question stringlengths 19 6.88k | answer stringlengths 38 33.3k |
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Problem Statement: How do I change the interconversion method used by Hysys for D86/TBP and D2887/TBP? | Solution: Go to Simulation/Oil Output Settings and change the interconversion method in the drop down boxes.
You can also go to the Basis Environment, Oil Manager, Oil Input Preferences/Assay Options and change the interconversion method there.
Keywords: interconversion, D86, D2887, TBP
References: None |
Problem Statement: In some situations, we need to fix the volume flowrate of a process stream in our model. How should we do it in Aspen HYSYS? | Solution: This requirement often means one of the two things,
1. If the process stream has lower volume flow, a make-up stream need to be mixed with the process stream, or
2. If the process stream has higher volume flow, a purge stream need to be used to take away materials from the process stream.
The obje... |
Problem Statement: Can I use HYSYS to model Liquid/Liquid contactors with the Amines Package? | Solution: HYSYS Version 2.3 and earlier versions did not have this capability.
Starting from version 2.4, this feature has been added into HYSYS, as a result of the incorporation of AMSIM v7.0. To model sour liquid sweetening process, please make sure to select the Li-Mather thermodynamics option when choosing your pro... |
Problem Statement: Why is Molar Flow reported incorrectly when using HYSYS Stream Reporter (HSR) 1.6 with Aspen HYSYS 2004.2 and later? | Solution: The original HSR 1.6 was fully tested for Aspen HYSYS versions 3.2, 3.4 and 2004, but not for v2004.2 and later. The incorrect Molar Flow is reported in this version of the HSR due to the fact that the internal Unit Type for Molar Flow was changed from Flow in previous versions to Molar Flow in v2004.2.
The u... |
Problem Statement: When you simulate a liquid blowdown situation using the Depressuring utility, you sometimes see a message displayed for Vessel - Liquid Level Initialization with 3 options Increase Temperature, Non-Equilibrium Vapour or 100% Liquid. A screenshot of this message is included in the attached image file.... | Solution: First of all, this message is displayed when the vessel has no vapour phase at the specified process conditions. The following is a brief summery of what Aspen HYSYS will do under these options and suggestions on how to make your choice:
1) Increase temperature
What will happen: The initial temperature of t... |
Problem Statement: Why I cannot export the compositions of a stream from an spreadsheet according to | Solution: 114048?Solution
This can happen because Hysys is giving more or the same calculation level to the stream and it should be giving higher priority to the Spreadsheet calculation.
According to the Calculation Order in a Spreadsheet, for optimal performance spreadsheet cells should have their calculation levels s... |
Problem Statement: Why does Aspen HYSYS sometimes report slug flow with slug length greater than the pipe length? | Solution: The calculated slug length can sometimes cause conflicts (seeSolution ID 128568). According to thisSolution the slug length is the average length of the liquid pocket at the indicated frequency. The bubble length is the average length of the gas bubble at the indicated frequency. If the slug length is greater... |
Problem Statement: How can I make a customized unit set as the default unit set? | Solution: Select the unit set and save it with a preference file.
For example, assume that you created a unit set of your own from cloning a HYSYS default unit set, changed the temperature unit to from degree C to degree K and left the rest unchanged. You named the unit set as My Unit Set. Whenever you open a HYSYS fil... |
Problem Statement: How do I keep the PFD window in HYSYS maximized? When I open a Stream or Unit Operation, the PFD shrinks. | Solution: In HYSYS versions 2.4.2 and earlier, there was a limitation with having multiple maximized windows open at the same time. This has been fixed for HYSYS 3.0 and newer versions.
The workaround in HYSYS 2.4.2 and earlier versions is to grab the corner of the PFD and 'stretch' it to the desired size. Once this is... |
Problem Statement: What is an MPC controller? | Solution: Model Predictive Control (MPC) refers to a class of algorithms that compute a sequence of manipulated variable adjustments in order to optimize the future behaviour of a plant. A typical MPC has the following capabilities:
1. Capable of handling multivariable systems with process interactions.
2. Encapsulates... |
Problem Statement: How can I get vapor pressure of a stream at stream temperature and pressure? | Solution: You can not calculate a vapor pressure at a Temperature and a Pressure. You can get vapor pressure only at a temperature. Because vapor pressure itself is the pressure at a particular temperature the liquid starts boiling.
The calculation procedure is simple.
Step 1: Delete the pressure of the stream (if ... |
Problem Statement: Why does the LNG temperature cross occur even though Auto Prevent Temp. Cross option is checked in Aspen HYSYS Dynamics? | Solution: To use the function of Auto Prevent Temp Cross, it's suggested to specify at least 10 zones to stabilize the Temperature/flow (see Aspen HYSYS manual Unit Operation Guide). As a thumb rule you can have at least one zone for every 15 deg C change in temperature. If you still find instability issues, you can in... |
Problem Statement: How does ICARUS calculate Pipe Testing? | Solution: Pipe testing is a function of the number of fittings and valves, and whether the pipe itself is jacketed, not jacketed, or lined or not lined.
It is also a function of the pipe length and diameter.
The basis equation is as follows:
CONSTANT = 4 by default
if pipe is jacketed or lined, then the CONSTANT = 20
P... |
Problem Statement: How does one select which streams are displayed in each Workbook tab? | Solution: To hide a stream:
1. Open up the Workbook and go to the tab of interest.
2. Right-click on the column pertaining to the desired stream and select Hide.
Alternatively:
1. Open up the Workbook and right click on the tab of interest.
2. Select the Order/Hide/Reveal menu option.
3. In the ensuing Order/Hide/Rev... |
Problem Statement: How to resolve Unable to load odbcji32.dll when trying to run interactive report | Solution: 1. Uninstall Microsoft Access Database Engine
On Windows 10 go to Settings > System > Apps & Features and search for access ...
Uninstall all versions of Microsoft Access Database Engine from your system.
On other systems use Uninstall or change Program or Repair or Remove Programs
Uninstall all versions of M... |
Problem Statement: The liquid level in my vessel is 97%, and I'm getting some liquid in the overhead vapor stream, Why is that? | Solution: The nozzles in Hysys are side ways, which means that if the liquid level rises such that the vapor space becames less than the nozzle diameter, the product stream will be two phase.
Keywords: Separator, Level, Nozzle
References: None |
Problem Statement: When there isn't any water in my stream, HYSYS has predicted the formation of hydrates. Why? | Solution: If water has not been included as a component in a stream or the stream water concentration is zero, HYSYS will perform hydrate formation prediction assuming the presence of free water.
Keywords: free water, no water, zero water concentration, hydrate
References: None |
Problem Statement: How does HYSYS calculate the Initial and Final Boilin Points (IBP and FBP) of my oil? | Solution: HYSYS uses the defaults of 1% and 98% for the IBP and FBP, respectively. With a 1% IBP value, HYSYS utilizes the boiling points of all components in the first volume percent of the given fluid and calculates a weighted average boiling point, which is used as the IBP for any further analysis. The final boiling... |
Problem Statement: Where does one specify the parameters for the Ergun equation in the Plug-flow reactor? | Solution: The Ergun Equation is a correlation derived by Ergun in 1952 for the calculation of the friction factor for a packed bed in a column as a function of Reynolds number. It is represented by:
f(p) = [150 / Re(p)] + 1.75
where f(p) and Re(p) are defined as:
f(p) = [Δp * D(p)] / [L * ρ * V(s)^2] * [(ε ^3) / ( 1 - ... |
Problem Statement: How do I control the Calculation Execution Rate of a Spreadsheet? | Solution: On the Parameters Tab of the spreadsheet, there is a Dynamic Execution frame (top right corner). There are three check boxes in that frame which control when will the Spreadsheet be called for execution. You have the option to execute the spreadsheet
Before Pressure-Flow Step
After Pressure-Flow Step
Each Com... |
Problem Statement: How do I get transport property data for the shell and tube side fluids as a function of the conditions in my heating and cooling curves in my heat exchanger? | Solution: The Property Table utility can be used to do this. You'll need one utility for the shell side and one utility for the tube side. The property table takes the composition of the stream and flashes at the conditions you specify. You can specify the range of temperature and pressure that you see in your heat exc... |
Problem Statement: What command line switches can I use with HYSYS? | Solution: These are all case insensitive.
Command
Function
/regserver
registers HYSYS for OLE Automation
/unregserver
unregisters HYSYS
/noregserver
skips registration (which is otherwise always done silently)
/BuildComselIndexFile
builds comsel.idx
/p<prefs filename>
sets preference file to be used
/s<script filename>... |
Problem Statement: What does the Prevent Temperature Cross in Depressuring utility? | Solution: This feature is intended to balance the heat duties for two sections inside the heat zones to prevent the temperature cross. The heat transfer area factors between the two sections are automatically adjusted based on heat duties. In practical terms, it is designed to prevent a temperature cross between the fl... |
Problem Statement: When modeling a Heat Exchanger in Dynamic Rating, is using Ft=1 a good approach? | Solution: When using the Dynamic Rating mode, the calculation mode is an integratedSolution, Aspen HYSYS splits the calculations among the heat exchanger and that's what it makes this mode more rigorous. In that way, Aspen HYSYS doesn't report the Ft correction factor, which is calculated as a function of the Number of... |
Problem Statement: Why do I still get a warning about Not Enough Information for Pipe Calculation even when all the dimensions of the pipe segment have been specified? | Solution: The most likely cause is that you also need to specify some information about the heat transfer for the pipe. Check that your information supplied includes the ambient temperature.
Keywords: Pipe segment, not enough information, calculation
References: None |
Problem Statement: I am trying to add 'Methane' to my case, but when I type 'M', methane disappears off the component list. What should I do? | Solution: Depending on which list you are searching through, 'Methane' has a SimName of 'Methane', a FullName/Synonym of 'C1', and a Formula of CH4. Methane will only appear in the list when you type 'M' if the SimName radio button is On.
Keywords: component, add
References: None |
Problem Statement: My Column indicates a yellow status and a message saying High Liquid Level on Stages, what does that mean? | Solution: The liquid flow off any single tray is calculated using the Francis Weir equation:
LiqFlow = const LiqDensity WeirLength * [(Height of Liquid above weir)^2]
If the tray section weir length is too small, or the liquid flow down the column becomes too high, liquid starts to accumulate on the tray till the Heigh... |
Problem Statement: Why I cannot change or edit the strip chart for the Depressuring Utility? | Solution: In order to:
Change the sampling interval
Remove variables from strip chart
Add variables to the strip chart
then one must either create a new strip chart with the desired attributes or modify an existing chart then re-run the depressuring utility. Any strip charts or variables added AFTER running the utility... |
Problem Statement: Can I view all of the notes in my simulation in one place? | Solution: Beginning with HYSYS 3.0, all the user notes contained in a case can now be viewed from the Notes Manager dialog. The Notes Manager simplifies the search for notes written individual Unit Operations and Streams. The Notes Manager has advanced searching capabilities. The user can search through all the notes t... |
Problem Statement: What is the difference between HYSYS Upstream R2 and HYSYS Upstream R3 license? | Solution: The only difference between them is that with R2 you have access to black oil, but with R3 you DO NOT. If you have both in your machine it will try R2 first. Aspen HYSYS V7.3 can use either of them.
Keywords: HYSYS Upstream R2, HYSYS Upstream R3
References: None |
Problem Statement: My controller says INIT what does this mean? | Solution: The INIT box usually indicates that the OP value displayed on the controller has been back-calculated either from another controller or a selector block. The OP value is determined based on the Kc term and the PV range specifed on the controller.
A controller can show INIT under two circumstances:
1. Th... |
Problem Statement: How do I add a new subflowsheet operation to my case using Automation? | Solution: The VBA procedure below (run this from Excel VBA) illustrates how to do this. The key lines are
Set hyNewTemplate = hyFlwSht.Operations.Add(strNewFSName, TemplateOp) hyNewTemplate.LoadTemplate
Set hyFlwSht = hyNewTemplate.OwnedFlowsheet
Where hyNewTemplate is declared to be of type TemplateOp and hyFlwSht is ... |
Problem Statement: What is the Acceleration factor on the Integrator window General tab? | Solution: The Acceleration factor is a way to increase the speed of the integration, thus speeding up the model. This is done through multiplying the acceleration factor by the step size to come up with the true step size used by the integrator. This is to say that increasing the acceleration factor above 1 is equivila... |
Problem Statement: My case used to use the Amines PP but I have changed it to something else and it's still asking for an Amines license. Why? | Solution: This is a bug in HYSYS 2.x that does not update the license requirement when you've changed from the Amines property package to something else.
The work around for this is:
Open the case, select all the objects in the PFD and export them to a file. Then, create a new case (with the same components & another P... |
Problem Statement: Where can I find the Properties Classes that are described in the Aspen HYSYS Thermodynamics COM Interface | Solution: If you need to program for COMThermo interface the objects are not available in the standard a??HYSYS 7.3 Type Librarya??.A You need to load a separate library.
Here is a list of the most common libraries mentioned in the reference guide:
Library Name:
Keywords: COMThermo, Library,
References: Guide? |
Problem Statement: How do I enter my distillation data ASTM D5236 in Aspen HYSYS? | Solution: Aspen HYSYS does not currently support D5236 standard. Aspen HYSYS does all calculations on a TBP basis in the Oil Manager. So, what is recommended to do is to find a software to convert D5236 into TBP or other standards which HYSYS can accept.
Another suggestion is that you review the testing procedure for y... |
Problem Statement: How can I add component molar flows to a WorkSheet? | Solution: Make sure the WorkSheet that you want to add to is open and has focus. Choose the WorkBook option from the Menu Bar and then choose Edit Page. From the Edit Page view choose the Add button. From the Variable Navigator view that appears choose the Variable you want to add to the WorkSheet, in this case Compone... |
Problem Statement: What do the Real Time and Real Time factor cells represent (on the Integrator window, General Tab) ? | Solution: If the the Real Time check box is checked it forces Hysys to run the model at real time, so one minute of the simulation time will correspond to one minute of real life.
The Real time factor cell is a measure of how fast the model is running and it is a factor between the simulation time and real time. So the... |
Problem Statement: The value of a user property (defined in the ‘User Properties’ folder) is not showing up in the Properties tab of some streams. | Solution: There may be several reasons for this occurrence. First, make sure that the referred property is activated for all streams in the flowsheet (this can be done accessing the Correlation Manager). Then, check the parameter Min. Def. Comp. (%) in the user-property tab in the Properties environment:
This parameter... |
Problem Statement: How do I get my reactive distillation column to converge? | Solution: If you are using the Sparse Continuation solver there are two things to quickly try.
Change from Rigorous to Pure on the 2/3 Phase page of the Parameters tab in the column view. When you treat the second liquid phase as Pure using the 3-phase solver, it allows simplification of the equilibrium calculations by... |
Problem Statement: How do I resolve an unsuccessful DBR PVT Pro Exchange Package setup when using Windows 7? | Solution: Fix the registry error on the 64-bit machine, follow this steps.
1. Open the registry by opening the start menu and typing regedit in the Search programs and files field
2. Allow the program to make changes to the registry (requires administrative access)
3. Locate the key HKEY_LOCAL_MACHINE\SOFTWARE\Wow643... |
Problem Statement: When I get the message saying: Error: Project evaluation failed in my trace Window what do I do? | Solution: This error is usually seen when you can get into the Design Tab, and you can use 'Check Design All Items' but when you go to run the Design Phase, you obtain the following error: *** Error: Project evaluation failed
You will need to check the following two items:
Ensure that your picasso.ini file (in the same... |
Problem Statement: What are the Product Block and Feeder Block buttons on the Dynamics Tab of a Stream? | Solution: A stream which has only one unit operation attached to it is called a flowsheet boundary stream. If a material stream is a flowsheet boundary stream, a Feeder block or Product block button is displayed in the Dynamics tab. A flowsheet boundary stream can be the feed or product of the model. Depending on wheth... |
Problem Statement: Why, after interpreting Aspen HYSYS LNG multi-heat exchanging streams in Aspen Energy Analyzer (AEA), are the composite curves and/or HX-network optimization results different from those in Aspen HYSYS LNG? | Solution: When there is a pure component/azeotropic stream with a long phase change region and high pressure variations in the multi-heat exchanging streams of a plate fin exchanger, the Aspen HYSYS LNG unit operation could be used to generate composite results. However, after interpreting these streams in Aspen Energy... |
Problem Statement: When I right click on a stream, I see the option Publish Stream. What is this? | Solution: Multiple HYSYS Cases can now be linked across multiple machines on a LAN or WAN. This is accomplished by linking the appropriate streams in a case with the streams of other cases. These links can be Live which means changes in the source stream are immediately and automatically transferred to the destination ... |
Problem Statement: Why does the Liq. Peak Flow display as empty in the Depressuring Utility? | Solution: The Depressuring Utility can be used to simulate the depressurisation of gas, gas-liquid filled vessels, pipelines and systems with several connected vessels or piping volumes depressuring through a single valve.
Keywords: Liq. Peak Flow, Depressuring, Liquid Flow Equation
References: s to vessel in this guid... |
Problem Statement: How does the split feeds option for the column operation in Aspen HYSYS work? | Solution: When you double click on the column, the Flowsheet page of the column property view will contain the checkbox which will allow you to split feeds. The checkbox may show up on the Connections page, depending on whether you are running a column based on one of our templates (where you will see a diagram) or whe... |
Problem Statement: How can I apply 'show table' option for all the streams? | Solution: You can select one stream and press 'shift' key from the keyboard and select the other streams of interest.
Once all the desired streams are selected, you can right click and pick 'show table'
Keywords:
References: None |
Problem Statement: How to find Henry coefficients and calculate the Henry constants. | Solution: Aspen HYSYS presents the Henry constant on the binary coefficient tab in the similation basis environment [Fluid Package | View | Binary Coeffs]. It is slightly confusing to read when you change the order of components [we recommend adding your non-condensable components first and then your condensable compon... |
Problem Statement: I am increasing scales on constraints to beyond the desired tolerance for the optimizer to find a feasible path. How do I ensure the optimizer meets my desired tolerances now that I increased the scales? | Solution: It appears as though it is sometimes necessary to increase the scales on constraints to beyond the desired tolerance in order for the optimizer to be able to find the feasible path. What can be done to ensure that the optimizer will be able to meet your desired tolerances when you are forced to increase scale... |
Problem Statement: HYSYS shows a tube or a shell outlet temperature that is different than what STX shows when STX is linked to HYSYS and it is on Rating mode. Pressure drops for both sides are transferred to STX as zero during the iterations when it is deleted on Design\ Parameters page in HYSYS. | Solution: When outlet pressure is not specified in HYSYS, the process conditions sent to STX are all based on inlet conditions. HYSYS then takes the calculated duty and pressure drop and re-calculates the temperature, in essence putting an isenthalpic valve after a zero pressure drop exchanger. The STX outlet screen sh... |
Problem Statement: What does the content of the bracket mean in NBP[0] or NBP[2] etc? | Solution: Hypothetical components generated by the Oil Characterisation function in HYSYS are named as follows:
NBP[x]y
(E.g. NBP[0]28)
x is just a marker to indicate which oil blend the hypo belongs to. For example if in the Oil Characterisation Environment you set up two blends then the hypos belonging to the first b... |
Problem Statement: I have a palm pilot and a portable computer with only 1 port. How do I run Hysys with a standalone (green) key? | Solution: You have the following options:
If you have a HYSYS key on the same physical COM port as the Palm Sync Cradle, the following have been successful:
Place the Hotsync Manager in manual mode (via right-click, Setup, General Tab). This will close the Hotsync Manager and allow HYSYS to use the COM port. When you n... |
Problem Statement: How can I copy all the data from one stream to another on my flowsheet, using OLE? | Solution: The simplest means of doing this is to use code like:
Dim SourceStream As HYSYS.ProcessStream
Dim TargetStream As HYSYS.ProcessStream
'.... Need to establish objects for our streams here ....
TargetStream.SpecifyAsFluid SourceStream.DuplicateFluid
This will specify T, P and molar flow in the Target Stream reg... |
Problem Statement: How do you enter the tube length and number of tubes for a U-tube exchanger in Aspen HYSYS? | Solution: The number of U Tubes specified should be the ACTUAL number of U-tubes, NOT the number of holes in the tubesheet (which is 2x the number of tubes).
The tube length entered should be the total length of the U-tube, including the U bend.
Keywords: u-tube, u tube, beu
References: None |
Problem Statement: How do I change default K values (Distribution coefficients) displayed on the worksheet tab for a given stream? | Solution: On the simulation basis manager go to the fluid package tab, open/view the fluid package in which you want the distribution coefficients to be changed.
Go to tabular tab and enable tabular properties.
Go to options branch and select the checkbox of the property you want to modify
Finally go to information bra... |
Problem Statement: Why does the Icarus cost engine increase the number of plates for a column imported from a simulation? | Solution: Icarus increases the number of plates if tray efficiencies are not specified in the simulation. ]
When this happens, the Icarus cost engine will assume the default efficiency specified in Process Design ->Design Criteria, and the default is 0.6. (The cost engine will calculate the Actual No. of stages = No. o... |
Problem Statement: Tips for running Gas Pipe in Aspen HYSYS Dynamics | Solution: For simplicity and more pressure drop correlations, it is recommended to use Aspen HYSYS pipe segment. The CGP unit operation is primarily designed for transient calculations with streams. Steady state calculations have been implemented primarily for initialization of the Pipe State prior to transient calcula... |
Problem Statement: How do I enable a User Variable on all streams / operations? | Solution: In order to enable a user variable on all streams / operations without going through each stream / operation individually, go to the Attributes tab on the User Variable editing window of the User Variable. (If no tabs are visible, click the downward pointing green arrow at the top right hand corner of the win... |
Problem Statement: How is the Latent Heat of Vaporization calculated in Aspen HYSYS? | Solution: The Latent Heat of Vaporization of a pure component is defined as the molar/mass enthalpy change occurred when it changes state from a saturated liquid to a saturated vapor, at constant pressure. In Aspen HYSYS, the Heat of Vaporization of a mixture is defined as the enthalpy difference between the bubble poi... |
Problem Statement: I have a simulation file which seems to be converged. However, Aspen HYSYS still displays error message(s) indicating Correlation Recall problems. What should I do? | Solution: The correlation recall problem can be eliminated simply via the correlation manager. From the top level menu, select Tools | Correlation Manager. First, look at the Messages tab to find out what Aspen HYSYS is complaining about. In the attached image file, Correlation recall problems.TIF, you can see, as an e... |
Problem Statement: How do I copy text from one PFD to another? | Solution: If your text is only one line long, this is easy. Just open the text box in the PFD you want to copy from and select the text, press Ctrl-C (for copy). Close the window and load the case (or PFD) you want to copy to. Insert a text box and simply hit Ctrl-V (for paste) inside the box.
If your text is multiple ... |
Problem Statement: How do I choose between the Li-Mather and Kent-Eisenberg Models for the Amines Package? | Solution: The creators of the Amines property package, DBR, have the following recommendations:
The Li-Mather model is recommended to be used for two amine systems and/or systems which are expected to fall outside the operating ranges recommended in the manual.
The Kent-Eisenberg model is recommended for single amine s... |
Problem Statement: How do I add components in a HYSYS case? How do I view fluid properties? | Solution: Please see attached document.
Keywords: components; fluid properties
References: None |
Problem Statement: A Process Simulator File (PSF) contains both process and physical property data that enables data generated by a program (normally a process simulator) to be transferred to an Exchanger Design and Rating (EDR) program. This knowledge base article describes the steps to create a PSF in Aspen HYSYS. | Solution: Attached is an extension which generates Aspen Exchanger Design & Rating (EDR) process input (PSF) files from an Aspen HYSYS simulation case that contains heat exchanger unit operations. To use this utility, you need only have Aspen HYSYS installed.
The procedure to create a PSF file from Aspen HYSYS is as fo... |
Problem Statement: How can I make a customized unit set as the default unit set? | Solution: Select the unit set and save it with a preference file.
For example, assume that you created a unit set of your own from cloning a HYSYS default unit set, changed the temperature unit to from degree C to degree K and left the rest unchanged. You named the unit set as My Unit Set. Whenever you open a HYSYS fil... |
Problem Statement: How do I keep the PFD window in HYSYS maximized? When I open a Stream or Unit Operation, the PFD shrinks. | Solution: In HYSYS versions 2.4.2 and earlier, there was a limitation with having multiple maximized windows open at the same time. This has been fixed for HYSYS 3.0 and newer versions.
The workaround in HYSYS 2.4.2 and earlier versions is to grab the corner of the PFD and 'stretch' it to the desired size. Once this is... |
Problem Statement: What is an MPC controller? | Solution: Model Predictive Control (MPC) refers to a class of algorithms that compute a sequence of manipulated variable adjustments in order to optimize the future behaviour of a plant. A typical MPC has the following capabilities:
1. Capable of handling multivariable systems with process interactions.
2. Encapsulates... |
Problem Statement: How can I get vapor pressure of a stream at stream temperature and pressure? | Solution: You can not calculate a vapor pressure at a Temperature and a Pressure. You can get vapor pressure only at a temperature. Because vapor pressure itself is the pressure at a particular temperature the liquid starts boiling.
The calculation procedure is simple.
Step 1: Delete the pressure of the stream (if ... |
Problem Statement: Why does the LNG temperature cross occur even though Auto Prevent Temp. Cross option is checked in Aspen HYSYS Dynamics? | Solution: To use the function of Auto Prevent Temp Cross, it's suggested to specify at least 10 zones to stabilize the Temperature/flow (see Aspen HYSYS manual Unit Operation Guide). As a thumb rule you can have at least one zone for every 15 deg C change in temperature. If you still find instability issues, you can in... |
Problem Statement: How does ICARUS calculate Pipe Testing? | Solution: Pipe testing is a function of the number of fittings and valves, and whether the pipe itself is jacketed, not jacketed, or lined or not lined.
It is also a function of the pipe length and diameter.
The basis equation is as follows:
CONSTANT = 4 by default
if pipe is jacketed or lined, then the CONSTANT = 20
P... |
Problem Statement: When I print my PFD, a bunch of overlapped letters are shown in the bottom of the sheet, how can I take them away? | Solution: This might be because the path to the file in your machine is extremely long, so the letters could overlap and it's not going to look good as you can see below:
There are two ways to take this away:
1. As this is caused by the large path in your machine in which the file was saved, you can try to save it in... |
Problem Statement: How can I enter Basic and Detail Engineering as a lump sum cost? | Solution: If you want the basic engineering going to one contractor, you will have to set up workforces under Engineering Workforce - By Discipline.
First, give each workforce a number. Here is an example:
Once you set up those workforces, then go back into Engineering Workforce - By phase, and specify the workforce ... |
Problem Statement: Where can I find I/O information in my output report? | Solution: The I/O information is located in the .CCP report in the section called MATERIAL AND MANPOWER SUMMARY - INSTRUMENTATION.
Remember, you need to specify a digital control center (DDCTL) (Process Control - CTL) in order to get I/O counts.
Keywords: I/O, ccp, material and manpower summary - instrumentation, i/o, ... |
Problem Statement: How can I merge multiple HYSYS cases into one case? | Solution: Pick one case that you want to be the main case.
Open one of the other cases and convert them to a template (Simulation menu, Main Properties option, Convert to Template; you can find more information about this process in the User's Guide, chapter 2).
Convert the other case(s) to templates.
Open the main cas... |
Problem Statement: How do I add an annotation to a PFD? | Solution: A? Use the letter A on the PFD toolbar to enter Annotation.
A? A Text Box will appear. You can enter the desired text.
A? Press OK key once you finish entering the Annotation.
A? To edit the annotation, right-click on the typed annotation to pick view properties.
A? ... |
Problem Statement: When I click on an item such as a stream on my PFD, I get a Hysys message of CLIPBOARD OPERATION FAILED or CLIPBORAD COPY IS NOT IMPLEMENTED. Why? | Solution: Typically, this message appears when a copy/paste function has failed.
However, in the first case (CLIPBOARD OPERATION FAILED) it was found that the source of the problem was a conflict between Aspen HYSYS and the software iFinger French-English auto-dictionary of Hachette-Oxford. The iFinger also conflicts w... |
Problem Statement: How can I calculate a stream Dew or Bubble Point in Dynamics? | Solution: In steady state this could be easily accomplished using a Balance operation - however this is not possible in Dynamic operation.
In the attached case the mixer operation has a User Variable (Design Tab ... User Variables page ...) that calculates the stream temperature if it were flashed at the same pressure ... |
Problem Statement: Can I output my PFD to AutoCAD? | Solution: Yes. This can be done by right clicking on the PFD and choosing Print PFD to File and Print to DXF File. To select the information to be printed to the DXF file, first select Setup DXF. By default, all the information is selected. The DXF output is the information in the flowsheet on the currently displayed P... |
Problem Statement: What does Ice Forms First mean? | Solution: It means that HYSYS predicts that ice will form before the formation of hydrate. When this is the case, HYSYS will not report a hydrate formation temperature.
Keywords: ice form first, hydrate
References: None |
Problem Statement: How to calculate pipe segment flow rate in Aspen HYSYS and Aspen Hydraulics by specifying inlet and outlet pressure. | Solution: 1. Calculate flow rate in the Aspen HYSYS main flowsheet.
In Aspen HYSYS, Pipe Segment contains four calculation modes: Pressure Drop, Length, Flow and Diameter. In order to calculate flow rate, we need to provide:
a. Pipe Geometry: pipe length and diameter
b. Heat transfer information
c. Inlet... |
Problem Statement: How do I prevent the error message Your Preference File is out of date or corrupted. It has been reset. | Solution: If you have multiple versions of Aspen HYSYS installed in your computer this could cause the corruption of one of your files for one version. If this is preventing you from using HYSYS without crashing you can repair it by going to your preference folder, located at: C:\Users\#My User#\AppData\Roaming\Aspen... |
Problem Statement: How do I access gas properties correlation data from VBA code? | Solution: The stream gas properties correlation values can be accessed by the function called GetCorrelationValue(parameters).The parameter names are those shown in the correlation picker table as shown below. This code is applicable for Aspen HYSYS V7.2 and higher.
The code segment to access the gas properties correla... |
Problem Statement: How do I enter ASTM D7169 in Aspen HYSYS Oil Manager or in Aspen HYSYS Petroleum Refining? | Solution: This test method extends the applicability of simulated distillation to samples that do not elute completely from the chromatographic system. This test method is used to determine the boiling point distribution through a temperature
of 720C. This temperature corresponds to the elution of n-C100.
Oil Manager... |
Problem Statement: For a 3-phase flow problem (oil, gas and water), does Aspen HYSYS calculate separate oil phase and aqeous phase velocities? | Solution: When a 3-phase correlation (Tulsa Unified Model 3-phase or OLGAS_3P) is used, separate oil phase and aqueous phase velocities are calculated. For all the other two-phase correlations, the oil and aqueous phase are combined into a single liquid phase.
Keywords: a 3-phase flow, pressure correlations, phase velo... |
Problem Statement: What would be the best approach to model a system with MEG, water and some light hydrocarbons in Aspen HYSYS? | Solution: When modelling a process in Aspen HYSYS the first and probably the most important step of the simulation process is the selection of the property package.
One of the limitations when selecting HYSYS Peng-Robinson (independently whether the pressure of the system is above 10 bar) is that there are some missing... |
Problem Statement: How does one select which streams are displayed in each Workbook tab? | Solution: To hide a stream:
1. Open up the Workbook and go to the tab of interest.
2. Right-click on the column pertaining to the desired stream and select Hide.
Alternatively:
1. Open up the Workbook and right click on the tab of interest.
2. Select the Order/Hide/Reveal menu option.
3. In the ensuing Order/Hide/Rev... |
Problem Statement: How to resolve Unable to load odbcji32.dll when trying to run interactive report | Solution: 1. Uninstall Microsoft Access Database Engine
On Windows 10 go to Settings > System > Apps & Features and search for access ...
Uninstall all versions of Microsoft Access Database Engine from your system.
On other systems use Uninstall or change Program or Repair or Remove Programs
Uninstall all versions of M... |
Problem Statement: How to set up a level controller on the shell side of a heat exchanger? | Solution: This is a workaround, and the the required steps are the following:
+ Add a spreadsheet to your simulation.
+Drag and drop the shell houldup liquid volume, from Dynamics tab, Holdup page to one cell in the spreadsheet.
+ Drag and drop the shell volume from Dynamics tab, Model page to another cell in the sprea... |
Problem Statement: How can I specify the Actuator parameters (rate, time constant, etc..) ? | Solution: These options appear on the Dynamics Tab, Actuator Page of the valve. However, you must have the HYSYS.Plant+ license enabled in order to modify these parameters. To enable the HYSYS.Plant+ license, go to the Options tab of the Integrator and select Use HYSYS.Plant+. The actuator parameters on the valve will ... |
Problem Statement: Can Aspen HYSYS be setup as a server application? | Solution: Yes, Aspen HYSYS can be setup as a server application but within certain constraints (as shown in the attached ApplicationServer.doc document).
As of Aspen HYSYS 2.4, we stopped officially supporting Aspen HYSYS installed on a network server (for all operating systems). The application was not developed nor... |
Problem Statement: How can I access the new Property Correlations in Aspen HYSYS 3.1+? | Solution: The .GetCorrelationValue method of the ProcessStream object can be used to access any stream property. It is the only way that the new stream properties added in HYSYS 3.1 (Dew point values, Wobbe Index etc.) can be accessed.
The .GetCorrelationValue method takes two parameters and returns a RealVariable:
Fun... |
Problem Statement: In an extension unit operation using the .Calculate method on the .ComponentMolarFraction property of a ProcessStream Realvariable will not work unless the array of values passed has been normalised. This was not the case in HYSYS versions prior to 3.0.1 | Solution: Normalise the array that is being passed. The code snippet below illustrates this.
Dim Comps As Variant
Dim hyProdStream As HYSYS.ProcessStream
Dim i As Integer
Dim Total As Integer
'...
'Get an array with which to fill with values
Comps = hyProdStream.ComponentMolarFraction.GetValues()
'Put some dummy value... |
Problem Statement: Do Bpcurves, GasProps, and Strmcopy extensions work with Aspen HYSYS V7.3 in Windows 7 64-bit environment? | Solution: Aspen HYSYS V7.3 is supported in Windows 7 64 bit machine, extensions should also work correctly. Aspen HYSYS is incompatible with Microsoft Office 64-bit.
Keywords: Windows 7, 64 bit, HYSYS V7.3
References: None |
Problem Statement: Is it possible to model a solid equilibrium in Aspen HYSYS? | Solution: Aspen HYSYS does not have the capability to predict the phase crystallization and there is not solid phase equilibrium data or methods inside of HYSYS that predict the behavior of a solid phase in the presence of other phases. This is why there are no solid with liquid, or gas or both equilibrium calculations... |
Problem Statement: How is the viscosity calculation made in the blend tab on the oil manager? | Solution: During blending, Aspen HYSYS internally combines all of the individual assay curves (TBP vs. weight percentage) and produces a single composite TBP curve. From this curve, Aspen HYSYS defines the hypocomponents and estimate their parameters such as Tc, Pc, MW, Accentricity, etc. The liquid viscosity coefficie... |
Problem Statement: Why does Aspen HYSYS (or any application) crash? | Solution: There are three general reasons why Aspen HYSYS (or any application) will crash.
1. Program bug.
2. Corrupt file.
3. Conflict with operating environment.
The user of the application must perform some basic diagnostic work to determine what the cause is of the crash which they are experiencing. When reporting ... |
Problem Statement: What is the difference between Straight and Relief side weir types? | Solution: There are two types of weirs available in Aspen HYSYS: straight and relief.
A relief weir lengthens the side weir without increasing the downcomer area. The relief weir sweeps back, then across the tray, enclosing some active area.
A straight weir follows the edge of the downcomer.
A relief weir is used... |
Problem Statement: In real separator ProSeparator correlations, what is the meaning of dm in Rossin Rammler Parameters? | Solution: The term dm is the mean particle size and it is related to d95, which is 95% of droplets are smaller than this diameter for the specified dispersion.
Keywords: Real separator, ProSeparator, Rossin Rammler Parameters
References: None |
Problem Statement: How do I convert the heat curve in the Heat Exchanger and Heater operations from a molar basis to a mass basis? | Solution: In order to generate a heat curve on a mass basis, you will need to create a Property Table utility according to the instructions provided below:
1. Select Tools | Utilities from the main menu and add a Property Table utility.
2. Choose the inlet stream to the Heater or the Heat Exchanger in the Property Tabl... |
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