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Problem Statement: Why doesn't the pump display horsepower on the Parameters page?
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Solution: The view for the pump is set up to display the energy (heat flow) of the pump. The typical units for heat flow are kJ/h or Btu/hr.
There is a workaround that will enable you to display the Power on the Parameters page. To use the workaround:
Save the attached zip file to disk.
Extract the files to the USER subdirectory where HYSYS is installed. [NOTE: the files must be extracted to this directory otherwise the workaround will not work.]
Restart HYSYS.
The pump should now display power.
Keywords: pump, power
References: None
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Problem Statement: When I define a COMThermo property package such as DBR Amine, Margules or Braun K10 I get a warning message and I cannot go back to the Simulation Environment.
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Solution: The warning message reads:
There was an error in setting up COMThermo. You may need to press the Extended PropPkg Setup or Finish Extended Flash to complete the set up.
The first thing you need to do is to click on the 'Extended PropPkg Setup' button:
Then click on 'Finish Setup' on the new window that opened
In the case of the DBR Amine select a Thermodynamic Model for the AqueousSolution
After this is done, click on the 'Extended Flash Setup' button
And then on 'Finish Setup' on the new window
After this, you should be able to go to the Simulation Environment
Keywords: Error
COMThermo
set up
Property Package
Fluid Package
DBR Amine
References: None
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Problem Statement: In the PID controller setup, specifically Parameters tab/Signal Processing page, you can activate filters.
What kind of filter is this?
Is the filter time the time constant?
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Solution: It is a first-order, low pass filter.
Yes, the filter time is the time constant.
Keywords: PID, Controller, Filter, time constant
References: None
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Problem Statement: The values for my pour point, flash point, Cetane Index (Diesel Index), Refractive Index, Reid Vapour Pressure, P/N/A (PONA) and/or RON look wrong. How is HYSYS calculating these?
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Solution: Information on this can be found in Utilities chapter in the HYSYS Operations Guide Manual (available on the HYSYS documentation CD or DVD shipped with the software). A table listing all the properties in the cold properties utility summarizes all the calculation methods and their range of validity. A quick summary of the correlations is given here:
Flash Point; API 2B7.1, validity, 150 0F < ASTM D86 10% (orNBP) < 1150 0F, -15 0F < Flash Point < 325 0F
Pour Point As per API 2B8.1, validity, 140 < MW < 800, 1 < API gravity < 50, -110 0F < Flash Point < 140 0F
The RON calculation is proprietary and its range of validity is D86 50% ~420 0F. It is only recommended for use with straight run gasoline's and light napthas. As it was developed mainly for mixtures of alkanes, it is therefore not suitable for the calculation of RON's for branched hydrocarbons such as trimethyl pentanes or pure components like benzene.
Keywords: pour point, flash point, Cetane Index, Refractive Index, RVP Reid Vapour Pressure, P/N/A, RON, PONA
References: None
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Problem Statement: Can I access data about the components in my case using Automation?
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Solution: Yes, the HYSYS Component object has all the information that you see in the Fluid Package view within HYSYS. This is accessible via the Components collection of the FluidPackage object. The syntax to get to this is as follows:
Dim hyCpts As HYSYS.Components
Set hyCpts = [Flowsheet Object].FluidPackage.Components
Set hyCpt = hyCpts.Item(H2O) 'Use the SimName (i.e. the left hand name in the HYSYS component list)
Then you can access data like Molecular weight, Formula, NBP using the properties .MolecularWeight .Formula .NormalBoilingPoint ....
The code below gives an example of this that produces a table in Excel containing some details about all the components in the currently open case. To use the code, paste it into Excel's VBA editor, set a HYSYS type library reference and press the Run button.
The attached spreadsheet includes all the functionality of the code below and also allows the user to pick which fluid package to report the components for. It includes a HYSYS 3.2 Type Library reference - For troubleshooting advice on common HYSYS / OLE Automation errors see KnowledgebaseSolution #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].
Public Sub ListCptsInCurrentCase()
'
'Description: Lists the components in the current case, along with some data about each
'
'Declare Variables
Keywords: None
References: None
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Problem Statement: Is the value of light ends basis in Aspen HYSYS Crude Manager expressed as percent of light ends or percent of total crude assay?
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Solution: The input of light ends should be expressed as the percentage of the whole crude, as seen on the screenshot the light ends for this case would be 1.409%, the remaining percentage would be the heavy components of the assay.
Keywords: light ends, assay, oil manager, basis, input
References: None
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Problem Statement: We have simulations that handle more than 256 streams. Is there a later version of the Stream Reporter (Version 1.6) that will allow more than 256 streams to be pulled from HYSYS into New version MS Excel?
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Solution: If you have new version MS Excel, you may go the code to comment out the following code in procedure WriteTable in Modules modWriteTable.
'Check that we have enough room - Excel is limited to 256 columns
If NumStreams > 256 - OutputStart.Column + 1 Then
NumStreams = 256 - OutputStart.Column + 1
MsgBox Due to Excel's 256 column limitation only the first & NumStreams & streams will be processed, , APPNAME
ReDim Preserve Streams(0 To NumStreams - 1)
End If
Keywords: HSR 1.6, Stream reporter, Excel
References: None
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Problem Statement: In Aspen Hsysy V7.2 and V7.3 Installation guide, only Multiflash V3.8 is supported. But the latest version of Multiflash is currently V4.0. Is the latest version V4.0 is applicable to HYSYS V7.2 and V7.3?
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Solution: The Hysys Multiflash interface automatically takes are of the Multiflash version, provided that Multiflash install creates the correct registry key. The key we are looking for are:
HKCU\Software\Infochem\Multiflash\COMTHERMO
Or
HKLM\Software\Infochem\Multiflash\COMTHERMO
Starting with version 4.0 the key is automatically created if the Hysys Upstream support is checked in the custom installation option. Note that the user MUST select this option during installation of Multiflash 4.0.
In addition, you need to make sure that the customer has one of the following upstream licenses:
SLM_RN_PML_HYSYSUPSTRM or SLM_RN_PML_HYSUPSTRM_R3
The old upstream license: SLM_HYSYS_Upstream does NOT work any more in V7.2
Keywords: Multiflash Version, Hysys upstream, installation key
References: None
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Problem Statement: How can I achieve a ''PFD1 to PFD2 cross PFD feeder connector? If I want to use a product stream of an existing PFD as the feeder stream of a new PFD, and the two PFDs are linked through this ''across PFD stream''?
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Solution: You can add a new PFD first.
Do not clone from the existing PFD.
Then delete any stream you want to link from the existing PFD, and re-add it again.
You will see the newly created PFD will contain this stream as well. And this stream is synchronized among all the PFDs.
Now you can start adding the downstream operations of this 'feeder stream in the new PFD.
Keywords: Stream feeder, across PFDs, synchronizing PFDs
References: None
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Problem Statement: How is Mass Flow converted into the Std. Gas Flow [STD_m3/h] variable reported in the ‘Properties’ page of any stream in Aspen HYSYS?
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Solution: The Std. Gas Flow is calculated from the specified or calculated mass flow, according to the Ideal Gas law at standard conditions (1 atm, 15 deg. C):
IdealDens = p0 Mw / (R T0)
where,
p0 – pressure at standard conditions (Pa)
Mw – gas molecular weight (kg/kmol)
R – ideal gas constant (8.314 J/mol/K)
T0 – temperature at standard conditions (K)
For a particular standard pressure and temperature, the mass density is only a function of the molecular weight. You can create a user variable to display this property for each stream or you can use the spreadsheet block in HYSYS to perform this calculation. In the file attached, a user property ‘IdealDens’ was defined in the Properties environment, where F2= p0 / (R T0)=1/23.644 kmol/m3 (based on previous standard conditions). This is used in all streams of the flowsheet.
Keywords: Mass Flow, Std. Gas Flow, Standard conditions, Density, Ideal
References: None
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Problem Statement: Pressure assignment in a mixer is either ‘Equalize all’ or ‘Set Outlet to Lowest Inlet’. Thus, the pressure of the mixed stream is either the lowest of all inlets, or all streams have the same pressure. The user may wish to mix a lower pressure stream to others at higher pressure, and have the outlet pressure equal to the highest value.
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Solution: Instead of using a Mixer, the user should use the Balance operation of ‘Component mole and heat flow’ and assign the desired pressure value to all streams connected.
Keywords: Balance, Mixer, Pressure
References: None
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Problem Statement: Why the component specification in the column changes after modification of the component list?
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Solution: When a component specification is added in the column, the component is taken from the array index in the component list. The column specification then uses this index. If the component list is re-ordered or a component is deleted from the list or a new component added in the list then the component in the original index will be replaced with a different component. This may result in a different component being used in the column component specification. The column may not converge with incorrect specification or give unreasonable results.
It is recommended to check the column specifications following any modification in the component list to make sure that the specifications have links to the correct components.
Keywords: Column Modelling, Component Specification.
References: None
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Problem Statement: How do I restrict what values the user can enter into a User Variable?
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Solution: For example, how do I prevent negative lengths?
The VariableChanging procedure allows the programmer to check what value the user is entering and if necessary to reject it using the AllowThisChange property.
The following example illustrates the use of this procedure.
Sub VariableChanging()
If ActiveVariableWrapper.NewRealValue <= 0 Then
'NewRealValue is always in HYSYS internal units (C, kPa, m, Flow/s etc...)
AllowThisChange = False
MsgBox Diameter must be positive,,Error Checking
End If
End Sub
Keywords: User Variable, NewRealValue, VariableChanging, AllowThisChange
References: None
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Problem Statement: Why is the lower heating value showing empty for some of my streams?
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Solution: The reason why HYSYS is unable to calculate the Lower Heating Value (LHV) for some streams is that some of the components in these streams do not have a specified Heat of Combustion value (You can check it in the Basis Environment, Component Property View, Point tab). To work around this limitation and obtain the LHV for these streams, there are some options:
1. For streams in which those components constitute a small fraction, you can provide a fictitious Heat of Combustion because it will not affect the results significantly. You can edit the Heat of Combustion value for individual components by double-clicking on the component name in the Selected Components list, and then clicking on the Edit Properties button. You can then find the Heat of Combustion entry and change its value. Note that the value shown on the component's property view may not change, but the new value will be used by HYSYS.
For HYSYS versions prior to 3.0.1, please follow the directions in the paragraph below...
You can clone the component in the Basis Manager and provide your own Heat of Combustion while noting that the use of a cloned (and therefore hypothetical) component instead of a HYSYS library component will cost some functionality in other areas (e.g. components which receive special treatment beyond standard thermo methods like TEG and have temperature dependent interaction parameters will lose this special treatment).
2. Alternatively, you can run the macro HEATING.WWB using the Macro Language Editor to calculate Higher and Lower Heating Values for any stream in the simulation using pure component heating values from GPSA (in BTU/ft3). Any components for which values don't exist, like H2O, CO2 and N2 are ignored. You can also input values if you desire. This macro can be found in the HYSYS directory under \Samples\ole\marcos\. You can also download it from our website at www.hyprotech.com.
3. You can also take advantage of our GasProps extension. This is an add-on program to HYSYS. Once properly registered, it can be used the same way as any ordinary HYSYS unit operations. Some assumptions/estimations are involved in this extension, allowing it to report the heating values for a gas stream where the heat of combustion data are missing for some components. This extension is attached herewith in a zip file with detailed instructions. It can also be downloaded from our website.
Please note that in versions of HYSYS older than 2.1.1, the Heat of Combustion for components like H2O, CO2, N2 and H2S is empty, resulting in the LHV also being empty. In v2.1.1, a value of zero has been specified for the Heat of Combustion of H2O, CO2 and N2 while a value was specified for H2S starting in v2.2. For cases created in older versions of HYSYS and re-converged in v2.2, you must press the Refresh button on the Components tab of the Fluid Package Property View to use the new thermo.
Keywords: lower heating value, empty, stream, heat of combustion, LHV, HHV, macro
References: None
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Problem Statement: How do I change the order of the tabs in my workbook?
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Solution: Point the mouse pointer to the tab that you want to move. Click the left mouse button and hold it down. Drag the mouse pointer down to the bottom of the tab and as soon as you go just below the tab, the mouse cursor will change into an arrow pointing upwards. Move the mouse pointer left or right until the arrow is positioned where you want the tab to be moved to, and then you can let go of the mouse button to finalize the move.
Keywords: workbook tab, workbook tab order
References: None
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Problem Statement: I need to create a standard Distillation Column. Do I need to worry about SubFlowsheets?
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Solution: No. You can use the built in Distillation Template and add the Column to your case. From the Main Build Environment it is possible to completely specify and converge the Column. The Column will still reside in the SubFlowsheet, but all basic information can be gathered from the Main Flowsheet.
Example: Adding side-strippers, pump-arounds, bypasses, etc. can also be added from the Main Environment. Adding other Unit Operations requires you to enter the Column SubFlowsheet.
Keywords:
References: None
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Problem Statement: Can HYSYS calculate steady state vapour liquid separation based on separator dimensions?
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Solution: The default HYSYS separator calculates steady state separation based on thermodynamic equilibria, based on the stream conditions and composition.
Note that this applies to versions of HYSYS up to version 3.0.1; starting with version 3.1 the Real Separator allows the user to include carryover and the effects of feed phase dispersion, feed conditions, vessel geometry and inlet/exit devices on carryover. For more information on the HYSYS Real Separator please refer toSolution ID 113864: Real Separator User Guide: How to model carry over in separators?.
Keywords: separator dimensions, calculation
References: None
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Problem Statement: How do I detemine which units HYSYS is currently using to display values?
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Solution: In versions prior to HYSYS 2.2, this was not possible.
Now you can use the CurrentDisplayUnit property of the UnitConversionSet class to recall the current unit used in HYSYS.
Keywords: Units, CurrentDisplayUnit,UnitConversionSet
References: None
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Problem Statement: How can I split a feed stream into pure component streams?
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Solution: The component splitter in HYSYS allows you to split a feed stream into pure component streams.
In versions up to HYSYS 2.4.x, the component splitter allows you to split a feed stream into two product streams, and to assign a fraction of each component to be directed to each of the two streams. For creating multiple pure component streams, in versions up to 2.4.x it is necessary to use multiple component splitters in series.
Beginning with HYSYS 3.0, the component splitter has support for multiple product streams. The user has the ability to enter a matrix of split fractions for each component to each of multiple product streams. This allows you to separate one stream into multiple pure component streams in one single unit operation.
Keywords: split feed stream; separate feed; pure components
References: None
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Problem Statement: How does the Write P-F Equations check box affect my Olga solver in OLGALink in Aspen HYSYS?
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Solution: On the Dynamics|OLGA control tab, the Write P-F Equations box if unchecked, this tells Aspen HYSYS not to include the OLGA link operation when it performs its pressure-flow solve. When this box is unchecked, then dynamic specifications need to be added to the streams attached to the OLGA link. So on the outlet stream from the OLGA link, the flow specification also needs to be checked on the dynamics tab of the stream view. This is not enforcing a boundary condition, however. It is just telling Aspen HYSYS not to add the equations for the OLGA link to its pressure-flow solve. Also, if an inlet stream is attached to the link, then the dynamic pressure specification also needs to be checked.
Note: The Aspen HYSYS stream mass flows will only be identical to the OLGA output at time-steps when a compositional flash has occurred. This is controlled on the Execution tab of the integrator. By default, this execution occurs every 10 timesteps. So the Aspen HYSYS stream will have the same phase mass flows as the OLGA output every 10 timesteps. This is because the OLGA simulator accounts for phase slip. So to get this phase slip into an Aspen HYSYS stream, a flash needs to be performed, the frequency of which is controlled by integrator settings.
Keywords: Write P-F Equations, OLGALink, mass
References: None
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Problem Statement: What do the coefficients C1 to C5 in the Fire Mode Heat Flux equation represent?
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Solution: The Fire Mode heat flux equation is shown below:
Q = C1 + C2*Time + C3*(C4 - Vessel Temperature) + C5 * (Liq. Vol. at time t = t / Liq. Vol. at time t = 0)
where
C1 - Constant Heat Flow to Vessel (kJ/h)
C2 - Constant Rate of Heat Flow Change (kJ/h/h)
C3 - Heat Transfer Coefficient between Vessel and Surrounding Air for Vapour-filled portion of Vessel (kJ/h/C) C4 - Outside Temperature (C)
C5 - Heat Flow applied to Liquid (kJ/h) (can be determined from the API equation for heat flux to a liquid containing vessel (API Recommended Practice 521)).
As an example, you can model the standard heat transfer equation
Q = UA(Delta T)
by setting C3 equal to UA, C4 equal to the constant temperature in the Delta T term and C1, C2 and C5 to zero.
Keywords: Depressuring, heat flux equation, coefficients
References: None
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Problem Statement: How do I add a property package to HYSYS or change the existing property package using OLE?
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Solution: HYSYS property packages must be referred to by their internal name when using Automation. Set the .PropertyPackageName property of the Fluidpackage to the appropriate internal name. For example use PengRob for Peng Robinson.
A list of these names is below:
HYSYS Name , Name to supply in PropertyPackageName
Amine , Amine
Antoine , Antoine
ASME Steam, AsmeSteamPkg
Braun K10, BraunK10
Chao Seader, CS
Chien Null, Cnull
Esso Tabular, EssoTabular
Exteneded NTRL, ExtNTRL
GCEOS , GCEOS
General Nrtl, GenNRTL
Grayson Streed, GSD
Kabadi Danner, KDSRK
Lee Kesler Plocker, LKP
Margules , Margules
MBWR , MBWR
NBS Steam, Steam84Pkg
NTRL , Nrtl
Peng Robinson, PengRob
PRSV , PRSV
Sour PR, SourPR
Sour SRK, SourSRK
SRK , SRK
Uniquac , Uniquac
Van Laar, VanLaar
Wilson , Wilson
Zudkevitch Joffee, ZJRK
The text between the dashed lines is a HYSYS macro which demonstrates the above. To use the macro, copy the text from between the dashed lines and paste it into the HYSYS macro language editor (Tools ... Macro Language Editor).
Sub Main
Set hyApp=Application
Set hyCase= hyApp.SimulationCases.Add(C:\Temp.HSC) hyCase.Visible=True
Set hyBasis = hyCase.BasisManager
Set hyFluidPkg = hyBasis.FluidPackages.Add(Steam) hyFluidPkg.PropertyPackageName = AsmeSteamPkg hyFluidPkg.Components.Add Water
End Sub
Keywords: Add, Property Package, Fluid Package, PropertyPackageName
References: None
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Problem Statement: HYSYS v2.4.1 Amines Package: I am getting a warning saying Property Package Ranges exceed. Are my results valid?
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Solution: The Amines package contains the thermodynamic models developed by D.B. Robinson for their proprietary amine plant simulator, called AMSIM (version 7.0 of AMSIM is used in HYSYS v2.4.1). The AMSIM package recommends temperatures between 25C and 125C be used. This is because the simulation results have been tested to match experimental/plant data at these temperatures.
You may have also seen a warning message similar to Acid gas partial pressure out of amines package range [0.0001 - 2000 kPa] in the trace window. This warning will appear when the stream does not contain any acid gas at all, therefore the partial pressure is zero and out of the range of the property package OR when you are, in fact, out of the applicable range.
The Amine property package is derived from measured data extrapolated over specific ranges, and the results may or may not be useful nor accurate outside these ranges, so we warn the users whenever they are outside any of the ranges. Some of the warning messages may be ignored as they may be a result of the stream in question and have no influence on the outcome of the simulation. For example, the partial pressure warning message will always show up for a Makeup Water stream because the stream would not contain any acid gas at all. In this case, being out of range probably does not have any influence on the simulation as that stream is not meant to contain any acid gas.
The messages are going to appear for all streams as the simulation cannot determine which streams to apply the range checks to and which streams to ignore. It is important that you pay attention to the warnings, and use your engineering judgement, as they may indicate why results may not be as expected, or may highlight a possible error when setting up the case.
Note that the Li-Mather model is much better at extrapolating outside the property package ranges than the Kent-Eisenberg model.
Please refer to the HYSYS Simulation Basis manual, Appendix C, for more information regarding the Amines Property Package in HYSYS.
Keywords: Amine, warning, yellow stream, error
References: None
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Problem Statement: Is pressure recovery factor (FI) the same as the valve recovery coefficient (Km)?
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Solution: Two factors are similar. One FI is for ANSI/ISA sizing method. KM is for Fisher method.
The liquid pressure recovery factor (Fl) corresponds to Km in the Fisher-based sizing method. It indicates the amount of pressure recovery between the valve?s vena-contracta and the outlet stream. Generally, the higher the value of the liquid pressure recovery factor, the greater the pressure drop that can be accommodated by the valve before the inception of choked flow condition. HYSYS sets the allowable pressure drop based on the calculated pressure drops at the choked and service conditions.
Keywords: Km, FI, pressure recovery factor, valve recovery coefficient
References: None
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Problem Statement: When the SULSIM extension is loaded in order to run a SULSIM Mode, users might get the message. SULSIM 6.0 must be installed and registered.
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Solution: HYSYS only works with SULSIM version 6.x. SULSIM 7 does not work within the HYSYS unit operation extension environment.
If you wish to run the HYSYS-SULSIM link you need the Linked version of SULSIM 6. There is also a Standard version of SULSIM 6 which does not support operation with HYSYS. Most users do not have the Linked version although this can be provided by Sulphur experts (SULSIM) if requested.
In the event that users wish to run the HYSYS-SULSIM Link, they will need to obtain a SULSIM 6 Linked install CD from SULSIM.
Keywords: SULSIM extension. HYSYS-SULSIM linked
References: None
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Problem Statement: How do I check my model for K - Values for each component in my column unit operation?
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Solution: To see the K-values for all components, go to Performance | Plots page, select the K values and then click View Table or View Graph. Once the table/graph is displayed, click the Properties button to configure which component values are plotted.
The component name tags can be changed manually by right clicking the graph and select Graph Control. The label can be changed under Data tab.
In order to see all the curves plot for all the components, transfer all component data from the table to excel, and plot the K-value for all components. Similarly, for light / heavy key components, you can plot the graph in the Performance | Plots page.
Relative volatilities are not reported directly in Aspen HYSYS since they are not used in the VLE (vapour-liquid-equilibrium) calculations (which are instead based on rigorous thermodynamics). The spreadsheet operation can be used to compute relative volatilities.
The relative volatility of component A to component B is defined as:
alpha = y_A * x_B / y_B * x_A
where y_ is the mole fraction of the component in the vapour, and x_ the mole fraction in the liquid.
[Coulson and Richardson, Vol 2, 4th Ed., p 433.]
Import these variables into a spreadsheet from the stream(s) you are interested in and do the calculation as per the above.
Keywords: K- Values, Relative volatility, Distillation
References: None
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Problem Statement: If I create a Workbook tab for my PID Controllers, two of the possible variables are Sampling Rate and Sample PV Every x Time Units, what is the difference?
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Solution: These correspond to two completely different aspects of the controller's operation:
Sample PV Every x Time Units
This is the number entered into the controller property window Parameters tab... PV Conditioning page, Sample PV Every (option of input)
When a time period is entered here (say x seconds). Then Hysys will only update the PV fed to the controller every x seconds. For the rest of the time the PV will remain at the same value it was at the start of each x second period. This is illustrated in the attached 2.4.1 case.
Sampling Rate
This number, accessible from the Monitor tab ... Properties window, controls how frequently Hysys adds points to the monitor plot.
Keywords: PID Controller, Workbook Variables, Sampling Rate, Sample PV Every x Time Units
References: None
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Problem Statement: How does the HYSYS network version know whether or not it has found the right key?
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Solution: Each network (grey/beige) key will have a key number but there is also a code associated with the key. For example key 8995 might have the code OPT65 associated with it. You can't see the code anywhere, only the key number. The install code on your HYSYS CD (the very long number on the sticker of your CD case that looks like HPL3797-34578....) is generated using the family code. So it is the install code that controls which key works with the HYSYS software. If you have more than one network key of the same family code on the sub-net than HYSYS can find either one of these keys and use the license off them.
If HYSYS has found the wrong key it will give you an error message A Hyprotech network security key was found that has an invalid serial number. No more licenses were available... To direct HYSYS to a specific key, create a HYSYS.INI file. A HYSYS.INI file states the IP address of the computer that the key is sitting on. This will direct HYSYS to only that computer. The HYSYS.INI file is a text file with the following two lines of text. Note the brackets and lack of spaces. Place the IP address of your keyserver computer where it says 192.139...
[RainbowKey]
[BroadcastAddress]=192.139...
Keywords: HYSYS, Network, Pre-SLM
References: None
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Problem Statement: Why does a pump start cavitating when another unit operation is connected upstream?
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Solution: Pump cavitates when the NPSH available which is calculated by Aspen Hysys is less than the user specified NPSH required. See KB 126063 .
From V7.2 and above, the NPSH calculation has been modified to include the elevation difference between the nozzle attached to the pump and upstream unit operation. See KB 127547
When the unit operation attached upstream of the pump e.g. a pipe segment has an elevation difference, the NPSH Correction calculation with elevation is given as
NPSH Correction with elevation = NPSH + Feed End Elev – Product End Elev
Where,
Feed End Elev is the elevation of the inlet feed stream at the beginning nozzle which is the same as the elevation of the upstream unit operation.
Product End Elev is the base elevation of nozzle (which is default zero for pumps).
NPSH Correction with elevation is the NPSH available calculated by Aspen HYSYS on Rating--> NPSH --> NPSH available as shown below.
If the calculated NPSH Correction with elevation is less than the user specified NPSH required, the pump will cavitate.
To avoid cavitation user can change the nozzle height to the elevation of upstream unit operation. This is located on the pump--> rating --> nozzle --> Base Elevation relative to Ground Level .
Keywords: Pump, Cavitate, NPSH, Pipe segment,
References: None
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Problem Statement: How is a minimum UA scale factor used in the heat exchanger in a dynamic simulation?
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Solution: ThisSolution is applicable for a heat exchanger using Basic Model running in dynamic mode.
The UA is specified for a basic model. The dependency of UA on flow can be applied using reference flow rates for the shell and tube sides as follows:
UAused = UAspecified x F
Where F is the scale factor. This is calculated as
F = (2*Fss*Fts)/(Fss+Fts)
Where,
Fss = (Mass flow current/Mass flow reference)^0.8 for shell side, and
Fts = (Mass flow current/Mass flow reference)^0.8 for tube side
The minimum flow scaled factor (F) is the lowest value which the ratio is anticipated at low flow regions.
The minimum scale factor can be specified as a positive value or negative value. A positive value ensures that some heat transfer still takes place at very low flow rates. A negative value ignores heat transfer at very low flow rates. A negative factor is often used in shut down condition if you are not interested in the results or run into problems shutting down an exchanger. If the Minimum Flow Scale Factor is specified, the above equation uses the ratio if the ratio is greater than the Min Flow Scale Factor. Otherwise the Min Flow Scale Factor is used.
In some cases you can use a negative value for minimum flow scale factor. For example if you use -0.1and if the actual scale factor is less than or equal to 0.1 then the Minimum Flow Scale Factor is 0.
A screenshot for the Dynamics Basic heat exchanger model is shown below.
The used scale factor and UA value is presented in the Performance tab from HYSYS v7.3 as shown in the screenshot below.
Keywords: Heat Exchanger, Basic Model, Scale Factor
References: None
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Problem Statement: How can I simulate a heat exchanger in HYSYS using EDR?
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Solution: If you have a heat exchanger model in EDR and want to use it on a HYSYS simulation you need to enable the option for EDR-Shell&Tube under Design | Parameters. After that, the EDR tab should be activated.
If the drop down menu does not show this option, then it means that the software is not installed on the computer and you need to get it installed.
After doing this, you need to go to the EDR - Shell&Tube tab and either import the existing file or input the geometry desired.
Remember that if you input a geometry you need to have the inlet streams fully defined and have no pressure drop specification or any temperature specification on the outlet streams.
Keywords: Heat exchanger
EDR TASC HTFS
References: None
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Problem Statement: How do I create a strip chart?
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Solution: Strip charts are typically used when dynamic mode operation is in use in HYSYS. The strip chart can be used to track historical data from a simulation, observe trends in the system behaviour as well as diagnose any potential problem areas. Strip charts can track many variables at once and not all variables need be of the same type, i.e. one strip chart may track pressure temperature and flowrate on the same graph. There are two ways to setup a strip chart in HYSYS.
Quick-create a strip chart for a particular object:
In any version following and including version 2.2 (build 3797), most unit operations have the facility to automatically create a strip chart based on a pre-defined group of variable sets. To quick-create a strip chart for a particular object, go to the Strip chart ply on the Dynamics page of the object's property view ( Note: to access the property view, either double click on the object in the PFD or select the object via the Object Navigator <F3> ). The strip chart ply will have a Variable Set drop down menu. Once you have selected a variable set, click on the Create Strip chart button.
Create and configure a strip chart via the Databook:
Most strip charts will be created and configured via the Databook as it allows the user the most flexibility in terms of selecting which variables to display on a particular strip chart. The following steps will illustrate how to create a strip chart:
Go to the Tools menu and select Databook.
Insert the variables which are to be displayed on the strip chart on the Variables page of the Databook. To insert a variable, click on the Insert button on the right hand side of the view, select the variable you want and then click the Add button. (Note: clicking the OK button will add the variable but will close the insert variable navigator. Clicking on the Add button will add the variable but keep the navigator active).
Go to the Strip chart page of the Databook. Click on the Add button and a new strip chart will be added ( new strip charts are named DataLogger1, DataLogger2 etc...).
To display variables on the newly created strip chart, select the strip chart from the Available Strip Charts list and check off the active box beside the desired variables in the Individual Strip Chart Data Selection list.
Once the variables have been selected, clicking on the View button will launch the strip chart so that the information can be displayed.
Variables can also be added to existing strip charts by dragging and dropping the variable onto the strip chart. To drag and drop, select the variable on its parent object property view. Right click on the variable and hold the right mouse button down while moving the mouse over to the strip chart. ( you should notice a bulls eye pattern appear when this is done. ) When over the strip chart, release the mouse button and the variable will be added to the selected strip chart.
Keywords:
References: None
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Problem Statement: How do I calculate Lower and Higher Gas Heating Values for a stream with hypothetical components?
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Solution: For lower heating value (LHV):
1. Go to Tools / Correlation Manager / Configuration / Gas / LHV (...) Basis
2. Click Activate Selected Global Correlation
3. Go to Stream / Worksheet / Properties - it will appear as LHV (...) Basis [Gas]
For higher heating value (HHV):
1. Go to Tools / Correlation Manager / Configuration / Gas / HHV (...) Basis
2. Click Activate Selected Global Correlation
3. Go to Stream / Worksheet / Properties - it will appear as HHV (...) Basis [Gas]
These correlations use the Heat of Combustion from the ISO 6976 (1995) - with a 15 degC reference temperature. Data is taken from hydrocarbons with nearest molecular weight. If the molecular weight is greater than decane, then heat of combustion for decane is used.
Keywords: LHV, HHV, hypothetical components
References: None
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Problem Statement: What is it new in Report Manager in V7.3?
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Solution: Report Manager has as a new option the possibility of browsing a template which must be a .wrk file. There are three templates available: Hysys, Heat Profiles and Petroleum Refining.
There is also the possibility of browsing a customize workbook (Create your own template). These are the steps to follow:
- Customize your workbook.
- Export it and Save it as .wrk file.
- Open the Report Manager
- Click ?Browse template? from the Excel Report window.
Another new option is available to create predefined text reports as: Full, Heat, Stream or Column reports with the option of including stream properties or a wide report.
Keywords: Report Manager, V7.3, HYSYS
References: None
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Problem Statement: What is a Compressor Surge Controller?
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Solution: A compressor will surge if its capacity falls below the surge limit. The surge controller determines a minimum volumetric flowrate that the compressor should operate at without surging. This is called the surge flow. The surge controller then attempts to control the flow to the compressor at some percent above the surge flow, typically 10%. The surge controller essentially acts like PID Controller operations. The control algorithms used to prevent compressors from surging are extensions of the PID algorithm.There are two major differences which distinguish a surge controller and a regular controller:
The setpoint of the surge controller is calculated and not set.
More aggressive action is taken by the surge controller if the compressor is close to surging.
Keywords: Controls, Surge
References: None
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Problem Statement: How do I change the default file location that appears when you save it?
|
Solution: Default location can be changed from Tools | Preferences | Files tab.
Under the Cases you can type a path for the network location.
Keywords: save file, default location
References: None
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Problem Statement: How do I model a counter current LNG exchanger?
|
Solution: At least two zones should be used in any dynamic LNG exchanger, this generally allows for more accurate calculations.
The use of more than 1 zone, often causes some confusion in the LNG setup since Hysys allows you to specify the inlet and outlet streams from each layer of every zone, which might result in a big number of possible setups.
For example, in modeling a counter current 2 sided LNG exchanger, there are two clear ways in connecting the streams:
1- Hot Stream In Zone 0, Cold Stream In Zone 0, Counter current box checked. Hot Stream out Zone 1, Cold Stream out Zone 1, Counter current box checked. See attached figure 1.
2- Hot Stream In Zone 0, Cold Stream In Zone 1, Counter current box checked. Hot Stream out Zone 1, Cold Stream out Zone 0, Counter current box checked. See attached figure 2.
As you can see from the attached figures, the first option is a Semi-Counter Current flow, since the streams out of zone 0, re-exchange in zone 1, resulting in an outlet temperature very close on both the hot and cold sides.
On the other hand, the second option is a True-Counter Current flow, and the outlet temperature of each side approaches the inlet temperature of the other side.
Keywords: LNG Exchangers
References: None
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Problem Statement: How can I quickly generate a report for a single stream/operation?
|
Solution: Right click on the icon, or in the title bar of the stream/operation properties window, and choose Print Datasheet.
Keywords: Datasheet
References: None
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Problem Statement: I want to set Tube Wall Cp and Density, but HYSYS won't take the values. Why?
|
Solution: You can only enter these values when the exchanger method is set to Dynamic Rating ... Detailed. (i.e. Dynamic Rating on Design .. Parameters page, and Detailed on Rating ... Parameters page)
Keywords: Dynamic Rating, Wall Cp, Wall Density
References: None
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Problem Statement: Cannot select new surface tension method for Chien Null property package
|
Solution: The new option for prediction of surface tension based on the API procedure 10A3.2 is available only for the following packages Chao Seader, Glycol Package, Grayson Streed, Peng-Robinson, PR-Twu, PRSV, Sour PR, Sour SRK, SRK, SRK-Twu, and Twu-Sim-Tassone.
Keywords: new, method, surface tension
References: None
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Problem Statement: Are the shell and tube Heat Transfer Coefficients calculated on a clean basis?
|
Solution: The shell and tube heat transfer coefficients do take the fouling factor into account. When this value is zero the shell and tube heat transfer coefficients are calculated on a clean basis.
You can input the shell and tube fouling factors on the Rating tab/Sizing page by selecting the appropriate radio button in the Sizing data group and entering the value in the Shell/Tube Fouling field.
Keywords: Heat Exchanger, Heat Transfer Coefficient, Fouling
References: None
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Problem Statement: What are the hot-keys for Aspen HYSYS PFD?
|
Solution: Function
Hot-Key
Zoom out
Page Down or Ctrl Down Arrow
Zoom in
Page Up or Ctrl Up Arrow
Zoom All
Home/Ctrl Home or End/Ctrl End
Toggle between last zoom levels
Z
Pan
Arrow or Shift Arrow keys
Centre PFD on cursor
Period key or C
Mirror about X axis
X
Mirror about Y axis
Y
Rotate 90
1
Rotate 180
2
Rotate 270
3
To default orientation
N
Display Stream Temperatures
Shift T
Display Stream pressures
Shift P
Display Stream molar flowrates
Shift F
Display Stream Names
Shift N
Display Stream mass flowrates
Shift M
Display Object description
Shift R
Display Outlet nozzle elevation
Shift O
Display Inlet nozzle elevation
Shift I
Select Object Label
L
Open Selected Object
V or E
Delete Selected Object
Delete
Show/Hide Object Palette
F4 or F10
Keywords: hot key, short cut, pfd
References: None
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Problem Statement: Before attempting to run any of the automation examples, ensure that you have the Visual Basic 5.0 MSVBVM50.dll and 6.0 MSVBVM60.dll run-time files installed in your Windows System32 directory.
|
Solution: Attached are the .dll files listed above.
Keywords: run-time, .dll, automation
References: None
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Problem Statement: How do I open UNISIM files with Aspen HYSYS?
|
Solution: UNISIM files can be opened in Aspen HYSYS. You need to save them as .XML format in UNISIM and then open it in Aspen HYSYS by choosing File > Open > Case and then select the .XML file as you can see below:
A
Now the XML file should load fine in HYSYS and you should be able to save back to *.hsc file.
For more information about what's an XML file please refer to the followingSolution 112787
Keywords: UNISIM, Hysys
References: None
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Problem Statement: What is Improved in Aspen HYSYS ? Combined Liquid Viscosity in Pipelines
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Solution: Most pipe flow correlations have been developed for two phase flow of gas and liquid. Therefore, if a third phase, like water, is present in the pipeline, then the two liquid phases are combined into a representative liquid phase. This combination requires the calculation of mixture properties like viscosity.
The estimation of the fluid viscosity is an important factor in accurately predicting multiphase flow through pipelines. Many factors can affect the apparent viscosity of a combined liquid phase. For example, if the oil and water form an emulsion, the combined liquid viscosity can have some unique features. Consequently, HYSYS users should have a choice in how the viscosity is determined for a combined liquid phase.
Current Liquid Combination Methods
Currently, if there are two liquid phases but neither is aqueous, then the HYSYS pipe segment model uses a non-polar mixing rule from Perry?s Handbook (3-282) to define the viscosity:
ln( m ) = m1 ln( m1 ) + m2 ln( m2)
where mi and mi are the mass fraction and viscosity of the phase.
However, if one of the liquid phases is aqueous, then the following mixing rule is applied:
Fo < 0.33: m = mw * [1 + 2.5 Fo( (mo + 0.4 mw) / (mo + mw))]
Fo > 0.5: m = mo * exp[ 3.6 (1 ? Fo) ]
0.33 < Fo < 0.5: m is weighted average of the two regimes
where Fo is the volume fraction of the oil phase. It should be noted that the correlation for Fo < 0.33 is the Taylor correlation described in the next section.
New Liquid Combination Methods
As previously mentioned, the viscosity of a mixed liquid phase can have a significant impact on pipe flow calculation results. It is therefore important that a user can control the method used for estimating the viscosity of a combined liquid phase. In certain cases, a simple volume-weighted viscosity may be appropriate:
m = mo Fo + mw Fw
where Fo and Fw are the volume fractions of the oil and water phases, respectively. However, this model may not be appropriate for some mixtures because the apparent viscosity of some mixtures may be larger than that of the individual phases.
Oil and water mixtures can often form emulsions; therefore, the mixing rules defined above may not be the most appropriate. In this case, the emulsion viscosity m is often expressed relative to the viscosity of the continuous phase mc:
m = mr mc .
The continuous phase is determined by the water volume fraction at an inversion point Fwi. When the water volume fraction is below the inversion point (Fw < Fwi), then the water is dispersed in a continuous oil phase. In the following, the subscripts c and d refer to the continuous and dispersed phases, respectively.
The simplest model for the viscosity is that mr is a constant of unity. This ensures that below the inversion point, the mixture viscosity is that of the oil phase and above the inversion point it is that of the water phase. However, because this is an extremely limited model, a more rigorous determination of the relative viscosity is desirable. Determining the relative viscosity mr requires experimental data of the particular system being modeled because it can depend on many factors such as the dispersed phase volume fraction, droplet diameter, and the shear rate. In order to generalize the modeling process, theoretical models and correlations have been developed for determining the relative viscosity. The following table describes some available viscosity models.
Author
Correlation
Notes
Keywords: None
References: s
Einstein (1906)
mr = 1 + 2.5 Fd
Theoretical model for very dilute systems. Included here for historical context
Taylor (1932)
mr = 1 + 2.5 Fd A
A = (0.4 mc + md)/(mc + md)
Extension of Einstein that included interactions but limited to low F. This correlation is currently used in the Fo < 0.33 regime.
Taylor, G. I., ?The viscosity of a fluid containing small drops of another liquid?, Prec. R. Soc. A, 138, (1932), 41-48.
Levinton and Leighton (1936)
mr = exp[ 2.5 A (Fd + Fd5/3 + Fd11/3 )]
A = (0.4 mc + md)/(mc + md)
Extension of Taylor for higher F
Levinton, A. and Leighton, A., ?Viscosity Relationships in Emulsions Containing Milk Fat?, J. Of Phys. Chem., 40, (1936), 71.
Guth and Simha (1936)
mr = 1.0 + 2.5 Fd + 14.1 Fd2
Extension of Einstein
Guth, E. and Simha, R., Kolloid-Zeitschrift, Vol. 74, (1936), p. 266.
Generic Polynomial
mr = 1.0 + K1 Fd + K2 Fd2 + K3 Fd3
Barnea and Mizrahi (1973)
mr = exp[ K1 Fd / (1 ? K2 Fd)]
Extension of Einstein for more concentrated solid particles
Barnea, E. and Mizrahi, J., ?A Generalized Approach to the Fluid Dynamics of Particulate Systems. Part 1?, Chem. Eng. J., 5, (1973), 171-189.
Brinkman (1952)
mr = (1 - Fd)-2.5
Fwi = 1 / (1 + mo / mw)
Extension of Taylor
Brinkman, H. C., ?The viscosity of concentrated suspensions and
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Problem Statement: I have supplied the correct number of specs for my distillation column, but the degrees of freedom is still showing as ?1' Why could this be happening?
|
Solution: If the Feed to the Column has not flashed, then this will be interpreted by the Column as a degree of freedom. The column will not begin to solve if all feed streams entering the column are not flashed.
Keywords:
References: None
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Problem Statement: Why is XML important? What new features does XML functionality bring to HYSYS?
|
Solution: Several new capabilities are made possible through the use of XML technologies. For instance, a HYSYS case can now be stored as an XML file giving an alternative to the traditional binary .hsc file. XML is the means of data transfer used by the new Case Linking and Collaboration capabilities. Finally, the Custom Stream Properties uses XML to store the user defined sets of properties that they wish to have displayed. More detail on some of these features follows:
.XML Case Storage
HYSYS 3.0 now has an alternative storage format to the traditional binary .hsc file. A HYSYS case can now be saved as an XML file. This file is a human readable file that follows the XML Data schema defined for HYSYS. The .xml case file can be reloaded and the HYSYS case will be reconstructed. This file does NOT contain all of the case data, but rather only the data necessary to reconstruct the case. Once an XML case file is reloaded the solver needs to be run in order to solve the flowsheet and calculate the results.
Case Collaboration & Linking
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 stream. Alternatively, the source stream changes can be manually transferred to the destination stream when the user requires the new information. This new capability relies on the use of the Run-Time Integration (RTI) Server which is installed with HYSYS 3.0. The RTI Server is the conduit through which the linked streams exchange data. Large plant wide HYSYS cases can now be broken into smaller more manageable cases and distributed to the engineers with expertise on the individual plant units. The entire model can then be linked together at the appropriate time to see the overall effect of the unit changes.
Case Security
HYSYS 3.0 has a new level of Case Security to ensure the integrity of the intellectual property contained within a HYSYS model. This feature was developed to give the Case author the required level of comfort when distributing HYSYS models that they have invested a lot of time and knowledge in. In addition to the ability to password protect a case, the author can also lock the case to a specific piece of computer hardware or Hyprotech security key. The user's password is given an expiration date to further protect the business interest of the case author. These capabilities are accessed from the Case Security option in the Tools menu.
Notes Manager
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 to find specific words or specific dates that the notes were written. The Notes Manager is accessed from the Flowsheet Menu.
Keywords: XML, new features
References: None
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Problem Statement: How to include the specific gravity rel. to air or any desired properties in workbook report print out
|
Solution: You can customize the workbook first, then in the report, add workbook as your datasheet object. See below screenshot on how to customize your workbook.
Then add workbook as your report datasheet object.
Keywords: Report customization, properties, workbook
References: None
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Problem Statement: How can I create an Excel report for my Hydrate Formation Utilities?
|
Solution: Download the attached workbook page and you can place it in ?C:\Program Files (x86)\AspenTech\Aspen HYSYS V7.3\Workbooks\? directory.
Click in the workbook icon in Hysys and go to Workbook -> Import -> Pages..
Select the Hydrate Formation Utility to append a new page in your workbook.
Go back to the Workbook menu -> Export -> To Excel..
Select the page you will like to export and click in the Export To Excel button.
Keywords: Hydrate Formation, Excel, Report, Workbook
References: None
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Problem Statement: When installing HYSYS V7.3_Patch 3 on Windows 7, users may see the following message:
a??Internet Explorer restricted this webpage from running scripts or ActiveX controlsa??
The installation will not continue until users configure ActiveX Controls permissions in Internet Explorer.
|
Solution: This knowledge base article describes how to resolve the Internet Explorer restriction on ActiveX controls. After double clicking on the Aspen HYSYS patch executable, a small window will appear (see picture above). The window is basically not allowing the ActiveX Controls to install and thus prevents the patch from installing. If the ActiveX Controls is not allowed to install, the a??Pre-configuring Process Modeling (HYSYS) V7.3. This may take a few minutes. Please waita?|.a?? Will appear and according to the task manager there is no activity on the CPU, but it is running.
Therefore, to avoid the a??please waita?? message allow the ActiveX control to install by expanding the condensed window and locating the option to allow the ActiveX control to install from the bottom of the window.
Keywords: HYSYS V7.3, Patch3, (7337) build, Install, Internet Explorer, Active X controls
References: None
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Problem Statement: What is the difference between the SLE and SLEV73 correlation in the tray sizing utility?
|
Solution: A? The SLE (Sherwood-Leva-Eckert) correlation is valid for towers operating above the loading factors of 20000 (liquid loading > 9200 lb/hr.ft2).
A? The SLEv73 (Sherwood-Leva-Eckert for HYSYS v7.3) is a superior representation of the graphical SLE curves when compared to the original HYSYS SLE correlation. This correlation is the same one found in Aspen Plus and listed there simply as SLE.
Packing Correlation
Keywords: SLE, SLEv73, tray sizing
References: s
SLE: as summarized in Equilibrium Staged Separations, Philip C. Wankat, Elsevier, New York, NY, 1988, pp. 420 - 425.
For more information please refer to
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Problem Statement: What is New in Aspen HYSYS V7.3 ? Integration of OLI?s Mixed Solvent Electrolytes (MSE) Capabilities in Aspen HYSYS
|
Solution: Aspen HYSYS V7.3 CP1 introduces the availability of the OLI Mixed Solvent Electrolytes (MSE) capabilities within Aspen HYSYS via a link. Prior to this release, Aspen HYSYS only supported a link to the OLI aqueous models.
In both cases, the OLI software must be licensed directly from OLI Systems or one of their partners. Both the OLI aqueous and mixed solvent electrolytes functionality will not work within HYSYS unless a valid license and installation of the software is available.
More Information
OLI Systems offer following two calculation models to handle different types of chemical processes :
a. Aqueous
b. Mixed Solvent Electrolytes
Prior to Aspen HYSYS V7.3 CP1, one would use the aqueous OLI model inside HYSYS by creating a component list and selecting components using the OLI aqueous databank. The newly created component list then was attached to a fluid package that uses `OLI_Electrolyte? as the property package. All the further property calculations then are routed through OLI Systems? provided API to get back various calculated properties as needed in the HYSYS simulation.
To use the new OLI MSE model inside HYSYS, the workflow remains mostly as described above except that the user selects the components from the OLI MSE components databank.
A HYSYS component list can only have components selected from either the Aqueous or MSE databanks. Once the user selects at least one component from either of the aqueous or MSE databanks, he will not be allowed to select components from the other databank to protect the integrity of the HYSYS component list (this is the restriction imposed by OLI Systems).
Keywords: None
References: None
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Problem Statement: When user click on 'Quick Size' option in Aspen HYSYS (2-phase or 3-phase separator) running in Windows Vista or Window 7 environment, it may show an error message Could not size separator: Interface Request Failed.
|
Solution: To fix this problem, a file called sepsize.dll in the Aspen HYSYS installation folder should be registered as follows:
1. From the Windows Start menu, choose Command Prompt (type 'cmd' >> press enter) to get a DOS prompt. From here user can register this dll file. Make sure user has full administrative rights to do this.
2. At the DOS prompt, find the directory that contains the sepsize.dll file. For example, if it is located in the same path as the HYSYS default path, your DOS command line will look like: C:\Program Files (x86)\AspenTech\Aspen HYSYS V7.3>
(Some tips: To switch from a different drive to the C: drive, type in cd C:\ at the prompt)
3. Register the dll. At the prompt, now type in regsvr32 sepsize.dll and Enter.
5. You should get a registration success message mentioned below
6. Right click on Aspen HYSYS and run as administrator. Now check 'Quick Size' option which should work now.
7. User may have to do the same procedure for other versions if there are multiple HYSYS versions installed on same machine by changing the last bit of directory, e.g. C:\Program Files (x86)\AspenTech\Aspen HYSYS V8>
Keywords: Quick Sizing, Separators, Window Vista, Window 7
References: None
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Problem Statement:
|
Solution:
Keywords:
References: None
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Problem Statement: How can I use a User-Defined Valve type in Dynamics?
|
Solution: For Aspen HYSYS versions 2.4.1 to 3.2, please read the attached document.
For versions 3.4 to current, Aspen HYSYS allows the user to input values in the curve information table, as shown in Figure1:
Figure 1. Curve Information Table
Keywords: Valve Type, Valve Operating Characteristics, User Valve Type
References: None
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Problem Statement: As optional information, the top and bottom temperature estimates can be provided in the column operation. Those values are used to initialize the temperature profile of the column and some convergence problems can be avoided if good estimates are provided.
|
Solution: Bottom temperature: in the main flowsheet add a new stream (Bttm-estimate for instance). Specify the pressure as the reboiler pressure and specify the composition as the expected composition of the bottom product. Specify the vapor fraction as zero and Hysys will calculate the bubble temperature of that stream. This value can be used as an initial estimate of the bottom temperature.
Top temperature: similarly, in the main flowsheet add a new stream (Top-estimate for instance). Specify the pressure as the condenser pressure and specify the composition as the expected composition of the top product. If the condenser is Full Reflux type, specify the vapor fraction of the dummy stream as 1, since this product is vapor and Hysys will calculate the dew temperature of that stream. If the condenser is Total, specify the vapor fraction as zero. If the condenser is Partial, specify the vapor fraction accordingly: zero if the composition of the distillate stream was used or 1 if the composition of the overhead stream was used.
Keywords: Column, Temperature, Estimates, Convergence
References: None
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Problem Statement: Can I automatically attach a process stream to a unit-operation on PFD?
|
Solution: 1. A Select the process stream
2. A Make sure Auto Attach Mode button is pressed on the PFD Toolbar
3. A On the object palette, select the unit operation say Pump
4. A Click on the PFD. The Pump will automatically attach to the process stream selected.
Keywords: Auto Attach Mode, Attach stream to Unit operation etc
References: None
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Problem Statement: Should I follow the Dynamic Assistant recommendations all the time?
|
Solution: The dynamic assistant is designed to follow a specific set of rules for Dynamic Specs. These rules might not suit your case at some point, so if you press No when you are prompted to see the dynamic assistant comments, HYSYS will attempt to start the integrator. If the model is specified properly the case will start running.
It is strongly recommended, that you read and consider the suggestions of the Dynamic Assistant. Once you have done this, you can decide which recommendations to accept and which ones to discard. Keep in mind though, that you DO NOT have to follow the suggestions the Dynamic Assistant provides.
Keywords: dynamic, specifications, assistant
References: None
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Problem Statement: How does Aspen HYSYS calculate the size and/or flow for a 2 phase relief valve?
|
Solution: The relief valve in Aspen HYSYS calculates for two phase flow as follows:
Where:
Vf = Vapour Fraction
VapFlow = flow calculated using the vapour flow formula (choked or non-choked)
LiqFlow = flow calculated using the liquid flow formula
The vapour and liquid flows are calculated according to equations 5.51, 5.52, 5.53 and 5.54 in Section 5.7.3 of the HYSYS 2004 Operations Guide manual.
This method is similar to the API 520 method.
Keywords: HEM, DIERS, pressure relief
References: None
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Problem Statement: What are the Surge Parameters of the Compressor Surge Controller?
|
Solution: There are a few parameters for the Surge Controller. These have also changed between Hysys 3.2, and Hysys 3.4 and later versions.
Hysys 3.2 and earlier.
1- A and B parameters. These are used to represent the Surge Curve of the compressor using the following Equation:
Q = Surge Flow (m3/sec)
H = Head (m)
H = A + B*Q^2
If you don't have the curve in terms of these parameters (most probably you won't), you can read two points from your curve (two Surge Flow values vs two Head Values) and use them to fit the above equation to your line and come up with the A and B values. (see also below)
2- Control Line (Default Value 10%):
This value decides how close the Actual Flow is to the Surge Flow when the controller starts to take action. I.e. If you use the default values, the controller will start to take action whenever the Actual flow is 10% above the Surge Line.
3- Backup line (Default Value 5%):
This is an intermediate point between the Control line and the Surge Line at which the controller will take more aggressive action.
4- Quick opening %/sec (Default Value 3):
This represents how aggressive the action taken by the controller when it hits the backup line is (in % OP/sec).
Hysys 3.4 and later.
1- A, B, C, D parameters. These are used to represent the Surge Curve of the compressor using the following Equation:
Q = Surge Flow (m3/sec)
H = Head (m)
H = A + B*Q + C*Q^2 + D*Q^3
If B and D are set to zero, the equation reduces to the same form as that used in Hysys 3.2 (the C term in Hysys 3.4 is then equivalent to the B term in Hysys 3.2).
See below for sugestions on how to get the four values.
2- Control Line (Default Value 10%):
3- Backup line (Default Value 5%):
4- Quick openeing %/sec (Default Value 3):
See discussion under Hysys 3.2 above.
How do I calculate the A, B, C and D parameters?
For Hysys 3.2 (and earlier), it is a relatively simple job to generate the A and B parameters as discussed above.
For Hysys 3.4 (and later), the B and D terms can be set to zero as a simplification, and the A and C terms calculated in a similar way.
To generate all four terms, a cubic regression is required. Any available regression tools could be used for this.
One option which is immediately available is to use the tabular option in the Hysys basis manager to do the regression. The tabular option is normally used to override normal Hysys calculated property data, but we can cheat and input data for head vs flow to get Hysys to regress the data.
The attached Hysys file (compressor surge curve regression.hsc) is already set up to do the regression, for either a 2 term curve (Hysys 3.2) or a 4 term curve (Hysys 3.4). Just paste your head v flow surge data into it, and you will get the required coefficients.
. Open the file, go into the basis manager and view the property package Basis-1.
. Select the Tabular Tab, click on the + symbol next to Information on the left hand side, and click on Density (L)
. for the 4 term expression, click in the ETHANE column, then click on the Prop Detail button, then click on the Table tab.
. enter Q and H data. Q data should be entered in the X (Temperature) column, H data in the y (Molar Density) column
. once all data has been entered, click on the regress button and then view the 4 terms (A,B,C,D) on the Coeff page.
. for the 2 term expression, click in the ETHANE column, then click on the Prop Detail button, then click on the Table tab.
. enter Q and H data. Q data should be entered in the X (Temperature) column, H data in the y (Molar Density) column
. once all data has been entered, click on the regress button and then view the A and C terms on the Coeff page. The A value corresponds to the compressor A term. The C value corresponds to the compressor B term.
Keywords: Controls, Surge, Regression
References: None
|
Problem Statement: What is a ratio controller?
|
Solution: The Ratio Controller is a special type of Feed Forward controller that maintains the ratio between two process variables. The Ratio Controller takes two inputs with the desired ratio as the SP and calculates an OP. Prior to HYSYS 3.0, this was done using a Spreadsheet Operation. A ratio controller operation was added in HYSYS 3.0.
A classic example of a use for a Ratio Controller is to maintain a desired fuel to air ratio for a furnace
Keywords: ratio; controller
References: None
|
Problem Statement: I'm using the new HTFS-Engines option, within HYSYS. What type of calculation mode is the new TASC interface using? Is it Checking, Simulation or Design?
|
Solution: The new HTFS-Engines option, within HYSYS, was implemented using Simulation. Using the given stream inlet conditions, the Simulation calculation mode is used to determine the heat load, pressure change and stream outlet conditions that will occur with the exchanger you specify.
If you need the Design or Checking calculation modes you can do that with the TASC User Interface via the <Export> facility.
Keywords: HTFS Engines, HYSYS-TASC link, mode, simulation, checking
Creation Date: 18-Mar-2003 08:25AM
References: None
|
Problem Statement: When opening Aspen Properties Database Manager, the error message Snap-in Failed to initialize or
Snap-in Creation failed occurs (See attached error message for detail).
|
Solution: 1. Go to Control Panel | Add/Remove Programs
2. Un-install the Microsoft SQL Server 2005 including the other SQL Components, and then reboot the system.
3. Install the attached SQLEXPRS32.exe from thisSolution.
4. Select the default option, select Mixed Mode Authentication and enter Aspen100 or any password. Select default options for the rest of the installation.
5. Run HYSYS to confirm the error message no longer occurs.
6. Run the Aspen Properties Database Configuration Tester to check if the databases have successfully connected.
(Start | Programs | AspenTech | Process Modeling | Aspen Properties | Aspen Properties Database Configuration)
Keywords: Snap-in, Microsoft SQL Server 2005, HYSYS v7.2, and APED
References: None
|
Problem Statement: Are there any Rate-Based Distillation examples available for CO2 capture and H2S removal from acid gas streams?
|
Solution: Several new sample cases illustrating the use of Rate-Based Distillation to model the removal of CO2 and/or H2S from acid gas streams using amines (MEA, MDEA, DEA, MEA+MDEA, DEA+MDEA) have been provided in Aspen HYSYS sample folder:
C:\Program Files \ AspenTech \ Aspen HYSYS (version V7.3 and higher) \ Samples
Keywords: Rate based distillation, CO2 capture, H2S removal, Amines
References: None
|
Problem Statement: What is the Compressor Stone Wall curve used for?
|
Solution: The compressor Stone Wall curve will limit the actual flow through the compressor to a certain upper limit that cannot be exceeded.
Keywords: Compressor, Stone Wall
References: None
|
Problem Statement: Can I use Automation to access user property values?
|
Solution: The .GetCorrelationValue method of the ProcessStream object can be used to access a user property attached to a stream. Simply pass the user property name and the type Standard.
[The GetCorrelationValue method is also used to access the value of property correlations linked to the stream (seeSolution 110955)]
For example, paste the following code into Excel's VBA editor, set a HYSYS type library reference, and press the Run button. It links to a user property called Sulphur that is unitless.
Private Sub GetUserProperty()
'Description: Uses the GetCorrelationValue() method of the stream (see KBSolution #110955)
' To access User Property values.
'Declare Variables
Keywords: None
References: None
|
Problem Statement: Why do Aspen HYSYS simulation files have a lock icon? This issue can occur if there is a permissions or access issue on the folder the files reside in.
|
Solution: There are two ways of removing the lock icon.
Method 1:
· Right click on the folder and click on “Properties�.
· Go to the tab “Sharing�.
· Click on “Share�.
· Select the user group from the dropdown e.g. everyone if you want to share it with everyone and then click on Share to remove the lock from the folder.
 The user group “Everyone� will have access to the folder then. The folder no longer has special permissions and Windows 7 will therefore remove the lock icon.
Method 2:
· Right click on the folder and click on “Properties�.
· Go to the tab “Security�.
· Click on the “Advanced� button at the bottom.
· Click on “Change Permission�.
· Select your user account and check the option “Include inheritable permissions from this object’s parent�.
· Click on apply to remove the lock icon.
The lock icon will be removed because the folder now inherits the permission of the parent folder. If that folder does not have any special permissions you will successfully remove the lock from the folder.
Keywords: HYSYS file with pad lock
padlock on file
file permission
HYSYS
Lock
References: None
|
Problem Statement: 为?Y么?a?Ireal separator (?^实`S??离Si)?I??离?A?E?a?a预计?I?v???k`??C`|?Ocarry-over(?g带?A应)?I`S应ZQ???a?C??ZQ????经设?e?D??Z?SZ??离Si??经??敛???H
|
Solution: ?p户应该检查?e????离Si?o?uSC?I`S应?E?u?B
?@?E???m???a?I?e???o?uSC?I?E?u?CZg???eSi?a两`S?ISE?E刚?D?Y这???o?uSCa?围?a?C???s论这???o?uSC?????Y为??让??离?@?I???e`S?E过?I?C?Y???o?uSC??总?i?L两`S?????E过?B换??话说?C?s`u?e`S?i?????o?uSC?E过?C?A?s?Y?o为carry-over(?g带)?A应?CZ?仅仅?Y?o为?o?uSC???x?a?#?a`S间??离SE?E???x?I?I???B
?p户应该尝试调???o?uSC?I???x?????a?C??ZO两ZO??时调???C?EZg??`u?L?e`S?e?????o?uSC?I?????o?u?o间?I?!?B?E积?B
Keywords: ?k???I??离?A?E?Creal separator-?^实`S??离Si, ?o?uSC?E?u???x?C?o?uSC???a?C两`S?CZO`S, CN-
References: None
|
Problem Statement: When you pass the pointer over any stream or unit operation, a banner like the ones on the images below is shown:
How can someone customize the properties displayed?
|
Solution: You need to go to Tools | Preferences and under the Simualtion Tab go to the Toot Tips option on the left hand side.
Now select from the Show PFD fly by section: 'Material Stream', 'Energy Stream' or browse through a unit operation. Then on the right hand side a list of properties should show up.
Check the boxes for the properties that you want to be displayed.
And close the Session Preferences window when you are done with the customization.
Keywords: Properties
Banner
Fly
List
Pointer
Label
Cursor
References: None
|
Problem Statement: Where I can find the Autorecovery files in Windows 7?
|
Solution: You will find the files in this path:
C:\Users\UserName\AppData\Local\Temp\
And the files will have this name:
Autorecovery save of FILENAME (0X861152).ahc
Keywords: Autorecovery, windows 7.
References: None
|
Problem Statement: How do I know I'm choosing the correct Amine in my Electrolytes property package?
|
Solution: The component names are different in the OLI Electrolytes package.
MDEA is MDEXH in Electrolytes, MEA is MEXH, DEA is DEXH.
Keywords: amines, MEA, MDEA, DEA, OLI electrolytes
References: None
|
Problem Statement: What does the Current Time represent (on the integrator window general tab) ?
|
Solution: The current time cell indicates how much time has past (in simulation time) since the integrator started the first time. This value can be set to zero at any time by the user.
Keywords:
References: None
|
Problem Statement: Why is the Pipesys value for viscosity for my Oil-Water mixture different than the HYSYS value?
|
Solution: There are different equations involved in the viscosity calculation in Pipesys and in HYSYS.
In Pipesys, the viscosity of a mixture of hydrocarbon liquid and water phase is calculated as:
Mu(m) = Mu(oil)^V(oil) * Mu(water)^[1-V(oil)]
where Mu(m) = viscosity of blended mixture
Mu(oil) = viscosity of oil phase
Mu(water) = viscosity of aqueous phase
V(oil) = volume fraction of the oil in the blended mixture.
This is a so-called ordinary mixing rule.
In Hysys, however, the mixing rule uses different expressions for viscosity.
For V(oil) > 0.5
Mu(m) = Mu(oil) * e^[3.6*(1-V(oil)]
For V(oil) < 0.33
Mu(m) = [1 + 2.5 V(oil) ((Mu(oil) + 0.4 Mu(water))/(Mu(oil) + (Mu(water))] Mu(water)
For 0.33 < V(oil) < 0.5
The viscosity is a weighted average between the two equations detailed above.
Different from the ordinary mixing rule used in Pipesys, our mixing rule, especially the one used for V(oil) greater or equal to 0.33, takes into consideration the emulsion formed in the blended oil-water mixture.
There is a catch, though. Whether or not the emulsion really exits in an oil-water mixture is a question which can only be answered based on experimental evidence. Without the support of experimental data, it is hard to say which mixing rule would better represent your oil-water system.
Keywords:
References: None
|
Problem Statement: Can PIPESYS read PIPEFLO files?
|
Solution: Unfortunately, it is not possible to read PIPEFLO files into PIPESYS.
Keywords:
References: None
|
Problem Statement: Why does report manager give two different liquid volumes for the depressuring utility?
|
Solution: In Aspen HYSYS V7.2 and all lower versions the Report Manager gives liquid volume in the Design | Connection section. This is the default value used by HYSYS when the simulation is run in dynamic mode.
The initial liquid volume is the value specified by the in the Depressuring Utility. The depressuring utility takes user specified value. The utility runs in dynamic mode and the initial default value is replaced by the user specified value when the calculations are performed.
In the most recent HYSYS version (V7.3), the Report Manager gives the liquid volume as the user specified value to avoid any misunderstanding.
Keywords: Depressuring Utility, Initial Liquid Volume, Report Manager
References: None
|
Problem Statement: If I change my strip chart variables, why do I have to re-run the scenario?
|
Solution: The depressuring utility only stores data when it is asked to do so. Otherwise, case size would grow very large. Therefore, if changes are made to the variables stored, the scenario must be re-run.
Keywords: depressuring; dynamic depressuring; strip chart
References: None
|
Problem Statement: How can I get rid of unwanted lines that appear in the PFD?
|
Solution: On occasion, unwanted lines appear on the PFD while making modifications to the PFD display (such as showing a summary table for a stream or unit operation), as in the figure below. In order to get rid of these lines, click on the Drag Mode icon in the PFD tool bar, then move the PFD a small amount in any direction using the Drag Mode feature. This will force Aspen HYSYS to redraw the PFD, resulting in an elimination of the unwanted lines.
To prevent the lines from appearing altogether, open your session preferences (select Tools | Preferences from the main menu) to the Simulation | Options pagetab and deactivate the Enable Cross Hairs On PFD checkbox.
Keywords: lines, PFD, delete, preferences
References: None
|
Problem Statement: Where can I find the Bulk Velocity, and Erosional Velocity in the ASW Variable Browser
|
Solution: You should be able to find it in Active Forms base object in pipe unitop
Keywords: Erosional velocity, bulk velocity, Aspen Simulation Workbook, Variable Brower
References: None
|
Problem Statement: How do I use the interpolation method for Aspen HYSYS Compressor/Expander Curves?
|
Solution: In the HYSYS compressor operation, a cubic spline method is used for the interpolation of the speed curves themselves and for the interpolation between speed curves. Here is an outline of the procedure:
When multiple curves of different speed are provided (for example three curves for 9000 rpm, 11000 rpm and 13000 rpm), given the flow F, the first step is to calculate the Head and Efficiency for the given flow (for each of the three curves) using a Cubic Spline Method (see below). When the three pairs of data available (9000 rpm, Head For 9000; 11000 rpm, Head For11000; and 13000 rpm, Head For13000), the next step is to find out the head for a specified speed for the speed specified (10000 rpm for example) using the Cubic Spline Method again. The same procedure is used to find out the Efficiency.
If you input multiple curves into the compressor and then run the compressor at a speed below the lowest curve (i.e. lowest speed), the method used in HYSYS includes a limited functionality of extrapolation when the point lies outside of the data. Note that extrapolation is generally not accurate enough depending on the degree of curve non-linearity.
Please find the attached file for detailed information about the cubic spline interpolation.
Keywords: Interpolation, compressor curves, the cubic spline
References: None
|
Problem Statement: How can I display Compressor / Expander power and heat flow separately on a specsheet?
|
Solution: In HYSYS whatever units are set for the display of 'Energy' will be used to display both the heater/cooler and compressor/expander duty.
If you want to display compressor / expander duties in power units then you can add the following user variable to a compressor / expander. The units of the User Variable must be set to Power
Sub PostExecute()
Dim Power As Double
Power=ActiveObject.Energy.GetValue(hp)
ActiveVariableWrapper.Variable.SetValue power,hp
End Sub
The value of the user variable will be included on the Specsheet for the compressor / expander.
Keywords: Compressor, Expander, Power
References: None
|
Problem Statement: How do I create a vapour pressure curve?
|
Solution: You will need to use the Property Table utility.
1. Select the stream that contains the composition you wish to find the vapour pressure curve for.
2. For the 1st Independent variable, select Vapour Fraction | Mode = State and set the value for the State to be 0.0 (i.e. the vapour pressure is equivalent to the bubble point).
3. For the 2nd Independent variable, select Temperature | Mode = Incremental, and choose a temperature range that suits your needs.
4. Switch to the Dep. Prop. page and select Pressure as the Dependent Property.
5. Press the Calculate button at the bottom of the window.
6. View the Results as a Table or Plot on the Performance tab.
Keywords: boiling point curve, property table, vapor pressure, dependent property, vapor pressure curve
References: None
|
Problem Statement: What are the Shell Baffle Types Hysys uses for Rating of Heat Exchangers
|
Solution: Shell Baffle type can be set on the Rating tab ... Sizing page ... Shell radio button of the Heat Exchanger property window.
Single, Double and Triple
These are the standard segmented baffle types as illustrated in the TEMA standards (8th Ed, p 31) or Perry (7th Ed, p 11-42)
Grid
These could equally be called rod type baffles. They consist of alternating horizontal and vertical sets of parallel rods (See attached file). These allow axial flow, and are mainly intended to support the tubes. They provide some heat transfer enhancement effect due to the turbulence generated.
Keywords: Exchanger, Shell Baffle Types, Single, Double, Triple, Grid
References: None
|
Problem Statement: Can I size a three-phase separator in HYSYS?
|
Solution: The Vessel Sizing utility does not currently support three-phase separator sizing. While in HYSYS Version 2.4.1 and up you can select a three-phase separator as the object for the Vessel Sizing utility, the calculations will be based only on the Vapour and Light Liquid flows, and will not take the Heavy Liquid (aqueous) phase into account. Therefore while the utility will provide results, these results are based only on the Vapour and Light Liquid phases and do not correctly represent the sizing of a three-phase separator.
Keywords: size, three-phase separator
References: None
|
Problem Statement: What is the difference between the GCEOS PR package and the standard PR package?
|
Solution: GCEOS model is used to define and implement your own generalized cubic equation of state including mixing rules and volume translation. When you select PR option from within the GCEOS it reduces to the PR EOS. This is the Standard PR, not HYSYS PR. The main difference between standard PR and HYSYS PR is the alpha function used (HYSYS PR uses a modified alpha function when acentric factor is greater than 0.49). It is recommended to use Hysys PR or PRSV property package, rather than using GCEOS and modifying this to PR. HYSYS PR is more advanced and continuously improved over the years e.g. binary coefficients.
Keywords: GCEOS, HYSYS PR, Standard PR
References: None
|
Problem Statement: How can I simulate a heterogeneous catalytic reaction in a PFR?
|
Solution: A heterogeneous catalytic reaction can be simulated in a PFR. The following document oulines some of the steps as well as some of the terms used in this operation.
Keywords: PFR, Catalytic, Void Fraction
References: None
|
Problem Statement: What is Weep Velocity?
|
Solution: On a tray if the gas rate is too low, much of the liquid may rain down through the openings of the tray (weeping), thus failing to obtain the benefit of complete flow over the tray. The gas velocity at which the weeping starts to occur is defined as weep velocity.
Keywords:
References: None
|
Problem Statement: How to model a Decanter in Aspen HYSYS?
|
Solution: Decanters are used to separate liquids where there is a sufficient difference in density between the liquids for the droplets to settle readily. Decanters are essentially tanks which give sufficient residence time for the droplets of the dispersed phase to rise (or settle) to the interface between the phases and coalesce. In an operating decanter there will be three distinct zones or bands: clear heavy liquid; separating dispersed liquid (the dispersion zone); and clear light liquid.
An example is illustrated in the C-3.hsc case file in the HYSYS Samples folder (C:\Program Files (x86)\AspenTech\Aspen HYSYS V8.0\Samples) .
The example file C-3.hsc uses two different fluid packages, VLE-Basis and LLE-Basis. The Fluid package VLE-Basis has NRTL-Ideal as property method and Water, Ethanol and Benzene as components. This basis uses the default binary interaction parameters and are good for predicting LLE. Thus if you flash a stream using this basis, it reports two liquid phases when encountered.
Where as the LLE-Basis Fluid Package uses the same property method and components, but the binary coefficients are estimated using UNIFAC-LLE method (based on the group contribution methods). This basis is only used with the sub-flowsheet 'DECANT', where you have a decanter to predict more accurate separation between the two liquid phases. Entire simulation, except the Sub-flowsheet, uses the VLE-Basis.
Keywords: Decanter
References: None
|
Problem Statement: Can I access the Envelope Utility via Automation?
|
Solution: Yes, although this cannot be achieved with any of the standard Automation methods. Since the Envelope utility is not yet fully wrapped for Automation access - you will note there is no envelope object in the HYSYS type library.
Instead a 'Backdoor method' must be used.
NB Backdoor methods are only recommended when there is no other alternative, the internal HYSYS monikers or messages may not remain constant between versions so care should be exercised when upgrading.
Two Excel 2003 files for Aspen HYSYS versions 2006.5 and V7.0 are attached to thisSolution that illustrate how to access the main envelope properties.
Note: These 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 of these examples. We invite any feedback through the normal support channel at [email protected].
Keywords: Envelope, Backdoor
References: None
|
Problem Statement: Sometimes it is needed to operate a column at isothermal conditions. How do I represent them in Hysys?
|
Solution: In real plants, such columns do have intermediate heat exchangers in almost every tray. A preliminary designSolution can be obtained in Hysys using duty streams and Temperature Tray specifications all along the column. The limit situation would be to install a duty stream in every stage, although some intermediate situation (less duty streams) can lead to a validSolution. The attached case shows a 24-stages ammonia absorber. It operates at a constant temperature of 65 C. Using 7 duty streams (and an equal number of necessary temperature specs) it is possible to operate such an absorber.
Keywords: Absorber, isothermal operation, design specifications
References: None
|
Problem Statement: How do I add a graphic file (.bmp) to the PFD?
|
Solution: Right click on the PFD and Select Insert Object.
Choose the Create From File Page and browse for the file you wish to insert.
The attached .jpg demonstrates how to accomplish this.
Keywords:
References: None
|
Problem Statement: Why is my Extension Unit Operation's PFD Icon Yellow?
|
Solution: HYSYS will outline a unit operation in yellow if it cannot complete its calculations. Usually, the unit operation will use its StatusQuery method to provide the user with a specific reason why the solve can not be completed, but the Not Solved warning will be provided by default.
To prevent this warning from being added, the unit operation must call the SolveComplete method of the Extension Container object when it has satisfactorily completed its calculations.
The unit operation's Execute is responsible for determining whether it has calculated all of the variables it wishes to calculate.
Keywords: SolveComplete
References: None
|
Problem Statement: How do I install OLGAS for my pipe segment?
|
Solution: You do not have to install OLGAS separately. When you install HYSYS, the OLGAS extension would have been installed automatically for you; however, you do need to purchase the OLGAS license in order to utilize this extension.
To purchase the OLGAS license, please contact your Hyprotech Sales Representative.
Keywords: OLGAS
References: None
|
Problem Statement: For Column flow rate specs what stream properties do the Volume and Std Volume Flow Basis correspond to?
|
Solution: The flow basis values in column specs correspond to the following stream properties.
Specification Flow Basis : Stream Property
Volume : Std Ideal Liq Vol Flow (Labelled Liquid Volume Flow prior to HYSYS 3.0.1)
Std Volume : Liq Vol Flow @ Std Cond (Labelled Std Liq Vol Flow prior to HYSYS 3.0.1)
See Section 1.6 of the HYSYS 3 Simulation Basis pdf manual (SimBasis.pdf) for more details of these stream properties.
Keywords: Flow Basis, Volume, Std Volume
References: None
|
Problem Statement: What is the stream cutter and how is it used?
|
Solution: A stream cutter serves to facilitate the transition between one property package and another.
In HYSYS 3.0 you no longer need to use Sub-Flowsheets when creating model with multiple Fluid Packages. Each Unit Operation and Stream can have its own associated Fluid Package. A Stream Cutter Operation is automatically inserted into the flowsheet at the point where a transition from one Fluid Package to another occurs. The Stream Cutter defines the Component Mapping and Transition Basis for the transfer. Among other things, this capability allows the use of separate Fluid Packages for the Shell and Tube sides of a Heat Exchanger. When the Fluid Package of a unit operation is changed, this change propagates to all streams and operations upstream and downstream until an operation with multiple inlets/outlets is encountered. At this point, a Stream Cutter operation is inserted in the flowsheet cutting the stream into two streams. The appropriate transition basis must be selected to solve the transition and flowsheet.
Keywords: cutter; stream; property package
References: None
|
Problem Statement: Does the component `?Therminol 62?? is available in Hysys?
|
Solution: Unfortunately, the only available components like that are the following and this is using Aspen Properties Component List inside Hysys:
If you decide to use one of the list above you need to go to the Simulation Basis Manager and add a component list but using Aspen Properties
And then a window like the following will appear, please click on Launch Find Component Window as you can see below:
Then a window like the following will come up and then you are going to be able to type the name of the component you are looking for and then click on Find now.
If there is no such a component that you want, you will need to create a hypo component, for this you will need at least one property and then Hysys will estimate the Unknown properties: For that please refer to the followingSolution
Keywords:
References: None
|
Problem Statement: What is the Pressure/Flow Solver?
|
Solution: The pressure flow solver is the main engine behind the Dynamic calculations in Aspen Hysys Dynamics. It relates the flow through the plant to the pressure drop. This allows for much more realistic behaviour of the model.
Each operation includes either a flow resistance relation (e.g. a valve flow is related to its resistance or pressure drop), or a pressure build-up relation (e.g. a vessel pressure is defined by flow in and out and how much accumulation occurs).
Keywords: Pressure solver
References: None
|
Problem Statement: Warnings or error messages pop up while my case is solving and the solver stops until I press OK. How do I prevent these messages from disrupting my case?
|
Solution: You can display any warnings and/or errors in the Trace Window to prevent the need for user intervention and to allow your case to solve without interruption. To send the errors or warnings to the Trace Window:
Version 3.1 or earlier:
Go to Tools\Preferences and on the Simulation\Options page, check the boxes for:
Display Errors in Trace Window
Display Numerical Errors in the Trace Window (Ignore Them In Dynamics)
Version 3.2 or later:
Go to Tools\Preferences and on the Simulation\Errors page, check the boxes for:
Display Errors in Trace Window
Display Numerical Errors in the Trace Window (Ignore Them In Dynamics)
For futher details of the meanings of HYSYS errors and warnings see:Solution ID 109101: What do Math error in Math library, Math overflow and Numerical error has Occurred error messages mean?
Keywords: solver, warnings, error messages, Trace Window
References: None
|
Problem Statement: When I want to import an assay from Crude Manager into Aspen HYSYS, I get the following message: The spiral module is not found.
|
Solution: This error occurs when the Crude Manager from SpiralSoft license cannot be found. You will need to contact SpiralSoft for an additional license for this function. http://www.spiralsoft.co.uk
Keywords: Spiral
Crude Manager
HYSYS
Assay
References: None
|
Problem Statement: Can I use valve Cv and Percentage Open to calculate the pressure drop in Aspen HYSYS steady state?
|
Solution: In Aspen HYSYS V7.2 and earlier, only HYSYS Dynamics can calculate pressure drop based on Cv and Percentage Opening. In HYSYS Steady State, you will have to set up pressure drop across the valve or use the User Variable to calculate based on Cv.
Starting with Aspen Hysys V7.3, In Steady State you will have an option to set up pressure drop or calculate the pressure drop using valve Cv and Percentage Opening.
First enable to option Use sizing methods to calculate Delta P from Design | Parameters page as shown below.
Then set the Valve Manufacturers, Valve % Opening and Cv as shown below.
Keywords: Sizing method, pressure drop, valve, Cv
References: None
|
Problem Statement: How do I get vapour fraction and enthalpy data along the heating and cooling curve in my heat exchanger?
|
Solution: If you are using the default End Point solver (Design Parameters page in Heat Exchanger view) then the LMTD is calculated based upon only the end point temperatures of the heating and cooling curves (four temperatures). When you look at the data on the Performance Plots page only these 4 points are shown and on the Tables page the enthalpy and vapour fraction are reported only at these points.
To view the data as a function of temperature or enthalpy, change the solver to Weighted (Design Parameters). This solver will calculate the LMTD's along the heating curve and sum them up. The default intervals is 5 but these can be increased on the Design Parameters page. On the Performance Plots page the heating curve will then be plotted at 6 points.
The WeightedSolution method is rigorous and should be used if there is any phase change on the either the shell or tube side of the heat exchanger. End Point takes less computation time to solve and can be used if no phase change is expected.
Keywords: heating, cooling, curve, temperature, enthalpy, heat exchanger
References: None
|
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