written assuming that the default convention of having column trays numbered Top Down is observed.)
Keywords: feed split, column sizing, tray sizing, feed tray, vapour feed
References: None |
Problem Statement: I accidentally selected the Dynamics (Fidelity) mode option within Aspen HYSYS. How can I remove the Fidelity License option that I have selected? | Solution: Open the case file in the Simulation Environment.
Click on Simulation on the menu bar and go to Integrator | Option. Now click on the Remove Fidelity button to remove the fidelity option.
Keywords: fidelity; dynamics; license; integrator; fidelity option
References: None |
Problem Statement: How are the heights and locations of vessel weirs and nozzles defined? | Solution: While modeling vessels in dynamics, it is important to know how the heights and locations are defined for their weirs, as well as nozzles. The document attached herewith provides a graphic description of such definitions.
Keywords: Weir, nozzle, vessel, dynamics
References: None |
Problem Statement: How do I send my Aspen HYSYS report to a colleague via e-mail? | Solution: Data from an existing report, as well as from any workbook, stream or unit operation can be saved in a comma delimited text file which can then be opened and formatted in Excel.
To save information using this format, open the desired object (i.e. workbook, stream or unit operation) and select File | Print from the main menu. When the print dialog appears, activate the 'Text To File' checkbox and press the Print button (note that when printing from the Report Manager, there is no need to select File | Print from the main menu, as the 'Text To File' checkbox appears directly on the Report Manager form).
After clicking the Print button, you will be prompted to name the file. The file will be given a '.txt' extension which can then be imported into Excel. Ensure that you specify 'All Files (*.*)' or 'Text Files (*.txt)' in order to see this file when opening from Excel.
Keywords: report, electronic, txt, output, file
References: None |
Problem Statement: I have just installed a subflowsheet but when I connected some streams in the PFD, the icon turned red. What should I check? | Solution: The most likely cause of this is that a Transfer Basis has not been selected for your material stream.
It is possible to use different property packages can be used inside a subflowsheet and its parent flowsheet. When performing a flash calculation on a fluid using two different equations of state, for example, it is not expected that the flash calculation will yield identical results.
As a result, for each feed or product material stream inside the subflowsheet which has a connection to a stream in its parent flowsheet, it is required that a Transfer Basis be specified. The Transfer Basis is used to tell Hysys which two variables should be used to define the thermodynamic state of the fluid for each boundary stream.
To select a Transfer Basis, open the subflowsheet property view and look at the Transfer Basis tab.
For example, suppose you have a fully defined product stream within your subflowsheet, and you wish to ensure that the temperature and pressure of the stream outside the subflowsheet environment are identical to those on the boundary stream inside. In this case, you can select the T-P Flash as a transfer basis. The temperature and pressure of the stream will be passed from the boundary stream in the subflowsheet to its corresponding stream in the main flowsheet, and the thermodynamic package in the main flowsheet will be used to calculate the enthalpy, entropy and vapour fraction.
Keywords: Subflowsheet red, transfer basis
References: None |
Problem Statement: How to fix the corrupted components list error message?
Applicable Version(s)
HYSYS V 2004.2 | Solution: ThisSolution is for the people who have not installed the Cumulative Patch 4 (CP4) for the HYSYS 2004.2 version. In most of the cases, installing this patch will take care of the problem with the corrupted components list message you are getting. All you need to do is to run the .exe file in the attached HYSYS CP4 patch zip file.
This error message is triggered due to a null property package or null component list (i.e. empty). Apparently, Aspen HYSYS should clean these up automatically, but in some instances it does not, hence the error. Installing CP4 should resolve this problem for version 2004.2. The defect has been fixed in version 2006.
If you still get the same message after applying CP4, please send your Aspen HYSYS file to us at [email protected] for further troubleshooting.
Keywords: corrupted components list, 2004.2, error message, CP4, patches, fix
References: None |
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