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Problem Statement: When attempting to translate a steady state model in Aspen Plus to Aspen Plus Dynamics, I get the following error message: | Solution: If you have Polymers in your component list, go to the Properties Environment and use button reorder at Components > Specifications to make sure that the polymers and segments are placed in the first lines.
Once you have changed the order of the component list, go back to the simulation environment, re-run the simulation in steady state and export it again to Dynamic mode. The error should disappear.
This is by design and it was designed to get rid of unwanted components during the translation from Aspen Plus to Aspen Plus Dynamics.
Keywords: Aspen Plus Dynamics; Fatal Error; Translation;
References: None |
Problem Statement: Swage is used in the Pipe segment in order to change the diameter of a Pipe segment taking into account accurate pressure drop an velocity change. However, in some occasions when reducing the diameter of the pipe segment the Swage gets ignored and you observe the following profile:
As you can see, the pressure profile behaves as though there was no Swage in the pipe Segment. | Solution: When using a Swage to reduce the diameter in a Pipe segment, what we see is that the reduction affects the velocity of the flow, increasing it abruptly and causing that the pressure decreases abruptly to compensate the kinetic energy increment. When the velocity of the flow increases until surpass the speed of sound in the fluid, then flow gets chocked and the Pipe Segment will not converge.
In order to prevent this chocked flow, the only alternative available is ignoring the swage, so the change of velocity and pressure due to the change of diameter will not be taken into account, and pressure drop and acceleration will be calculated using the new diameter.
To show an example, please check up the attached simulation file in which we will review the pressure profile in a pipe segment with three different diameter reductions, and using the Mach number calculator unit, we will review the mach number of the fluid in each case. To know more about the Mach number calculator consult the KB What is the Mach Number Unit Operation Extension?
To review the profiles, go to the pipe segment, go to Performance tab and click on View profile bottom. Their you can see the results as table or plot, just click on Plot, select Plot and select Pressure or vapor velocity to review the profiles.
Case1: Diameter reduced from 150 mm to 125 mm
Mach number along the fluid:
Velocity profile:
Case 2: Diameter reduced from 150mm to 115mm
Mach number along the pipe segment:
Velocity profile:
Case 3: Diameter reduced from 150mm to 110mm
Velocity profile:
Hence, as we can see, in the case 1, when the reduction does not accelerate so much the fluid, the results are correct, but, in case 2 the pipe segment has already a chocked flow and the mach number calculator displays a warning telling that it is already Out of range, which means that this results, although they seem correct, indeed they are not reliable. And finally in the case 3, where the reduction is major, the pipe segment simply miss calculate everything after the reduction and the pressure profile does not take into account the change of the diameter, since taking it into account will lead to a not converged pipe segment due to chocked flow.
This behavior is correct, since Aspen HYSYS is not designed to work with supersonic fluids, so its calculations are reliable only with mach numbers bellow 1.
Keywords: Swage, Pipe Segment, Mach number, diameter reduction
References: None |
Problem Statement: When launching Aspen Watch Maker, the following pop-up error message comes up:
Run-time error ‘50003’: Unexpected error | Solution: This issue is caused by Microsoft Windows being outdated. Check your machine for any pending Windows updates and apply the most recent updates to resolve this error.
Keywords: Watch, maker, run, time, error, 50003, ‘50003’, unexpected, error, windows, update
References: None |
Problem Statement: Why There is a Weird “SUL ppmw” Row in MBO HTML Reports? | Solution: First, the sulfur properties is usually defined as weight percentage (wt%). So why do we see this row in the HTML report of MBO that has “SUL ppmw” in it?
“ppmw” stands for “Parts per Million Weight”. It is also a unit that measures towards weight. In MBO, if the SUL wt% is less than or equal to 0.01%, MBO by default will convert that SUL wt% to SUL ppmw behind the scenes.
The problem with this is “Heel” is NOT converted. It is rounded from a number to 1 decimal place. So you see in the screenshot above, the “0.1” under Heel is still in wt% but the other numbers are converted to SUL ppmw. This will be changed to consistent unit starting from V12.
Keywords: None
References: None |
Problem Statement: Why Do You See a Mismatch of Objective Function at the Top of the Full | Solution: Report and the Economic Summary Section?
Solution
The reason this is happening is because the top OBJFN is taken from the Matrix Analyzer and the OBJFN from Economic Summary is taken from the execution log.
The solution to this is to uncheck “Use Tighter Bounds on Qualities”. The reason is because the model is already running optimal with a good OBJFN, it does not have convergence issues so this option is not needed.
Unchecking this will remove the inconsistency between the two numbers.
Keywords: None
References: None |
Problem Statement: Why Sometimes You are Seeing Inconsistent Property Values in PRMAP and Final Matrix Analyzer? | Solution: The simple answer to this is the model has conflicting data. First, please check the execution log for W069s. AN example is as below:
*** Warning. Property AAA for BBB in Table BLNALL Previously Defined
What these warnings mean is the same data is defined in more than one place in the model and one has overwritten the other. That’s why you might see an inconsistency between PRMAP and Matrix Analyzer or an inconsistency between manually calculated properties and Matrix analyzer.
Here is the setup that caused this problem. Consider a property AAA in stream BBB. It is defined in BLNPROP:
BLNPROP AAA
BBB 2
*
The stream is also defined as an assay data in table ASSAYS:
ASSAYS Crude CCC Crude DDD
IAAABBB 0.89 0.17
*
If there is no recursion for this property, BLNPROP has the highest order of precedence. It will overwrite the internally generated table QPOOL which the assay data goes into. However, this property is a crude cut property and it needs to recursed. It should NOT be in BLNPROP. This will cause confusion in calculating this property.
So the solution is to add property AAA of stream BBB into PGUESS table instead, to account for the fact that it is a recursed crude cut property.
PGUESS AAA
BBB Initial Guess Value
*
Keywords: None
References: None |
Problem Statement: The stream report in Aspen Plus from version V9 and on can be easily customized by selecting the properties to be displayed, adding properties and selecting the order of the displayed variables, and sometimes users need to use those reports in other simulations. | Solution: When the stream report is modified, the recommendation is saving this as a template, so you can use it for other streams. To save it as a template click on Save as a template, it will ask for a name, the description is optional.
Then you can go to other stream reports and select this template to be used instead the Full default template. To make another template the default template just go to File\Options\Advanced and down is a section where you can indicate the default template for all the streams. Consult KB 62474 for more details.
To use the created template in other simulations, the templates need to be exported, this can be done clicking on the Template arrow option:
Then a window will appear with the default templates and the ones created by the user, select the template to be exported, and clicking on export will generate a .apsst file, type a name for this file and indicate the folder where it is going to be saved.
Importing the template to other simulations is pretty simple, just go to another simulation, click on the Template button and the click on Import, browse for the .apsst file of the desired template and the template will be available to be used in the new simulation.
The templates are commonly available in other simulations in the same machine without using Import/Export option, however sometimes a template might not be available in other simulations or maybe the template is required in another machine, so in these cases the solution is importing the .apsst file.
Keywords: Import template, export template, template, stream report
References: None |
Problem Statement: When modeling an Incinerator unit a Inlet Gas is required, as well as a Fuel Gas stream and an Air stream. However the only required flow is the Inlet Gas, for the other two only their composition, pressure and temperature are needed, how are those flows calculated? | Solution: The goal of the Incinerator unit is to convert the remaining particles of H2S in the tail gas clean up, thus the incinerator prioritizes the burning of the inlet gas stream. The incinerator does this using a fuel stream, since burning the acid gas stream requires energy, so the incinerator also needs a stream of air needed to burn the acid gas stream as well as the fuel gas considering the air excess indicated when specifying the outlet oxygen mole fraction.
Then, the incinerator only requires the acid gas inlet stream flow since this is exactly the flow that it is going to burn. Thus according to the flow of the gas inlet stream it will calculate the stoichiometric amount of the inlet air stream defined, it performs the combustion and calculates a product stream, this is called the first burn and with it, the incinerator does an energy balance to calculate the energy needed to burn this acid gas stream
-Duty = Feed gas stream Heat + Air needed Heat – First Burn Heat
But as this energy needs to be provided by other source, then the Incinerator will calculate the amount of Fuel needed to provide this energy, and it calculates the air flow needed to burn the fuel gas stream plus the excess specified. In the image bellow, it can be seen the energy balance for the burning of the fuel, and how the energy released from this process is exactly the needed to burn the acid gas fuel, which was expected since the overall Duty of the incinerator is zero, hence the exact amount of energy needed by the acid gas burning is the energy provided by the burning of the fuel stream.
Summarizing this process:
1. The Fuel stream flow is calculated based on the energy needed to burn the inlet Acid Gas stream
2. The air flow is calculated according to the air needed to burn both, fuel and inlet gas streams, plus the excess indicated when specifying the oxygen composition in the outlet stream.
Keywords: Incinerator, Flow, Energy balance, sulfur unit, Sulsim
References: None |
Problem Statement: After running the model, warning W617 “Property XXX in Row YYY Differs from ZZZ” is displaying in the Execution Log. How do I clear this message? | Solution: To clear this message check for any inconsistencies between the property in table ASSAYS and table INDEX or Property Calculation Formula.
If you have verified there are no inconsistencies, but you are still getting the warning, check if the property giving the error is being calculated from two or more properties defined in table ASSAYS. If it is a new property defined through table INDEX or through Property Calculation Formula, this warning shows when there are zero values for the existing properties in table ASSAYS. If this is the case, the warning should not affect your results but if you wish to clear this warning, you will need to assign non-zero values to the existing properties in table ASSAYS (I-Rows), or suppress it through table REPORT.
In V10 and V11, this warning no longer shows when it is related to zero value properties. If you are using V9 or older with zero value properties, this warning can be ignored or solved with the solution described above.
Keywords: ZASS, error
References: None |
Problem Statement: How to stabilize recipes in Aspen MBO? | Solution: In blend operations, it is preferred to use similar recipes for a given product to reduce the complexity of blend execution. In Aspen MBO, there is a setting “Recipe Stabilization” to satisfy this requirement.
Users could go to Settings>>Blend. Under Recipe Stabilization, enter a positive value for Deviation Penalty. You may start with 100 and experiment with different values to see the effect on recipes.
Below is an example to illustrate how a deviation penalty is applied.
Assume product U87 has blends B1, B2, and B3, each of which uses component ALK. The blend percentages of ALK are 0.29 for B1, 0.2 for B2 and 0.3 for B3.
The component percentage average for U87 is therefore (.29 + .2 + .3)/3 or 0.27.
The component percentage deviation or the total deviation from the average for this example would be:
abs(0.29-.027) + abs(0.2-0.27)+abs(0.3-0.27)
If a recipe deviation penalty parameter is defined in the Deviation Penalty field found on the Settings dialog box Blending tab, the component percentage deviation would be multiplied by the deviation penalty and would be reported as the RecDev Pen value in the Blend Details section of the optimization report. Recipes would then be generated where deviations are less and that are therefore closer to each other.
Keywords: None
References: None |
Problem Statement: It is common that users compare thermodynamic models between Aspen Plus and Aspen HYSYS such as NRTL and observe differences in VLE behavior of binary mixtures between both applications. | Solution: Aspen HYSYS and Aspen Plus have different databanks of components and have differences in the thermodynamic models used by them. NRTL model is exactly the same in both applications, however what is different is the form of calculating the parameters. NRTL equation is as follows:
In order to match the VLE behavior from both applications, the models used are NRTL in Aspen Plus and General NRTL fluid package in HYSYS. Aspen HYSYS has two models about NRTL, for checking the differences between these fluid packages please go to the following KB: What is the difference between NRTL and General NRTL fluid packages in HYSYS?
General NRTL parameters in HYSYS:
And this is the way Aspen Plus calculates the binary parameters for NRTL:
Hence, according with the parameters calculation, the option 1 of General NRTL from HYSYS can be used to model Aspen Plus NRTL binary parameters in HYSYS, and it means that it can be done the other way around.
The steps to copy the binary parameters from Aspen Plus into Aspen HYSYS are as follows taking as reference a Butanol-Toluene mixture:
1. Go to NRTL binary parameters in Aspen Plus and see the parameters
2. In Aspen HYSYS select General NRTL and copy the parameters from Aspen Plus, but keep in mind that matrix in HYSYS is built as follows
So, according to the parameters available in this case Aij and Bij can be copied, and Cij from Aspen Plus is Alp1ij in HYSYS, all other parameters are zero in this case.
3. In HYSYS you can run a TXY analysis using the Unit operation Equilibrium. Select the components and select Plot. To know more about this analysis, please refer to KB How to run a binary VLE analysis in Aspen HYSYS?
4. And in Aspen Plus you can run a binary analysis to compare the VLE results
Keywords: NRTL, General NRTL, Binary Paremeters
References: None |
Problem Statement: When entering the inputs of a stream, one of the flow options is Stdvol, which is standard liquid volume, but when looking at the stream summary the volume calculated is different even though it is at standard conditions. | Solution: The Standard Liquid Volume (Stdvol) basis uses the standard liquid volume property of a component (VLSTD) and its units are volume/mole, which is a property given at standard conditions, 1 atm and 60F, and it does not depend on temperature nor pressure, VLSTD property can be consulted in Methods|Parameters|Pure components|Review.
Thus, when using a Stdvol flow as input in a stream the mass is calculated using the VLSTD. Hence this stdvol will not be the same as the calculated in the simulation by the selected method.
For instance, a mixture of water, ethanol, propanol and toluene has been used to show better this difference, 1 cum/hr of each component has been entered in a single stream at standard conditions, 60F and 1 atm, using different Methods, and when reviewing the stream results, the volumes are as follows:
It can be seen that none of the Methods could calculate exactly 1 cum/hr, this is because each method has different correlations and equations to calculate the volumetric flow. To calculate the mass and mole flows in the simulation, Aspen Plus uses the VLSTD as follows:
So, when entering a value of 1 cum/hr of Stdvol, Aspen Plus just calculate the mole flow that comply the VLSTD, hence when multiplying the VLSTD by the mole flow calculated, the entered value of Stdvol will be obtained:
If the streams conditions are different from the standard, then the difference is going to be bigger, and if the stream is a vapor or has a significant amount of vapor, the volumetric flow rate is going to be extremely different from the stdvol flow. For vapor we recommend entering standard vapor volume flows as mole flow basis using units based on scf or scm.
Keywords: Standard volume, Volume Flow, VLSTD, Stdvol
References: None |
Problem Statement: In occasions a simulation is running well and it converges, but after setting a Sensitivity Analysis and running again the simulation, it does no converge anymore. | Solution: This problem is not about the simulation but convergence, the Sensitivity analysis will run all the cases that has been indicated and, by default, it will run the base case at last, which means that if the manipulated variable has a large range of values, and the manipulated variable input in the base case has a value closer to the initial points, when the solver goes back to that value it will fail due to the distance between the final point of the sensitivity and the base case input.
The solution is move the base case to a point close to the initial or the final point in the sensitivity, then in the options tab change the Execution options, there users can decide if the base case is executed at first, at last, or even if the base case is not executed at all.
This selection will depend on the base case inputs, for instance, if you are varying a mas flow from 10 to 300 in the sensitivity and the flow input in the base case is 25, the Execution option should be changed to Execute base case first, as this input is closer to the starting point in the sensitivity. It is important to note that with "Execute base case first" when the simulation has completed, the stream and blocks will show the results of the last sensitivity case and NOT the base case.
Keywords: Sensitivity, Execution Options, convergence, sensitivity analysis
References: None |
Problem Statement: The incinerator is an adiabatic unit, so the real duty calculated using the heat flows of the streams is always zero, but when reviewing the Performance tab in the incinerator, it reports a Duty different from zero. | Solution: When modeling an Incinerator unit inside the Sulfur Recovery Unit, it requires an inlet gas feed, a fuel stream to burn it and an air stream for combustion. This unit is adiabatic and its duty is zero.
The reported duty is different because the incinerator parts the process into two, it first calculates the energy needed to burn the gas feed stream and then it completes the balance when burning the Fuel stream. The steps are as follows:
1. First it calculates the exact amount of Air needed to burn the gas stream (stoichiometric amount) which means that it calculates the fraction of the Air stream fed needed
2. It calculates the product stream of burning the gas stream, this product stream is named the first burn stream
3. Finally, using the heat flow of this first burn stream, the energy balance is calculated and the Duty calculated is the one that is reported. This Duty is the energy required to burn this gas stream.
The energy balance of burning the gas feed is as follows.
-Duty = Feed gas stream Heat + Air needed Heat – First Burn Heat
In the following image the first burn flow is displayed as well as its heat flow and the flow of air needed to burn it. So, the duty calculated is the result of the energy balance of burning the gas feed stream.
This cannot be reproduced as the first burn stream and the fraction of the air stream needed to burn it is calculated internally.
Keywords: Incinerator, Duty, Fluid Package, Sulfur unit.
References: None |
Problem Statement: How to migrate Aspen Report Writer templates from old versions to V11 and beyond? | Solution: In V11, Aspen Report Writer is enhanced to support use of 64-bit Windows. The new function “Template Migration Tool” could be used to migrate old templates to new templates in newer versions, which mainly updates the directory path of RW functions from library AspenRpt.xlam.
Template Migration Tool is located under ARW menu. Old template(s) and location of new template(s) should be defined in the migration wizard dialog.
Keywords: None
References: None |
Problem Statement: How to copy a datasheet of one object from an existing datasheet of another similar object? | Solution: Often times a project may involve many equipment of the same type, it would be convenient to be able to use an existing equipment datasheet as leverage to create new datasheets of other equipment of that type. There is not a particular feature available to copy datasheet directly because this approach would cause a major concern with data consistency maintenance within the workspace. The proper approach is to copy data at the object attributes level. After the data are copied over to the second object, the datasheet of the second object will essentially be a copy of the original object's datasheet. There are two ways users can approach this:
Create object as clone:
ABE allows object to be copied as clone. The object created as clone will share data in certain attributes with its parent object. Hence, once the user populates data in the parent object, the same data values will also be pushed forward to the clone objects and vice versa. The clone object datasheet will pick up these values to complete its fields. For more details about cloning, please refer to this article: https://esupport.aspentech.com/S_Article?id=000096334
This approach is suitable for situations in which we have foreseen ahead of time the need for data sharing and would like to create a fix data sharing structure between objects. For copying data on a case-by-case basis, the user should consult the second option below.
Use script:
We provide an out-of-the-box script to perform data copy between objects. This script is a Method script that can be used for any types of equipment class. The script is named: "CopyObjectData" and located in the KBs folder:
C:\AspenZyqadServer\Basic Engineering37.0\WorkspaceLibraries\KBs\ExampleScripts\
The user will need to install this KB before it can be used. To install and execute a KB script. Please refer to the following article:
https://esupport.aspentech.com/S_Article?id=000062079
Keywords: None
References: None |
Problem Statement: When running cases in PIMS and using SQL server as an output database, no cases are running and the following error is showing: “The solution data was not written to the database. No reports will be created”
This error has been registered when using “Microsoft OLE DB Driver for SQL Server” as the driver in Provider tab of the Data Link Properties window. | Solution: To solve this error, go to General Model Settings > Output Database. Click the button with the three dots … next to “Connection String” field. In Data Link Properties window, go to All tab and check for any values in the Extended Propertied field. If there is something in this field delete it so it’s blank.
Click OK to save and exit. Try running PIMS again.
Keywords: PIMS database, case stacking
References: None |
Problem Statement: How will MIN and MAX blank entries in process limit rows impact matrix L/G rows in V10 and beyond? | Solution: In Aspen PIMS, PROCLIM table is used to impose limits on process conditions and recursed properties in a submodel. ZLIMxxx and Zproxxx rows are used create process limits and in the matrix Z rows will be replaced by E, L and G rows. In V10 and later versions, if there is no entry for MIN or MAX of Z rows, the corresponding L row and G row will become free rows.
For example, the MIN of ZSEV and MAX of ZCON are blank in PROCLIM and CASE tables. So, in the matrix, LLIMSEV and GLIMCON rows are freed.
Keywords: None
References: None |
Problem Statement: Why am I getting Input Errors (like Error 1166) when running a Fired Heater?
The specified flow sequence, through the convections banks and/or the firebox is inconsistent | Solution: Input Error 1166 concerns the flow history through the convection banks. For example, in the following screenshot the connections are then shown as in the second diagram. Stream 1 enters bank 3, then bank 1 and finally into the firebox. Stream 2 enters bank 2 only.
The user will need to define the "Process stream number in the bank" and the "Stream inflow from", Stream outflow to".
Keywords: Error, 1166, Fire Heater, Convection Banks
References: None |
Problem Statement: How do I create a new Border Label? | Solution: See attached Word document for the procedure for creating new Border Label. You will find a "PPIDcustom" KB script that is ready to be use with "Example1" label file. Further instructions to compile "Example1" label and customize "PPIDcustom" script are provided in the attached document.
Keywords: Border, Label, PPID
References: None |
Problem Statement: Which license keys are required to use Datasheets within ABE V11? | Solution: The License keys used by the different ABE Servers when connecting from Simulator (Aspen Plus/Aspen HYSYS) are:
Enterprise Server: License key - Aspen Zyqad when accessed from Datasheets button in Simulation or Safety Analysis environment (Aspen Plus and Aspen HYSYS).
Local Server:
License key - RN_EIE_ABE_ACTDATA when accessed from Datasheets button in Simulation (Aspen Plus and Aspen HYSYS).
License key - TR_EIE_ABE_PSVDS_LDB when accessed from Datasheets button in Safety Analysis (please note this is a tracking key)
Keywords: License Key, Aspen Basic Engineering, Datasheets, Simulation, Safety Analysis
References: None |
Problem Statement:
Is it possible to transfer data between heat exchanger design tools and ABE (Aspen Basic Engineering)? | Solution:
Exchanger design is an important task and is typically done in tools such as EDR or HTRI. During the FEED phase, users may need to obtain process data either from the simulator or ABE and then store calculated results back to ABE workspace.The amount of information involved in this workflow is huge. Hence automation can greatly enhance the workflow and increase the productivity of data transfer between ABE and EDR/HTRI.
This data import/export activity can easily be done with Thermal Design interface in ABE Explorer. Users have the flexibility to transfer data bi-directionally between ABE and EDR/HTRI.
In this example, you will find an EDR file (.edr) and a HTRI file (.dbo). By default, HTRI saves files as .dat files. But for the import, we need a .dbo file. To get this file, users can go to File > Export and choose the file type .dbo from within HTRI.
Steps to import data from EDR/HTRI to ABE:
A S&T (Shell and Tube) exchanger object should already exist within ABE. From Explorer, go to Tools > Thermal Design to open the interface. The first step is always to choose your exchanger and appropriate Case because immediately upon choosing the HTRI/EDR file, the data will be transferred.
Once the exchanger and Case have been selected, go to File > Import From > File… For an HTRI .dbo file, you will need to change the file type in the lower-right corner of the Open File window. Navigate to the file’s location and hit ‘Open’.
Open Excel Datasheet Editor and create a new ‘AT Shell And Tube Heat Exchanger’ datasheet to see the results.
To export data from ABE to EDR/HTRI, repeat the above steps but at step 2, select "Export To" instead of "Import From".
Keywords: None
References: None |
Problem Statement: Project items cannot be claimed in Aspen Basic Engineering V11 Drawing Editor | Solution: In V11, to claim an item in the Drawing Editor, users will find that they cannot select the items in the drawing to perform claiming. To perform this function in V11, users will need to first claim the drawing to be either "Shared" or "Exclusive." This will make the drawing available to the project (claiming the drawing status to be "Shared" does not necessarily claim all objects in the drawing - the claiming status of each object with respect to a project is prioritized and protected). Follow the steps below to perform claiming in V11 Drawing Editor:
1. In ABE Explorer, log in to the project you would like to claim the drawing, navigate to "All Diagrams" to show all drawings, then right click on the drawing you would like to claim > click "Claim" > Select either "Shared" or "Exclusive" and hit OK ("Shared" means the drawing can also be claimed by another workspace). If you would like to make this drawing available to other workspaces as well, repeat this step for the other workspaces.
In this screenshot, "Exclusive is grayed out because the drawing had already been claimed "Shared" by project "p1" and "p2." If it was a new drawing, both options should be available.
2. After the drawing has been claimed for the project, you can proceed to log in to that project in the Drawing Editor. Open the drawing. Now, you can select an object and click on "Edit" > click Claim to claim the object. As mentioned, the claim status of an object with respect to a project is prioritized over the drawing claim status.
Keywords: Drawing document, PFD, equipment claiming
References: None |
Problem Statement: Stream Summary Datasheet does not populate stream data in the correct order. | Solution: There are two things to check when the user finds their stream summary datasheet not populating data in the expected order (skipping columns resulting in blank columns):
1. Verify the index set for the attribute. Open the stream summary datasheet in the Datasheet Definer and verify that the columns are set with the correct increment and order.
2. Verify the column's Excel Field Name: As shown in the screenshots below, the first column has Field Name “Field3975”, while the next one is “Field3960”. ABE will populate 3960 field first and continue following the order (3961, 3962, etc.). Hence, ABE treats the first column as the last column even thought the index has been set correctly from step 1.
This issue would also cause any Sort KB to not work properly.
1st column:
2nd column:
3rd column:
Keywords: :
Aspen Basic Engineering, sort, wildcard not working, index not working, Datasheet Editor, KB script
References: None |
Problem Statement:
Why are Dimension Set and Dimension Units options grayed out? | Solution:
The Explorer interface provides the ability to change dimension set and dimension units for the entire workspace in Aspen Basic Engineering (ABE). Users, however, may find that these options are grayed out
User likely does not have appropriate privilege in his role. Each user role is assigned a set of privilege by the workspace administrator. Ensure that the current user have the required privilege to modify dimension set/units as shown below
Keywords:
Global units, global dimension
References: None |
Problem Statement: What are the different copy options in the Drawing Editor? | Solution: ABE has multiple options to copy an object. Below are descriptions of the available options:
Copy:
Users can create a copy of the existing object. This option will create a new object with attributes populated based on the original object. Data is only copied once. There is no live link between the two objects.
Paste Link:
Paste Link adds into the PFD a new symbol of the existing object. There is no new object created in this case. This allows users to add representation of the existing object in different PFDs without adding redundant objects to the workspace.
Clone:
Clone creates a new object with link to the existing object. The two objects will share data in certain attributes that have clone link turned on. Any data change in those attributes of either object will be reflected in the other object.
Keywords: : Aspen Basic Engineering, Copy options, Drawing Editor, Visual Representation, Icon, Symbol
References: None |
Problem Statement:
Why is ABE V11 Mapper Not Able to Transfer Second Liquid Phase Properties from HYSYS Simulation? | Solution:
With ABE V11 and V10 Mapper integration inside HYSYS, users can selectively transfer desired stream properties (or referred to as attributes in ABE environment) to be used in their datasheets. However, users may find that properties for second liquid phase are not transferred even though the attributes are selected to be transferred. This issue could be overcome via using the legacy Simulation Importer in ABE Explorer. We have also released patches to remedy this issue in ABE V11 Mapper. If users wish to use the Mapper rather than the Simulation Importer, they will need to install two patches - one for Aspen HYSYS V11 and one for ABE V11. The links to the patches are included down below:
https://esupport.aspentech.com/apex/S_SoftwareDeliveryDetail?id=a0e4P00000JBrXCQA1
https://esupport.aspentech.com/apex/S_SoftwareDeliveryDetail?id=a0e4P00000JnRJiQAN.
Keywords: :
ABE V11 Mapper, Second Liqiuid Phase, Data Transfer, Properties, Attributes
References: None |
Problem Statement: Name extension and limitations for the Workspace name in ABE. | Solution: The Workspace name has no extension limit for characters. The only characters not supported for names are the following:
\ / : * ? < > | &
Keywords: Workspace, Name, ABE
References: None |
Problem Statement: How to know if ABE V11 is installed in a user machine (Local Server)? | Solution: Since V11 for in Safety Analysis (for Aspen HYSYS and Aspen Plus) the Datasheets are now created with Aspen Basic Engineering (ABE). Please check the following article to know how: https://esupport.aspentech.com/S_Article?id=000065633
IMPORTANT: This information is to verify the installation of an ABE Local Server.
To know if this feature installed, check the following information:
Check the ABE applications are installed in the computer in Windows Start Menu | All Programs. Look for the Apen Basic Engineering folder.
In Task Manager | Services, the service AZ370 Broker must be listed and Running.
If these are not in the machine, it is necessary to install the features. ABE can be installed apart from the other Aspen applications. Follow the steps in the next article to install ABE V11:
https://esupport.aspentech.com/S_Article?id=000055845
Keywords: Safety Analysis, Datasheets, Aspen Basic Engineering, Installation, Local Server
References: None |
Problem Statement: How to use KB scripts in ABE? | Solution: KB scripts are codes written in VB.NET programming language. KB scripts allow the user to access objects and data in the workspace database. The codes can be used to automate data editing process by applying prescribed rules.
Below is the workflow to install and enable KB script for use in a workspace. It is assumed that user has already had their KB code ready.
Open Rules Editor (Go to Start > type Rules Editor - ABE V10) .
Paste your KB script into the editor window and make sure to have the correct code structure for your KB module type > Click on Tools tab > Compile.
Save the KB script into the corresponding KBs folder that the current workspace is using. Typically this folder is under C:\AspenZyquadServer\Basic Engineering19.1\WorkspaceLibraries\KBs
Navigate to the workspace libraries folder of the current workspace. Typically this folder is located at C:\AspenZyquadServer\Basic Engineering19.1\WorkspaceLibraries. Look for "StandardLibrarySet.cfg" and open it with notepad.
Add the following line under the line of KBScriptDirectory = "KBS"KBScripts = "<name of the kb you just created>"
Click File > Save to save the .cfg file.
Open ABE Administrator tool. Right click on the desire workspace and reload it.
After the workspace finish reloading, connect to the workspace in Rules Editor.
The script is now installed. For Rules and Methods types of script, users will need to execute it. For Events and Triggers, the scripts initiate automatically.
To execute a script, open Rules Editor. Make sure the desire workspace is connected. Click on Run tab > Select the appropriate script type to run (either Rules or Methods) > There will be a dialogue box prompting for KB selection to run. The new KB name should appear here.
Alternatively, users can also execute Methods or Rules directly from the Explorer interface. The navigation step is exactly as in the Rules Editor environment. The Explorer approach is more convenient to manage and review data changes, so it's intended to be used in production whereas the Rules Editor is intended for building and testing new scripts.
Keywords: None
References: None |
Problem Statement: Troubleshooting Offline-to-online task on Aspen Online projects | Solution: There are several ways offline-to-online task can fail, and each has its own troubleshooting workflows.
If offline-to-online fails to load the model:
Increase shared memory limit (see link) – once per machine.
Use SQLExpress for APED – once per installation
Fully initialize the simulator using the user account that is used by Aspen OnLine service – once per installation per account
Use same log on account for simulator as the AOL service
Account used for service does not have high enough privilege – use PsExec.exe (ATTACH) to run model as Local System and ensure it runs
Possible Cause Solution Comment
Shared memory limit is too small Increase shared memory limit (KB) Once per machine
SQLExpress isn't used for APED See "Failed to initialize APED" KB Once per installation
Simulator isn't fully initialized or does not have permissions to run Manually open the simulator using the AOL Service account (Use PsExec.exe if need to run as Local System). NOTE PsExec.exe is attached to this article Once per installation per account
If offline-to-online hangs due to invisible dialog:
No CPU associated with simulator and no error message (after message says Opening Simulator)
Use interactive service to make it visible, then correct model to prevent dialog boxes
If offline-to-online hangs fails with “BatchGet” issue:
There is an issue with a node inside the simulator
Set nodes per batch to 1 to see which one is causing the problem
Exclude the problematic node by adding VariablesToSkipDuringOff2On.txt to project folder (see KB94976)
Contact AT support at the same time so that we can patch the crash
Keywords: aol, offline, online, troubleshoot, model
References: None |
Problem Statement: Why is the Plant Data feature not opening/working on my simulation? | Solution: The Plant Data feature is used to connect your simulation to plant data in a data historian and/or in an Excel workbook and schedule runs using the latest data to monitor plant performance.
Plant Data achieves this by using another AspenTech product called Aspen OnLine. Aspen Online service must be running in order to use Plant Data features. You can check this using the Services dialog box on a Windows machine.
Since Aspen OnLine requires port connectivity and client-server enabled communications, any Aspen OnLine project needs to be stored in a local C: drive folder, otherwise, it will not work (Plant Data included). Note: You cannot use a network folder to store any part of the project.
Using a network folder as the Offline folder of a project is no longer supported. No part of the project may now reside on a network folder.
Files for models using Plant Data cannot be run from or saved to network drives.
Keywords: Data, plant, folder, aol, troubleshoot
References: None |
Problem Statement: How does the CO2 Freezing Utility calculate its point? | Solution: Aspen HYSYS uses the selected property package (limited to Peng-Robinson and SRK) to calculate the fugacities of CO2 for different phases and equate them as a condition for the equilibrium. The triple point of CO2 is also used to compute the CO2 Freeze Out Temperature.
Aspen HYSYS uses a modification of equation 1 from the article CEP_CO2FreezeReprint (attached) to calculate the activity coefficient for CO2 for the liquid and vapor phases;
The parameters shown in the equation are described in the “Nomenclature” session of the article attached. The modifications made from this equation follow the laws of thermodynamics and are proprietary to Aspen Technology. Thus, technical details cannot be divulged. However, the user may want to compare the results from the simulation to those from experimental data presented in the article attached.
The CO2 Freeze Out Utility uses the following algorithm to calculate the Freeze Out temperature for a defined stream:
The equilibrium data are retrieved from various sources and depend on the hydrocarbons present in the mixture (methane, ethane, octane, benzene, etc.) Some sources may be found in the
Keywords: CO2; Freeze Out; Utility; Triple Point; Aspen HYSYS;
References: .pdf file attached. |
Problem Statement: What is the recommended procedure to migrate Aspen Basic Engineering from one version to another version? | Solution: The attached document explains the important steps that we recommend users to follow when migrating ABE to a newer version. Migration in ABE involves copying and re-compiling template files in the libraries folder. Users should use this document as a guideline to ensure template files are properly migrated. In some cases, further care must be taken when users have a significant number of customization done in their workspace.
Note: the document was written for a migration from V9 to V10, hence the location path references ABE V9 and V10 folders. The guideline instructions, however, applie to any versions.
Keywords: Moving to newer version, workspace libraries, ztx and ztf recompile, generate datasheets in batch, symbols migration, KBs migration, datamodel migration
References: None |
Problem Statement: What is the scope of Rules and Global Methods? Do they apply to my sub-project workspaces? | Solution: When users create sub-projects in a master workspace. All KB scripts installed in the master workspace will be available for use in the sub-project. However, the scripts execution will be applied only to the currently logged in workspace. Sub-project is treated as a distinct workspace from its master workspace. This is the behavior for both Global Methods, Local Methods, and Rules as well.
Besides, the difference between Global Methods and Local Methods is rather on the subject it applies to. Local Methods apply the code to a particular object while Global Methods apply the code to all objects specified in the class.
Keywords: None
References: None |
Problem Statement: For many pieces of equipment, very little (if any) data is transferred to the ABE equipment from the simulation. This is because the simulations are typically very conceptual. For example, in a simulation a drum may only be simulated as having one inlet stream. But in reality, it could easily have 3 inlets. The same applies to compressors; some customers model a multi-stage compressor using a single compressor unit operation in the simulators. Others model each stage with its own individual compressor unit operation (i.e., 3 separate compressor units for a single 3-stage compressor) and interstage equipment. For this reason, upon import ABE doesn’t really know how the compressor is meant to be setup in the model, so no data is automatically populated on the datasheet.
In this example, the user always models each stage of a compressor as a unique unit operation in HYSYS. So they would have 3 compressors on their flowsheet, each one representing a stage of the 3-stage compressor. They wanted to be able to automate the population of process data to the compressor datasheet. | Solution: In the attachment, you will find a KB script that is used to run a Local Method on compressor objects. Install this KB script to your workspace before moving on. If you are not familiar with using KB script in ABE, please search for "How to use KB script in ABE?" article in our support site.
One or more (preferably 2 or 3) CentrifugalCompressor objects and Primary Streams with flow data should already exist in the workspace. Using one of the compressor objects, create a new datasheet using the out-of-the-box ‘AZ Centrifugal Compressor’ template. Run the local method ‘Set Comp. Stages’.
The first pop-up window is where the number of stages are specified and each compressor stage should be appropriately chosen from the drop-down list (i.e., if in the simulation K-100 is stage 1 and K-101 is stage 2, then these should be chosen respectively).
The next pop-up window will ask the inlet/outlet streams of each stage. Notice that the number of inlets/outlets is dependent on how many stages was specified in the previous window. After the appropriate streams have been selected, notice how the datasheet has now been populated with simulation data.
Also included in the KB is a filter for compressors that can be seen in Explorer and used wherever needed.
Keywords: None
References: None |
Problem Statement: How do I improve performance in PIMS v11 when the model folder is on a network drive? | Solution: The xpress file format was changed to "full format" from compact in PIMS v11 due to random PIMS crashes that were due to an issue with the xpress compact format. The writing of the xpress basis files may cause the slower performance in PIMS v11 compared to PIMS v8.8 when a model folder is on a network drive.
To get v11 running faster, you can do the following:
Open the model in PIMS using a UNC (Universal Naming Convention) path. In the Open Model dialog (menu option Model->Open), specify the UNC path in the top address bar. For example, specify \\machineName\folderName\PIMS_Model_Folder
If running a single case, then check the option "Perform Single Case Optimization on Separate Process" in the Parallel Processing tab in the Non-Linear Model (XNLP) settings (under Model Settings)
By opening the model using a UNC path causes a temporary folder to be created on the local machine for the xpress basis files. After the solve, the xpress basis and log files are copied to the networked model folder. By creating the xpress files locally and then copying them after they are created helps the execution performance.
The creation of the temporary folder for the xpress files are only done for case parallel thus the reason to run a single case using case parallel using suggestion #2 above. When running a case stack, case parallel is automatically used so there is no reason to have the option "Perform Single Case Optimization on Separate Process" checked.
Keywords: None
References: None |
Problem Statement: Organic Rankine Cycle example | Solution: The Organic Rankine Cycle or ORC unit is a system based on a closed-loop thermodynamic cycle for the generation of electric and thermal power, especially suitable for distributed generation. ORC systems can generate electric and thermal power exploiting multiple sources, such as renewables (biomass, geothermal energy, solar energy), traditional fuels and waste heat from industrial processes, waste incinerators, engines or gas turbines.
The Rankine Cycle technology is based on the principle used in power plants: a fluid is heated and evaporated into steam. The steam drives a turbine, which is connected to a generator to produce electricity. The same principle is held for ORC, but organic fluids or refrigerants are used instead of water.
The following example was made with water as the thermal fluid and iC5 as the process fluid. A Case Study was also generated to check how the thermal fluid flow rate directly impacts the power requirements for the compressors.
Keywords: rankine, cycle, organic, power, plant
References: None |
Problem Statement: .
The slug model concept is based on the principles from Bendikson (1984), where bubble/slug and mist flow models are implemented in the system. | Solution: .
Transition from slug to mist flow is numerically considered as a limit of the bubble/slug model. When the Bendikson (1984) model option is selected, the C0 and U0 velocity parameters are calculated by HYSYS for the general form of the translational velocity Eq1.
c = C0 Vm + U0 Eq1.
where:
c: translation velocity of slug
Vm: superficial velocity of two phase mixtures
C0: velocity constant
U0: centre mass averaged velocity constant.
Key words.
Slugflow constants, constants, slugflow.
Keywords: None
References: None |
Problem Statement: There are two different approaches that can be used to convert performance curves:
1. Convert operating point from off-design condition to reference condition, then calculate flow/head relation using the manufactory performance curves.
2. Convert manufactory provided performance curves from reference condition to Off-Design operating condition and calculate flow/head relation using the new curves.
In this article we will discuss about the approach used in Aspen HYSYS and how are the equations deduced for this approach. | Solution: Aspen HYSYS has always been intended to use approach 2, For V10 and newer versions, the equations are consistent with approach 2, which means that they convert manufactory provided performance curves from reference condition to off-design operation conditions.
Derivation of the equation:
We are considering the Mach number of the compressor. The Mach number (M) is the ratio of the flow velocity (V) divided by the speed of sound within the fluid (vsound).
The speed of sound can be calculated based on the temperature (T),
Where γ= adiabatic constant, R = gas constant MW = molecular mass of Gas, and T = absolute temperature, K1 = combined constant.
The relationship between compressor speed N and flow velocity can be written as
V = 2πDN = K2 N
Where K2 = 2πD and N is compressor speed. So, the Mach number can be expressed as:
If we assume the Mach numbers are same between operating condition and designed condition, where “ref” refers to the reference points on the manufacture performance map, and “act” refers to off-design condition, then we will have:
We will assume the compressor internal volume does not change, then we will have following relationship.
CONVERTING MANUFACTORY CURVES FROM REFERENCE CONDITION TO ACTUAL OFF-DESIGN OPERATING CONDITION
This will give us the speed formula we used in our Aspen HYSYS Help Guide:
We will have our volume flow formula in Aspen HYSYS help
Where:
Tref = Temperature at reference/design conditions
Tact = Temperature value from the simulation
MWref = Molecular Weight at reference/design conditions
MWact = Actual value of Molecular Weight from the simulation
Qcorr = Qact = Corrected volume flow in the curve
Qref = Volume flow in the original MW curve
Ncorr = Nact = Corrected speed for each corrected curve
Nref = Speed for the original MW curve
We use these formulas to create the corrected map for display, converting manufactory provided performance curves from reference condition to Off-Design operating condition and calculate flow/head relation using the new curves.
Keywords: Off-Design correction, corrected curves, compressor curves
References: None |
Problem Statement: When modelling compressors and expanders, it is possible to link them to other compressors or expanders to represent that their shafts are physically connected, but doing this provokes that only one of the linked compressors gets mapped by APEA. | Solution: Linking compressors and expanders in HYSYS means that:
1. The speed of each linked unit operation is the same
2. The sum of the duties of each linked compressor or expander and the total power loss equals zero
Linking compressors/expanders can be done in the Design tab, in the option Links, in the following image you can see that Compressor K-101 is linked to Compressor K-100:
Thus, when linking two unit operations and using the Activated Economics you will observe that just the unit which was linked is being mapped by Economic Analyzer.
This happens because when linking compressors in HYSYS, it means that both linked units are indeed one and thus they will be driven off by a common driver. The cost engine will design the machine based on the inlet and outlet conditions for the first stage and last stage that are linked, as you can see in the outlet specifications in APEA, and calculating the number of stages based on the specification provided. So, as these compressors are indeed just one and are using the same shaft, the power driver should be reported just once.
If you want to have two separate machines, you will have to unlink the compressors, map both of them and enter the driver power for the first compressor and then select no driver for the 2nd compressor in order to avoid double dipping.
Keywords: Linked compressors, APEA, Activated Economics
References: None |
Problem Statement: How to change the Mass and Molar Enthalpy sign? | Solution: It is possible to change the sign for the Mass and Mole Enthalpy values if the user needs to report in this form.
Note: These steps are only for change the way Aspen HYSYS reports the value. This won’t affect the calculations.
Please follow these steps:
1. Go to File | Options | Units Of Measure.
2. Copy any of the Units Sets you have or those by default and give it a name.
3. In Display Units list, look for an Enthalpy unit (Mass Enthalpy or Molar Enthalpy), select it and click on Add. In the new window name the new Enthalpy unit and here the user can input a Unit Conversion. There type -1 in the first textbox.
4. Click in OK for the User Conversion and for the Units Of Measure.
5. Now a new Enthalpy unit has been created in the new Units Set. Be sure to work with it in the Simulation environment.
This change will only apply to -kJ/kg. For another units, like -BTU/lb, the user must repeat the steps.
Keywords: Enthalpy, Mass, Mole, Unit Sets, Sign, Report
References: None |
Problem Statement: What do I do if my Aspen Online interface doesn’t open? | Solution: If customer is having problems opening the Aspen Online Graphical User Interface (GUI), first review the services list to see if the service “Aspen OnLine V11.0” is running.
Possible reasons for AOL service not running:
Service startup type is set to Manual
Service is set to Automatic, but the system is slow and service did not start up during reboot (set it to Automatic Delayed)
Incorrect/expired password for the log on account
SQL Express 2014 service not running (if using Local System account)
Instance not selected (if using Local System account)
Use “select instance” batch file (found under C:\Program Files\Aspen Online V11.0\)
If the service is running but GUI still can’t launch:
AOL Service appears to be running, but it didn’t connect to SQL or localdb or SQL Express successfully
Hanging AOL processes – stop service, kill process, start service again before restarting GUI
Look for log files in C:\ProgramData\AspenTech\ AspenOnLineV11.0\system
Keywords: aol, gui, launch, troubleshoot, problems
References: None |
Problem Statement: There is a yellow bar at the bottom while No error is found in Result | Message tab? | Solution: The yellow bar is due to the messages present in View | Error Messages: 'Networks where KO drums are present within a loop may not converge for multi-phase systems'
In this case, it is saying multi-phase separators may not converge in looped systems.
If the yellow bar is present, the user needs to verify convergence of the model. If the case has converged then, the user can ignore the yellow bar. If it didn't, the user needs to review the Error Messages list and resolve them.
Keywords: KO Drum, Yellow bar, Multi-phase separator
References: None |
Problem Statement: When the user makes changes to a pipeline event, for example Crude Pipeline Shipment and clicks on Events -> Refresh, the event does not revert to its original state. For other type of events, clicking on Events-> Refresh brings them back to their previous state. Please refer to the attached document for an example. | Solution: This is a known issue in APS and will be fixed in the upcoming patches in V10 and V11.
Keywords: None
References: None |
Problem Statement: How to adjust indexes by location? | Solution: Location Indexing lets the user manipulate the costs of a Code of Account (COA) range to make the project prices more faithful to the project location data. To do Location indexing, follow the steps below:
Right click in the Indexing form.
Click Select. Any index files available are listed, select the one you want to edit and click OK. The index file will be loaded, and the Select an Indexing File window will disappear.
Right click the Indexing form again and click Edit (or double click the Indexing form).
Double click Location(**) in the Indexing window. The Location Indexing window will open.
Type the location description.
In the From Icarus/User COA cell type the COA from which the range will start or click the red arrow to search by COA subcategories. Click the Select button in the COA Subcategory Selection window.
The Equipment COA Selection window appears.
Click Select in the desired COA. The COA will be automatically entered in the From Icarus/User COA cell.
Do the same in the To Icarus/User COA cell to indicate the end of the COA range.
Type the amount to escalate material costs and/or the amount to escalate man-hour costs. In this example, the price increases by 55% due to the location price difference.
To escalate another range, click Add.
Click OK to close the form and apply changes.
Note: This is different from the Change Plant Location to performed in the Decision Analizer since this Location Indexing does not affect the Quoted equipment
Keywords: Indexing, Location, Prices, Modification, Escalation
References: None |
Problem Statement: .
It is possible to import pre-build Flare models into a new Aspen Flare System Analyzer model, and there is no limit, but after trying to import more than 3 Flare models simulation crashes. | Solution: .
Once you have imported the third model into AFSA follow the listed steps, to avoid crash issues:
Save the file as new then.
Close the new saved file.
Open it again and import the missing models into the new one.
NOTE: You must follow the pattern of saving a new file once you have imported a third model.
The imported models will not have the same arrange that the original one, and it will be needed to manually order the pipelines.
Key words.
Import flare models, models, limit of flare models, import flare
Keywords: None
References: None |
Problem Statement: When trying to convert the input file from PORII to HYSYS V11, I get a message below:
Then no matter if I click “Cancel Selection” or “Continue with DBR Amines”, an error message pops out: "You cannot leave basic manager, please correct the issues manually and select OK to continue, cancel to stop model conversion". | Solution: It's caused by the property package. Since DBRAmine was sunset in V11, we are now using Acid gas package as a replacement.
To fix this, you can manually modify the inp. file by eliminating the highlighted line:
After the converting finished, added it back in HYSYS manually.
Key Words
PROII to HYSYS Converter
DBRAmine
Acid Gas
Keywords: None
References: None |
Problem Statement: When using Aspen Fidelis Reliability Flow Profiles and Pipe Flow Limits, once a pipe tries to go above a Pipe Flow Limit and then drops back to below the Pipe Flow Limit, Fidelis keeps a Unit Max Capacity value and applies it in the future when the Flow Profile continues to be dynamic. | Solution: This issue is present in AFR V11 CP2 (V11.0.2) and has been resolved in AFR V11 CP5 (V11.0.5). Please download the AFR V11 CP5 upgrade package using this link:
https://esupport.aspentech.com/apex/S_SoftwareDeliveryDetail?id=a0e4P00000MI8bJQAT
Keywords: None
References: None |
Problem Statement: How to resolve the error “Error starting service AZ370Broker. The service did not start due to a logon failure”? | Solution: When ABE Local Server is installed, by default an account is created to manage the Broker Service.
If during the software installation the following message appears the broker service can be started manually right after the installation:
The most common cause of this is an invalid password specified for the Broker account during the install.
Also, if the password given to this account is unknown, the user can create a new one.
IMPORTANT: This information is valid when working with ABE Local Server.
Follow the next steps:
Go to Computer Management
Unfold Local Users and Groups and double-click on Users
Right click on the Broker user (the default name starts with AZ370_...) and select “Set Password”.
For V10 the default name is AZ191_
Click on “Proceed in the next window.
Set the new password and confirm. After this, a confirmation message will appear.
Additionally, if ABE Local Server it’s been reinstalled, the old server password will persist after the new install. You must manually edit the password for the Broker Service and the Aspen Zyqad Server
Navigate through Control Panel | Administrative Tools| Services.
Right click on AZ370Broker (for V11) and select Properties. Note that for V10 the name of the broker is AZ191, for V9 is AZ181.
Select Logon tab and type the new password in.
Navigate through Control Panel | Administrative Tools | Component Services, click Computes | My Computer |DCOM and right click on Aspen Zyqad (XXX) Server and select Properties.
Click the Identity tab and enter the new password.
Click in Apply
Restart the AZ(XXX)Broker Service.
Keywords: ABE Local Server, Installation, Logon Failure
References: None |
Problem Statement: Model vanishes when it is opened or saved with a very long filename. | Solution: There is a limit to the number of characters for the filename plus path of 240.
This is a Windows issue not specific to Aspen Plus since Windows Explorer and other applications such as Notepad have the same issue.
Fixed in Version
In future releases, there will be a warning dialog upon saving indicating if the filename plus path is too long and give users a chance to enter a shorter name.
Keywords: None
References: : VSTS 415457 and 427474 |
Problem Statement: How to create a Workspace in a Local Server? | Solution: In the article https://esupport.aspentech.com/S_Article?id=000065633 shows how to create the Workspace from Aspen HYSYS and Aspen Plus web client to import PSV data and generate the Datasheets in V11.
The next steps are to generate a Workspace with the ABE Administrator. These steps are applicable for V9, V10 and V11.
For creating a Workspace with an ABE Local Server installed, follow these steps:
Go to Windows Start | Aspen Basic Engineering and open the Administrator application.
Go to Action | New Workspace
In the Create Workspace Wizard click on Next in the first screen. In the second, give a Name to your Workspace, a description (optional) and for Database Type select MS SQL Local DB.
Click on Next until the Wizard finishes.
Now the Workspace must be created and listed.
Keywords: Workspace, Solo Server
References: None |
Problem Statement: How to add Boiling Point Curves to a Workbook? | Solution: The following steps explain how to add the Boiling Point Curves values to the Workbook.
In Simulation environment, go to Workbook.
Under “Workbook” tab, go to Setup.
In the Setup page, add a new Workbook Tab.
From the list navigate to Utility Objects, select Boiling Point Curves and click OK.
For this new Tab, click on Add button to add variables.
In the next list the different standards are listed (ASTM D1160 Atm, ASTM D1160 Vac, ASTM D2887, TBP, etc) and other properties.
Navigate to the desired standard and unfold the option (e.g. True BP) and select every or the points to be reported. Then, add them in the list.
Click on Done.
Important: The curves listed in the Workbook are from the streams with the Boiling Point Curves Stream Analysis attached.
Keywords: Boiling Point Curves, Workbook
References: None |
Problem Statement: There are cases that we need to control the rate of change of a certain variable in a dynamic simulation. Let’s say, for example, that a controlled heating system has a limitation (or a constraint) that prevents it from heating the fluid at a rate larger than 5°C/min. This type of constraint will impose a difference in the total time for your system to reach the steady state that you may be interested in account for. How can we model this type of limit in Aspen HYSYS Dynamics? | Solution: 1. In the Model Palette, select the Transfer Function Block
2. Define your Process Variable Source (Optional) and your OP Target.
3. In the Parameters tab, configure the Maximum and Minimum Ranges allowed for your PV and OP.
4. Select the Rate Limiter Parameter and define your Max. Rate of Change for the variable previously connected. This rate can be configured either in absolute numbers or percentage.
Note: Do NOT forget to activate the Rate Limiter. If you do, even though it may be correctly configured, it will not execute during your run.
Once the rate limiter is activated, you can easily check the rate of change in a stripchart.
Keywords: Rate Limiter; Dynamics; Rate of Change; Aspen HYSYS;
References: None |
Problem Statement: How to change the date format globally for the datasheet in Datasheet Editor? | Solution: A user can run this query in ABE Explorer by following the instructions. After the user runs the query, any current datasheets or the ones the user wants to issue in the future will have the same format as dd-mmm-yyyy. For setting other different date formats, please refer to the document How to change the script.docx.
1. Open the query in Notepad.
2. Open ABE Explore and go to View -> Query Editor
3. Copy / Paste the query into Query Editor and click submit.
4. Check it by opening any of your current datasheets that have been issued. Please refer to this snapshot. You will see the same date format on the top right corner.
Keywords: Date format, Datasheet, Query Editor
References: None |
Problem Statement: How to solve connection errors when running APS/MBO with TLS 1.2 enabled? | Solution: APS/MBO do support TLS 1.2 from V8.8 CP6 onwards.
TLS 1.2 is supported when connecting to SQL Server in APS/MBO and there should be no impact on products, but correct updates to clients and servers should be applied. For V11 and later versions, APS/MBO are updating to .Net framework 4.7 so that problem with earlier versions of .NET framework is eliminated.
For SQL Server 2012 R3, Microsoft added support for TLS 1.2 to SQL Server 2012 R3 clients and server in cumulative update 1.
There is a catch for ADO.Net clients because TLS 1.2 is available only in the .NET Framework 4.6. For earlier versions of the .NET Framework, you may have to apply a Windows update so that ADO.NET can support TLS 1.2 communications for the client. The Windows updates that enable TLS 1.2 support in earlier versions of .NET framework are listed in the table in the “How to know whether you need this update” section of KB3135244 from Microsoft.
In some cases, the error message below could happen when opening APS/MBO model with TLS 1.2 enabled.
The error is related with security configuration. Followings are steps to solve the issue:
1.In Control Panel, click Administrative Tools, and then double-click Local Security Policy.
2.In Local Security Settings, expand Local Policies, and then click Security Options.
3.Under Policy in the right pane, double-click System cryptography: Use FIPS compliant algorithms for encryption, hashing, and signing, and then click Enabled.
4. Ran gpupdate /force in cmd
If it doesn’t work, please go to C:\ProgramData\Microsoft\Crypto\RSA and grant "Network Services" Read permission to "MachineKeys" folder. Then restart server to have a try.
APS SQL model DSN should be configured with “SQL Server Native Client” protocol, rather than “SQL server”.
Follow these steps and enable only TLS1.2 on SQL Server machine as well as machine where APS is installed.
Local security settings on SQL server machine:
Registry setting on SQL Server machine:
Enable only registry for TLS1.2. Disable other TLS and SSL registries if enabled.
Local security settings on machine where APS is installed:
Registry setting on machine where APS is installed:
Everything in the registry should be disabled except for TLS 1.2.
For custom tools or VBA macros for APS and MBO, the custom code should also be updated to use TLS 1.2 connection.
The connection string should be in following format.
Provider=SQLNCLI11;Data Source=xxx;Initial Catalog=xxx;UID=xxx;PWD=xxx;
Provider=SQLNCLI11;Data Source=xxx;Initial Catalog=xxx;Trusted_Connection=Yes;
Keywords: None
References: None |
Problem Statement: In real control processes, the response of the control system may not be immediate. To account for such time delays between the controller output signal and the process variable response, the concept of dead time (or time delay) will be used. How to consider this feature in Aspen HYSYS Dynamics? | Solution: s
In Aspen HYSYS Dynamics, the time delay must be configured by using a Transfer Block located under the Dynamics & Control session of the Model Palette:
Under the Parameters tab, configure the delay parameters (gain and dead time) with the desired values.
Note: Do not forget to check the "Delay" box under "Active Transfer Functions". Otherwise, even though the transfer block may be correctly configured with the desired parameters, the Delay task will not be active during the simulation run. This is valid for any transfer function you decide to use for this block.
Keywords: Dead Time; Delay; Time Delay; Controllers; Aspen HYSYS Dynamics;
References: None |
Problem Statement:
How to add new discipline to ABE? | Solution:
Discipline is a way to assign unique access to view and edit specific attributes in Aspen Basic Engineering. This feature allows multiple disciplines to collaborate together while preventing accidental cross-discipline data input. Follow the steps below to assign new discipline to your workspace:
1. Go to your Class Library Editor, pick a class attribute that you plan to assign the discipline to.
Right click on the attribute > Select Attribute Properties. On the Class Attribute window, click Edit next to Discipline entry.
Alternatively, you can right click on the attribute > Select Assign Discipline > A new dialog should pop up, and you can create a new discipline. Finish this step and recompile your class store as usual.
2. Open ABE Administration tool, reload your workspace. It's recommended to then close and reopen your Administration tool. After this, you should be able to see the new discipline when you try to add new discipline here.
Keywords:
Aspen Basic Engineering, mechanical engineering, process engineering, capital cost estimator
References: None |
Problem Statement: In Aspen HYSYS each time the user opens a file that contains a custom unit set, this unit set will be stored in the Aspen HYSYS preferences file | Solution: To clean all the custom unit sets that have been stored in Aspen HYSYS please follow these steps:
Open File Explorer/Windows Explorer
Type %AppData% into the address bar and click enter
Navigate to the AspenTech folder
With Aspen HYSYS closed, delete the file Aspen HYSYS V#.PRF
Keywords: Unit Set, Clean, Stored
References: None |
Problem Statement: Aspen HYSYS - OLGA compatibility | Solution: The HYSYS-OLGA Link Extension software enables you to combine an OLGA pipeline transient simulation with a Aspen HYSYS Dynamics process model. The OLGA Link is seamlessly added to the Aspen HYSYS flowsheet just like a standard unit operation. From within Aspen HYSYS, you then connect to an OLGA server, and load and run the OLGA model with inlet and outlet stream(s) connected to the HYSYS model.
The following table shows the compatibility between Aspen HYSYS, OLGA Link Extension and OLGA software:
Aspen HYSYS Version Default OLGA extension version in Aspen HYSYS OLGA version
V12 OLGA Link Extension 7.3.3 OLGA 2014.2
OLGA 2015.3.1
OLGA 2016.2.1
OLGA 2017.1.0
OLGA 2018.1.0
V11 OLGA Link Extension 7.2 OLGA 2014
OLGA 2015.3.1
OLGA 2016.2.1
V10 OLGA Link Extension 7.0 OLGA 2014
V9 OLGA Link Extension 7.0 OLGA 2014
Keywords: Compatibility, Aspen HYSYS, OLGA, Extension
References: None |
Problem Statement: Based on UHX-12.5.9 in the ASME code the equation is:
but Aspen Exchanger Design and Rating (EDR) Mechanical is showing:
Why the Diameter is equal to the Do or DL instead of showing 4Ap/Cp? | Solution: Aspen EDR Mechanical calculates the Ap (Area enclosed by perimeter) and Cp (Perimeter of the tube layout based on the actual layout) but if for whatever reason the actual layout is not available to calculate this:
Aspen EDR Mechanical will use Do. Otherwise it will use DL, the 4Ap/CP formula as shown above that corresponds to the Code formula.
Note: Using Do is always more conservative.
Keywords: UHX-12.5.9, Diameter, DL, Do, Ap, Cp
References: None |
Problem Statement: How do the RVP definitions in the Cold Properties Utility treat hypothetical components? | Solution: In Aspen HYSYS, the Cold Properties utility includes several methods to estimate the Reid Vapor Pressure as mentioned in the following article: RVP definitions in the Cold Properties Utility. Since the correlations are calculated flashing the fluid, it doesn't ignore hypothetical components.
Keywords: Hypothetical, Component, Cold Properties, Utility, RVP, ASTM correlation, API methods
References: None |
Problem Statement: How to create/modify a Datasheet Template in Datasheet Definer? | Solution: ABE includes several Datasheets templates in its Libraries. A user can modify an existing one or create one from scratch with the Datasheet Definer.
To create or modify, follow the next steps:
For modifying an existing Datasheet template, go to step 3.
For creating a new Datasheet Template, first build a draft in Excel and save it as .xlsm (Excel with Macros) type and place it in the route: C:\AspenZyqadServer\Basic EngineeringXX.X\WorkspaceLibraries\Datasheets.
Open the Datasheet Definer VXX, log in the Workspace and open the file from here (File | Open | File…).
Open the Datasheet Excel Template file (xml)
Important: if the file is opened directly in Excel, this procedure can’t be done.
Click on Datasheet button and give a Title and make sure to select a suitable Object Class View in the Datasheet option.
Add the fields (Values, Bitmaps, etc) in each cell.
Assign an attribute to each cell by selecting the cell and in the Field button.
With the document ready save the file and click on Validate the Fields to check for any error.
Click in “Generate Template” button and save the new generated documents in the next route: C:\AspenZyqadServer\Basic Engineering37.0\WorkspaceLibraries\Templates.
Be sure the name is the same as the Datasheet Title in step 3.
Two files will be generated with the extensions .ztf and .ztx.
Once the process is complete close the Excel application and open Administration - ABE V11.
Right click on the Workspace is being used and select “Reload Workspace”.
Keywords: Datasheets, Templates, Edit, Create, Datasheet Definer
References: None |
Problem Statement: What is the implication of negative flow in a run? | Solution: The reason the flow rate is negative in a node is because the pipe segments are attached backwards.
In Aspen Flare System Analyzer (AFSA), each pipe segment has two connection points: a red connection (upstream) and a blue connection (downstream); AFSA assumes a flow direction from upstream to downstream.
So, if the user connects the nodes backwards (from downstream to upstream) a negative sign will be added to denote that the actual direction of flow through the pipe is contrary to the specified connection.
Keywords: Negative, Flow, Direction, Upstream, Downstream
References: None |
Problem Statement: How to run collect in background using the task scheduler in windows. | Solution: The scheduled task approach can be performed with the following steps:
Create a file in notepad and copy the lines below where "C:\collect" is the directory where your collect input files are stored and "exmpl" is the name of your collect input file (the one with no extension).
call cd C:\collect
echo Y | collect -exmpl DCU_DEBUT
Save this file and change the extension from .txt to .bat and place it in the same directory as your collect input files.
Open Task Schedule, you can search for it from the start menu.
Create a Basic Task
Give it a meaningful name and description
Select to run the task when the computer starts, this way if the computer shuts down and comes back up it will restart and click Next Select that the task will start a program and click Next Click Browse and navigate to the location of the batch file you just created and select it.
3. Select the open to open properties after you click finish and click Finish. Set the properties as follows General Properties
4. Triggers
5. Actions properties
6. Conditions tab in properties:
Then click OK In Task Scheduler right click your new scheduled task to run collect and select Run Check Task Manager to confirm that collect.exe is running Wait 5 min and open command prompt to run an extract and confirm you are collecting data.
Log out of the system and log back in 5 min later and extract data again to confirm collect is still collecting data.
Key words:
Collect ,background
Keywords: None
References: None |
Problem Statement: In Aspen HYSYS, the user can integrate different heat exchanger with Aspen Exchanger Design and Rating (EDR) to perfrom rigorous calculations. However, in some ocassions this option is not available inside the heat exchanger. | Solution: This could be caused as the Aspen HYSYS and Aspen EDR versions are not the same or Aspen EDR is not properly install in the machine.
To solve this please follow these steps:
1. Ensure the default version for both products are the same by running the set version as shown in the following article How to run the EDR Set Version utility?
2. Ensure that all the require registries (attach in a pdf) have a registered state in the machine; if not register all
3. If the previous points are properly covered but still the issue persist, please contact for support assistance
Keywords: Integration, Heat Exchanger, Rigorous, Show, Available
References: None |
Problem Statement: How to select language for Aspen Tech Engineering products in V11? | Solution: In version 11, users can select the desired language for Aspen Tech Engineering products. The translation concerns only the interface of the programs Hysys, Aspen Plus, Aspen Properties and does not apply to the Help menu. The following languages are currently available:
English
Japanese
Chinese
Russian
The default language is English. After installing version 11, users can select desired language from the list using “Select Aspen Language Utility” tool.
Key words
Localization, select language, Language Utility
Keywords: None
References: None |
Problem Statement: Description of changes to the Aspen PIMS-AO Run Execution Dialog box for V11 | Solution: In Aspen PIMS V11, the Run Execution Dialog box has a few changes. Below is a screenshot of the updated dialog.
There is now an indication of how many cases have been selected and will run (see red box)
The Run Global Optimization option has been moved to the left (see blue box)
There is a new feature to automatically turn on infeasbility penalties which is shown below in the green box. Note that when this new Penalties feature or Global Optimization is turned on, you will also get a corresponding indication of this in the top banner of the dialog box as shown in the purple box.
Keywords: None
References: None |
Problem Statement: While generating the code for a Fortran procedure, I get the following error:
"No suitable C/C++ compiler was found - compilation aborted" | Solution: To use a Fortran procedure in ACM, the user is required to have the proper version of the Intel Fortran Compiler and Visual Studio installed on their machine.
Starting in V7.x and similarly in all 8.x releases, we only support the Intel Fortran compiler, which does not include Visual Studio but it requires it as a pre-requisite; because, the Fortran procedure code needs to interface with C++ code inside ACM.
The supported version of Visual Studio and Fortran Compilers for ACM V8.x, V9 and V10 are as follows:
Version Supported Fotran Compiler Supported Visual Studio
V8.0 Intel FORTRAN 9.0, 9.1, 10.0, 10.1, 11.0, 11.1 or 12.0 Microsoft Visual C++ .NET 2010 Professional edition
V8.4 Intel Fortran 9.0, 9.1, 10.0, 10.1, 11.0 11.1, 12.0, or 13 Microsoft Visual C++ .NET 2010 Professional edition
V8.8 Intel FORTRAN 9.0, 9.1, 10.0, 10.1, 11.0, 11.1, 2011 (V12), 2013 (V13), 2013 SP1 (V14), or 2015 Microsoft Visual C++ .NET 2013 Professional edition
V9 Intel FORTRAN 9.0, 9.1, 10.0, 10.1, 11.0, 11.1, 2011 (V12), 2013 (V13), 2013 SP1 (V14), or 2015. Microsoft Visual C++ .NET 2013 Professional edition
V10 Intel FORTRAN 9.0, 9.1, 10.0, 10.1, 11.0, 11.1, 2011 (V12), 2013 (V13), 2013 SP1 (V14), or 2015. Microsoft Visual C++ .NET 2013 Professional edition
V11 Intel FORTRAN 2017 Professional Edition or higher, 64-bit. Microsoft Visual Studio 2017 Professional edition or higher, 64-bit.
Please note that for version V9 and V10, exporting unit operations to Aspen Plus or HYSYS no longer requires a compiler.
KeyWords
Procedures, Fortran, ACM, Visual Studio
Keywords: None
References: None |
Problem Statement: Sometimes you might see the following error message pop up after validating the matrix.
What could be the cause of this? | Solution: This is because the user only generated the matrix but didn’t solve it. That’s why PIMS will pass the validation phase but not actually generate any results. Please make sure you have “Solve Matrix” option enabled in the run dialog box.
Keywords: None
References: None |
Problem Statement: IP21 installation hangs up while performing the pre-install steps.
Depending on your Windows operating system version and service pack revision, files downloaded from another computer may have their block property set as a preventive measure. The files must be unblocked prior to the AspenONE installation. | Solution: Unblocking of all the files may be achieved when the zip file itself is unblocked before its contents are extracted. If the installation zip file was extracted before the block property was checked then Delete all the AspenONE installation files and folders that were created when the zip file was extracted. Unblock the zip file by right-clicking the zip file and selecting the Properties option from the context menu and then clicking Unblock, if shown. Note; if the Unblock button is not shown then the files are already unblocked.
Extract the AspenONE installation files again and proceed with the installation.
KeyWords:
blocked
freezes
Keywords: None
References: None |
Problem Statement: How to Resolve the Data Results Pane Not Showing in the Results Window in PSCP? | Solution: Sometimes after you configure your input Excel tables correctly and run the model, the detailed data pane showing results including Supply, Demand, Inventory, etc doesn’t show up in the Results Window. This data is used to generate DPO_SOLUTION_BREAKOUT tables in the Access database and sometimes we’d like to copy the data to an Excel spreadsheet or query it to better analyze. How should we resolve this?
Go to Regedit, and delete key HKEY_CURRENT_USER\Software\AspenTech\Aspen Petroleum Supply Chain Planner.
Restart PSCP and re-run the model again. You should able to see the data populated again now.
Keywords: None
References: None |
Problem Statement: Sometimes if we open a PIMS model that has text column entries in a different language, we might see the characters changing to strings of messy code instead of regular language. How to avoid this? | Solution: First, make sure the Language Selector option is set to the language that you’d like to display. You can do a search in start for “Language Selector”.
Then you’ll need to go to Control Panel -> Clock and Region -> Region. Change everything to the country of that language you are trying to display.
Keywords: None
References: None |
Problem Statement: How to Display the Breakout Column Data from the Results Window to show in the Access Database? | Solution: 1. In Program Options in PSCP, go to General -> Check “Use Breakout Columns in Solution Output Tables”. This will make warning message 3160W go away if you are experiencing it.
2. In PSCP, go to Run -> Run Single Case -> Report Option -> Select Breakout Tables option.
3. Run the PSCP model. After it finishes running, go to Results Databases section and right click on the Results.mdb file. Select Write out Breakout Tables option.
4. Check in the Results.mdb file and see if the DPO_SOLUTION_BREAKOUT tables are populated with new data. If you have any Excel queries, you should also be able to pull them from these tables now.
Keywords: None
References: None |
Problem Statement: Add or remove clients to an existing license reservation file. | Solution: To add or remove users from the reservation file, first, go to the following route on the license server:
C:\Program Files (x86)\Common Files\AspenTech Shared\SLM Administration Tools
And Execute the file: Wlsgrmgr.exe
Once it opens, click on the File option, and then click on Open.
Proceed to select the current reservation file lsreserv located in the following route:
C:\Program Files (x86)\Common Files\SafeNet Sentinel\Sentinel RMS License Manager\WinNT
And click Open:
Note: you can create a backup of the current reservation file before editing it.
Select on the lower half of the screen the group created on the reservation file, right click on it and select the Properties option.
On the Properties window, select the Members tab and to add new users or computers click Add.
Proceed to add the user name, this must be the Active directory user name with the User option and Included selected. Press OK to finish, repeated this step for each user to add.
If you wish to delete any user, just select it from the list and click on the Remove button. To finish click the OK button.
Save the modified file, for that select the File option and then click Save. This will overwrite the reservation file.
The following step is to activate the reservation file, and this step will restart the license service, so Ideally, there shouldn’t be any application using AspenTech license at this moment.
To activate the reservation file, on the license server, go to the folder:
C:\Program Files (x86)\Common Files\SafeNet Sentinel\Sentinel RMS License Manager\WinNT
Run the loadls.exe file with administrator rights and click the Remove option, then run the Loadls.exe again with admin rights and this time click on the Add option.
Keywords: None
References: None |
Problem Statement: I have set up a SQL database for PIMS results - that works fine. However, the tool does not active when selected, either from the PIMS menu or by directly running DbMain.exe. The mouse pointer changes briefly and then nothing else happens. How to get it work? | Solution: The first thing you should check if you have privileges to create the folder "Pims Database Management" under the ProgramData folder. The full path is C:\ProgramData\Aspentech\Pims Database Management. This folder is where the settings for the Pims Database Management tool will be stored. The user will need to have access to this folder.
Two workarounds to try:
- Try running PIMS with elevated privileges. Right-click on the PIMSWIN.EXE and select "run as administrator".
- See if you can manually create the "Pims Database Management" folder at C:\ProgramData\Aspentech. Then run the database management tool from PIMS and see if it works.
If you are not able to create the folder, then this will be a problem because the tool will try to save the settings file there.
If that is not the case, please delete two files: connectionsHistory.xml and connections.xml in folder C:\Users\<username>\AppData\Roaming\Aspen Technology Inc\Pims Database Management.
Keywords: SQL Server Management Tool
results
database
References: None |
Problem Statement: Unable to install .NET Framework 3.5 on Windows Server 2012.
For Windows Server 2012, you need to use "Add or Remove Features" to install .NET Framework but encountered the following error. "Specify an alternate source path"
Specifying alternate source via command line failed as welll.
dism.exe /online /enable-feature /featurename:NetFX3 /Source:D:\sources\sxs /all
Cause
This behavior can be seen if the system is configured to use Windows Server Update Services (WSUS) instead of the Microsoft Windows Update server for servicing. | Solution: 1.Start the Local Group Policy Editor (gpedit.msc) or Group Policy Management Console(gpmc.msc).
2.Expand Computer Configuration, expand Administrative Templates, and then select System.
3.Open the Specify settings for optional component installation and component repair Group Policy setting, and then select Enabled.
4.Select the Contact Windows Update directly to download repair content instead of Windows Server Update Services (WSUS) check box
5. Ensure Windows Updates Service is set to Manual or Automatic
Keywords: .NET Framework 3.5
References: None |
Problem Statement: This knowledgebase solution documents common issues with installation and licenses. | Solution: 1. Ensure ports 5093 and 5094 UDP and TCP are open – The SLM server uses these ports to communicate over the network and without it, can cause installation issues. Often, we see complications with 3rd party software such as Symantec and MacAfee which despite being disabled locally will still operate a domain policy preventing these ports passing through. You can ensure the required TCP and UDP Ports are open by using IPerf - How to ensure that the TCP / UDP port required by the Aspen installer to connect to the SLM Server are open?
2. Install the prerequisites – Within the aspenONE installation media is a folder - 3rd Party Redistributables. This contains Microsoft .NET Framework 3.5 and 4.6.2 which are both required for the AspenTech software to run correctly. In some cases, MS SQL Express 2012 is required too. Many Windows components are required to be installed ahead of the setup.exe. A list of these can be found here including IIS – for server - How to enable IIS on Windows Server 2012 R2 and for desktop - How to enable IIS in Windows 8.1
3. Running setup.exe as an Administrator – ensure that you have the correct rights to install the AspenTech software. Being a user with power user rights is not enough and you must be a local or domain administrator. Consult your local IT to assist with the installation if you are unsure.
4. Using a dongle – If using a dongle, problems can often surface if the driver has not been installed correctly. You will need to obtain an aspenONEDVD (engineering or manufacturing). Run the setup.exe and click the install and configure SLM software icon from the Welcome screen. Expand SLM Tools and check the dongle driver checkbox, followed by clicking Next. Plug the dongle into the USB port once this has completed. To confirm that the dongle is working, run the SLM Configuration Wizard and click the Config button. If you see Sentinel Hardlock at the top of the Locking Information screen, then the dongle is working.
License won’t install
The SLM manager can get confused very easily by multiple license files, so checking the installation directory for multiples and duplicates then removing these can assist. Remove all of the license files to a temporary folder and reinstalling the license file as per this article - How do I install a new license file?
KeyWords
Howto
Licensing
SLM
Keywords: None
References: None |
Problem Statement: License Server can’t be running and the warning 85 is displayed on the event logs | Solution: License server is not running and there are the warning 85 in the Windows application logs as below.
“Sentinel RMS License Manager was unable to initialize from the license code”
Please check the License file as follows.
Windows Start -[All Programs] - [AspenTech] - [AspenSLM] -[AspenOne SLM License Manger]
Click [License Profiler], License Profiler window appears.
On the [ License server], select [Local License File]
On the [License File], select your license file.
Click [Load Information]
Click [View License], then the license key information is displayed.
Please check [Birth Date]The license file can be used from the date set on [Birth Date].
If the date set on the [Birth Date] is later than the current day, this license file is not valid at the moment.
Please try to use this license file from the date set on the [Birth Date]
Keywords: SLM
Warning 85
References: None |
Problem Statement: What is the procedure for requesting an emergency license? | Solution:
When your license server is down due to unforeseen circumstances, you can request an emergency license to use while you work on restoring your service:
To request an emergency license, following the steps below:
1. Collect the information needed for AspenTech to generate the license:
A) License System Name: it can be obtained by opening your current license file with the Windows Notepad. The System Name is the last field in the first line, as outlined in red below. You can also provide a copy of your file to AspenTech.
B) SLM Locking Information from the from the server in which you will be installing the license. Run the locking utility from the following article.
2. Call the Support Hotline at 1-888-996-7100 and select option 0. This is the recommended method for contacting AspenTech when you are facing a critical and urgent issue. A support representative will work with you to generate the license.
Keywords: License Request
Emergency License
Temporary License
References: None |
Problem Statement: What difference between pressure drop calculation methods across the Orifice in Aspen Hydraulics? | Solution: There are several calculation methods for the pressure drop across the Orifice in Aspen Hydraulics:
Static Pressure Balance: Assumes no pressure drop.
Total Pressure Balance: Ignores frictional pressure drop. Includes accelerational pressure drop.
Contraction / Expansion: Model the orifice as a contraction to the throat, followed by an expansion to the outlet pipe, using the selected Swage Calculation Method
Crane - 2 Phase: Calculates frictional pressure drop using the K factor from Crane Technical Paper 410. For two phase flow, uses equivalent density based on two phase multiplier from HTFS Design Report 38 (available on Exchange).
Crane - Homogeneous: Calculates frictional pressure drop using the K factor from Crane Technical Paper 410. For two phase flow, uses overall/homogeneous density.
HTFS: Calculates pressure drop using orifice model from HTFS DR38.
The Compressible Transition defines the pressure drop as a fraction of the inlet pressure at which compressible flow pressure drop calculations will be used. For fractional pressure drops larger than the specified value, compressible calculations will be used. Specify 0 to always use compressible calculations or 1 to always use incompressible calculations.
From the Swage Calculation Method drop-down list, users can select one of the following methods:
Total Pressure Balance: Ignores frictional pressure drop. Includes accelerational pressure drop.
Crane - 2 Phase: Calculates frictional pressure drop using the K factor from Crane Technical Paper 410. For two phase flow, uses equivalent density based on two phase multiplier from HTFS Design Report 38.
Crane - Homogeneous: Calculates frictional pressure drop using the K factor from Crane Technical Paper 410. For two phase flow, uses overall/homogeneous density.
HTFS: Calculates pressure drop using swage contraction/enlargement models from HTFS DR38.
Key words
pressure drop, Orifice, pressure balance, Swage Calculation Method, HTFS, Crane
Keywords: None
References: None |
Problem Statement: Is it possible to install Hysys V9.0 and PIMS V10.0 on one machine? | Solution: Different version of Engineering and MSC are not coexist on one machine due to DLL files sharing between them.
Key words
Different versions, installation, version compatibility, Engineering and MSC
Keywords: None
References: None |
Problem Statement: How do I set my Stream Summary Template as the “default template” for my entire simulation in Aspen Plus? | Solution: In the new stream summary report (or stream results folder), you can set your own template to select only the properties you wish to see. In order to do that, please follow the steps below:
1. Open the simulation whose stream summary you would like to customize.
2. In the stream results summary page, customize the report so that it shows your properties of interest and save it as a new template.
Note: if you would like to know more about stream report capabilities, please refer to the KB Article: Stream Summary Workflows in Aspen Plus V9.
3. Now, to set your new template as the default template for all your streams, go to File >> Options >> Advanced
4. Scroll down to Stream Results Summary session and change the default template to the one you've just created.
5. Apply the changes and your template will be available to all your streams as the default setting whenever you access the stream results page.
Note: It is important to notice that these changes will only be applied to the streams whose results were not previously manually changed. It does NOT overwrite any previous changes made by the user in the streams report summary.
Keywords: Stream Summary; Aspen Plus; Template; Customize; Default;
References: None |
Problem Statement: Is there a way to limit how long a license can be checked out? | Solution: AspenTech currently doesn’t provide a mechanism to restrict the usage of licenses to a certain time limit. Based on our experience, AspenTech recommends that such restrictions be managed through internal advisory policies and guidelines. Administrators can use aspenONE SLM License Manager or SLM License Profiler to review usage and duration. Usage monitoring can also be scripted using a the lsmon command line utility. Refer to https://esupport.aspentech.com/S_Article?id=000093745 for more details
Keywords: SLM
Software License Manager
Sentinel RMS License Manager
References: None |
Problem Statement: Some of the dependent variables are OFF in the DMC controller but the Control Weight column shows a non-zero weight for them. Are these Control Weight values just for display or do they actually have weight in the dynamic move plan calculation when the variables are turned off? | Solution: This control weight value you see is not just for display purposes and it is being used, just not directly within the dynamic move calculation. The weight is used to ensure the ECE tuning across all CVs remain consistent before going into the dynamic move plan. CVs that are Off are not actually included in the dynamic move plan, since we don’t care where they go or how they move, but they do have an impact on the CVs that are On, like a pre-processing step before going into the move plan.
This is by design and is done to prevent a change in the tuning if a variable status changes. The ECE tuning is all relative, the ratio between the ECEs is what matters to the controller dynamic move plan. If you turned Off a CV and dropped its ECE from comparison, depending on what its ECE values were, other CVs could become more or less important dynamically. The purpose in calculating the control weights is to ensure consistent dynamic tuning across all variables even as variables are turned Off or On.
As an example, if you had a dynamically important CV turned Off and we dropped its ECEs from consideration and suddenly turned it On, then variables that were being controlled tighter would suddenly have looser dynamic control as the more important variable was being focused on. This inconsistency in the behavior would make dynamic tuning more challenging, as you would have to consider how the CVs behaved based on which CVs were On or Off.
In fact, with the current behavior, you can change a dynamic ECE for a variable that is Off and depending on how much you change it, you can force the dynamic behavior of CVs that are On to change. I don’t advise making dynamic tuning changes to variables that are Off but having consistent behavior when variables are On or Off is the reason that this is observed.
Keywords: : control weight, controlweight, pcws, dmc, cv, dependent
References: None |
Problem Statement: Getting A1PE users list from Aspen Process Data Rest through SQLplus | Solution: Attached to this solution there are two text files that will be needed to perform this solution. Please follow the next steps.
Download the the text file named “LicenseCall” and put it on Disk C, inside the folder named “temp” so the route to the file will be c:\temp\licensecall.
Right click and Edit the file, on line 6 change the “user” and “password” to a user and its password that has access to the web server
Change the name of the file from LicenseCall.txt to LicenseCall.vbs
Download the text file named “GettingA1PEusers” and copy the contents of the text file into Aspen SQLplus Query Writer.
After running the query, a list of the users that have A1PE open will be shown
Keywords: A1PE users
APDRest
SQLplus
References: None |
Problem Statement: Aspen IP.21 Configuration Excel Add-In can be used to create InfoPlus.21 tags as well as update/create Cim-IO transfer records with reference to the names of items in the Distributed control system. It does this with the assistance of SQLplus procedures stored in the database.
KB 134444-2: How are the ProcedureDef records used by Aspen InfoPlus21 Configuration Excel Addin created? describes how these procedures are created the first time the various add-in functions are used.
There have been some known issues with the execution of the Aspen IP.21 Configuration Excel Add-In which can be resolved by installing improved SQLplus procedures. | Solution: In detail, the latest procedures should fill in free occurrences in existing transfer records that have the exact required configuration you selected on the configuration panel in Excel. If there are insufficient free occurrences in such existing records then new transfer records will be created. If you do not want it adding occurrences to existing transfer records then you need to update their sizing fields to remove the free occurrences. Perhaps whatever problem you are experiencing can be resolved in that way.
The second suggestion is to remove the existing procedures from the Aspen InfoPlus.21 database and allow the Add-In to recreate them. In Aspen InfoPlus.21 Administrator, locate AtXl_DbSchema (defined by ProcedureDef) and "Make Unusable" and then delete the record, repeat for AtXl_UpdateTags. You can then recreate them by simply using the Aspen IP.21 Configuration Excel Add-In. You can then determine if the problem you were experiencing has been resolved.
If problems persist, you can import the executable code of the procedures using a recload file provided in the attachments section of this knowledge base article (download the file now). Then delete AtXl_DbSchema, AtXl_UpdateTags records from the database (and also AtXl_GetDefRecs which is included in the file) using the same method as described before. You can then install new versions using the recload utility. To do this, in Aspen InfoPlus.21 Administrator, right click the database node in the tree and select "Load Records..." context menu.
On the "Load Records" dialog, select the "Available in this system" radio button, specify the full path location of the AddinConfigProc.rld file and then click OK. You should see similar results to this:
Loading Records from File <path>\AddinConfigProc.rld
- AtXl_DbSchema
- AtXl_GetDefRecs
- AtXl_UpdateTags
Text Records Loaded from File <path>\AddinConfigProc.rld (702 lines)
To avoid confusion, you should also delete the associated (now obsoleted) sql source files from the $COMPRESS_SOURCE folder (default path = C:\ProgramData\AspenTech\InfoPlus.21\db21\group200\sql).
Note, the attached recload file was created with the procedure code created for MES V11 Cumulative Patch 1. It can be used on V10.1 and V11.0 InfoPlus.21 databases.
Keywords: Invalid target for assignment: reserved word "AS"
Error writing to
Field is not changeable
AT_IoGet_0010_0002 1 IO_TAGNAME
Invalid RECORD value
AspenTech.SQLplus.DataProvider
AsnInv
References: None |
Problem Statement: How to make Oligomer volatile when using equations of state method? | Solution: Equations of State method is using fugacity coefficient for flash calculation so the oligomer is volatile in default. Segment property is used for the calculation of oligomer. But the volatility may not be a correct because this model is purposely designed for high molecular polymer. User need to adjust following parameter to get the reasonable volatility.
- Adjust parameter for Segment. (For example, PCSFTR, PCSFTU and PCSFTV need to be adjusted)
You can see the test result, the test has been done for Ethylene oligomer with 5 repeat unit and Hexane mixture.
For this case, only the PCSFTR of ethylene segment has slightly adjusted from 0.04 to 0.03
Keywords: PC-SAFT, Oligomer
References: None |
Problem Statement: How to make Oligomer volatile when using activity coefficient method? | Solution: Activity Coefficient method is using PLXANT parameter for flash calculation. But the default PLXANT value for polymer (or oligomer) is set to low value to disable the vaporization. And most of polymer activity coefficient method (except PNRTL-IG) is using RK EOS for vapor fugacity calculation. User need to adjust this value if needed.
User need to adjust following parameter to make the oligomer volatile.
- Adjust PLXANT parameter for Oligomer.
- Adjust TC, PC, OMEGA to reasonable value, default value from POLYMER Databank has very high value.
The test has been done with POLYNRTL method for Ethylene oligomer with 5 repeat unit. Phase diagram has calculate with Hexane.
Keywords: Activity Coefficient, POLYNRTL, Oligomer
References: None |
Problem Statement: Why am I not getting a warning message when my PSV line velocity exceeds the defined limit (set as percentage of sonic velocity)? | Solution: The velocity constraints are applied for single-phase (not homogeneous) line sizing. This line sizing method is only available for vapor and steam orifice sizing; direct integration orifice sizing will always use homogeneous line sizing regardless of the fluid phase. In V10 homogeneous line sizing, we don't calculate a critical velocity, thus the velocity constraints (which are related to the critical velocity) do not have any effect.
We addressed this limitation with the Aspen Hydraulics-based line sizing in V11, where we can calculate a critical velocity for any flowing fluid state and use it as a reference for velocity constraints, though note that in the Hydraulics line sizing in V11 we only support an outlet velocity constraint.
Key Words:
Safety Analysis, velocity limit, exceed sonic velocity constraints
Keywords: None
References: None |
Problem Statement: Can I use an input solution generated in a previous case of the same PIMS run? For example, I run cases 1 and 2, but I want an input solution created from case 1 to be the input for case 2. | Solution: PIMS has Table CASE keywords that can be used to do this. Keyword SAVESOL tells PIMS to save an input solution file with the number designated in column B. For example, this entry tells PIMS to create input solution file 1 at the end of solving case 1.
Once that input solution file is created, subsequent cases can use it via the LOADSOL keyword as shown below. As shown in the following image you can use the keyword SAVESOL 1 to save an input solution while solving Case 1, and then you can use the keyword LOADSOL 1 to use this solution as an input solution for Case 2. As shown in Case 2, you can generate a new input solution and also use the previously generated solution.
One thing to keep in mind when doing this is that it assumes the cases are being processed sequentially and that case 1 has finished and created the file before case 2 begins. If the cases are run on a single processor then this will be the case. However when parallel processing is used, you cannot control the order of the cases and case 1 may not yet be complete when case 2 is begun. In this scenario, the file would not yet be available and this could result in an older version of the file being used (from a previous run of case 1).
Note 1:
LOADSOL and SAVESOL
Keywords: are not supported in 3rd normal format of Table Case.
References: None |
Problem Statement: Aspen Process Explorer and Process Data have been installed on a machine, however when Excel is opened, the Process Data Add-in does not load. | Solution: The error can be caused by:
- Problem related to the registration of the new Excel Process Data Add-in.
- Problem related to the installation of the VSTO (Visual Studio Tools).
- Problem related to the installation of Microsoft Office Interop files.
1. For problems related to the registration of the new Excel Process Data Add-in:
Please download the attached file, ensuring you use the appropriate version for the Operating System (32 or 64bit).
Once the file is downloaded, change the extension to .BAT and run from a command prompt.
It is best to run the Command Prompt with Administrative rights: Right Click on the Command Prompt icon in Windows and select "Run As Administrator".
Once this has been accomplished and if no error is returned, retest using the Excel Process Data Add-in.
If an error is returned it is most likely the inability to load the GAC (Global Assembly Cache) extensibility.dll version.
2. For problems related to the installation of the VSTO (Visual Studio Tools):
Follow the link below to download the latest version of Microsoft Visual Studio Tools for the Microsoft Office System (VSTO):
https://www.microsoft.com/en-us/download/details.aspx?id=56961
Once the installation has completed, reboot the machine and retest. You may need to re-run the .BAT file mentioned above.
3. For problems related to the installation of Microsoft Office Interop Files:
To verify if the files are correctly installed you can navigate to c:\windows\assembly folder and find Microsoft.Office.Interop.Excel file, Version 12 is for Excel 2007 and version 14 is for Excel 2010.
If the file is missing, go to the following sites to download the Interop assemblies:
Office 2010
Office 2007
Once downloaded please install and then reboot the machine and test.
Keywords:
References: None |
Problem Statement: How to simulate Polyurethane with Aspen Polymers Plus? | Solution: Polyurethanes are a family of polymers produced by pseudocondensation reactions involving diisocyanates. They are characterized by the presence of urethane (~NHCOO~) groups in the polymer backbone. These materials are used to produce adhesives, engineering plastics, and foam sheets.
The attachment contains the Aspen Plus simulation files and a Word document which explains the reaction mechanism and rate expression. The Aspen Plus file also illustrates how to define the non-databank segment in a polymer simulation.
KeyWords
Polyurethane
Segment
Polymer
Keywords: None
References: None |
Problem Statement: This example demonstrates how to estimate the solid enthalpy of formation (DHSFRM) and the solid Gibbs free energy of formation (DGSFRM) of a compound to match the temperature of sublimation and the enthalpy of sublimation. | Solution: For components of type "Solid" the reference state is defined through the solid enthalpy of formation (DHSFRM) and the solid Gibbs free energy of formation (DGSFRM). If these properties are not given, they can be estimated from the temperature of fusion/sublimation and the enthalpy of fusion or sublimation, respectively. Note: Normally, you would do a data regression, but this would involve two adjustable parameters (DGSFRM and DHSFRM) using only one data point (i.e., the heat of sublimation at temperature of sublimation) which is likely to be unsuccessful. So it is necessary to use a workaround.
This example uses carbon dioxide. From the literature we know that CO2 sublimes at -78.4 C, with the enthalpy of sublimation being 6.030 cal/mole. In the example file, the stream class is set to MIXCISLD and CO2 is listed twice on the Components Specifications Selection sheet, with different component IDs. One ID is designated as a solids phase component, the other as a fluid phase component.
A simple HEATER can be used to enable the use of design specifications. The HEATER operates at the temperature that is assumed to be the temperature of sublimation. Note that both the input stream and the HEATER are at -78.4 C, our target temperature: The goal is to manipulate the thermodynamic parameters while the system has to be isothermal to avoid latent heat effects, etc.
The heat of sublimation is the difference between vapor and solid enthalpy. This is set in a design-spec with DHSFRM being the variable. The equilibrium condition (equality of chemical potentials, GV = GS) is used in a second design-spec to obtain a value for DGSFRM. Note: You need to access a results variable (dummy) in order to get the right sequence for the calculation. Alternatively, you could set the sequence on your own. The resulting parameters can be entered in Properties/Parameters/Pure Component.
KeyWords:
Solids
Thermodynamic parameters
Keywords: None
References: None |
Problem Statement: Using RPlug with countercurrent coolant, Aspen Plus calculates the coolant inlet temperature and overwrites the temperature of the inlet stream. To confirm this calculation, the following message appears in the control panel:
INFORMATION WHILE CHECKING INPUT SPECIFICATIONS
BLOCK NAME: B2 MODEL NAME: RPLUG
RPLUG WILL CALCULATE THE THERMAL AND PHASE STATE
FOR THE INLET COOLANT STREAM
If the user wants to set the coolant inlet temp it is possible to use a design specification. In the design specification the user can vary the coolant outlet temperature in the RPlug or the flowrate of the coolant.
If the user accesses only the temperature of the inlet coolant stream, difficulties will arise. If the coolant outlet temperature is varied, AspenPlus gives the error message that no sampled calculated variable is being set for the specification. If the coolant flow is varied, the simulation runs but the design specification does not seem to work. | Solution: This is a known problem in Aspen Plus. The Aspen Plus simulator is sequential which means that information is supposed to always flow downstream. However, in some cases such as this one certain blocks push information backwards.
The design specification checks that information is sampled that is actually dependent on the varied variable with the implicit assumption that information only flows downstream. For the case if the coolant outlet temperature is varied, this results in an error message since the defined variable is upstream of the manipulated variable.
The sequence algorithm knows that the design specification needs the coolant inlet temperature. If the coolant flow is varied, the design specification convergence loop does not contain any blocks since the only variables involved are in the coolant stream.
The trick for both cases is to define an additional dummy variable that is actually downstream of the RPlug block. The design specification information checker will be satisfied since a defined variable is downstream of the manipulated variable. Also, the sequence generated will include the RPlug block once there is a variable downstream of the block that is defined,
An example file is attached.
KeyWords
RPLUG
COUNTER-COOL
DESIGN-SPEC
Keywords: None
References: None |
Problem Statement: How is it possible to decant an aqueous - hydrocarbon mixture using the Free Water approach?
Inconsistent temperature profiles occur when decanting a fluid through an adiabatic/isobaric Flash3 model using Vapor-Liquid-FreeWater for the global phase selection. Even though the flash specifications are Pressure Drop = 0 and Duty = 0, the outlet product temperatures are higher than that of the single feed stream. | Solution: Most users intuitively use the Flash3 for decanting. This is a good choice for chemical systems where a rigorous two liquid flash is desired. However, for petroleum mixtures where the shortcut of using Free Water (assuming that the aqueous phase is pure water) is being used, a Flash2 with a Water Decant stream should be selected. There are no phase qualifiers in the Flash3 model; therefore, it performs only a Vapor-Liquid-Liquid flash and not a Vapor-Liquid-FreeWater flash.
In the above problem, a feed that has been flashed using a Vapor-Liquid-FreeWater phase enters the Flash3 block. Then, the Flash3 model performs a Vapor-Liquid-Liquid flash. The 2nd liquid phase leaves as an aqueous phase stream saturated hydrocarbon (usually saturated with trace amounts of hydrocarbon) and not a pure water stream.
Since the fluid enters using the results of Vapor-Liquid-FreeWater flash, and leaves the Flash3 using the results of a Vapir-Liquid-Liquid, there is a thermodynamic inconsistency which manifests itself by a temperature change.
Conversely, the Flash2 model''s water decant stream is actually a pre-defined free-water phase stream. Only pure water (steam table) is assumed to leave in the water decant product stream. The Flash2''s valid phases should be set to Vapor-Liquid-FreeWater and a product stream should be connected to the water decant product port on the Flash2 icon on the flowsheet. Since the feed in this case is flashed using Vapor-Liquid-FreeWater and the products are flashed using Vapor-Liquid-FreeWater, the temperatures are consistent for an adiabatic, isobaric flash.
Note: The Decant block does not work well for FreeWater calculations. Even with the Decanter''s Liquid-FreeWater calculation option selected, inconsistent temperatures are calculated.
Attached is a file that compares the results using Decant, Flash2 and Flash3.
KeyWords:
Petroleum, Free Water, Vapor-Liquid-FreeWater, Decant
Keywords: None
References: None |
Problem Statement: Are there any application simulation examples delivered with Aspen Plus? | Solution: Application examples are delivered with Aspen Plus. These simulations are delivered as backup files with associated output formatting files within the Aspen Plus GUI directory in a sub-directory called app, e.g., C:\Program Files\AspenTech\Aspen Plus xxxx\Gui\App. Fortran files are also included for user subroutines.
There are also many other examples available on the Online Technical Support Center's Example Library for Aspen Plus.
Delivered Aspen Plus Examples
The following files are available in the app sub-directory:
Filename(s)
Demonstrated Application
3phase.bkp
Reactive Distillation production of methylchlorate by
esterification of chloroacetic acid with methanol.
The Aspen Plus features demonstrated are:
1) Reactive distillation
2) Three-phase distillation
3) Column with total boilup (i.e. zero liquid bottoms flow
rate)
4) Internal column specification with feed flow
manipulation
5) Use of Decant model
bayer.bkp
usrbay.f
bayer.tff
h2o_only.tff
Bayer digestion circut where gibbsite (Al[OH]3) is removed
from bauxite.
The Aspen Plus features demonstrated are:
1) Hydrometalurgy uses of simulator
2) Design specifications
3) In-line Fortran
4) Sensitivity analysis
5) Stream report format customization
cdu.bkp
Atmospheric crude tower.
The Aspen Plus features demonstrated are:
1) PetroFrac model
2) Tray-sizing and Tray-rating
3) Tray property reporting
pen.bkp
penext.f
penfrm.f
This flowsheet models a penicillin recovery system using a
Podbielniak extractor.
The Aspen Plus features demonstrated are:
1) In-line Fortran
2) Sensitivity Analysis
solvent.bkp
Separation of acetone and methanol using water to break
the azeotrope.
sour.bkp
sour.tff
Removal of hydrogen sulfide, ammonia, and carbon dioxide
from water.
The Aspen Plus features demonstrated are:
1) Electrolytic distillation
teg.bkp
Sensitivity analysis of gas drying with TEG.
The Aspen Plus features demonstrated are:
1) SR-POLAR equation of state - application in high
pressure non-ideal system
Polymerization Examples
The following files are available in the app\Polymers Plus sub-directory:
Filename(s)
Demonstrated Application
hdpe.bkp
usrprp.f
Solution polymerization of ethylene.
ionicSB.bkp
Ionic polymerization of Styrene Budadiene Rubber in a
batch reactor.
ldbe.bkp
usrhpe.f
This flowsheet models a high-pressure LDPE tubular reactor
flowsheet with four sections, two initiator injection
points, and high and low pressure separators.
nylon6.bkp
This is a model of a NYLON-6 process VK column reactor.
pmma.bkp
Polymerization of methyl methacrylate(MMA) in a batch
reactor.
pp.bkp
Ziegler-Natta gas-Phase polymerization of propylene.
ps.bkp
Styrene polymerization in two CSTR's followed by a plug
flow reactor.
psea.bkp
Regression of propagation and termination rate constants
for a styrene-ethyl acrylate Batch reactor.
sbd.bkp
Copolymerization of styrene and butadine in a batch
reactor.
sty_dist.bkp
Optimization of inhibitor concentration to supress
formation of polystyrene in a column reboiler.
suspensionEPS.bkp
usrgel.f
Expanded Polystyrene Suspension Batch Polymerization
rigorously accounting for 2 liquid phases with reactions
occuring in organic phase
userfort.dll
Pre-build user DLL for usrprp.f usrhpe.f and usrgel.f
userfort.dlopt
Dynamic Linking Options file for userfort.dll
KeyWords
applications
Keywords: None
References: None |
Problem Statement: How is it possible to create non-databank ion, salt and a completely dissociated electrolyte? | Solution: Attached is an example on how to create non-databank ion, salt and a complete dissociated electrolyte.
The values for the parameters entered in this example are all fictitious and meant for example only. The minimum number of parameters needed were entered.
The parameters for the new salt and ions are entered on the Property/Parameters forms.
The parameters entered are as follows:
New Salt:
MW
Molecular Weight
DHSFRM
Solid enthalpy of formation at 25 C
DGSFRM
Solid free energy of formation at 25 C
CPSDIP
Coefficients for the DIPPR solid heat capacity equation
VSPOLY
Coefficients for the Solid molar volume equation
PLXANT
Coefficients for the Extended Antoine vapor pressure equation
New Electrolye:
MW
Molecular Weight
DHSFRM
Solid enthalpy of formation at 25 C
DGSFRM
Solid free energy of formation at 25 C
PLXANT
Coefficients for the Extended Antoine vapor pressure equation
New Ion:
MW
Molecular Weight
DHAQFM
Aqueous enthalpy of formation at infinite dilution and 25 C
DGAQFM
Aqueous free energy of formation at at infinite dilution and 25 C
PLXANT
Coefficients for the Extended Antoine vapor pressure equation
The first element of PLXANT is set to -1e20 for all new components in order to make these components non-volatile. See solution 104189 for more details.
The chemistry for the salt dissocition and the complete dissociation of the new electrolyte is added to the Reactions Chemistry Global form.
Chemistry:
NEW-SALT <--> NEW-ION+ + CL-
NEW-ELEC --> NEW-ION+ + OH-
Keywords: ion, electrolyte, salt
References: None |
Problem Statement: How to simulate the Claus process | Solution: The textbook version of the Claus Process is:
2 H2S + SO2 -> 3 S + 2 H2O (750 F, 25 psi) (1)
User can use RGIBBS or REQUIL to simulate the process. REQUIL would be a good choice if user knows the distribution of different sulfur forms in the product streams so that the equilibrium reactions can be entered accordingly, such as:
2 H2S + SO2 -> 3 S + 2 H2O
(2)
10 S <==> 4 S2 + 0.25 S8
(3)
On the other hand, RGIBBS does not require user to enter any reactions and it will figure out the distribution of different forms of sulfur in the product stream by minimizing the gibbs. Therefore, RGIBBS is recommended.
In modeling the Claus process, user should not follow Reaction 1 to use S to represent all the elemental sulfur products. Using S would result in an incorrectly low sulfur yield. According to a paper by J. Chao (J. Chao, "Properties of Elemental Sulfur", Hydrocarbon Processing, November 1980, p217-223), the most abundant sulfur vapor species present at high temperatures is mainly S2 (diatomic sulfur). At low temperatures (room temperature), S8 is the more stable form. So at high tempeatures, one can select S2 to represent sulfur and enters the reaction in REQUIL as:
2 SO2 + 4 H2S = 3 S2 + 4 H2O (4)
This will result in a significant sulfur yield. On the other hand, if one enters Reaction 1, very little sulfur would be generated. Using S instead of S2 is most likely the source of error in modeling such sulfur processes. At lower temperatures, user should consider add S8 to the component list.
Two example Aspen Plus simulations are attached. The simple model contains two RGIBBS blocks operating at two different tempeatures (450 F and 1000 F). At 450 F, the model shows S8 is the most significant product. At 1000 F, the overall conversion was reduced, but the S2 in the product stream increased. This is a very reasonable result for these two cases. The more complex example includes a burner and separators to model a 2-Stage desulfurization unit.
The physical property parameters for the vapor species S2 through S8 are available in the INORGANIC databank. The model uses the Ideal property method and only databank property values. Note that accurate modeling of the Claus process requires accurate theromodynamic data for the different forms of sulfur pertinent to the physical property models selected. The information given here serves as a guideline for user to consider.
KeyWords
RGIBBS
Claus
Sulfur
Keywords: None
References: None |
Problem Statement: An Example of Styrene Production from Ethylbenzene - Badger process | Solution: Attached is a rudimentary Aspen Plus model for styrene procuction by the Badger Process. The process information and conditions used in the model are based on Kirk-Othmer "Encyclopedia of Chemical Technology", 3rd Edition, John Wiley & Sons, New York, 1980. Vol 21, page 783.
KeyWords:
Styrene
Ethylbenzene
Badger
Keywords: None
References: None |
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