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Problem Statement: The values of mass exergy reported for a stream are different than the ones the user is expecting. | Solution: This is most likely due to different reference conditions in the calculation. Even though for certain properties Aspen HYSYS uses 15 deg C (60 deg F) as the reference temperature, exergy uses by default a value of 25 deg. C. To change this, access the Correlation manager and set the desired values of temperat... |
Problem Statement: Which Fluid Package in Aspen HYSYS do I use to model a system with Methyl-Mercaptan and Ethyl-Mercaptan with a set of light hydrocarbons? | Solution: A significant amount of work has been conducted in exploring the Vapor-Liquid Equilibrium (VLE) data between Mercaptan and Hydrocarbon mixtures. Denyer et al (1949) studied the azeotropic effect of Mercaptan and Hydrocarbons and Lee et al (1978) explored VLE data for H2S and light Mercaptan binary systems.
Th... |
Problem Statement: How can I minimize some objective functions, while maximizing others in the same Optimizer problem? | Solution: The individual items of the objective function are included in the Derivative Analysis associated with the optimizer. Some items may be associated with cost and some with revenue. The differentiation of cost and revenue items are done by the parameter called “Price” providing positive or negative value. A neg... |
Problem Statement: What are the various password security features available in Aspen HYSYS? | Solution: 1. Flowsheet Locking
The user is able to lock the process flow diagram (PFD) or a sub flowsheet. While it is locked they will not be able to create or delete model objects or change the topology. The user will be able to add certain logical operations such as set and adjust and use the spreadsheet function.
I... |
Problem Statement: I have a 2 phase feed (a vapour phase and a 'water-containing' liquid phase) to my 3-phase separator. Why is Aspen HYSYS treating this liquid phase as a non-aqueous phase in my 3-phase separator? | Solution: By default (from version 7.1), for a liquid phase to be considered 'aqueous', EITHER of the two (2) conditions below has to be TRUE:
- If the mole fraction of the water is greater than 0.5 OR
- If the mole fraction of water is less than 0.5 but greater than the total hydrocarbon fracti... |
Problem Statement: Whenever I try to vary the composition of a stream in a Case Study, the “Input Composition for Stream” window pops up as I run the case, and even when I click on OK the composition is still not modified in the results of the analysis. How do I fix this? | Solution: To modify the composition of a stream through a case study, you must use a Spreadsheet.
1. Define your stream of interest (Temperature/Pressure/Vapor Fraction Flow and Composition) add the spreadsheet to the simulation.
2. Within the spreadsheet go to Spreadsheet tab and in any column (i.e. column B) ... |
Problem Statement: When you right click on an unit operation and select Print Datasheet, the datasheet preview shows that the unit set is different to the current unit set showed in the flowsheet and workbook. | Solution: The unit set used for the datasheet can be modified using the Format / Layout button.
The default unit set is <Current>. However, this can be customized only for printing purposes.
Keywords: print, datasheet, unit set
References: None |
Problem Statement: Why does reactor appear to be solved (“OK� status and exit streams blue) when it has not? | Solution: This is because Aspen HYSYS activates (by default) the ‘Act as a Separator When Cannot Solve' checkbox to operate the reactor as a simple 2 phase separator whenever the reactor is not solved. This checkbox is only available for Conversion Reactors, and can be deactivated if you want HYSYS to report ‘not s... |
Problem Statement: How to get transport properties (e.g. density, viscosity) from each tray in the column. | Solution: Transport Properties information for each tray comes under column performance tab.
Go to the column << performance << plots and select transport properties and say view table.
Keywords: Column, Tray , Transport Properties, Density, Viscosity, Performance, Plots
References: None |
Problem Statement: How do I set the default shutdown duration? | Solution: The default shutdown duration is determined by the combination of values for Minimum Lot Size and Process Time for Shutdowns in the table TDAT.
The Minimum Lot Size parameter should be set to the physical lower limit or the minimum volume that might be run between setups.
Process Time defines the amount of ti... |
Problem Statement: How to get Gas Properties in Hysys Workbook tab? | Solution: Gas Properties (and other property values in Correlation Manager) can be retrieved on Workbook tab by selecting the Calculator option from the workbook SetUp àSelect Variable(s) ForMain option. See the following snapshot for the location of the same.
Keywords: Workbook, Gas Property
References: None |
Problem Statement: What is the Off-Design Correction option inside the compressor? | Solution: Two parameters can be entered for performance curves: Design Temperature and Design Molecular Weight. A screenshot showing this addition within the compressor form is shown below:
When these are supplied, HYSYS corrects the characteristic curves to the equivalent/corrected curves at operating conditions. To... |
Problem Statement: I am converting a file from PROII to HYSYS. Where are the property packages defined in the PROII input file? | Solution: It is possible to use the PROII to HYSYS Convertor to change the simulation into a HYSYS file. Inside the PROII input file the property package is specified under the section entitled the Thermodynamic Data. An example from the PROII input file is found below:
THERMODYNAMIC DATA
METHOD SYSTEM=PR, TRANSPOR... |
Problem Statement: Why the lbf*ft/lbm units change back to ft when I choose them for the Head Units in a Compressor curve? | Solution: The automatically change of lbf*ft/lbm to ft units by HYSYS in the Head Units cell of a compressor is by design, and it is an expected behavior since they are essentially the same. It would be redundant to have these two units separately.
Let’s examine the head produced by a pressure difference of 50 lbf/ft... |
Problem Statement: Are there any tools available to help me decide which property package to use in my simulation? | Solution: New in Aspen HYSYS 2006, the Property Wizard is available from the fluid package window as shown in the figure below:
The Property Wizard can be used to generate a list of potential thermodynamic models based on some general process information provided by the user.
Note that detailed information for ... |
Problem Statement: How are Slug Length and Bubble Length defined in the Pipe Segment Slug Tool calculations? | Solution: For a given two phase system, 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 than the pipe length, then there is no slug flow in the pipe.
Keywords: slug ... |
Problem Statement: How do I model Wound Coil Exchanger using Aspen HYSYS? | Solution: Wound Coil heat exchangers (WCHEs) are required for a wide range of applications involving fluid treatment. They must support broad temperature and pressure ranges as well as single- and two-phase streams.
To model Wound Coil (or Spiral Wound) Heat Exchanger (WCHE) we use LNG unit operation in Aspen HYSYS, ... |
Problem Statement: Can Aspen HYSYS validate hydrate formation prediction when a free water phase is in equilibrium with a liquid hydrocarbon phase? | Solution: Liquid phase hydrate prediction is a known limitation in Aspen HYSYS. The Vapour model is currently deemed the most suitable model for predicting liquid phase hydrates. The liquid phase hydrate prediction results should be checked carefully and compared with literature or field data whenever possible.
Refer t... |
Problem Statement: How can I ignore or unignore a unit operation through automation? | Solution: Unit operations in HYSYS have the property .IsIgnored:
· .IsIgnored = True will ignore the unit operation
· .IsIgnored = False will unignore the unit operation
Attached is a sample Excel file with code to demonstrate how to do this. It can be used with an active HYSYS simulation.
Keywords:... |
Problem Statement: When using Aspen Properties for a HYSYS simulation, several questions arise regarding the possibilities, benefits and limitations.
· When should I create an Aspen Properties package from HYSYS?
· When should I create it in Aspen Properties and import it?
· Should I customize i... | Solution: Aspen Properties is commonly used to customize property packages: estimating data, adding non-databank components, performing regressions of parameters, etc. It also contains all of the most important databanks of pure components, allowing the creating of robust property packages for simulation.
Since Aspen P... |
Problem Statement: How can I modify stream names for internal streams? | Solution: By default, HYSYS takes the name of the external stream and automatically re-name the internal stream with the name of the external stream attached.
If you want to modify the name of the internal stream so you have different names for internal and external streams (one name inside the column environment and... |
Problem Statement: On the PSV Line Sizing results how are the Maximum DP In Line and Out line values calculated? | Solution: By default the Maximum DP In Line is calculated as 3% of Set Pressure. This can be modified in the Line Sizing Limit Settings editor. Click on the Constraint Setting button in the Line Sizing tab to customize this option.
According to the Default Valve Settings, the Out Line result is calculated as 10% of Se... |
Problem Statement: Why are the Print and Print Snapshot options disabled in the Aspen HYSYS File / Print menu? | Solution: This behavior only occurs when trying to print an input form/window when working inside the Safety Analysis environment. The reason of this is that the Safety Analysis includes the capability to print out all the information present in the input and result windows through the Documentation Builder and/or the ... |
Problem Statement: Can I use Critical Properties Utility with Sour PR fluid package?
I see the following message “Utility Critical Properties is not available with the property package being used.� | Solution: The Critical Properties Utility was written based only on Peng Robinson. In part this is because only the PR equation of state applies a correction for the molecular attraction term which involves the acentric factor. Sour PR is actually a 2-part property package: the vapor is modeled by PR but the liquid is ... |
Problem Statement: Customer is not able to load any Hysys model that uses PIPESIMLINK. Will Aspen HYSYS Upstream license enable the PIPESIM functionality? | Solution: Aspen HYSYS Upstream license alone will not enable the PIPESIM functionality on any version of Hysys. The following two licenses are required for PIPESIM functionality in Hysys V7.2 and V7.3 :
1. Upstream RN_PML_HYSUPSTRM_R3 license from AspenTech
2. PIPESIM license which has to be purchased from Schlumberg... |
Problem Statement: How do I use automation to add or remove components from a simulation? | Solution: To modify the components used in a given case, you must either access a specific component list, or the component list associated with a specific fluid package:
Set myBasisManager = myCase.BasisManager
Set myFluidPackage = myBasisManager.FluidPackages.Item(FP_Name)
myFluidPackage.Components.Add <Component_N... |
Problem Statement: How to model a Rupture disc in HYSYS Dynamics. | Solution: There is no direct way to model a Rupture disc in HYSYS. User can model a Rupture disc using a Relief Valve in HYSYS.
1. Assign the Set pressure = Full open pressure = desired rupture pressure.
2. Specify an Orifice Area and make the Discharge Coefficient = 0.62 for the Rupture disc.
3. Go to Dynamics tab and... |
Problem Statement: Can Pipe Segment operation be used to calculate Pressure drop in slurry line? | Solution: Most of the pipe correlations for the Pipe Segment (e.g. Beggs & Brill and so on) were developed for 2-phase flow (vapour-liquid) and a few (e.g. OLGAS 3P) for 3-phase flow (vapour-light liquid-heavy liquid). But none of the pipe correlations in the Aspen HYSYS Pipe Segment will give reliable results when sol... |
Problem Statement: How to Ignore the Subflowsheet? | Solution: The Ignore check box option is available on the Parameters Tab.
To ignore a subflowsheet, double click on the Subflowsheet and go to Parameters TAB and check the Ignored check box.
Keywords: Subflowsheet, Ignore, check, box
References: None |
Problem Statement: Sometimes, we model two fluids using PIPESYS under similar Reynolds Numbers, but the the pressure drops are significantly different. | Solution: The explanation lies in the hydraulic treatment of flow pattern in PIPESYS. After the units are calculated, you can get the flow pattern on Results tab | Detail datasheet. PIPESYS only recognizes laminar and turbulent flow for hydraulic calculations. If one of your fluid is in laminar and the other is in tran... |
Problem Statement: When the simulation includes a relatively large number of Adjust operations, it is often useful to quickly diagnose the status of these blocks, as their | Solution: is iterative (prone to convergence issues). Also, Adjust blocks may be used only sporadically to determine normal desired conditions (and be subsequently ignored).Solution
1. Using the Adjust manager.
Assuming that this is a problem relevant when you have multiple Adjust blocks, you can choose ‘Simultaneous... |
Problem Statement: Why can I not specify certain shell types using the Aspen HYSYS heat exchanger model? | Solution: TEMA shell types G, H, X, J and K are currently unavailable because the required models have not yet been implemented in Aspen HYSYS. If a user attempts to select one of the aforementioned shell types, the following message will appear in the trace window:
G, H, X, J, K shell types are not supported yet.
This... |
Problem Statement: How do I decide if I should select a direct action or reverse action on the controller interface? | Solution: When the setpoint value (SV) is fixed, the relationship between process value (PV) and manipulated Output Value (MV) can be direct action or reverse action as shown below and select accordingly.
Direct action: The controller action in which the MV increases as the process variable increases or decreases as PV... |
Problem Statement: I want to adjust the solubility of my components for my simulation. This is accomplished in SimSci Pro/II by adjusting the Henry's Law Constant. Does Aspen HYSYS have a compatible method to accomplish this? | Solution: Aspen HYSYS offers you the possibility to do it with the tabular options in the property fluid package.
1. In your simulation add the components you want to adjust its solubility.
2. Go to the Fluid Packages folder, select the package you are working with and go to the Tabular tab. In this, toggle “En... |
Problem Statement: Extension source code built in VB6 is migrated to .Net and has been successfully complied to generate two dll files (name.dll and interop.Hysys.dll)
The extension, however, does not register successfully because it could not load the file or assembly Interop.HYSYS.dll
See error below.
Attempting to ... | Solution: This usually stems from a problem that Windows will search for dependencies in the path of the executable rather than the path of the target dll when registering a dll.
TheSolution is to copy the Interop.HYSYS.dll next to regextn.exe, which would be in C:\Program Files (x86)\AspenTech\Aspen HYSYS V#.#\, possi... |
Problem Statement: What is the application of the Feed Basis option of Carry Over Model in the 3 phase Separator? | Solution: The Feed Basis carry over model is applicable when the user intends to specify or knows how much fraction of a particular phase of the separator inlet feed stream is carried over in another phase of the separator product stream.
Refer to the attached simulation created to illustrate this.
10% of the light l... |
Problem Statement: The Quick Size utility in the Separator unit operation (Rating tab, Sizing menu) is a fast method for sizing a converged separator based on the criteria as stated in:
Evans, Frank L., Equipment Design Handbook for refineries and chemical plants - Volume 2, 2nd Edition, p. 154, Gulf Publis... | Solution: Use the Vessel Sizing utility from Equipment Design (accessible from the Navigation pane). A new vessel sizing case must be created, and the converged separator unit operation attached. The user will be able to specify the sizing criteria, construction and costing information from this utility. See image snap... |
Problem Statement: Reports created by Report Manager can be printed as pdf's. However, users can also export the results and format to Excel. | Solution: 1) Open Report Manager and create report with desired Datasheets.
2) Enable the option ‘Text to File’ and click ‘Preview…’
3) In ‘Format’, configure how you would like the data to be displayed.
4) Check the format in ‘Preview…’ of the previous menu.
5) Choose ‘Print to File…’ and sav... |
Problem Statement: How do I avoid mass imbalance in Depressuring utility? | Solution: Mass imbalances when using Dynamic Depressuring utility with a zero liquid or vapor flow is a known issue. One way you can reduce the imbalance by using small time step size (~0.01 sec).
Using a greater step size, the vessel appears to relief more mass than it should actually relieve. Depressuring systems inv... |
Problem Statement: The labels for all or some objects in the flowsheet have all disappeared. How can I restore them? | Solution: The labels may have been hidden or deleted, accidentally or on purpose, by the user or other users sharing the file. The following procedures should be able to restore labels in most cases:
Consider this example, where all labels are hidden:
1-Select all objects in the flowsheet (or just the ones with hid... |
Problem Statement: How to use the Script Manager. | Solution: 1. Find the script from the ribbon tab “Customize”.
2. Open the Script Manager. If you want to create a script, use Directories to locate the folder you want to store the script, and then press “New”. Be careful, if you are window 7 user, some of the directory is only for system administrator, and you... |
Problem Statement: When a gauge pressure is defined in a Set logical operation a warning message appears: Non-unity multipliers cannot be used with units that have offsets from the internal units used by HYSYS. This includes all forms of temperature and gauge pressure units as well as any user defined units that have n... | Solution: The normal pressure gauge units are not allowed to be used in the set block. If it were possible, every time a user changed the units of pressure, the results of the simulation would change without any warning.
Users can create their own pressure units by clicking on pressure units in the Units Of Measure (F... |
Problem Statement: List the Flow Regime code convention that Aspen HYSYS Upstream uses for Pipe Segments | Solution: The following table lists the Flow Regime code convention that Aspen HYSYS Upstream uses for Pipe Segments.
H----V Horizontal vapour only
H----L Horizontal liquid only
HB---- Horizontal bubble flow
H-A--- Horizontal annular flow
H--G-- Horizontal slug flow
H---S- Horizontal stratified flow
H-AG-- Horiz... |
Problem Statement: What are the variables passed from Aspen HYSYS and retrieved from OLGA using the Aspen HYSYS-OLGA Link extension? | Solution: The Link extension passes a few key variables for the connected Inlet and Outlet streams.
For all streams, the temperature, pressure, gas fraction, and water fraction are passed to OLGA.
Additionally the total mass flow will be passed to SOURCE connections. In the case of a SOURCE connection, OLGA will use th... |
Problem Statement: Why the pressure drop is decreasing in my system with a Swage instead of increasing | Solution: A smaller pressure drop in the system with a swage is because the pressure increases in your pipe is due to the diameter increases across the swages between the pipe segments of different sizes. Fluid flow across an expansion results in a decrease in fluid velocity and hence a recovery of velocity head as pre... |
Problem Statement: After applying Emergency Patch 133193, OLGAS-2P correlation is not working anymore in Pipesys extension in Hysys V7.3 | Solution: In order to use OLGAS-2P correlation in Pipesys extension, you will need to follow the procedure in the knowledgebaseSolution (ID:115126) to download the license file and add the environmental variable.
Keywords: OLGAS , PIPESYS
References: None |
Problem Statement: By default, the Workbook in Aspen HYSYS displays the composition using the basis mole fraction. How this basis can be changed to mass fraction? | Solution: In order to change the basis of the composition in the main case and sub-flowsheets, users can follow the procedure below:
1. Go to the Home menu and select Workbook.
2. Go to the Composition tab.
3. Check the button Include Sub-Flowsheets located on the bottom right side.
4. Select Setup ... |
Problem Statement: Why is the Net Positive Suction Head available (NPSHa) reported in the pump unit operation greater than zero for a saturated liquid at the pump inlet? | Solution: The NPSHa calculation is based on the ADDITION of a static pressure term AND velocity head term. The static pressure term is proportional to the difference of the static pressure and vapour pressure terms (i.e. zero for a saturated liquid).
However, the velocity head term is not zero and is proportional to th... |
Problem Statement: How do I make the utilities show up on a material report print out? | Solution: When adding a report datasheet, you must select the Utilities button from the filter option.
Then select the utility objects:
Keywords: Utilities, report, print out
References: None |
Problem Statement: Referring to the curve fitting equation from | Solution: ID 133788, I understand that if I plot Q^2 vs H for a fixed operating speed, I should get a straight line. However, it does not give me a straight line which makes me wonder that if the curve is fitted to the mentioned equation in HYSYS. Please explain.
Solution
The method of fitting used in HYSYS may not gua... |
Problem Statement: How are pool fire and jet fire defined? | Solution: Pool fire: In a vessel containing a liquid, when the liquid spills out and ignites.
Jet fire: In a vessel containing only a gas, if the flange leaks and the high pressure gas escapes and ignites.
Key Words
fire, types, definition
Keywords: None
References: None |
Problem Statement: Aspen HYSYS V7.3 does not solve exchanger using EDR with Input error 1124 The data input for E-Shell inlet nozzle loc. A problematic case file and solved case file is attached to show the problem. | Solution: It happens with E-shell and D-shell case files built prior to EDR V7.3 integrated in HYSYS. When you load the old HYSYS models in HYSYS V7.3 you will see the message Input error 1124 The data input for E-Shell inlet nozzle loc. if there is any inconsistency between the inlet nozzle location and the distance b... |
Problem Statement: When trying to access the Documentation Builder in the Safety Analysis environment, it does not work. What could be the reason? | Solution: The reason could be related to the MS Access version installed on your computer. When the user clicks on the Documentation Builder button, the COM call to open the .mdb files is fired. This step can fail with MS Office 2007 because we use a 2012 version of Microsoft Office.Interop dll and backwards compatibil... |
Problem Statement: How to do I include the vapor properties such as density and viscosity in a column profile report using the Plots Datablock? | Solution: By default, Aspen HYSYS has activated the report option only for light liquid properties. If you want to include the vapour properties, you need to add them. This can be done as follows:
1. Go to Column editor in Performance tab > Plots section. Highlight Transport Properties and Click on View Table...
   ... |
Problem Statement: Aspen HYSYS ActiveX: how to configure a user variable to apply a proportional ratio between component flows of different streams. | Solution: ThisSolution provides an example of how to link flowsheet variables in our simulation through a user variable, while applying some proportional criteria between them. In the example, the macro implemented will fix the component mass flow of the stream “2� as a proportion of the Ethylene mass flow present ... |
Problem Statement: Why are the critical temperature and pressure calculated by the Phase Envelope utility different from those calculated by the Critical Properties utility? | Solution: The two utilities use different algorithms and so discrepancies are expected between the two results.
The envelope is calculated on a dry basis, using the technique developed by Michelson and as a natural byproduct of theSolution sequence, the critical point is derived. Some special treatments are involved in... |
Problem Statement: How can I see Molecular weight , Density, Viscosity, Surface Tension and specific heat capacity for every stage in the column? | Solution: Procedure 1:
Double click on the column and click on Performance | Plots | Transport Properties | Select view table
It will display the transport properties listed above.
Procedure 2:
You can export the internal stream to the main environment and see the properties there.
Please follow theSolution below:
http... |
Problem Statement: How do you adjust the flowrate or the amine concentration in Makeup unit operation? | Solution: You can't adjust the amine concentration or amine flowrate using Adjust block because these variables are not exposed in Adjust block. However a workaround is available, by which you can access these variables.
If you create a HYSYS Spreadsheet, these variables can be dragged and dropped into the Spreadsheet,... |
Problem Statement: What is the Off-Design Correction option inside the compressor? | Solution: Two parameters can be entered for performance curves: Design Temperature and Design Molecular Weight. A screenshot showing this addition within the compressor form is shown below:
When these are supplied, HYSYS corrects the characteristic curves to the equivalent/corrected curves at operating conditions. To... |
Problem Statement: I am converting a file from PROII to HYSYS. Where are the property packages defined in the PROII input file? | Solution: It is possible to use the PROII to HYSYS Convertor to change the simulation into a HYSYS file. Inside the PROII input file the property package is specified under the section entitled the Thermodynamic Data. An example from the PROII input file is found below:
THERMODYNAMIC DATA
METHOD SYSTEM=PR, TRANSPOR... |
Problem Statement: Can I include several objective functions in the same optimization problem in Aspen HYSYS? | Solution: In the Original optimizer, the user can only select one objective function. With the Hyprotech SQP optimizer, multiple objective functions can be handled. This option requires the previous setup of a Derivative Analysis.
In the Objective function menu of this analysis, add ObjFunc as shown below.
Keywords: SQ... |
Problem Statement: Why do I see more wax deposits in a pipe when the inlet temperature increases? | Solution: There are two factors that can cause the wax deposition to increase with increasing temperature.
The first factor is that increasing temperature results in lower viscosity and higher diffusivity, both of which have the effect of increasing the mass transfer coefficient calculated using the equations inSoluti... |
Problem Statement: How to prevent the over-specified error when using the rigorous heat exchanger in Aspen HYSYS with vapour fraction specified. | Solution: When simulating the condenser/vaporizer with HYSYS methods (such as Simple Weighted), this calculates the heat overall transfer coefficient (UA). The calculated UA is based on specified outlet temperature or vapour fraction (VF =0, or 1). However, when the exchanger is linked with rigorous method using Exchan... |
Problem Statement: How to show replace the AspenTech logo with a custom logo on Aspen HYSYS reports. | Solution: By default Aspen HYSYS report file will show the AspenTech logo. However, it provides the feature to change the logo. To do that,
1. Open File|Options|, and then go to Report
2. Users can user “Select” button to load their own logo to replace Aspen Tech logo.
Users will have to make sure that the lo... |
Problem Statement: How is the relief load obtained in Safety Analysis in Aspen HYSYS? | Solution: Starting from Aspen HYSYS V8.3, user can use Safety Analysis to size PSVs in the process flowsheet. The PSV sizing requires relief load to be available. Currently, there are three ways to obtain the relief load:
1. Manual - User input relief load for sizing the PSV.
2.
Keywords: Relief Load, Safety Analysis
R... |
Problem Statement: I need to use the backdoor method for certain variables. How can I find out their monikers? | Solution: Some variables used in Aspen HYSYS are not directly exposed as an automation interface, such as the variables used in the Performance Table of a Heater or a LNG Exchanger. Those variables have not been fully “wrapped� and cannot be directly accessed through Automation. However, the backdoor method can be ... |
Problem Statement: Where can I change component efficiencies calculated by the Amine Package for a column in Aspen HYSYS? | Solution: Aspen HYSYS estimates the stage efficiency for CO2 and H2S based on the tray dimensions. When the internal column diameter, the outlet weir length and the outlet weir height are known the AMSIM property package can estimate the stage efficiency base on that mechanical tray dimensions.
Tray dimensions can be e... |
Problem Statement: How do I obtain the Heating Values and Wobbe Index of gas at normal conditions? | Solution: Aspen HYSYS gives the Heating Values and Wobbe Index at standard conditions (15 deg C and 1 atm). The users have the option to change the condition from 15 deg C to 0 deg C if the values are required at normal condition. This option is available in the correlation manager. The knowledge baseSolution ID 138937... |
Problem Statement: How to change the fluid package of a single or multiple components in Aspen HYSYS V8. | Solution: The procedure to change the fluid package is no longer trough right click on the items but you need to go Home Tab> Simulation> Fluid Package association. In there you will be able to set the default property package to use for each flowsheet.
If you want to only change the property package for some items, th... |
Problem Statement: In the Parameters page of the compressor, you can specify the curve input options as Multiple IGV (Inlet guide vanes). What does this option mean? | Solution: The Multiple IVG option allows you to provide multiple sets of curves in the Rating Page / IGV Curve Collection.
Each set of curves corresponds to one IGV position value.
The Curve IGV allows you to specify the inlet guide vane position that the entered curve set data is at (or for).
The Current IGV specifies... |
Problem Statement: A user characterized the same crude in both HYSYS (using Peng-Robinson fluid package) and AspenPlus (using Peng-Rob property method) respectively, then set up the column with the same configuration in both simulators.
For the same feeds, the user gets slightly different results.
Why can't I get the c... | Solution: Historially, a significant amount of development work went into the improvement of Peng-Robinson fluid package. One of the areas of such development work is the estimation of binary interaction parameters (BIPs). HYSYS estimate BIPs for crude hypo components based on boiling point and density. The estimated B... |
Problem Statement: How to hide/reveal streams from workbook table | Solution: Here are the steps you can follow to reveal all the streams' properties from workbook.
1. Open the work book by clicking “workbook” on the Home ribbon bar. Once you do that, HYSYS will show Workbook ribbon bar, and automatically bring you there.
2. Press the “Setup” on the right up corner to bring the Setup ... |
Problem Statement: What is the role played by the “PV Work Term Contribution” option for vessels in dynamics mode? | Solution: The attached document discusses the impact of the PV work term option by comparing its influence on the results delivered by the simulator to the ones returned by hand calculations. It is accompanied by the simulation file “PV.hsc” in version V7.3.
Keywords: PV work term, HYSYS Dynamics, work energy, irrevers... |
Problem Statement: Explanation of common run-time errors using the property ImportedVariable for a SpreadSheetCell class. | Solution: In Aspen HYSYS, a spreadsheet operation can be used to bind conditions of different streams and units by using the functionality of importing and exporting variables. Because it is an operation, variables are automatically updated. However, if we try to access the imported and exported variables through our V... |
Problem Statement: What is retrograde region and retrograde condensation? | Solution: For multicomponent gas mixtures, the cricondenbar (point N) and the cricondentherm (point M) represent the highest pressure and temperature respectively where both liquid and vapor phase exist together. The critical point (point C) is where the bubble point (0% vapor) and dew curve (100% vapor) meet. Then we ... |
Problem Statement: When importing a stream from one model to another, the following dialogue box is displayed:
The fluid package / template that is being imported contains different component data for a User Property that already exists in this case.
You have four options: [Create Local], [Updat... | Solution: Create Local - the imported component values of the user property is put into the property slate for the imported fluid package
Update - the existing user property will be updated with the all of the new data from the imported fluid package
Ignore - the old values for the existing ... |
Problem Statement: When a .csv file is imported into Aspen HYSYS petroleum assays then the stream associated with the csv assay reports 1.#Q000 for enthalpy, entropy and heat flow parameters. | Solution: The characterization feature allows the assay to be recut over a range of temperatures. With .csv files, only the data for a specific distribution of cuts are specified and there is not enough information inside the file for the assay to recut automatically. If the user experiences this error they will need t... |
Problem Statement: Why the standard gas flow does not match with the actual volume flow at standard conditions? | Solution: The following screenshot shows that the standard gas flow and actual volume at standard condition do not match.
Standard gas flow is based on the molar volume of an ideal gas at standard conditions. It is a direct conversion from the stream's molar flow rate, based on the following:
• Ideal Gas ... |
Problem Statement: In the Fire Semi-Dynamic Flash calculation method in safety analysis, how is the temperature difference between each of the flash iterations calculated? | Solution: When conducting a Semi-Dynamic Flash the user can edit the temperature difference between each flash iteration step. The parameters to edit the iteration steps is within the ‘edit flash table’
Within the edit flash table the user can edit the maximum iteration temperature and ‘# of flashes.’ The relieving tem... |
Problem Statement: How do I ensure my company logo appears correctly in the datasheet report? | Solution: The company logo can be included in the datasheet report as shown below.
The logo can be added via Files/Options/Reports. See the screenshot below.
The logo should be saved as 16 or 256 colour bitmap file. If this is saved as 24 bit bitmap then the logo will not appear correctly in the datasheet report.
Keywo... |
Problem Statement: In the Vessel Sizing utility how is the Total Length (reported under Performance tab | Sizing Results) of a vertical separator calculated? | Solution: The total length is calculated using one of two equations depending on the user specifications. In most situations these two equations should lead to the same length calculation.
Length = Diameter*L/D + 1/2*Diameter
-or-
Length = 1/4*Diameter + Demister Thickness + Inlet Nozzle To Demister + Sump To Inlet Noz... |
Problem Statement: Is it possible to adjust tray efficiencies with the Sparse Continuation Solver? | Solution: The Sparse Continuation Solver is not designed to handle stage/component efficiency. As a limitation of the solver, the tray efficiency is not taken into account by the Sparse Continuation Solver. You should work with a theoretical number of stages.
To work with efficiency tray and two liquid phases, please r... |
Problem Statement: When I input my assay data as D2886, the results do not represent my crude correctly. Why? | Solution: The API methods used by Aspen HYSYS to convert from D2887 to TBP have some limitations. For the correlations to work, there is a maximum allowable temperature difference between cut points.
For example, the method has a maximum allowable temperature difference of 30 F for cut points in the 95 - 100% range. If... |
Problem Statement: My depressuring utility returns the error Unknown Vessel Metal Thickness. How do I fix it? | Solution: Add the value for Vessel Metal Thickness in Design | Heat Flux | Heat Loss Parameters | Conduction:
Keywords: Dynamic, depressurization, thickness
References: None |
Problem Statement: You can develop a unit operation extension with different levels of access with the help of a licence file or key code. This allows developers to expose to the users more or less information by an appropriate configuration of the visibility manager in Viewer Editor (viewed.exe). However these hidden ... | Solution: It is possible to limit access to a variable's value by manually modifying the edf file and implementing the VariableQuery function of the ExtensionObject interface in your extension model. The changes to the edf must be done in a text editor such as Notepad or Visual Studio and cannot be done in viewed.exe.... |
Problem Statement: Why Does the Tray sizing Utility give the warning: Downcomers are backed up? | Solution: This occurs when aerated liquid backs up into the downcomer due to increased tray pressure drop, liquid height on the tray or fractional losses in the downcomer apron.
When the back-up liquid in the downcomer exceeds the tray spacing, liquid accumulates on the tray above causing downcomer flooding.
Downcomer ... |
Problem Statement: When should I use the Tray Packing Sizing and Rating (TPSAR) analysis? | Solution: Use the Tray Packing Sizing and Rating Analysis to perform rigorous design and rating/sizing calculations of a converged Acid Gas column. Packing or tray information can be specified relating to specific tower internals, such as tray dimensions or packing sizes, design flooding, and pressure drop specificatio... |
Problem Statement: I have several streams and unit operations in the main flowsheet. I want to transfer them into a subflowsheet. | Solution: Select all the streams and unit operations you want to transfer, then right click on the selected objects and use the Combine Into Sub-Flowsheet option.
After this, the selected items are transferred into a new subflowsheet.
For V7.3 and older versions, the option is included inside the Cut/Paste Objects.
Key... |
Problem Statement: I have a Fire scenario for a PSV, and I want to use the Supercritical calculation method. However, when I try to select it, it doesn't appear on the dropdown menu. | Solution: The supercritical option can be used to rigorously calculate the relief load for a vessel that contains only a single phase at relieving conditions, with no subsequent phase change during the fire.
There are two reasons why the Supercritical calculation method might not be appearing as an option for the calcu... |
Problem Statement: How to setup the Aspen HYSYS-OLGA Link extension? | Solution: A step-by-step procedure to use the Aspen HYSYS-OLGA Link extension is shown below:
1. Add the OLGA link located in the palette under Upstream buttons. The Aspen HYSYS Upstream license is checked out when the unit operation is placed on the flowsheet.
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2. Ensure that the OLGA and Aspen HYSYS servers are con... |
Problem Statement: 1) How can I select the appropriate pump for certain conditions?
2) How can I access pump data from several manufacturers from Aspen HYSYS?
3) How can I simulate a pump using incorporated data for a specific vendor’s model? | Solution: The answer to these questions is PUMP-FLO, the world’s largest database to size and select the right pump for your application. Access it through Aspen One Exchange in the button showed in the Design/Parameters menu of the Pump unit (available from V8.2).
This opens the Exchange tab, where PUMP-FLO can be se... |
Problem Statement: How are the liquid volume flows and liquid volume fractions calculated within the composition section of the material stream worksheet? | Solution: Calculating the liquid volume flow for each component:
The molar flow of a component in a stream is converted to a volume flow. The volume flow of each component can be viewed by choosing 'Liquid Volume Flow' as the Basis in the composition section of the material stream worksheet. HYSYS does the following ... |
Problem Statement: How do I extend SLI set? | Solution: SLI is automatically managed by the simulator. If you extend the TIM set, SLI will be automatically extended the next time the simulator is run.
For more information, please also refer about the SLI and DTU entries in SCM Help.
Keywords: SLI set
TIM
DTU
References: None |
Problem Statement: Simulator runs twice if the Planning Board is open. This occurs when user performs an activity on the Planning Board and when a routine executes the M SIM command. | Solution: It is by design that the simulator will run twice if the planning board is open and M SIM command is fired - once for the command and once because the planning board is opened. (M SIM runs when the planning board is opened).
Keywords: Simulator
References: None |
Problem Statement: Where does the built-up backpressure value (7.252 psi /0.5 bar) come from in Safety Analysis environment? | Solution: The 7.252 psi or 0.5 bar (depending on the units set) is a default value with no technical basis. The user can and should change this value for their particular analysis.
In order to changes this value go to the selected sizing scenario. In the Scenario Setup tab look for Total Backpressure and click on Edit ... |
Problem Statement: Quick Start Deployment Guide for IP.21 Process Browser and Plant View | Solution: Plant ViewTM provides access to plant data within Aspen PlusTM or Aspen HYSYSTM so that plant data can be viewed side-by-side with simulation results. Â
Activating Plant View requires three components:
           1. Aspen InfoPlus.21 V8 or other plant data historian
           2.... |
Problem Statement: How do I change reference temperature for the calculation of HHV and LHV in Aspen HYSYS? | Solution: HHV and LHV reported under Gas Properties are calculated at 15C and 1 atm.
If required user can change this reference temperature to 0C from Correlation Manager | Gas.
Note: Heating values reported under standard properties are calculated at 25C and 1 atm.
Keywords: Heating value basis, LHV basis, HHV basis... |
Problem Statement: The internal stream inside my column subflowsheet environment does not report the same values as the column stage data? | Solution: Inside the column environment it is possible to export stage data from inside the column into a stream located within subflowsheet environment. The steps for this process are documented inside knowledge baseSolution 144437. After the column has converged, the internal streams in the column subflowsheet will ... |
Problem Statement: How do I setup a feedforward controller in Aspen HYSYS through the PID controller? | Solution: The setup of the feed forward controller in Aspen HYSYS can be configured within the PID controller. The option to select a feedforward controller is within the parameters tab within the PID controller. The user must select to enable the feedforward controller:
The feedforward controller consists of a lead-la... |
Problem Statement: When using the tray sizing utility, what are the results of the Trayed tab in the Performance section? | Solution: The columns that are displayed are the following:
Delta P This is the total pressure drop considering the sum of dry pressure drop, clear liquid height on the tray, and any residual pressure drop terms that might apply to the column. The units are the pressure units the current unit set has in your simulatio... |
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