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Problem Statement: Does the Aspen InfoPlus.21 Mobile application support SSL Encryption (HTTPS protocol)? | Solution: Yes. We recommend that all customers use SSL encryption (https protocol) for any data that is sent over the internet. This certificate needs to be purchased separately from a third party vendor. For more information/Microsoft solutions on how to configure IIS to use the https protocol please refer the Aspen InfoPlus.21 Mobile Implementation guide
Keywords: InfoPlus.21 Mobile
SSL Encryption
https protocol
References: None |
Problem Statement: What are the uses of a dataset? | Solution: We can use the dataset for three things:
? Interactive Steady State Detection Tuning (in AOD Desktop you can drag and drop the dataset onto the application to initiate the SSD Tuning dialog)
? Trend view of the historical data (in AOD Desktop double-click on the dataset)
? Make an initial guess at input engineering limits (using the Initialize button in the Input Validation tab of the Configure Application dialog)
Keywords: Usage of dataset
References: None |
Problem Statement: If an ACM model uses user provided libraries (the *.acml files), where should the *.acml files be placed such that the ACM model driven by Aspen Online Deployment would be able to access them? | Solution: On the target machine where the ACM model would run, manually place the associated *.acml files in folder C:\Program Files\AspenTech\AMSystem V7.1\Lib
Keywords: acml, library
References: None |
Problem Statement: Using Aspen IP.21 Browser Graphic Studio, a project is published to aspenONE Process Explorer but when viewing a preview image on the Menu Tree in the Process Explorer web site the user is presented with a completely black image:
You also notice that the problem appears to be random, sometimes you see the expected images after publication and other times one or many images appear blank. Why is this happening? | Solution: When publishing graphics the Aspen IP.21 Browser Graphic Studio is taking a screen capture for each one. This can go wrong if it is disturbed by switching to another window, etc. This is easily reproduced by opening one of the Aspen demo projects and publishing it to aspenONE Process Explorer but click the minimize button immediately after you begin the process. After it has completed you will see that all the images in the publish path will be the same black image.
The apparent random nature of this can be explained by the fact that sometimes you may have switched the active window away from Graphic Studio when publishing a large project and other times you did not.
If you find such an unexpected preview image then you will have to republish the graphic, making sure you leave the application window open and visible.
Keywords: jpg image
picture
screen capture
References: None |
Problem Statement: Is is possible to use Aspen Framework (AFW)/Aspen Local Security in order to secure Aspen InfoPlus.21 Mobile application? | Solution: No. Aspen InfoPlus.21 Mobile uses its own security model (either Microsoft Windows Active Directory or Windows Local Security) in order to secure access to pages and tags. However we can connect to an Aspen InfoPlus.21 system that uses database security from this mobile application. For more information on how to accomplish this please refer the solution 131154
Keywords: InfoPlus.21 Mobile
AFW Security
References: None |
Problem Statement: When deploying a composite (CLP) application with DMC3 controllers (CCF + MDL3 files), the controller never become active in CLP, but the log files show that the controllers are checking-in into the CLP and the CLP is performing the calculations. However, the results are not implemented by the individual controllers. | Solution: The root cause of the problem is that CLP at this point does not work with the multi-objective optimization performed by Smart Tune. CLP still uses the traditional single objective optimization and provides the CLP targets, Cost and Cost criterion to the controller variables. However, since the furnace controllers in were configured with Smart Tune, they cannot use the information provided by CLP. Thus making it seem as if the CLP is not running. The fix to this issue is to disable the configure Smart Tune configuration using the steps below-
1. Uncheck the "Configure Smart Tune configuration using APC Builder" switch in the CCF | Options (under the General tab) and save the settings.
2. Navigate to the Configure section of the CCF using the left side panel, locate and set SMTENB = 0
3. Reload the updated CCF file online.
This will get the CLP and controllers communicating properly once again. Please note that it is important to perform all three steps listed above in order to disable Smart Tune.
Keywords: CLP
Composite
Smart Tune
DMC3
MDL3
References: None |
Problem Statement: The pack rating section in a RadFrac block is causing this error message:
PRESSURE NOT UPDATED DUE TO PRESSURE DROP CALCULATION ERRORS.
What is the cause of this error? | Solution: The error occurred in the pressure drop correlation, which is based on plots. In some situations, extrapolation has to be used to calculate the pressure drop and the results might be unreliable. Therefore we issue an error message when the "Update section pressure profile" is checked to warn the user. The message is quite generic as we cannot state exactly under which conditions meaningful to the user, the error detected may occur. The error may occur because the predicted pressure drop is excessive, or very small. You can avoid the error by turning off the pressure update to check the results.
The status of this error has changed from version to version. For example it was happening in older versions such v7.3, but it was simply not reported.
In V9 we changed the default pressure drop correlation to Wallis as we found that it is more reliable and accurate in most cases.
Keywords: radfrac, tpsar, packing, pressure drop, CQ00731961
References: None |
Problem Statement: How to validate the BAD data before input data goes into input calculation module of Aspen Inferential? | Solution: This article describes about the process of validating any bad data as input, before it goes to the input calculation module of Aspen Inferential?
1. Open Aspen Inferential quality (IQ) config -> Right click on Validation folder-> properties
2. Select the inferential name and Input Calculation, in the module. Specify the variables you wish to validate for BAD value. Select Add.
3. The entry will be added as shown below.
4. It can be further specified, whether the BAD data is due to flatline, spikes etc. To set that, go to the “Data Validation� section.
5. Select the detection criteria. The last highlighted section helps to specify the value that will be used to replace the BAD value.
Once the above procedure is completed, the inferential can be loaded online, using Aspen APC manage or Aspen production control web server.
Keywords: Input calculation module
BAD data validation
IQ Config
Inferential
References: None |
Problem Statement: After creating a Cim-IO interface to the Zenon OPC UA server, using Cim-IO Test API to attempt to read data from the UA server, it failed with the following error.
Status is 'Request Failed'
Facility=78
Driver Status=1002
or
Status is 'Bad Tag'
Facility=78
Driver Status=1006
The browse path to the UA tag is as follow:
Objects/SICAM_UA/OPC_GWY/B217_SERVER&!B217AKCTRL/GGI017/AnIn4/mag.f[MX]
Using 3rd party OPC UA client such as UA Sample Client from OPC Foundation, there is no issue in reading value from the UA tag in the Zenon OPC UA server. | Solution: In order to read data from Zenon OPC UA server in Cim-IO Test API, it is necessary to escape certain characters using the ampersand (&) character.
For the UA tag in questions, the following characters need to be escaped with ampersand character.
· exclamation mark (!)
· dot character (.)
As such, the browse path to use in Cim-IO Test API will be as follow:
Objects/SICAM_UA/OPC_GWY/B217_SERVER&!B217AKCTRL/GGI017/AnIn4/mag&.f[MX]
Keywords:
References: None |
Problem Statement: While trying to register the Aspen Process Data COM add-in specifically the file named AspenTech.PME.ExcelAddin.ProcessData.dll using the batch file available with KB 134243 and KB 135431, you may receive the error "RegAsm : error RA0000 : Could not load file or assembly 'Extensibility, Version=7.0.3300.0, Culture=neutral, PublicKeyToken=b03f5f7f11d50a3a' or one of its dependencies.". This solution explains how to resolve this error. | Solution: The following folder must be present in order to register the ProcessData.dll: C:/WINDOWS/assembly/GAC/Extensibility/7.0.3300.0__b03f5f7f11d50a3a/
Check to see if it exists by using CD command in a command prompt window:
Alternatively, look for Extensibility using File Explorer. See folder C:\Windows\assembly:
This assembly is installed with Microsoft Office but for that to happen you must also have all the required installation options selected.
Assuming that the assembly is missing but you have already installed MS Office then you must add “.NET Programmability Support” in order to register the add-in. To do this, follow these instructions:
1. Open Programs and Features from the Control Panel.
2. Right click Microsoft Office and click Change:
3. In the Microsoft Office installer wizard select the “Add or Remove Features” radio button and click Continue button.
4. Expand the Microsoft Office programs tree, select Microsoft Excel and right click the “.Net Programmability Support” option. Select “Run from My Computer” to install it:
You should then be able to run the batch file without seeing the Extensibility error.
Keywords: MS Office
Excel
References: None |
Problem Statement: How are STCVMAX/STCVMIN linked to STCVDELTA in V7.3.0.3?
In V7.3.0.3, the SmartStep parameter STMLIMLNK became obsolete. It appear that the test limit (STCVMAX/STCVMIN) and operator limits are still linked by the test margin (STCVDELTA), although it is not possible to choose how they are linked anymore. So, based on that, how these parameters are connected on V7.3.0.3? | Solution: Internally, STCVMAX/STCVMIN are set to the same values of UDEPTG/LDEPTG. However, when a step move is calculated, it uses STCVMAX-CVDELTA and STCVMIN+STCVDELTA as the effective CV limits.
Keywords: None
References: None |
Problem Statement: SmartStep 6.0 / 6.0.1 has been installed and the application will not start.
SmartStep manage is started, and it flashes only and does not come up.
User goes to a dos window and navigates to aconline/bin and
attempts to Start the SmartStep from a dos prompt and gets a SmartStep initialization error. | Solution: It has been determined that with some installation, the mpf region creation has not be done completely. If you go to windows explorer and look in the aconline/sys/mpf folder, there should be a smartstep.dir. If this file does not exist, it indicates this is most likely the reason for the application no starting.
Go to a dos prompt and issue the following command:
smartstep_manage -s X ( X being the number of SmartStep applications that you expect to be running.)
Start SmartStep Manage.
KeyWords
Keywords: None
References: None |
Problem Statement: Variables incorrect marked as critical even though they were not originally set as critical | Solution: The problem shows up only on controllers where the Critical Status Indicator (CRIDEP and CRIIND) parameter is read from a DCS tag. When the communication between APC server and the OPC gets disconnected, the controller is unable to read the CRIDEP from the DCS tags, and therefore it automatically reset this to 1 (critical) internally to keep the controller process running. This results in the message that the variable is marked critical even though it doesn't show up as critical on the Web.
Keywords: CRIDEP
CRIIND
Critical Status
References: None |
Problem Statement: Do min/max test moves up/down parameters affect user target changes? | Solution: Yes, the user target move will follow the same constraints as specified by STMVMAXU/D. This means, if the requested target move size is larger than STMVMAXU/D, it will be implemented over sequential cycles.
It may seem that the target move is being reset by the max test move, so that large moves require multiple target changes. The minimum test move may also appear to be interfering with the small target moves that do not get written out.
As long as the application is running a Test mode, the move size in a single cycle is always bounded by the STMVMAXU/D and STMVMINU/D, both for a calculated step move or a user initiated target move. However, STMVMAXSTEP only affects a calculated move; not the target move.
It is a known defect that when using MultiTest mode, the user target move more than STMVMAXU/D will only be implemented in one cycle for a size up to STMVMAXU/D and the remaining will be forfeited. This defect has bee fixed in V7.1.
Keywords: test, moves, target, smst, smart step
References: None |
Problem Statement: How can a SmartStep Tester be removed from the Webviewer?
An attempt was made to unload & delete a SmartStep application from SmartStep Tester Manager. It became clear in Manager that the application had been removed, but the Production Control Web Server continued to show the application. Then the user decided to restore normal DMCplu control via creating the DMCplus controller from DMCplus Manage. The DMCplus controller was successfully created, loaded and running. This part of DMC status was correctly reflected in the PCWS. | Solution: The action to take in this situation is stopping and restarting the dmcp_viewsrv.exe on the DMCplus server. There are batch files in the AspenTech Shared directory, dmcpview_shutdown.bat and dmcpview_startup.bat. Running these batch files and stopping and restarting this process will not disrupt the running applications.
Check for the dmcp_viewsrv in the process list of the Task Manager, double click the dmcpview_shutdown.bat in the AspenTech Shared directory. Confirm the dmcp_viewsrv.exe is no longer in the process list in the Task manager. Double click the dmcpview_startup.bat and confirm the dmcp_viewsrv.exe returns to the process list.
Return to the PCWS and use the Scan Now button on the Preferences page to refresh the offer from dmcp_viewsrv.
Keywords:
References: None |
Problem Statement: No Aspen SmartStep Application in Installation List of Products | Solution: You can run our new combined 2006.5 version of SmartStep/DMCplus onlines with only a Aspen SmartStep online license. It will throw you into Aspen SmartStep mode and not let you leave it.
A DMCplus online installation license key is needed to get the combined software installed.
They should already be getting DMCplus Desktop keys with Aspen SmartStep so that they can build the models and applications. This is unchanged from early releases of Aspen SmartStep.
DMCplus_Desktp_Inst
DMCplus_Model
Smartstp_Tester
Keywords: None
References: None |
Problem Statement: Michael Harmse provides this comprehensive document on automated response testing techniques.
His tutorial makes extensive use of examples and illustrates the latest features.
Many examples and usage guidelines are provided. | Solution: Download the attached pdf file (about 9 Mbytes).
Keywords: DMCplus
SmartStep
References: None |
Problem Statement: How to reduce the size of the files produced by PIMS-AO optimization execution. | Solution: There are settings that can reduce the size of the files produced by PIMS-AO run. Note that if all of this output is turned off, some features may be affected. Try to turn options off and then if necessary, specific options can be reactivated to support functionality that is needed.
In the Reporting Settings > Outputs tab:
1. Uncheck "Save Case MPS Files"
2. Uncheck "Create MPSBCD File"
3. Uncheck "Create XLR File"
4. Uncheck "Create XLPTC File"
5. Check "Delete *.map and *.fil Files at the End of the Run"
In the Reporting Settings > Selection tab:
1. Uncheck all the selected reports
In the XNLP Settings > Advanced tab:
1. Set Trace Level to None
In the General Model Settings > Miscellaneous tab:
1. Uncheck "SAVESVF"
2. Uncheck "CRUDEXLS"
3. Uncheck "Save Copy of Assembed Tables to Spreadsheets Using Excel"
In General Model Settings > Output Database tab, button Options:
1. Uncheck "Output MpsBcd Database Data"
2. Check "Compact Database"
3. Uncheck "Create Report Writer Queries"
Keywords: PIMS-AO
Setting
References: None |
Problem Statement: Depending of network configuration, ports used by CIM-IO need to be assigned to use specific ports numbers. This solution provides step-by-step guide on how to properly assign specific ports number for a CIM-IO for OPC configuration. | Solution: Changes on ports numbers should be done directly on Windows service file on CIM-IO server having related process stopped, to do this:
On InfoPlus.21 Server:
1. Open InfoPlus.21 Administrator and locate the Logical Device record which you wish to change ports number under the CIM-IO node; select it and set the value of IO_DEVICE_PROCESSING to OFF.
2. Open InfoPlus.21 Manager and stop tasks related to the task (TSK_A, TSK_M, etc. for example, if you logical device is called OPC1, then you should fine TSK_A_OPC1, TSK_M_OPC1, etc.)
On the CIM-IO server:
3. Open CIM-IO Interface Manager (CIM) and stop the logical device by right click on it name on the left tree and select Stop; close the application after it. (See note 1).
4. Go to C:\Windows\System32\drivers\etc and look for a file call Service, open it on a notepad with admin privileges (it is not recommended to use other text editor different than notepad).
Edit the entries related to the logical device, for example, for a logical device called OPC1, entries on this file should be like:
OPC1_SCÂ nnnn /tcp
OPC1_STÂ nnnn /tcp
OPC1_FWÂ nnnn /tcp
OPC1Â nnnn /tcp
Where nnnn correspond to the port number for each CIM-IO process (scanner, store, forward and asyncdlgp). Ensure that Service file end with an empty line, for example:
(See note 2)
5. Re-open CIM-IO Interface Manager. You should see the new ports number under the Port colum once the logical device has been selected on the left tree. Right click on it and select Start.
Back to InfoPlus.21 Server:
6. Open InfoPlus.21 Manager and start the task stopped on step 2.
7. Open InfoPlus.21 Administrator and set back IO_RECORD_PROCESING to ON (this was previously set to off on step on step 1).
Note 1: Starting with V8.4 a tool called CIM-IO Interface Manager is provided as tool to create and manage logical devices for CIM-IO, you can find more details on solution 140186. If you’re using a previous version, logical device processes should be stopped using the InfoPlus.21 Administrator or the StartStop.exe utility on CIM-IO server.
Note 2: Starting with version V8.4 ports numbers are not required to be written on the Windows’s Services file on the Aspen InfoPlus.21 server. If you’re using a previous version, ensure that Services file on both machine (Infoplus.21 and CIM-IO server) have the same ports numbers and entries.
Keywords: CIM-IO
Ports
References: None |
Problem Statement: Can we incorporate component fugacity into adsorption isotherm? | Solution: Aspen Adsorption V9 allows using component fugacity instead of component partial pressure. However, the isotherm type “Partial Pressure� still needs to be selected and Aspen Properties need to be used to supply component fugacity values. To enable this option, please follow:
Gas_Bed > Configure Block > Isotherm > Use Fugacity in Isotherm > True
KeyWords
Isotherm, Fugacity, Partial pressure
Keywords: None
References: None |
Problem Statement: How does changing the number of nodes in adsorption gas bed model affect the simulation? | Solution: Aspen Adsorption gas bed models are spatially discretized. Discretization methods are used to solve the necessary Partial Differential Equations (PDE) across the bed. Larger number of discretization points (number of nodes) will ensure a smaller distance between nodes and hence better accuracy.
By default, the number of nodes is set to 20. However, user can increase it at Gas_Bed > Configure Block > Configure > General
Although increasing number of nodes improves model accuracy, it slows down the simulation. So, the user is advised to make balance between these two performance criteria.
Key Words
Gas Bed, Nodes, Discretization
Keywords: None
References: None |
Problem Statement: How to Edit Transforms in APC Builder for Case and Master Model? | Solution: Please note that there are two transform icons in APC Builder and it can get confusing which transform button to use while editing the transform information or even while adding a transform.
Transforms in APC Builder can be added on the case level or to the master model level.
If a case (with a transformed variable) is used to update the master model, the transforms automatically get carried over to the master model. However please note that if the transforms in the master model level are removed, it would only be removed from the master model and would continue to stay at the case level. If the master model is updated from the case again, then the transforms will again be carried over to the master model. Editing the transforms on the master model level should be done by using the Transform button displayed when Master Model node is selected, while transforms on the case level are done using the Edit Transforms button in the Edit Variables tab for case. Failing to do so could lead to a situation as shown below in the image –
The image below shows that following are the options available in apc builder for editing/adding transforms
An alternate option to import transforms from Master model to the case is by using the ‘Get transform from Master’ button. This can be found on the case editor.
Editing/adding transforms in case editor can also be done by using the scatter option. The scatter plot option provides more flexibility of toggling the transformation fitting. As shown in the image below, the black dot can be moved to edit the fitting shown for the transformation.
Keywords: Transforms
APC Builder
Case Editor
References: None |
Problem Statement: What are the steps for linking simulation tags with Aspen InfoPlus.21 from Aspen OTS? | Solution: Refer to the attached word document for step by step instructions including screen shots and descriptions.
Keywords: linl , IP21, Info Plus
References: None |
Problem Statement: After installing the latest version or patch, DMCplus Build shows validation errors that were not found in previous versions. What does this validation look for? | Solution: Recent versions of DMCplus Build enforce a more strict entry and variable validation. This new validation looks for:
- Entries defined in "variable type" collections must be unique across all "variable type" collections (i.e. Independents, Dependents, Test Groups, and Subcontrollers).
- Entries defined in "singleton" collections must be unique across "singleton" collections (i.e. Configure, General, ET, CSS, and Calculation Declarations).
The same entry name can be defined in a singleton collection and in a variable collection without causing a conflict. This is because variable collection entries get a 3-digit numeric suffix added to them in order to make them unique across variables.
In other words, duplicate entries that only appear in IND or DEP variable types are not going to have a problem. The problem occurs when the same entry is defined in both IND and DEP variables. So, consider we have a user entry called ABC defined in MV1 and CV1. As a result, ANY calculation that attempts to use one of these values will be using a Shared instance of the same user-defined entry in the context. This is because any entry defined inside the variable scope will be added as "ABCnnn" where nnn is the variable index.
User-entries need to be defined using unique names across IND and DEP variable type. This is the reason why all the “built-in” parameter names are different between IND and DEP variable types. For instance, the upper operator limit in IND variable types is ULINDM while in the DEP variable types is UDEPTG.
This variable validation has been present in the new APC Builder platform however; it was not enforced in DMCplus until V8.5 CP5.
Important note
This validation does not prevent users from saving the configuration file in DMCplus Build, nor from loading it and starting the control process. The main issue appears in the controller calculations. Duplicate entries are often the culprit for unexpected calculation results in the controller operation.
We want to prevent any problem in the controller operation and want users to avoid running into any “wire crossing” issues, that is why we added this stricter variable validation routine.
It is not advisable to load and start a controller without taking care of the duplicate entries as it may cause issues in the calculations execution.
Keywords: Validation, duplicate entries, DMCplus Build
References: None |
Problem Statement: Consider a case where CV measurements are calculated as a function of another (user-defined variable) input being read in from the DCS. Ex. the composition (CV) of a product at top of a column is calculated as a function of overhead column temperature (user-defined variable). For such cases, the calculated CV (built-in inferential) do not change when simulating the controller behavior offline using APC/DMC3 Builder. | Solution: The reason calculated CVs do not change during simulation is because the inputs to these CVs- Temperature and Pressure, which are built as user-defined variables and are read from DCS are not changing during simulation (no inputs coming for these variables from DCS during simulation mode). There are two options for the user to simulate the prediction and control of these variables in the offline mode-
1. Open Simulation view and navigate to Configure Simulation (Simulation tool bar) and select the Disable Calculation option. When this option is enabled, the APC Builder engine will disable all internal calculations that have been defined in the controller. This option would allow the inferential CVs to change when running the simulation. However, it might not be the ideal solution in situation where would need to have bulk of the calculations active while only disabling a select few in the calculation list (like the inferential calculations) as all calculations get disabled when using this option.
2. Open Edit Calculation page for the controller, navigate to the calculation you wish to disable and comment out the lines that need not be used (with a single quotation mark at the beginning of the line). If the entire calculation set is disabled, it would be necessary to add a dummy line (Ex. A = 0) to keep the Calculation view from throwing an error message. Commenting out the calculation line is essentially disabling the calculation. When the lines are commented out, the variable mapping associated with the parameters involved in the calculation also disappear. Save the Calculation and run simulation, which would now allow the calculated (no longer) CVs to change during simulation. Please note that once the simulations are completed, you would need to open edit calculations, uncomment the calculation lines that were commented out earlier and re-map the variables to the correct controller parameters to allow the calculation to work when the controller is deployed online.
Keywords: Built-in Inferential
Calculated CVs
APC Builder
DMC3 Builder
References: None |
Problem Statement: When upgrading a file from V8.4 to a newer version, the upwards compatibility dialog does not load. How can I upgrade the databanks to the newer version?
Cause
There are two situations where this situation can happen:
1. A file is created in V8.4 and an older databank is manually selected; when the file is upgraded, no dialog will pop up.
2. A file is created in V7.3 and in V8.4 the option "keep the old databank" is selected; when this file is upgraded, no dialog will pop up. | Solution: The upgrade databanks dialog is active only if the file is using the most current databank of the PUREXX databank. Fore example, in V8.4, the default databank is PURE28, for V9 the default databank would be PURE35
To fix this issue, the users would need to go to Components | Specifications | Enterprise Database and make sure that the latest version of the PUREXX databank is selected
Â
Keywords: Upgrade compatibility, pure databank
References: None |
Problem Statement: In the Stream Report, results are reported with only 8 significant figures. However, in some cases, higher precision is required. Is it possible to increase the precision in the results? | Solution: The stream report has a limit on the amount of significant figures that can be reported. Adding more than 8 significant numbers would only complete the values with zeros in V8.8 and earlier.
To increase the precision of the results in the report in V8.8 and earlier, users can:
· Select a large unit for the desired property
· Set up a calculator block that calculates a given property with a given large unit of measure that will reveal more significant figures
In V9 and higher, more significant figures can be added using the Format option on the Display Options for the Stream Summary for any property.
For example, to increase to 10 significant figures in a fixed format, specify:
This will show on the form as follows:
Keywords: Significant figures, decimal numbers, stream report
References: None |
Problem Statement: How do you globally define a new Template for the Stream Results? I have created a new Template for my stream results. How do I get it used for all streams forms that I open? | Solution: Go to the File Options Advanced page. You can Change the Default template for the Stream results summary.
Note that if a form has already been opened, it will continue use that template when re-opened.
Keywords: Stream Results
References: None |
Problem Statement: How can you identify which the a particular file has been created from the version incompatibility error message?
For example, to what version does the message "This file was created with newer version (23.0) of Aspen Plus and is not compatible with the current version (21.0)" refer. These versions are not the same as the general product version such as 2006.5 or V7.2? | Solution: The dialog show when selecting "About Aspen Plus" from the Help menu indicates the Aspen Plus version.
You can refer to table below to find out associated version number used in the messages.
Aspen Plus version
Help About Version Number
2004.1
13
2006
20
2006.5
21
V7.0
22
V7.1
23
V7.2
24
V7.3
25
V7.3.2
26
V8.0
27
Keywords: version, build number
References: None |
Problem Statement: How do I report mass specific heat for the total stream & its phases and get this reported for all streams? | Solution: Additional properties can be added using Select Properties with the new Stream Summary.
For example, open a file and run.
1. Go to the Result Summary | Streams form.
2. In the Property Sets section of the Stream Summary ribbon, click on Select Properties or scroll to the bottom of the Streams Material sheet and click on "<add properties>"
3. Click Add and select Mass heat capacity, mixture CPMX-M.
4. Click on Calculation Options tab and select the phases desired.
5. Click OK and they will appear in the stream summary.
6. Click on Save as New in the Template area of the Stream Summary ribbon to use this template when you are on other Stream forms.
7. If you want this Template to be used globally, you can select it on the File Options Advanced sheet.
Keywords: V9 Stream Summary
References: None |
Problem Statement: In the new V9 interface, how do I add vapor pressure to the stream report? | Solution: To add vapor pressure in stream reports, follow these steps:
1. Go to Results Summary | Streams.
2. At the bottom of this table please click on Add Properties.
3. Look for Vapor Pressure (will show by component) and Bubble Point Pressure (for the mixture).
4. Once the properties are shown save the template.
5. If you want to see this properties in each stream results table please go to the stream results and add this template to the stream.
Keywords: Vapor Pressure, Stream Report, Add Properties
References: None |
Problem Statement: I have downloaded the latest compilers.cfg file and the configuration is "OK"; however, I am still not able to compile and link my subroutines using Intel Visual Fortran 2016 and Visual Studio 2015 or Visual Studio Express 2015. | Solution: By default, the Visual Studio 2015 and Visual Studio Community 2015 do NOT install Visual C++ (and associated tools). You now have to select the Custom installation option and then check Visual C++ under Programming Languages.
The documentation now mentions that Aspen Plus needs the Visual C++ and the associated tools and files.
Keywords: IVF16_VCX14 Intel Fortran 16/2016 and VS Express 14/2015
IVF16_VS14 Intel Fortran 16/2016 and Microsoft Visual Studio 14/2015
References: : CQ00710288 and CQ00607064 |
Problem Statement: When I modify the stream summary and click on Send to flowsheet, table displays the default format for the stream summary. How can I keep the changes I made? | Solution: In Aspen Plus V9, in order to maintain modifications to the Stream Summary you need to save two things:
1. Template - Templates control which data is displayed and how it is displayed. If you add or remove properties, or if you change the order, you are modifying the template, which means to keep the changes you need to save the template as a new one. In the Template section of the Stream Summary ribbon, click on Save a New to save the new template with the modifications.
2. Stream group - Stream Groups control which streams are shown and how they are ordered in the Stream Summary (by default, they are in alphabetical order). If you change the streams or the order to be displayed, you need to save the Stream group as a new one. In the Stream Group section of the Stream Summary ribbon click on Save a New to save the stream group with the modifications.
Note that you will need to re-run the simulation before you send the Stream Summary to the flowsheet to keep the modifications you made.
Keywords: Stream summary, flowsheet, stream table
References: None |
Problem Statement: The Data Specification dialog in the Aspen Production Record Manager Get Production Record Data COM Add-in function is used to add columns (such as characteristics, statistics, etc...) to display in the results set.
The dialog provides the option to use Cell | Solution: The above error message is received due to a limitation on a number of characters allowed in the array. The limit is 132 characters.
A workaround is to use an array with only a few items whose total character count doesn't exceed 132 characters.
This issue will be addressed in a future release of the APRM Add-in.
Keywords: None
References: to populate the display area. The example below shows the Characteristic specifier dialog.
However, when a large number of items is referenced using the above dialog, the following error may be returned by the Add-in:
Error writing the formula to the spreadsheet. Please make sure it is valid. |
Problem Statement: This knowledge base article describes the methods to control the geometry of the Gantt display. | Solution: You can control the following geometry of the Gantt display:
1. Facility Height.
2. Blank Space on top of Facility.
3. Width of the Facility Header
Method 1:
Using the below options in the CNTLS table:
1. FACHT - Facility Height
You can enter the number of pixels for facility height for drawing the Gantt Rows.
2. FACTOP - Facility Top Blank SpaceÂ
You can enter the number of pixels to use as the blank space reserved for top of the facility.
3. FACHW - Facility Header Width
You can specify the number of characters to use as the width of the Facility Header.
Method 2:
Using the Format tab on the Planning Board’s Ribbon you can now adjust the Gantt dimension
Keywords: None
References: None |
Problem Statement: This knowledge base article describes the use of WHILE in Rules. | Solution: WHILE is used in Rules to loop though a logic for a fixed number of times or until some condition is met. The WHILE statement uses a local variable as a counter and increments its value with each iteration.
Breaking a WHILE loop occurs when the maximum number of iterations specified in the CNTLE is encountered or when a BREAK statement is encountered.
Syntax:
WHILE ?variable
Example:
WHILE ?A
Keywords: None
References: None |
Problem Statement: This knowledge base article describes how to configure a Scroll View in XML. | Solution: The ScrollView is a view configuration that is used to scroll the content vertically or horizontally.
Syntax:
<ScrollView
Type = “ScrollView�
VerticalScrollbar = “Visible�
HorizontalScrollbar = “Visible�
>
Settings Description:
· Vertical Scrollbar:  Controls the visibility of the vertical scrollbar.
· Horizontal Scrollbar: Controls the visibility of the horizontal scrollbar.
Both the above settings take one of the following options:
Auto:Â Â Â Â Â Â Â Scrollbar is displayed only when the content fits in the space.
Disabled: Scrolling is disabled and dimension of child view is restricted to that of the ScrollView.
Hidden:Â Â Â Scrollbar is hidden and the dimension of child view is unconstrained.
Visible:Â Â Â Â Scrollbar is always displayed.
Keywords: None
References: None |
Problem Statement: Installation of Aspen IQ Model Powertools 1.3 generates a message indicating that Aspen IQ Desktop is required. Aspen IQ Desktop 3.1 has already been installed and is present.
This is a known bug. | Solution: Uninstall the Aspen IQ Desktop 3.1 software and re-install with the Aspen IQ Model Powertools.
KeyWords:
Aspen IQ
Powertools
Aspen IQ Model
Keywords: None
References: None |
Problem Statement: Does the new BLOWDOWN®  tool in Hysys need the Dynamics license? | Solution: The BLOWDOWN® simulator that has been incorporated into Hysys since V9.0 will need the dynamic license for it to be loaded and run in Hysys.
Keywords: BLOWDOWN®, Dynamics, License
References: None |
Problem Statement: Why I can see following “Unable to load project� error message when I am trying to import Aspen Plus backup (bkp) file in Aspen Process Economic Analyzer(APEA)? | Solution: We have implemented to import Aspen Plus backup(bkp) file to Aspen Process Economic Analyzer(APEA) from V9 onwards.
This error you are getting is due to version compatibility issue. You cannot import older versions Aspen Plus backup(bkp) file to Aspen Process Economic Analyzer V9. In order to remove this error, you need to save this again backup(bkp) file by using Aspen Plus V9. After this you can successfully import backup(bkp) file to Aspen Process Economic Analyzer(APEA).
Keywords: Aspen Process Economic Analyzer, Aspen Plus, Backup(bkp), Import
References: None |
Problem Statement: When I import Aspen Plus backup(bkp) file to Aspen Process Economic Analyzer(APEA), does it require extra Aspen Plus tokens? | Solution: We have implemented to import Aspen Plus backup(bkp) file to Aspen Process Economic Analyzer(APEA) from V9 onwards. In previous versions of Aspen Process Economic Analyzer(APEA) we can able to import Aspen Plus document(apw) and compound(apwz) files which may lead to consumption of extra Aspen Plus tokens as Aspen Plus is opened in background.
In Aspen Process Economic Analyzer(APEA) V9 if you import Aspen Plus backup(bkp) file it does not require extra Aspen Plus tokens.
Keywords: Aspen Process Economic Analyzer, Aspen Plus, Backup(bkp), Tokens, Import
References: None |
Problem Statement: What database versions are supported in Aspen Fleet Optimizer V9.0? | Solution: Aspen Fleet Optimizer V9.0 operates with Windows Server 2008 R2 SP1 and Windows Server 2012 R2. Aspen Fleet Optimizer V9.0 does not support earlier versions. Aspen Fleet Optimizer V9.0 operates with Oracle 11g (11.2.0.4) and Oracle 12c (12.1.0.2). Aspen Fleet Optimizer V9.0 allows supports MS SQL Server 2008 R2 SP4, MS SQL Server 2012 SP2, and MS SQL Server 2014 SP1.
Keywords: None
References: None |
Problem Statement: Why is there an increase in the Production Control Web Server (PCWS) IIS log files in V8.8 and later releases? | Solution: Starting V8.8, the web server IIS log files increased. This is a by-design behavior. The reason why this is seen in V8.8 (and later releases) is that PCWS began performing a full rebuild of the secured asset permissions when the cache refresh happens. This fixed an issue with the web interface not being able to recognize the changes made to role/permission in some cases.
If the IIS log files are filling up the disk, it is suggested to disable AFW logging in IIS. Find below the procedure:
1. Open Internet Information Services Manager (IIS), on the left side tree click on the Web server name, just under Start Page. Look for Logging under IIS and double click on the icon to open the feature.
2. Disable logging on the Actions panel on the right side.
3. Finally, run an IISRESET command in a command prompt instance (Make sure the command prompt is opened as an Administrator) to force the logging change to take effect.
Keywords: IIS
AFW logging
PCWS
References: None |
Problem Statement: PIMS Silent upgrade receives message "The Aspen mMDM adapter component will be removed as part of this uninstall. Please make a backup copy of the following files before continuing if you have modified the default adapter’s configurations" | Solution: If Aspen mMDM adapter component has been installed and XML files were modified by an AspenTech application, then users will get this error message asking to backup these files. This message occurs during a Silent uninstall of the mMDM adapter component or during a silent upgrade of the mMDM adapter component.
We have created a script which can run before the uninstall script or before the upgrade script, so a pop up message will not be displayed during the silent uninstallation or upgrade.
Please follow the below steps to stop receiving this message:
1. Download and extract the attached ZIP file RemovePopUp.zip
2. Run the following command either using CMD or a deployment tool (example: Microsoft SCCM).
a. cscript RemovePopUp.vbs
Note: The mMDM adapter component will get installed as part of many Aspen Manufacturing Applications.
Keywords: mMDM adapter component
UnInstall
Upgrade
Pop Up
References: None |
Problem Statement: How do I impose turndown capacities for process units? Please note that this is not Min capacity. The program should able to take select the value of capacity between minimum and maximum or the unit capacity should be zero. | Solution: The solution for your problem is to use Mixed Integer Programming. Table MIP allows the user to define the threshold variables through the columns LBD and UBD.
A variable that represents the capacity of the unit needs to be used in table MIP to impose the threshold bounds.
For example let us consider the example in which we set up the turndown capacity for the Diesel Hydrrotreater represented by the unit SDHT
1) The column SDHTMIP represents the capacity of the unit SHDT. The E-row equates sum of the activities of SDHTHD1 and SDHTDCD, (which are both feeds to the unit) to SDHTMIP. In other words, the column activity SDHTMIP represents the total capacity.
2) The variable SDHTMIP is the Table MIP is bounded as follows:
*TABLE
MIP
MIXED INTEGER PROGRAMMING
*
*
THRESHOLD
*
BOUNDS
ROWNAMES
TEXT
LBD
UBD
*
*
('000
('000
*
BPD)
BPD)
*
THRESHOLD BOUNDS:
SDHTMIP
N Butane
2.3
The LBP defines the minimum value the variable SDHTMIP would take. By means of this structure we define the capacity could be minimum of 2.3 or nothing.
3) Please see the following in the output. The SDHT is operating at minimum capacity. The capcity without MIP is less than that.
Keywords: MIP
References: None |
Problem Statement: Error "unknown map for event data type", while restarting Aspen InfoPlus 21 repository. How do I resolve? | Solution: This solution article describes about steps to perform in case the Aspen InfoPlus 21 archiving stops. The repository will stop and color will be red.
The error displayed will be "unknown map for event data type" in error.log file located in the repository folder (C:\ProgramData\AspenTech\InfoPlus.21\c21\h21\"Repository folder")
Below steps needs to be tried in case the problem appears:
1. Try to restart the Aspen InfoPlus21 database and check if now repository could be started
2. Try repairing the archive from Aspen InfoPlus21 manager -> Actions-> Repair archive
3. Start the repository using DOS command - C:\Program Files(x86)\AspenTech\InfoPlus.21\c21\h21\bin>h21arcck –rrepositoryname –fileset no. -o -x –d
If still, the repository could not be started, there could be a possibility that the DAT files are corrupted. In that case, please follow the step 4.
4. Stop IP21 database, delete event.dat & cache.dat file, Restart IP21 database.
This should start the repository. But, if the problem still there, please contact AspenTech support.
Keywords: Unknown map
Event.dat
Archiving stopped
Repository
References: None |
Problem Statement: How to resize an undersized valve | Solution: In Aspen Plus, when the valve design option is selected, with either the outlet pressure or pressure drop specified, choking flow can occur.
When choking is predicted, the design method ignores the effect of choking, resulting in an under-estimate of the valve % opening. When the simulation is exported in Pressure Driven mode into Aspen Dynamics, the flow will not match that in the steady state simulation, and the simulation may fail to initialize. This is because the Dynamics Valve model accounts for the effect of choking. To run the simulation successfully, any valves for which the design option is used and choking is predicted, must be resized. To do this:
1. For each Valve block, invoke the Resize script
2. Run the simulation in Initialization mode
3. For each Valve block, invoke the Resize script again
4. Re-run the simulation in Initialization mode
The dynamic simulation can now be run as normal.
Keywords: Resize valve, choking
References: None |
Problem Statement: How is the Heater block modeled for reverse flow? | Solution: The pressure drop in the heater is related to the outlet volumetric flow rate by:
ΔP = K x Rho x FV_out2
Where:
K = A constant determined by fitting to steady-state conditions
ΔP = Pressure drop
Rho = Mass density at outlet conditions
Fv_out = Outlet volumetric flow rate
If the steady-state simulation predicts a pressure rise, the pressure drop equation is not used. Instead the pressure difference will be specified. When reverse flow is enabled, Heater is modeled as an instantaneous mixer followed by a single input, single outlet flow resistance with heat transfer. Therefore, depending on the local pressure gradients during simulation, it is possible for some of the feed streams to be in forward flow and some to be in reverse flow, so bypassing the flow resistance/heat transfer section of model and not receiving the Heater duty.
Recommendations:
1. Do not use Constant Duty for the Heat Transfer Option when using Heater in reverse flow simulations. Instead, it is better to use either the Constant Temperature or LMTD Heat Transfer Option in Heater to model the heat transfer in a more realistic manner. The reason for this is that with a fixed heat duty, as the flow rate becomes small, the process temperature is driven above its upper bound towards infinity. To avoid this, an in-built procedure in Aspen Dynamics attempts to ramp the fixed duty to zero to keep the temperature within its bounds. However, when the flow reverses, the possibility of a discontinuity in the temperature can lead to convergence problems with this procedure.
2. Use Calculated for the Pressure Drop Option when using Heater in reverse flow simulations. If Fixed for the Pressure Drop Option is used, the pressure drop across Heater will not vary with flow rate, which will result in unrealistic behavior when the flow reverses during a dynamic simulation.
Keywords: Heater, reverse flow
References: None |
Problem Statement: What is model cleanup and how do I use it? | Solution: PIMS provides a feature called model cleanup that allows the user to quickly purge unnecessary files that have been generated by prior model runs.
The cleanup function can be accessed by the icon or through the menu MODEL | CleanUp Model(s). Once activated, the model selection dialog box will open. This allows the user to select which model or models are to be cleaned and provides an indication of how much space is currently consumed by the files that will be purged (see the "Temporary" column). If a model has no temporary files which are eligible for the selected cleanup options, then the model will not be listed.
Before selecting the desired model(s), click on OPTIONS to make sure the cleanup is configured as you desire. Select all the file types that you would like to be removed from the selected model directories.
It is always a good idea to purge the Work Files. This removes any temporary files that PIMS made during a previous run.
If the Report Files are selected then all .txt, .htm, .lst, etc. files will be deleted from the model folder. This includes all reports from old or recent runs. So if there are some old reports that you want to keep, move them to a different folder first.
If the Spreadsheet Report Files are selected, this will only effect the listed report spreadsheets that were made by PIMS. PIMS will not delete any Excel files generated by the user.
The database options allows the user to purge the database tables or while leaving the database file intact, or delete the entire results.mdb database table.
Once the desired options are selected click OK to go back to the model selection dialog. All the models in the same directory as the currently opened model will be displayed. Select the desired model(s) and click OK. PIMS will remove the selected file types from the selected models.
If you are archiving a model for backup reasons, it is a good idea to clean it up. This saves space by minimizing the contents of the archive and all the deleted files can be regenerated by re-running the model.
Keywords: cleanup
archive
References: None |
Problem Statement: Web.21 comes with MS FrontPage add-ins which can be used to generate custom Web.21 asp pages. This article describes the process to use the Web.21 add-ins with MS FrontPage.
Note: The Web.21 add-ins are installed with the Web.21 Graphic Studio. | Solution: In FrontPage, click on the 'New Web.21 ASP File' button. This will add a Web.21 header to the top of the web page.
Place your datapoint fields, APEx trend plot objects, etc. on the web page by clicking on the specific Web.21 object button in FrontPage. Double click on the object and configure the datasource and tagname/Record&Field (on objects where this is applicable.)
In order for this page to work with Web.21 it must be saved as an ASP page. Equally important, the page must be saved to the Web.21 folder where the other Web.21 ASP pages are stored. By default this is:
C:\Inetpub\wwwroot\AspenTech\Web21.
Open the page in Web.21 by typing in the name of the ASP file after the standard Web.21 URL. For example, for a server name of 'HKLAP' and a custom ASP file named 'FrontPageTest.asp' you would type the following in the URL to open the page:
http://HKLAP\Web21\FrontPageTest.asp
KeyWords
Keywords: None
References: None |
Problem Statement: Most fields in a Point Detail (Detail Display) page are configured to allow users to write directly to the IP.21 database unless:
IP.21 security has been implemented and
Users are limited to "Read" access on the record.
Even if users have "Write" access, it could be desirable to limit the specific fields in a record that they are allowed to modify via Web.21. | Solution: Modified Point Detail pages for IP_Analog, IP_Discrete and PMC records are attached to this solution. Separate sets of the files (IPAnalog.asp, IPDscret.asp, PMCAna.asp and PMCDisc.asp) have been created for versions 6.0.x and 2004.x. These modified pages provide read-only access to record information and prevent ALL user-changes to associated records in the IP.21 database via the Point Detail pages.
To install:
Download the applicable zip file and move the contents to the \Inetpub\wwwroot\AspenTech\Web21 folder.
Backup or rename the original files.
Rename the newly-downloaded .asp files to IPAnalog.asp, IPDscret.asp, PMCAna.asp and PMCDisc.asp
KeyWords
detaildisplay
pointdetail
read
readonly
PMC
Keywords: None
References: None |
Problem Statement: In the specific situation when a client who wants to use Aspen IP.21 Process Browser (formerly known as Aspen Web.21) does not have Aspen Process Explorer (APEX) installed and does not have permission to download ActiveX controls, a prompt to download the Web21Controls.cab will occur each time Aspen IP.21 Process Browser graphic is opened. | Solution: Although Aspen IP.21 Process Browser graphics are Java class, ActiveX control is still required since Aspen Process Data, Timeline control and other APEX middleware are used with Graphic plots.
On client machines that are set to disable ActiveX downloads, Aspentech recommends that the CAB file components be initially installed by a user that has administrator privileges.
1. Login to the client using Administrator account or account that has sufficient privileges to install & register COM components.
2. Open the Aspen IP.21 Process Browser home page and click on the Plots tab which gives an option to download/register components needed for graphics to display properly.
3. Allow the page to install\register the ActiveX components as needed and as soon as its completed click on Container Downloaded button which directs to the plots page.
In situations where you need to register the Web21Controls.cab file manually please refer to the solution 116737
KeyWords
activex
graphic
web21controls
Keywords: None
References: None |
Problem Statement: Where can I find more information about the Tray/Packing type used in Aspen HYSYS Column Internals? | Solution: For sizing and rating calculations, Aspen HYSYS Column Analysis tool divides a column into multiple sections. Each section can have a different tray type, packing type, and diameter.
In the column internals, you can choose from the following five commonly-used tray types:
Tray type
Vendor Site
Sieve
Bubble caps
Sulzer-Nutter Float Valve®
Sulzer Floating Valves
Koch-Glitsch Ballast®
Ballast Tray Valves
Koch-Glitsch Flexitray®
Flexitray Valve Trays
You can also use any of the following types of structured packings:
Packing type
Vendor Site
Goodloe®
Goodloe Structured Packing
Glitsch Grid®
Glitsch Structured Packing
Norton Intalox Structured Packing
Intalox Structured Packing
Sulzer BX, CY, Mellapak, and Kerapak
Sulzer Structured Packing
Koch Flexipac, Flexeramic, Flexigrid
Flexipac Structured Packing
Flexeramic Structured Packing
Flexigrid Structured Packing
For detailed information, please contact the vendors.
Keywords: Tray type, packing type, vendor bulletin.
References: None |
Problem Statement: Can I model a slide valve in a compressor within Aspen HYSYS? | Solution: No unit operation in Aspen HYSYS can directly model a Slide valve.
The workaround is to manipulate the Suction volume to mimic the effect of slide valve which can
control the suction gas volume of compressor.
Â
Keywords: Slide Valve , Suction Volume, Screw compressor
References: None |
Problem Statement: Overview of Software License Manager (SLM) Server changes from aspenONE versions V7.3 through V9.0 | Solution: The table below provides the major enhancements and bug fixes that were included in each of the Software License Manager (SLM) Server releases from 8.4 through 8.6.1 that correspond to aspenONE versions V7.3 to V9.0
SLM Server Version
aspenONE version
Major Enhancements and Bug Fixes
8.4
V7.3, V8.0, V8.1, V8.2, V8.3
· Licensing for Virtualized Environments; Sentinel RMS provides you the capability to license and control your applications under virtual environments.
· Enhancements have been made in maintaining the license server-side persistence data for commuter licenses.
· Increased Size of Private Vendor Information
· Problems Corrected in This Release:
o The Sentinel RMS SDK v8.3.0, including the license server, could not be installed successfully on Windows 2000. The problem is corrected in this release.
o The license update call succeeded even when the IP address was changed at run-time. The problem is corrected in this release.
8.5.3
V8.4, V8.5, V8.6, V8.7, V8.8
· Usage Log File Enhancements:
o The log comment data inserted by the vendor in various RMS APIs can be anonymized and represented as SHA-256 based unique hash in the usage logs using the anonymous logging option
o Introduced Additional Transaction IDs in Usage Log
o Inclusion of Log Comments in the Usage Log Entries
· Problems Corrected in This Release:
o WlmAdmin displayed incorrect sharing limit.
o Incorrect RMS version displayed in the Application Event Viewer Log.
o License release entry is missing in usage logs for some cases.
o Incorrect behavior observed in the case of redundant server setup with regards to token count on WlmAdmin and license request.
o The License Manager start up status messages in command-line did not display the complete message.
o Incorrect NumKeys value is displayed in the usage log file when new usage log file is created by the License Manager.
§ Incorrect usage and timestamp shown in the usage log.
8.6.1
V9.0
· Dynamic Length Packet for Client-License Manager Communication; Up to v8.6.0, RMS supported fixed length packets for client-License Manager communication. However, all available bytes of payload or data might not always be used during information exchange, causing network performance decline. Starting v8.6.1, the License Manager and client library supports dynamic length packets.
· Introduced License Manager Start-up Option to Increase Socket Buffer. In this release, a new License Manager start-up option (sbm) is introduced. This option can be used for increasing the default socket buffer size of the License Manager. This option is useful in scenarios when multiple client applications are getting timed out while accessing the License Manager. Using this option, an administrator can specify a numeric multiplier value to increase the current buffer size by n times—subjected to the condition that the resultant buffer size is within the maximum permissible size allowed by the operating system. Otherwise, the buffer size is not updated. The allocated socket buffer size is logged in the Windows event log of the Sentinel RMS License Manager
· Problems Corrected in This Release:
o Increased Limit of the Number of Trace Log Backup Files: The maximum number of backup trace log files is increased from 100 to 10,000. For example, if the trace log file name is trace.log then the first trace log file will be trace.log.00 and the last trace log file in the series will be trace.log.9999.
o Prevent trace logs from being overwritten
· Remove dependency on setting OS locale to US English
Keywords: SLM
SLM versions
SLM enhancements
SLM bug fixes
References: None |
Problem Statement: How can one prevent Aspen IP.21 Process Browser (formerly Aspen Web.21) from prompting the users for credentials? | Solution: When a user navigates to the home page for Aspen IP.21 Process Browser they may be presented with a request for their credentials. To prevent the request, make an adjustment to the Microsoft Internet Explorer (IE) Security Settings to be either of the following:
Automatic logon only in Intranet Zone
Automatic logon with current username and password
These settings may be found in IE beneath Tools => Internet Options => Security Tab. On the Security tab there will be four zones presented - Internet, Local intranet, Trusted sites, and Restricted sites:
Pick the zone to which the Aspen IP.21 Process Browser Server belongs and click 'Custom Level'. Scroll to the bottom and look for the User Authentication - Logon section:
The change may be made here.
Note that if the Custom Level button is unavailable one may right-click the IE icon and choose 'Run As Administrator' to enable it.
Additional Information
The following URL will take one to the Aspen IP.21 Process Browser home page:
<computer name>/web21
Please substitute the name of the machine hosting Aspen IP.21 Process Browser in place of <computer name> in the example above.
Keywords:
References: None |
Problem Statement: What units are available in the PSV Sizing tool in Aspen HYSYS? | Solution: In the Safety Environment of Aspen HYSYS, reports are available in both metric and English units. Please refer to F1 help for further information.
Note that in versions prior to Aspen HYSYS V9.0, some reports would only export to Excel in metric units. This has been resolved in Aspen HYSYS V9.0
To request an upgrade, please click here.
Keywords: Relief Sizing, reports, Documentation, Builder, datasheet, units, PSV
References: None |
Problem Statement: Is there a way to change the standard orifice sizes for a PSV? | Solution: In the Aspen HYSYS Safety Analysis Environment, the flange sizes in the Line Sizing tab, are populated according to the American Petroleum Institute (API) standard guidance table. However, they do not cover all the valve sizes used in the industry.
In such cases, you can now (starting in Aspen HYSYS V9.0) use the Orifice Manager to edit the flange sizes.
You can find the Orifice Manager on the Home ribbon in the Safety Analysis Environment, under the Preferences Manager:
If you activate the checkbox next to the orifice, the fields in the table activate and you can edit them accordingly:
These changes can be saved as a preference set as well to be used in future simulations.
Keywords: pressure relief, flange rating, safety valves
References: None |
Problem Statement: How is the Relieving Pressure calculated in the Safety Analysis Environment of Aspen HYSYS? | Solution: Relieving pressure is calculated as the set pressure plus allowable overpressure.
where
is the calculated relief pressure
is the set pressure
is the overpressure
You can view the details of the calculation by clicking on the Edit button which is next the relieving pressure value in the Scenario Setup in order to see the details.
All pressures used in the calculation must be in gauge. Also note that the Set Pressure may be linked to the Design Pressure specified on the Equipment tab. You can unlink the Set Pressure and the Design Pressure on the PRD Data tab.
Keywords: set pressure, relieving pressure, overpressure, PSV
References: None |
Problem Statement: Does the Fire Scenario in the Safety Environment of Aspen HYSYS calculate the latent heat? | Solution: Starting in Aspen HYSYS V8.6, the PSV Sizing capability offers a latent heat calculation. Once an initial % vaporized and final % vaporized are specified in the fire scenario, the PSV Sizing capability will estimate a latent heat value based on the energy required to take the
Keywords: PSV sizing, latent heat, fire scenario, safety, environment
References: Stream's liquid inventory from the initial % to the final % vaporized.
For more information you can refer to KB 143077
Note that the PSV Sizing capability in Aspen HYSYS V8.3 and V8.4 require the user to manually input the latent heat of vaporization to calculate the relief load per API 521. |
Problem Statement: How can I put the solver on hold or activate it via automation? | Solution: To put the solver on Active or On Hold:
You can use the property .CanSolve of the solver object.
Attached you will find an example Excel spreadsheet. Any simulation has to be active (open) for this Excel spreadhseet to work.
Keywords: OLE, macro, VBA
References: None |
Problem Statement: How do I use the Stream Property Spec of a non-draw stream as a Column Specification? | Solution: The stream property spec of a non-draw stream in a column is not available directly. However, using this workaround we can specify the non-draw property spec as a specification:
1. Enter the column subflowsheet
2. Double click on the tower and go to Design | Side Draws, create a side draw stream and select the Tray Number from which is extracted
3. Define zero flow to this dummy draw stream, so it won’t change the results
4. Go back to the main flowsheet and define the Stream Property Spec in the Column using this new draw stream
Keywords: Stream property spec, column specification, side draw, draw stream
References: None |
Problem Statement: How to resolve the OLE Registration Unsuccessful pop-up message which occurs while using Set Version in Aspen HYSYS | Solution: To resolve this, Select Set Version in Aspen HYSYS >Right Click > “Run as administrator".
The OLE Registration will then be successful.
KeyWords
Set Version, OLE
Keywords: None
References: None |
Problem Statement: How to install the missing DMCplus context service if its missing after installation without a reinstall of entire Aspen APC Suite? | Solution: If DMCplus context service is missing and all the other services are present then it indicates that the installation is faulty and it failed to install some components.
Verify if all the other Aspen APC offline tools work correctly. If the issue is only with the DMCplus Context service, which prevents from loading and starting controllers using Aspen APC manage then the following steps could be used:
1) Open Command prompt (Run as Administrator).
2) Navigate to the folder Program Files <x86>/AspenTech/APC/Online/bin and run cimio_dmcp_regserver.exe command which helps in installing the DmcPlus context service.
3) Verify if the DMCplus context service can start and applications can be deployed.
If the cimio_dmcp_regserver.exe is missing then it indicates that the installation of the Aspen APC software is faulty and a complete uninstall and reinstall of Aspen APC suite should be necessary.
Keywords: DMCplus Context
APC installation
References: None |
Problem Statement: Column Hydraulics - Detailed Internal Method? | Solution: In response to your query for K value calculation in column environment, please find the response below.
A. The Use Tower Diameter Method is a simple heuristic in which k is assumed proportional to the column diameter squared.
Originally, in the attached case file, k= 18 [kg/sec/sqrt(kPa-kg/m3)] at D= 5.79m. So, k/D**2 equals 0.537. With time, this last value is adjusted to k/D**2= 0.1 In this way, this k is just related to geometry.
2. In the detailed method we have the formula
k= MolarVaporFlowToAbove /sqrt( DryDeltaP * MolarDensity)
Both k's are used in the expression below as
Flow= k *sqrt(DeltaP)
The difference is that, in the second case above (2), k is updated as the simulation proceeds.
Keywords:
References: None |
Problem Statement: How can I make visible the Filters and Folders tree views in Explorer? | Solution: You can hide and show the Filters and Folders widnows in Explorer by going to View tab and unchecking/checking the Folder tree view and Filter tree view
Keywords: filters, folders, Explorer
References: None |
Problem Statement: Users may notice that in the Results | Pressure/Flow Summary window a Friction factor is reported, but it does not state whether it is the Fanning friction factor or the Moody friction factor. Since it is an important parameter for pressure drop calculations, it is needed to know exactly what this reported friction factor is. | Solution: The Friction factor reported by Aspen Flare System Analyzer (AFSA) on the Results | Pressure/Flow Summary window is the Moody friction factor ().
For example, consider a pipe transporting complete vapor, for which the following information is reported:
- Friction Factor = 0.012
- Reynolds number (Re)=14,530,887 (Turbulent Flow, Re > 4000)
- Internal diameter (ϕ)= 482.6 mm
- Absolute pipe roughness (e)= 0.04572 mm
- For this example, the Round equation is set for solving for the Fanning friction factor ():
The Fanning friction factor results in 0.003.
The Moody friction factor is related to the Fanning factor by .Now, multiplying 0.003 by 4 results in 0.012, which is the value reported for the Friction factor on the Results | Pressure/Flow Summary (for this example). Therefore, it confirms that the Friction factor reported by AFSA is the Moody friction factor.
If the user needs to get the Fanning friction factor (), it will be only needed to divide by 4. Information related to the equations used for the different flow regimes may be found on the Help Menu (use the F1 hot key) by searching for ‘Vapor Phase Pressure Drop Methods’.
Keywords: Friction factor, Fanning, Moody, pressure drop, vapor phase.
References: None |
Problem Statement: How can we quantify the Reliability of a Series system and a Parallel system? | Solution: Series System
· Consists of multiple components
· Failure of 1 component results in the corresponding system failure
· System Reliability is the product of the component Reliabilities
Overall Reliability (Rs) for a Series System:
Rs = R1 * R2 * R3
where, R1, R2 and R3 are the individual Reliability values for the Components in Series.
Parallel System
· Offers a higher level of system Reliability but at a penalty of cost (capital and maintenance)
· Reliability is the sum of the component Reliabilities minus the product of the Reliabilities.
Overall Reliability (Rs) for a Parallel System:
Rs = R1 + R2 - (R1)(R2)
where, R1 and R2 are the individual Reliability values for the Components in Parallel.
Keywords: Series system, Parallel system, Series vs Parallel System, System Reliability
References: None |
Problem Statement: Briefly overview the different statistical distribution types available in AFR. | Solution: Current statistical data distribution types available in AFR are as follows:
- Exponential
· The most commonly used distribution
· Constant Failure Rate (probability of failure is the same in the first 100 hours as it is in the period 10,000-10,100 hours)
· 63.21% of all values fall below mean (36.79% chance of surviving past mean)
· Parameter 1 = Mean Time Before Failure (MTBF) in hours typically
· Parameter 2 not used
- Weibull
· Age Related Distribution
· Accounts for "wear" or "infant mortality" Â
· eta characteristic life Â
· beta shape factor (main influence) Â
· beta = 1 Exponential, beta > 1 failure rate increases with time, beta < 1 infant mortality
· Parameter 1 = eta, Parameter 2 = beta
Â
- Normal
· Also called Gaussian or Bell Curve
· Often used for MTBF or MDT
· mu - mean
· sigma - standard deviation
· Parameter 1 = mu, Parameter 2 = standard deviation
- Log Normal
· Used when positive "skewedness" is shown
· Sometimes used for MTBF, MDT
· MuAL mean Antilog
· SigF standard deviation factor
· Parameter 1 = MuAL, Parameter 2 = SigF
- Triangular
· The Triangular distribution is most useful in cases where you are modeling subjective estimates that lack a more specific theoretical foundation
· based on three parameters; minimum, maximum and most likely values
· failure parameter "1" is the minimum value
· failure parameter "2" is the maximum value
· failure parameter "3" is the most likely value
- Uniform
· The Uniform Distribution is also known as the Rectangular Distribution
· A uniform distribution is one for which the probability of occurrence is the same for all values of X (time).
· failure parameter "1" is the minimum value
· failure parameter "2" is the maximum value
· failure parameter "3" is not required
- Constant
· Constant a defined period of time that does not vary between failures. Used often for scheduled maintenance periods.
· parameter 1 only
- Never
· Never component will not fail in any life cycle unless specifically coded in VBA user coding. No need to put in "~infinite" MTBF. i.e., Exponential 10E+10
· Parameters not used (ignored)
- 3P Weibull
· Age Related Distribution with start time offset
· Accounts for "wear" or "infant mortality" and "time zero" offset (no failure will occur before this time)
· eta characteristic life Â
· beta shape factor (main influence) Â
· failure parameter "3" is "time zero" offset
· beta = 1 Exponential, beta > 1 failure rate increases with time, beta < 1 infant mortality
· Parameter 1 = eta, Parameter 2 = beta, Parameter 3 = time offset Â
-Â 2P-Constant
· Similar to Constant Distribution type, however, with an additional parameter (parameter 2) called "First Occurrence"
· The repeating cycle of Time Between Failures (TTF) will not begin until the time specified by this new parameter 2, at which time the component will fail and any subsequent failures will have TTF equal to the value specified in Parameter1.Â
· Changing mechup, opup, or currentage of a component with this distribution will result in the component immediately going into the TTF cycle specified by parameter 1.                                    Â
- Schedule             Â
· Has a single parameter (Distribution Number) distribution type
· Refers to the Schedule defined in the new "Schedule" tab in the Ram Data Editor (RDE) that will cause the corresponding component to change states as described in the corresponding schedule
· All other Failure Parameters (1 and 2) and all Repair Distribution selections are ignored when Schedule is selected as the Failure Distribution
Keywords: Exponential, Weibull, Normal, Log Normal, Triangular, Uniform, Constant, Never, 2P-Constant, Schedule, MTBF, MDT, TTF, RDE.
References: None |
Problem Statement: What is the significance of Available Capacity, Mechanical Capacity, Max Capacity, Set Capacity and Utilized Capacity in AFR? | Solution: Available Capacity
This is the ability of the unit to produce based on both the mechanical states (mechup) and operational states (opup) of components comprising the model. This is a READ ONLY PROPERTY.
Mechanical Capacity
This is the ability of the unit to produce based only on the mechanical states (mechup) of components comprising the model. "Turned-off" components have no effect on this capacity. This is a READ ONLY PROPERTY.
Max Capacity
This is the "Turn Up" capacity of a unit. This is a READ/WRITE PROPERTY at run time, and can be altered from VISIO or the RDE at design time.
Set Capacity
This is a property that the user can use to influence unit capacity with VBA. Set Capacity is reset to equal Max Capacity at each event, and is basically an override of Available Capacity. The only factors potentially constraining a unit below this value are constraints from other units and tanks. This is writeable from VBA and is intended as a tank level management tool. This property should not be used to "fail" units, instead use the mechup and opup properties of resident components to induce unit failures. This is a READ/WRITE PROPERTY at run time.
Utilized Capacity
This is the actual production of the unit based on all factors including equipment mechanical and operational states, external influences of other units and tanks, and user manipulation of SetCapacity. This is a READ ONLY PROPERTY.
If there is no turn-up capacity in the model then utilized capacity will always be equal to or less than available capacity.
Keywords: Available Capacity, Mechanical Capacity, Max Capacity, Set Capacity, Utilized Capacity.
References: None |
Problem Statement: What are the Port and communication protocols with AtOMS and AORA Client to connect with Server? | Solution: · Both AtOMS and AORA using Microsoft ODBC / UDL to connect with Server application.
· So, in principle, Microsoft ODBC Standards are used by AtOMS and AORA.
Please refer below link from Microsoft for their PORT (ANSWER: 1433) and communication protocols (ANSWER:TCP)
https://msdn.microsoft.com/en-us/library/cc646023.aspx#BKMK_ssde
http://superuser.com/questions/237508/what-ports-does-ms-sql-server-use-for-odbc-connections
http://www.justskins.com/forums/odbc-standard-tcp-port-138245.html
You can also search google for more details.
Keywords: PORT, PROTOCOL, AtOMS, AORA
References: None |
Problem Statement: How to resolve security issues with User Login in AtOMS ? | Solution: To resolve the problem, with user log-in , please try the following.
1. Log-in with the user , for example “John”, on the specific machine
2. Go to windows services, and restart “AFW Client Security Service”.
3. After restart, please try to launch AtOMS Client with correct users profile, in the BPE.
The above solution should Resolve any user access related Problem
Keywords: AFW
User accees
AtOMS
References: None |
Problem Statement: Why do I get an error " You do not have permission to login. " when using MOC? | Solution: When connecting to the MOC client you are prompted with a logon window and when you enter your usernmane and password you may receive the message
To resolve this issue you will need to check the following configuration steps needed for a user to authenticate
1. Check to make sure that the user has been added into the AFW Security Manager.
A. Open AFW Security manager
B. Click on 'Roles' and either add or check that the user has been added into the correct Role(s) and is
enabled. The active directory group or user account needs to be added to the role. This cannot be a nested
active directory account or a Local Global domain account.
C. Click on 'Applications' and 'Aspen Production Execution Manager' and add the user role to the object and
make sure its enabled.
D. You may need to clear the AFW cache on server and client. You can follow the steps in solution 130453 to
do this.
E. Check the AFW URL by opening the AFW Tools and make sure you have the correct path in the URL field.
2. If the AFW is configured correct the ensure that the Active Directory account has all completed information.
Regardless of the type of account you are using local or A/D account all fields of the properties of the account
much be filled out. For example first name , last name.
3. Check the MOC settings. You will need to be an Administrator or have Security access in MOC to change
settings.
A. Open MOC and the 'Config' Module and click the 'Workstation' button. If you have Workstations configured
for security or for RPL phases you need to make sure that the correct workstation name is entered here. The
workstation name could be the Short name or the Fully Qualified Domain name depending on your network.
4. You may also get this error if the user has been deleted and re-added to the system. In the 'Config' module
open the 'Users' and check to see if the account already exists. If this does please contact support if the
above does not resolve issue.
Keywords: Unable to login
Permission
MOC
APEM
eBRS
References: None |
Problem Statement: When I switch to Dynamics mode (from Steady State), and start my integrator, my tank level immediately jumps to 100%. Why? | Solution: In Steady State mode, HYSYS ignores any holdup (or liquid level) related information because this is irrelevant to the steady state mass balance. Upon switching to Dynamics mode, HYSYS will flash the tank inventory. If in steady state the tank feed was subcooled (or saturated) liquid only, there will be a liquid product only (and no vapour product).
If the "Initialize From Products" option is chosen and the integrator started (in Dynamics mode), flashing this stream will result in no vapour space within the tank and the tank level will jump to 100%.
If the desired initial liquid level is to be less than 100% (i.e. there is a vapour space, possibly with other components), then one of the other options "Dry Startup" or "Initialize from User" should be used. More information on these options can be found in the [F1] help.
As an example, if this was a water tank, being fed with 25deg.C water (at 1.5bar), there will be no vapour outlet in the Steady State. Flashing the product stream for Dynamics (using the "Initialize From Products" option) will result in 100% liquid level as this fluid is subcooled. If an "air" space within the tank is desired at the simulation start, the "Initialize from User" should be used, with the fraction of air specified.
Keywords: 100% liquid level, Initialize from Products
References: None |
Problem Statement: When I reduce the efficiency on my column top stage, I get a consistency error. Why? | Solution: The issue relates to the vapour fraction value in certain chemical systems. The error arises in columns without a condenser (or at least a condenser located in the column subflowsheet). A low column top stage efficiency can result in liquid being carried over (in the vapour) in the overhead 'vapour' stream. As such, in the column subflowsheet, the vapour leaving this subflowsheet is 2-phase. However, in the MAIN flowsheet, the stream exiting the column unit operation is expecting a vapour fraction of unity (i.e. a saturated vapour stream). As such, these conflicting values for vapour fraction will result in a consistency error.
There is a plan to have this issue resolved. However, in the meanwhile, there is a workaround.
In the Column environment, route the overhead "vapour" (i.e. 2-phase stream) to a 2-phase separator pot. Use the vapour stream from this separator as the vapour product of the column system. Allow the liquid outlet to be exported to the main flowsheet as well.
In the main flowsheet, use a mixing tee to recombine the 2 phases into a single stream.
The solver can now be reinstated and there should be no further consistency error related to column efficiencies.
Keywords: column efficiency, consistency error
References: None |
Problem Statement: How to perform collinearity analysis in DMC3 Builder V9.0? | Solution: Download the attached pdf document which contains a tutorial on how to perform collinearity analysis in DMC3 Builder V9.0.
Also attached is a dataset .clc file and a model .mdl file which were used for the example provided in the tutorial.
Keywords: DMC3
Constrained Identification
Mass balance
References: None |
Problem Statement: Do properties added to the Stream Results table in Aspen Plus V9 automatically appear in aspenONE? | Solution: aspenONE Web application is used to easily share Aspen Plus and Aspen HYSYS models and compare with actual plant data, side-by-side. This is why is really useful to report specific properties using tables.
If user customizes Stream Results table in Aspen Plus V9 and wants to see the same in aspenONE, user needs to create a Custom Table rather than Stream Results Table. For example to see Bubble and Dew Point in aspenONE you need to follow the next steps.
Add the property to a stream in Aspen Plus
Copy the properties to a custom table in Aspen Plus
Upload the model to aspenONE Drive
View the custom table in aspenONE
Keywords: Custom Tables, AspenONE, Stream Table, Aspen Plus
References: None |
Problem Statement: Why can I see the following error when I create a user-defined utility and attach it to a HeatX block?
ERROR WHILE CHECKING INPUT SPECIFICATIONS BLOCK NAME: HX MODEL NAME: HEATX STATE VARIABLES MUST BE SPECIFIED IN A UTILITY REFERENCED BY A HEATX BLOCK | Solution: In Aspen Plus, the state variables are temperature, pressure, and vapor fraction. It is mandatory to define the state variable in the material stream. Although you have defined this Utility as type General (User Defined) and specified heating and cooling values, you will get this error until you have specified default Aspen Plus Utilities.
In order to overcome this issue, you have to specify the inlet/outlet conditions for that Utility . You must also specify the component of that Utility in your model.
You can also provide Hot/Cold Inlet & Outlet material streams to a HeatX block along with the specification.
Keywords: Utility, State Variables, HeatX
References: None |
Problem Statement: I have two reactor vessels that are linked to PFD vessel objects. I want to switch the vessels which link to PFD objects without redrawing both PFD objects. I made this by switching the item number on Nozzle sheet Datasheet.
Right now, they are switched but the nozzles on the sketch for Vessel 1 shows on the datasheets for Vessel 2 and vice versa. How can I switch nozzles on vessels so they correctly populate the nozzles sheet datasheets? | Solution: Nozzles can be switched between vessel objects following the below procedure:
1. Go to ABE Explorer, and display vessel attributes. Then remove all nozzles as shown below.
2. Display the attributes of the other vessel and remove all nozzles as above.
3. Next, insert existing Item on Nozzles, select the nozzle from Existing Item menu
4. Do the same with the other Vessel.
5. After that, Reload workspace.
6. Then, open Nozzle sheet Datasheet for each Vessel, you will see that nozzles were switched on Datasheets.
This also can be done with other ABE objects which have a parent-child association, i.e. major equipment internals.
Keywords: Nozzles sheet datasheet, workbench, parent-child association.
References: None |
Problem Statement: :
How-to-export-stripchart-historical-data-to-a-csv-file? | Solution: 1) Go to the Dynamics menu and select Stripcharts
2) Select the Stripchart you would like to see the data
3) Click Edit
4) Select the tab Historical
5) Click Save to .CSV File
Keywords: csv, historical, stripchart
References: None |
Problem Statement: My calculated pump efficiency is above 100% - what could be causing this? | Solution: Such a situation usually occurs when pump curve(s) have been input. The user would have input efficiency / flow data for the generation of the pump curve. On the flowsheet, if the flow input value to the pump (possibly calculated from an upstream unit operation) is outside of the flow data range, HYSYS will extrapolate this curve. In some cases, if the flow is significantly outside of the data range, it is possible that this extrapolation will result in an efficiency of greater than 100% being estimated.
Keywords: Pump, 100% efficiency
References: None |
Problem Statement: Why do I see less sulfur conversions in the Thermal Stage result in the Performance Summary compare to the results in the Furnace, as shown below: | Solution: User may see this difference if the "Allow simulation of back-reactions in the WHE" is checked in the Waste Heat Exchanger in the thermal stage, as shown below:
By default, the Allow simulation of back-reactions in the WHE check box is selected; you can clear it if desired. Various reactions occur in a typical Waste Heat Exchanger. These reactions include H2 + S re-association reactions and CO + S reactions. Select this check box to use empirical models (originally created by Sulphur Experts) which predict the extent of these reactions for your simulation. We recommend that you select the Empirical furnace model for your Reaction Furnace when this check box is selected, since these models were developed directly with the Empirical Kinetic reaction furnace models.
Keywords: Sulsim, Sulfur conversion
References: None |
Problem Statement: How to model a Rupture Disk in Aspen HYSYS Dynamics | Solution: There is no unit operation available to model a rupture disc, however you can use a relief valve instead. In general, you should follow the procedure below to set up a rupture disc:
Add a Relief valve from the Object palette
Specify in Design | Parameters the Set Pressure and Full Open Pressure. These values represent when the rupture disc will be broken to relief pressure. Both values should be the same.
In Dynamics | Advanced select Fail Open. This means that when the valve gets to the set pressure it will be completely open.
In Rating | Sizing under Orifice Area enter the area value for the rupture disc.
In Dynamics | Specs select the check box for “Enable Valve Hysteresis” and select a low pressure value to keep this valve open even when the pressure is lower than the set pressure. This is needed since a rupture disc cannot be closed in real life.
Note: Hysteresis is the dependence of the state of a system on its history. In this case the valve will remain open because in one point in the past it reached the set pressure value.
Please refer to the attached sample case in which RV-100 represents the rupture disc. In the strip chart, you can track the following variables:
Pressure at inlet stream to rupture disc
Pressure at outlet stream to rupture disc
Percentage open of rupture disc
Pressure in stream 1 (Feed of the simulation) this is the value that will be modifiedRun the dynamics case and take notice of the simulation settings and inputs:
There is an event scheduler that will increase 50 kPa per minute the pressure in stream 1 until rupture disc reaches the set point and will open to 100%. There is also a controller to close VLV-100, this valve is feeding the tank, and is used as an emergency stop for the process. You will notice that even if the pressure is bellow set pressure when the system has been restored, the rupture disc is not closed.
Keywords: Rupture Disc, Relief, Relief Valve
References: None |
Problem Statement: How can I identify whether my current license file has the option to commute? | Solution: In order to identify whether a license file is commutable, you must check the license file and confirm whether commuting is enabled. Only network based license files will have the commuting option.
1. To check whether the license file is commutable,
please navigate to Windows Start > All Programs> AspenTech folder > Common Utilities > SLM License Profiler.
2. Locate your license file and click the Load Information button and then the "View Licenses" button. Once the license information is retrieved - scroll to the right and find the column named "Commutable"
If it is Yes - Licenses can be commuted.
If it is No - Licenses cannot be commuted.
Please refer to the screenshot below:
For more details on how to commute a license, you can refer the below link:
https://esupport.aspentech.com/S_Article?id=kA80B000000CetdSAC&articleType=Tech_Tips__kav&avId=ka80B000000Ceu1QAC
KeyWords
SLM, Commute, License file
Keywords: None
References: None |
Problem Statement: How do I obtain the vapour and liquid phase enthalpies in the performance page of the Heater Block? | Solution: The Heater Block in Aspen HYSYS only gives the enthalpy for the overall phase in the Performance page. If the user requires the enthalpies for the individual phases then the Properties Table available in Stream Analysis can be used. Follow the procedure given below to generate the enthalpy plots for the individual phases.
Open the inlet stream to the Heat block and select the Analysis page available under Attachments.
Create Property Table from the available Stream Analysis
Select Pressure for Variable 1 and State as the Mode.
Enter the inlet and outlet pressures for the heater as state values
Select Temperature for Variable 2 and Incremental as Mode.
Enter the inlet and outlet temperatures for the heater as Lower and Upper bounds
Select Dep. Prop on the left.
Add two variables: vapour and liquid phase enthalpies.
Now Click Calculate.
When the calculation is complete, the plots for the enthalpies can be found in the Performance page.
Keywords: Heater Block, Performance Plots, Phase Enthalpies
References: None |
Problem Statement: How to simulate compressor settle-out in Aspen HYSYS Dynamics? | Solution: Compressor settle-out is the differential pressure drop that results in a compressor trip at the maximum pressure increase across it. A compressor trip or shutdown occurs in the event of various alarm conditions. Some examples include high vibrations in the compressor or loss of lube oil in the compressor. During these shutdowns it is important to avoid entering the surge region as well, which means very fast acting recycle valves must be implemented.
After the compressor is tripped, a differential pressure drop across the compressor will develop if there is no depressurization occurring. This differential pressure is what is known as "settle-out pressure". The following example will illustrate this concept in greater detail.
This example will leverage a completed model built in Aspen HYSYS Dynamics to simulate compressor settle-out.
Keywords: Compressor, Settle-Out, Event Scheduler, Dynamics
References: None |
Problem Statement: Natural gas hydrates are solid crystalline assembles snow. Its formation is usually caused by presence of "free" water, low temperature, and high pressure. The presence of H2S and CO2 also promotes formation of hydrates. Hydrate formation is rapid and the plugged pipeline can be costly to clean up. This will result in costly downtimes.
Typical mitigation methods include:
· Dehydrating the fluid
· Maintain the temperature above the formation temperature
· Inject hydrate inhibitor | Solution: Using the Aspen Hydraulics and Aspen HYSYS to:
· Determine the potential location of hydrate formation
· Investigate the methods of mitigation:
o Thermal Insulation
o Injection of hydrate inhibitor
· Optimizing the inhibitor injection rate
You will learn to:
· Leverage hydrate formation utility in Aspen HYSYS and Aspen Hydraulics
· Monitor the pipeline behavior using tools within Aspen Hydraulics
· Use hydrate formation utility to optimize the inhibitor injection rate
Keywords: Pipeline Hydraulics, Aspen HYSYS Upstream, Aspen HYSYS, Hydrate, Hydrate Inhibition
References: None |
Problem Statement: When browsing SQLplus Reporting (http://<serverName>/sqlplus), the Section Type, buttons, etc. are shown as blank. | Solution: This is due to missing registry entries in the server on which SQLplus Reporting is installed. Perform the following steps to resolve the issue.
Open Windows Registry Editor by entering regedit in Run dialog box.
Browse to the registry entry HKEY_LOCAL_MACHINE\SOFTWARE\Wow6432Node\AspenTech\InfoPlus.21. If it is missing, create it.
Expand the registry entry to check whether there is a key called SQLplus. If it is missing, right-click on InfoPlus.21 and select Key from context menu.
Rename it to SQLplus.
Right-click on SQLplus and select Key from context menu. Rename it to Report.
Right-click on Report and select New | String Value from context menu. Add the following entries.
Reports - C:\ProgramData\AspenTech\SQLplus
Templates - C:\Program Files (x86)\Common Files\AspenTech Shared\SQLplus\xsl
It will look similar to the following screenshot.
Note: Ensure that the folder path exists on the server.
Keywords: None
References: None |
Problem Statement: How to add an Excel spreadsheet into a datasheet sketch field without extra rows/columns? | Solution: When adding an Excel spreadsheet into a datasheet sketch field, it will be shown with either extra rows or columns if previous formatting has been applied to such spreadsheet and deleted with the 'Clear' option in Excel.
So, to successfully embed a spreadsheet into a sketch field keeping the user defined format, avoid the use of the 'Clear' option.
Keywords: Excel Datasheet Editor, Excel, XLS, Spreadsheet, Datasheet, Sketch field, Rows, Columns.
References: None |
Problem Statement: How is the expander Mafi-Trench efficiency modeled in Aspen HYSYS? | Solution: The Mafi-Trench curve correlates the isentropic efficiency with the ratio of the expander tip speed over the stage isentropic enthalpy change. Atlas Copco uses a similar approach.
Aspen HYSYS models the expander’s Mafi-Trench efficiency using the method based on the curve approach proposed by the Mafi-Trench Company. The definitions for the U2/CO and other parameters are defined in the attached paper (‘Tutorial on Cryogenic Turboexpnders’, by Jigger Jumonville, Atlas Copco Mafi-Trench Company LLC).
The equations for both curves are shown below:
1) Mafi-Trench:
2) Atlas Copco:
However, there is a bug in the Mafi-Trench efficiency curve in Aspen HYSYS. The operating point lies out of the curve and the calculated efficiency and power are therefore incorrect. For more information, read the Known Issue article 000044607: 'CQ00752353: The Mafi-Trench Efficiency Curve for Expanders does not work properly in Aspen HYSYS'.
Keywords: Expander, Mafi-Trench, Atlas Copco, Efficiency Curve.
References: None |
Problem Statement: When trying to generate a procedure code from Tools | Generate procedure code, the following error message is issued: ‘No suitable version of Visual Studio was found’ appears:
ACM v9 only supports Microsoft Visual Studio C++ 2013. No other versions are supported. Is it possible to use Visual Studio 2015? | Solution: ACM v9 searches for the environment variable VS120COMNTOOLS, which is created when you install Visual Studion 2013. This variable is the path to the installation of Visual Studio (C:\Program Files (x86)\Microsoft Visual Studio 12.0\Common7\Tools\).
To use Visual Studio 2015 with ACM v9, create a new system variable VS120COMNTOOLS under: My computer | Properties | Advanced Settings | Environment Variables…; and set to the path of installed Visual Studio version:
Note that you must close and restart ACM if you change environment variables
Keywords: Generate Procedure Code, Error, VS120COMNTOOLS, Microsoft Visual Studio Version.
References: None |
Problem Statement: Aspen Calc GUI provides ways to export calculation as XML files which can be useful to move calculations to a new server, share the calculation with other users or simple have a backup of the calculation. However, the Aspen Calc GUI just allows the creation of a single XML file at a time. This solution provides a way to export every calculation inside an Aspen Calc folder as an XML file using a single Aspen SQLplus query. | Solution: Copy the query below to the Aspen SQLplus query writer-
local calccmd, CalcName, Calculation, CalcFolderName, GroupName, XmlCalcsPath char(255);
calccmd = CreateObject('CalcScheduler.CalcCommands');
CalcFolderName = 'TestFolder' --Change folder name as needed
XmlCalcsPath = 'C:\Temp\' --Change this for a known folder, must end with /
For each CalcName in calccmd.GetCalculationList Do
If CalcName Like '%'||CalcFolderName||'%' Then
Calculation = calccmd.GetCalculationObject(CalcName);
Set output XmlCalcsPath || Replace(CalcFolderName in Cast(CalcName as CHAR)) || '.xml';
Write '<?xml version="1.0"?><AspenCalc>';
Write calccmd.SaveCalcXML(CalcName);
Write '</AspenCalc>';
Set output default;
End;
End;
Change the value for variable 'CalcFolderName' to the name of AspenCalc folder that have the calculations to export (use the value empty like '' to get all calculations) and 'XmlCalcsPath' to the path where the exported XML file will be created.
Keywords: SQLplus
Aspen Calc
XML
References: None |
Problem Statement: In rare instances the Aspen IP.21 Process Browser controls do not install automatically when a client is prompted to download and install them and the following error message may be returned:
Component download/registration failed! - Please check your registry/security settings | Solution: Firstly since this is a thin client you will need to download the AtWebControls.cab files from the IP.21 Process Browser Server. Default location for this file is c:\Inetpub\wwwroot\AspenTech\AspenCUI\
1. Download this file to the client machine as well as the AtWebControlsThinClient.zip file attached to this KB.
2. Copy both files to a location on the client machine, eg. c:\Controls
3. Unpack both files to this location
4. Edit the AtWebControlsThinClient.bat file to ensure paths are correct - note, this script assumes that the C-drive contains the main Windows and Aspentech installations:
For 64 bit Window Operating System the files must be installed into: C:\Program Files (x86) and C:\Windows\SysWOW64
For 32 bit Window Operating System the files must be installed into: C:\Program Files and C:\Windows\System32
5. Open a MS-DOS prompt using "Run As Administrator" option.
6. Go to location, eg. cd c:\Controls
7. Run the batch file and follow the prompts.
Once you have completed, open Internet Explorer and browse to the IP.21 Process Browser website and select to view a Trend.
Keywords: Web21
trend
invisible
empty
References: None |
Problem Statement: Control Valve Failure: Dynamic Gas Blow-by | Solution: Disclaimer: This article and the example provided is for instructive purposes only. Any model calculations and methodologies should be verified depending on your specific regional and/or project requirements.
This Aspen HYSYS Dynamics example covers how to model the effects of gas blowby resulting from a control valve that fails 100% open. The article serves as a brief overview of the attached example and a walk-through the general mindset as you prepare a dynamic model.Â
Keywords:
References: None |
Problem Statement: When trying to connect to Aspen InfoPlus.21 database in Aspen Tag Browser, the status bar is showing error as per below screenshot. | Solution: The Aspen Tag Browser depends on the AspenTech SQLplus ODBC driver to connect to the Aspen InfoPlus.21 database. The above is due to missing registry entry for the Aspen SQLplus ODBC driver.
To resolve this issue,
1) Launch Windows Registry Editor.
2) Browse to HKEY_LOCAL_MACHINE\SOFTWARE\Wow6432Node\ODBC\ODBCINST.INI.
3) Check to see whether there is a registry key called AspenTech SQLplus.
The registry key AspenTech SQLplus has the following entries as shown in table below.
Name Type Data
Driver String Value C:\Windows\system32\ip21odbc.dll
Setup String Value C:\Windows\system32\ip21odbc.dll
UsageCount Dword (32-bit) Value 0
KeyWords
Keywords: None
References: None |
Problem Statement: How is the viscosity for hypocomponents calculated? | Solution: To calculate the viscosity for a hypocomponent, the expressions below are used:
z = exp( exp( A + B * log ( T * 1.8 ) ) ) - 0.7
x = ( -0.7487 - 3.295 * z + 0.6119 * z^2 - 0.3193 * z^3 )
visc = ( z - exp( x ) ) * dens * MW / 1000
where,
dens = gmol/L
T = K
About Coefficients A and B, HYSYS uses the following estimation method to calculate the Liquid Viscosity coefficients A & B point properties:
For non-Hydrocarbon or NBP < 270 K, Letsou Stiel is used.
For Hydrocarbon and NBP < 335 K, NBS viscosity is used.
For all other cases, Twu is used. For more information, please refer to the original publication by Dr. Twu (Chorng H. Twu, Internally Consistent Correlation for Predicting Liquid, Viscosities of Petroleum Fractions, Ind. Eng. Chem. Process Des. Dev. 1985, 24, pp 1287-1293, Eq. 19).
Keywords: Hypocomponents, Viscosity, Coefficient A, Coefficient B
References: None |
Problem Statement: How can I use the homotopy tool in Aspen Custom Modeller? | Solution: Homotopy provides a way of moving from one converged solution to another solution with different values for one or more of the homotopy variables. It is a useful technique where it is difficult to obtain convergence for a particular specification, but where you already have a converged solution for a different specification.
Homotopy works by moving along a path to the new solution, and solving a number of interim points along the way. Let HOM1 be the vector of values for the homotopy variables at the point you have already solved, and HOM2 is the vector of values for the point to which you want to move. In a homotopy simulation, your AspenTech product attempts to solve a number of points at values for the homotopy variables of: Homotopy = HOM1 + theta * (HOM2 – HOM1)
Where:
Theta=Homotopy parameter. This is a number that is moved from 0 to 1 at the successive solutions. When theta is 1, this corresponds to the specification HOM2. You can control the way theta changes between successive solutions.
Please have a look at the Ssmeth acmf file available at C:\Program Files (x86)\AspenTech\Aspen Custom Modeller V8.8\Examples\SSMeth.
In the All Items pane of the Simulation Explorer, click Flowsheet. In the Contents pane, double-click the script named RunHomotopy. This script initializes the homotopy target variables and enables homotopy.
To see the results of running this script, from the Tools menu, click Homotopy. In the Homotopy dialog box, you can change the initial and target values of the variables by double-clicking the variable names in the list. To start the solution, click the Run button.
Fixed or Initial variables can be dragged and dropped on to the Homotopy tool.
The simulation solution is moved from the current solution point to the solution at the target values of three fixed variables: Feed Flowrate Reactor Temperature Reactor Pressure
Keywords: Homotopy, convergence
Keywords
Homotopy, convergence, solution
References: None |
Problem Statement: In the Pipe Segment ‘Slug Tool Results ‘, what are the implications when the frequency indicates Min or Max? | Solution: The slug tool evaluates slug flow characteristics at a given slug frequency. This slug frequency is either a User Specified value or as calculated by Hill & Wood correlation in the Slug Tool Frequency Options.
The slug tool result table displays slug properties (lengths, velocity, holdup, pressure gradient etc.) for each position along the length of the pipe.
The View Cell Plot shows the full range of possible slug frequencies (tabular and graphical form) for a single position in the pipe and their corresponding slug properties.
The slug properties displayed on the slug tool results are the corresponding properties for the Hill & Wood correlation or User Specified frequency on the slug tool frequency option.
When the correlation or User Specified frequency on the slug tool frequency option lies outside this range of possible frequencies, the field in question shows either the minimum or maximum.
"Min" means that the frequency (calculated by the Hill & Wood correlation or the User Specified frequency) is less than the smallest possible frequency available in Cell View Plot.
"Max" would mean that correlation or User Specified slug frequency is greater than the largest possible frequency for which slug properties were calculated.
For more information on Slug Tool Analysis refer to Knowledge Articles
134725-2: Why does Aspen HYSYS sometimes report slug flow with slug length greater than the pipe length?
128568-2: How are Slug Length and Bubble Length defined in the Pipe Segment Slug Tool calculations?
Keywords: Min, Max, Slug, Tool, Results,Hill & Wood
References: None |
Problem Statement: Is it Possible to Control Heating/Cooling Medium Level in Shell Side of Heatx Block? | Solution: A slight workaround is needed. The attached zip is a V9 example with boiling propane cooling down hot oil. In this model, dynamics for the heat exchanger with nominal inlet and outlet volumes of 1m3, and sent to pressure driven AD. AD models the dynamic heatx as a volume followed by an instantaneous heat exchanger followed by another dynamic volume. In the attached dynf, on the heatx configure form user needs to changed everything to Instantaneous except the ColdOut (this is optional - you could keep all the other volumes and this would still work). The ColdOutVol is vapor-liquid. It's total volume is specified above as 1m3, and it's liquid volume is a function of heat transfer. Therefore it is necessary to added a flowsheet equation relating the area of the exchanger (which is usually fixed) to the level of the refrigerant:
K as pos_large(Fixed,0.219479);
BLOCKS("B1").A_exch = K * BLOCKS("B1").ColdInVol(1).Vl;
And then changed A_exch spec from "fixed" to "free". Now the heat transfer area of the exchanger is a function of the refrigerant level. To control this level we need to expose Vl as a control variable in HeatX. To do this you need to copy the library HeatX model to Custom Modeling and write 1 declaration and 1 equality:
Vl as output volume;
Vl = ColdOutVol(1).Vl;
Declaring as "output" means an output control signal can be connected. Attached is the complete example. User need to be careful to specify the OP minimum on the PID to >0 (e.g. 1%) otherwise if the refrigerant flow hits zero, the model calculates Q=0 and the refrigerant level does not change. Specifying 1% calculates a low but non-zero Q allowing the level to go all the way to zero (i.e. almost all refrigerant vaporized). Obviously there is an upper limit - you can specify level = heat exchanger volume because you would need a very high U, A and refrigerant flow.
Keywords: Heatx, Level.
References: None |
Problem Statement: The ‘Go to Parent’ flowsheet in the Flowsheet/Modify tab appears disabled for certain files when the following workflow is performed:
1-Access sub-flowsheet in simulation environment
2-Change to Safety Analysis, then back to simulation environment (where sub flowsheet is still displayed).
3-If user clicks ‘Go to Parent’, user is sent back to Safety Analysis environment.
4-Going back to Simulation environment, opens subflowsheet, with ‘Go to parent’ option disabled. | Solution: Instead of using the (now disabled) ‘Go to parent’ function, choose to display flowsheet in the View tab. This takes the user back to the main (parent) flowsheet.
Keywords: Safety Analysis, Simulation, Sub-Flowsheet, Parent Flowsheet
References: None |
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