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Problem Statement: How to manage the FileCache created by Aspen Mtell | Solution: Aspen Mtell will create File Cache files on user machine when using Agent Builder to query SQL Server or Historian Server. The cache will be used when a user try to query same data from SQL Server or Historian.
User C:\ drive may get full if the Cache file size grows big. You can delete the FileCache contents with no adverse effects to your Aspen Mtell application or data. Be sure to close down all Aspen Mtell applications before doing so.
Go to C:\ProgramData\AspenTech\Aspen Mtell\FileCache folder and delete Cache and policy folders.
Keywords: File cache
Cache
References: None |
Problem Statement: In the results database of a PPIMS model, we see the in PrInventory table (and some other tables as well), the column “Marginal Value” could not be interpreted the same way as marginal value in the full solution report. What does it mean?
In the above example, the Marginal Value is not 0 although the closing inventory is neither at the minimum or maximum limits.
If you look at the column variable directly, it shows the column Dj (marginal value of a column variable) to be 0 in the matrix analyzer – This is correct. So what does the “Marginal Value” in PrInventory really means? | Solution: The “Marginal Value” in PrInventory doesn’t mean the marginal value of that stream. It represents the negative of the respective material balance row (either VBALXXX or WBALXXX, with “XXX” being the name of the stream) divided by the length of that period. Using the same example shown above, lets look at the material balance of that stream (URG):
The Pi Value (marginal value of a row) is 3477.27. In table PERIODS, we see that the length of period 1 is 31 days. –(3477.27 / 31) = -112.17. That’s where the number you see in the above screenshot came.
If you are only looking for the marginal value of URG, you should directly go to the full solution report or the matrix analyzer. The marginal value of PrInventory table is not meant to directly show the column marginal value to you.
Keywords: None
References: None |
Problem Statement: Is it possible to model in detail the condenser and reboiler in a column? | Solution: You can do a detailed modeling of a condenser or reboiler for a RadFrac column by connecting a heat exchanger to a column using pseudo streams. You need to define a pseudo stream on RadFrac to represent the fluid to the condenser and reboiler. Be careful to connect the pseudo stream to the correct connection ports.
Start by connecting a new stream to the pseudo stream connection port on the RadFrac block in the flowsheet view. The pseudo stream connection port is typically located on the right side, towards the center of the RadFrac icon.
Then feed that stream to a HeatX block, add the fluid to the HeatX feed, and do NOT return the column fluid.
Under the RadFrac | SetUp | Streams | Pseudo Streams form, specify the flow to be from liquid stage N-1, for the rebolier and vapor from stage 2, for the condenser. The heat duty calculated in the column for the reboiler and condenser is used as an input for the HeatX blocks. Alternatively, you can use a calculator block to equate the duty of the column to the duty of the heat exchanger.
Once you have the HeatX solved in shortcut you can move on to a more rigorous calculation using Activated EDR.
The pseudo streams are not accounted for in the source unit's mass or energy balance. In this case, the sum of the feed streams equals the sum of the non-pseudo Product streams for the RadFrac column. However, the pseudo stream is part of the mass balance for any unit that is connected to the downstream side of the pseudo stream. See the attached example file.
Alternatively, you can use the Reboiler Wizard to configure a HeatX block and a Flash2 block to model the reboiler of this column as well.
Keywords: Pseudo stream, HeatX, detailed, heat transfer
References: None |
Problem Statement: What are some of the key differences between PIMS-DR and PIMS-AO? | Solution: The core optimization algorithm is different in PIMS-AO than DR. PIMS-AO is generally faster, more accurate, and have less probability of running into local optima.
In PIMS-DR, the core optimization algorithm is called “recursion”. When calculating properties of different streams in a pooling submodel, PIMS-DR needs to linearize the non-linear terms. This depends on the user to provide a good enough starting point for the optimization process to start.
In the above example, the user needs to provide an initial estimate for the SPG of NAP, NP2, NP3. Also the N2A of the same three streams as well. The properties will be treated as values. The initial estimate is the starting point of the algorithm, so a “bad” initial guess will cause the algorithm to go into local optima.
The solver of DR uses recursion to update these values until they converge within the error tolerance.
In PIMS-AO, this problem is treated differently.
The properties of streams are treated as variables. The user still needs to provide initial guess, but because PIMS-AO’s solver could take non-linear terms, it takes these non-linear equations directly into the solver. This means it doesn’t rely on recursion. There are also settings you can tune to avoid local optima and generate more accurate results.
PIMS-DR PIMS-AO
Optimization Algorithm Recursion: Properties depend on initial starting point and updated by each recursion pass Iteration: Takes non-linear equations directly and takes properties directly as variables
Performance No multi-processing available in DR Multi-Processing: Allows users to use all logical cores in their machines. This will improve solving performance drastically
Accuracy The user is only able to start with 1 starting point. This is the initial guess values the user provides Multi-Start: The user is able to use more than 1 starting point. The algorithm will calculate with respect to all starting points and choose the best result. This minimizes the probability of local optima
Calculation The user is able to add linear calculations in data tables Non-Linear Equation: The user is able to add non-linear calculations to the model. The solver is able to take those equations directly
Troubleshooting The user is able to use data assistant to troubleshoot infeasibilities and other issues XLR Viewer: The user is able to use XLR Viewer to troubleshoot. XLR viewer tells the user what variables are causing infeasibilities. It is a better designed user interface and easy to use
Analytics The user can set up different cases to evaluate different scenarios after the run Sensitivity Analysis: Allows user to run Parametric Analysis, Goal Programming, and other built-in functionalities user can directly run without hassling with setting up cases manually
Keywords: None
References: None |
Problem Statement: How do you use homogeneous nucleation for particle generation throughout the course of a polymerization? | Solution: Attached is an example of butylacrylate and vinylacetate emulsion with homogeneous nucleation and continuous addition of monomers which shows how the particle generation continues throughout course of polymerization which is a feature of the homogeneous nucleation.
The emulsion polymerization model is applicable to emulsion polymerization processes where nucleation occurs by both the micellar and homogeneous mechanisms or to seeded polymerization. A wide variety of processes are used in emulsion polymerization.
In emulsion polymerization, free-radical propagation reactions take place in particles isolated from each other by the intervening dispersion medium. This reduces termination rates, giving high polymerization rates, and simultaneously makes it possible to produce high molecular weight polymers. One can increase the rate of polymerization without reducing the molecular weight of the polymer. Emulsion polymerization has more recently become important for the production of a wide variety of specialty polymers.
To appreciate the complexities of emulsion polymerization, a basic understanding of the fundamentals of particle formation and of the kinetics of the subsequent particle growth stage is required. A number of mechanisms have been proposed for particle formation. It is generally accepted that any one of the mechanisms could be responsible for particle formation depending on the nature of the monomer and the amount of emulsifier used in the recipe.
The two common mechanisms for particle formation are:
Micellar nucleation - micelles, which are aggregates of emulsifier molecules, act as the site of nucleation
Homogeneous nucleation - the radicals produced in the aqueous phase polymerize with dissolved monomer and precipitate out to form precursor particles. The precipitated precursor particles coagulate with each other until a stable particle is formed
In an Emulsion Polymerization Reaction, the nucleation is specified on the Reaction | Phases | Particles sheet.
For more details on the Emulsion model, go to the Help under Aspen Plus
Keywords: None
References: -> Aspen Polymers Reference Manual -> Aspen Polymers Reaction Models -> Emulsion Polymerization Model.
For an example that illustrates how to use the emulsion model to simulate styrene butadiene copolymerization, see the Help under Getting Started with Aspen Plus -> Tutorials -> Aspen Polymers Applications -> Styrene Butadiene Emulsion for details. This is an example of a process that follows micellar nucleation and subsequent growth is the production of styrene-butadiene rubber (SBR) latex in semi-batch reactors for paper coating applications.
The example file is located in
..\AspenTech\Aspen Plus Vxx\GUI\Examples\Polymers\Polystyrene\sbd.bkp
In the attached example of butylacrylate and vinylacetate emulsion with homogeneous nucleation, it can be observed that the average particle diameter of the particle diameter of the particle decreases after increasing in the initial period. This is due to the continuous production of small particles which tend to reduce the diameter of the particle. In a real system, as agglomeration of the particle takes place, we would not expect a decrease in the particle size.
We have deliberately chosen monomer chain transfer constants to give a DPN of 1000 and a DPW of 2000. The kinetic constants are in the range of values reported in the Ph.D. thesis by Dimitratos.
Some adjustment to kinetic constants were made to get the expected values for the number of particles and the size of the emulsion particles. However, this example illustrates important aspects of the homogeneous nucleation such as the effect of critical chain length, kinetic constants etc. on particle formation and growth in the homogeneous nucleation process..
Reference: Dimitratos, State, “Estimation of Butylacrylate and Vinylacetate Polymerization" Lehigh University, 1988. |
Problem Statement: The value for DCPLS in PURE37 seems incorrect. The value in earlier versions seems reasonable. | Solution: DIPPR changed the liquid CP correlation for EG from equation 100 to 124, but the converter did not support this equation at the time we converted the data for PURE37. DCPLS is used only in predicting solid solubility of molecular species. If necessary, the value can be added on the Properties Methods | Parameters | Pure Components | Scalar form.
Fixed in Version
Targeted for the next release.
Keywords: None
References: : VSTS 498659, 498105, 488081 |
Problem Statement: After editing my backup (.bkp) file in text editor such as Notepad or Wordpad to remove an ADS section that was corrupt, the file crashes when opening in Aspen Plus. | Solution: We do not generally advise editing backup files directly, but this is sometime done to fix issues with the files. If you edit the file in Notepad, you must be sure to set the Encoding to ANSI on the Save dialog box. If it is set to a Unicode option such as UTF-8, this will render the file unreadable by Aspen Plus.
Keywords: None
References: : VSTS 498676 |
Problem Statement: What are some steps you can follow to maximize your AspenTech support experience while working from home? | Solution: AspenTech Support is available to assist you while you are working from home with a variety of services, including but not limited to:
Access Technical Support via chat, phone, e-mail or web
24x7 Customer Care Service
Access to online Knowledge Base including product documentation
Assistance in resolving software installation issues
Assistance in identifying defects and resolving product usage issues
For more information, visit our Customer Services Guide
To maximize your support experience when receiving remote assistance, we recommend the following:
While Chrome is the recommended browser, Internet Explorer 11 and higher, and Firefox are supported. Ensure you have the latest version installed. Please make sure to visit the Support Site FAQ if you are having any issues navigating through the site.
Test your WebEx connectivity. WebEx is the remote access tool AspenTech Technical Consultants use to remote into your system for support.
Visit our Working From Home FAQ article for tips on setting up your AspenTech software when working from home.
If you haven’t already, register on the support site for access to the knowledge base and documentation.
If you are already registered on the support site, make sure to update your contact details in your support profile page so we can reach you while you are remote. Ensure your mobile phone number is up to date.
Take the Support Site tour to learn about the different resources.
Keywords: Remote Support
Homeworking
AspenTech Support
COVID-19
References: None |
Problem Statement: How to run Aspen Plus simulation from the command prompt (Aspen Plus Simulation Engine). | Solution: You can use the Aspen Plus user interface to develop the simulation model for a run and view the results, but when you have very huge flowsheet to run, you may consider to run the Aspen Plus simulation engine separately from the user interface. Doing this is one way to achieve maximum performance for large flowsheets, but you will lose the convenience of a graphical interface.
A sImulation can be run without the need to open the Aspen Plus User Interface. What you need is to run the Aspen Plus generated input file using Aspen Simulation Engine in the Customize Aspen Plus window.
To run the Aspen Plus simulation engine standalone:
1. Open up your existing simulation either .bkp or .apwz.
2. From the File menu, click Export.
3. In the Save As Type field, select Input File (.inp). Enter the Run ID for the filename.
4. Run Aspen Plus Simulation Engine from Start Menu | All Programs | AspenTech | Process Modeling V8.X | Aspen Plus | "Aspen Plus Simulation Engine" (for V8.0 & V8.2) or "Customize Aspen Plus VV.X" (For V8.4 and above)
NON-INTERACTIVE Run using Aspen Plus Simulation Engine
1. If you just want to run the simulation file without need to edit any input, which we consider as NON-INTERACTIVE Run, you can just directly input command "Aspen runid" as mentioned below.
2. From the prompt in an Aspen Plus Simulation Engine window (ls like normal Windows Command Prompt, you have to direct to your working directory), enter the command: Aspen runid (eg. If you saved your file name as cyclohex.inp, then your command will be Aspen cyclohex)
3. The "Aspen runid" command will immediate execute your input file and complete the run of your simulation then show you the warning messages if any.
4. When the run is complete, you can directly view the text version of the run results in the runid.rep file, or you can view the results graphically by importing the runid.sum (summary file) file into the user interface by opening Aspen Plus, and from the File menu, click Import and in the Files Of Type box, select Summary file (.sum).
5. From the file list, select the Run ID and click OK.
6. You can now review the results and modify the input in the user interface, as if you had made the run from within the user interface.
INTERACTIVE-Run with Aspen Plus Simulation Engine
1. If you want to edit the input file before you run using Aspen Plus Simulation Engine, you can either manually open up the .inp file using Notepad application or use the input language in Aspen Plus Simulation Engine.
2. Before you can use input language to interactively run your simulation using Aspen Plus Simulation Engine, you need to add a command in your .inp file.
3. Open up your .inp file using Notepad, and add the sentence "SIMULATE INTERACTIVE=YES" in the text as shown below and save it:
4. Once you added the above sentence in the .inp file, same as previous, use the command "Aspen runid" to run the simulation input file that you have just saved as above.
5. When running Aspen Plus interactively, you can communicate with Aspen Plus by using interactive commands to perform actions (for example, executing part or all of the simulation or displaying results). You enter commands at the Aspen Plus prompt (A+>).
Refer to the documentation "Aspen Plus Vx.x Input Language Guide" from http://support.aspentech.com/ to understand the input language (and associated keywords) Aspen Plus uses to communicate between the GUI and Engine.
Keywords: Aspen Plus Simulation Engine, Input file, Input Language, inp, command prompt
References: None |
Problem Statement: How do I obtain a license to run the Aspen HYSYS OLI Interface? | Solution: To use the Aspen HYSYS OLI Interface, you must first obtain the license directly from OLI Systems.
See (http://www.olisystems.com/contact) for more details.
Keywords: None
References: None |
Problem Statement: Getting “BATCH21_SP_GET_GENEALOGY has too many arguments specified.” while plotting Genealogy plot in AspenONE Process Explorer.
A new plot type, Genealogy, has been added to aspenONE Process Explorer V11 to perform Track and Trace analysis. However while trying to create a new plot, you encountered the following error. | Solution: You need to upgrade the APRM Database to version 16 in order to use this new feature in v11.
Run Aspen Database Wizard.
Select Aspen Production Record Manager and click Next
Select Update the existing database and database objects and click Next
Click Next
Select Microsoft OLE DB Provider for SQL Server / Oracle depending on which database is used.
Enter the details and click on Test Connection
Ensure Test Connection succeeded and click OK, click OK again.
Click Next
Click Next again.
Click Finish
Click Close
Keywords: Genealogy
Too many arguments
References: None |
Problem Statement: Why are my custom logos not displayed when using Web Datasheet? | Solution: The cause could possibly be due to ABE not able to copy the image file from "C:\AspenZyqadServer\Basic Engineering37.0\WorkspaceLibraries\Templates" to "C:\Program Files\AspenTech\Basic Engineering V11.0\SoloClient\wwwroot\Datasheets\images" for solo version, or to "C:\inetpub\wwwroot\AspenTech\aspenONEABE\Datasheets\images" for standalone version.
The workaround is to manually copy the file to the above location. The user will need to provide Admin right to perform this action.
If the file has been moved to the above folder and the image still not displayed properly, it's likely that the html file is referencing the wrong bitmap file. This has been seen to happen when the custom bitmap name coincides with the OOTB bitmap file provided by AspenTech (bitmap1.bmp and bitmap2.bmp). The user can try renaming the custom logo to a different name, then manually open the html file (using notepad) to make sure it's referencing the correct bitmap file. The html file is typically located in the following folder:
"C:\AspenZyqadServer\Basic Engineering37.0\WorkspaceLibraries\Templates\html5"
The line to look for should look like the image below:
Keywords: None
References: None |
Problem Statement: Why am I not able to compare the loaded assay vs the existing Assay in the Assay data in APS? | Solution: This is a known issue in the existing versions of APS. The user is not able to compare the loaded assay vs the existing Assay in the Assay data. The steps are as follows:
* Open the demo model with the next login: User: ADMIN no password
* Go to Integration/PIMS to APS/Import Crude Assays
* Go to the Assay Data tab expand all crudes from first to last
* In the last crudes you will notice that they cannot be expanded:
This is going to be fixed in the upcoming patches of the versions.
Keywords: None
References: None |
Problem Statement: Why do you see a “Script Error” when running the Results Window in V11 PSCP?
or | Solution: The script error occurs when you have a colorful map attached to the “Maps” section of your PSCP model. A colorful map means you are using the latest V11 map features, attaching maps including .bmp, .gst, .ptm, and .xml map files. The workaround is not to use colored maps but use greyscale maps instead. You can also click “Yes” on the error message to proceed with your Results Window. This is a known issue in V11, and will be fixed in the next patch of V11 PSCP (CP2).
Keywords: None
References: None |
Problem Statement: Why are ABE Windows strangely cropped and not displayed properly? | Solution: In some machines, ABE Windows may get cropped as shown below. Resizing the Windows does not help show more information on the right.
This is a known issue in ABE interface display compatibility with Windows. The current workaround is to adjust the scaling of Windows display. Reducing the scaling factor will allow more objects to be displayed:
Keywords: None
References: None |
Problem Statement: How to avoid the file missing when Office 2016 is installed on the system for Aspen V11 Media? | Solution: We need to manually check/add the registry key under HKEY_LOCAL_MACHINE\SOFTWARE\Microsoft\Office\ClickToRun\Configuration before the installation.
1) Right click the “Start” button and choose “Run” box.
2) Type “regedit” to the “Run” box and press Enter
3) Navigate to “HKEY_LOCAL_MACHINE\SOFTWARE\Microsoft\Office” and check if there is “ClickToRun” registry key,
If yes, please make sure the string value of “Platform” is set under “HKEY_LOCAL_MACHINE\SOFTWARE\Microsoft\Office\ClickToRun\Configuration\”;
If no, please manually add the string value of “Platform” and registry keys under “HKEY_LOCAL_MACHINE\SOFTWARE\Microsoft\Office\ClickToRun\Configuration\”;
The value Data is based on your office bit-ness, either “x86” or “x64”.
Note: How to know the bit-ness of Office you installed.
(1) Open Excel Application
(2) Go to task manager to check Microsoft Excel Process under Process.
If the process name is “Microsoft Excel”, then the office on your machine is 64bit.
If the process name is “Microsoft Excel (32bit)”, then the office on your machine if 32bit.
4) Then install Aspen V11 Media.
5) After finishing the media installation, the registry keys you added can be removed.
Keywords: None
References: None |
Problem Statement: Why is the Reload Simulator Automation not loading the changes in the beginning linefill? | Solution: If the user reloads the simulator manually, they can see the changes in the linefill. But, if we try to reload the simulator using automation, the changes are not loaded. For example, running the VBA code:
Private Sub ReloadSimulator()
Dim pss As Object
Set pss = CreateObject("Orion.Application")
Dim result As Boolean
result = pss.ReloadSimulator
Set pss = Nothing
End Sub
will not show the changes in the Beginning linefill events. But, if you Reload the simulator using the Simulator-> Reload Simulator option, the changes are shown as expected.
This is a known issue in the versions, with a good workaround available i.e, using the Reload Simulator option.
Keywords: None
References: None |
Problem Statement: Why does liquid water (aqueous phase) occur in the vapor stream out of Sulsim condenser model? | Solution: This is a known problem with the current implementation of entrainment modeling in the condenser. There is no issue with vapor phase calculation inside the condenser. The condenser might have been specified with entrainment of liquid sulfur. The liquid sulfur is expected in this case, but not the aqueous phase. However, the forced specification of liquid sulfur after the condenser alters the phase behavior of the vapor stream; thus, we may find some small amount of water condensing to form the aqueous phase. Typically this amount of water vapor condensing is very small, and can be ignored.
Keywords: None
References: None |
Problem Statement: In ABE V11 Drawing Editor, Gap/Ungap of connection does not work properly. | Solution: This is a known issue, and is addressed in V11 CP1. For urgent fix or alternative workaround, users can resolve this issue by following the below procedure:
Close any instance of the Drawing Editor.
Go to the installation folder where UserServices is located. The default location is C:\Program Files\AspenTech\Basic Engineering V11.0\UserServices\bin
In this bin folder, paste the cmd attached in this article.
Open an instance of cmd or PowerShell as Administrator, and navigate to the path of bin folder.
Run the cmd. Please see attached screenshot for reference.
The user should see a bunch of dll’s registering. Once it’s finished, re-open Drawing Editor, and try Gap option again.
Keywords: None
References: None |
Problem Statement: Attempt to enable FAST Aspen Fidelis Reliability (AFR) V11 Excel Add-in returns “license checkout failed” error. | Solution: When attempting to enable the FAST AFR V11 Add-in in Excel, AspenONE SLM Manager sends a pop-up message that says” License checkout failed”. Even though Aspen Fidelis Reliability main application launches without any issues and a valid license is available.
This is a known issue, in Aspen SLM Client V11, when a dongle license is being used and the Add-in is configured in MS Excel 2016. A fix is available in the attached emergency patch.
Installation Instructions
Ensure no AspenTech products (any version) are running.
Ensure user account has Administrator Privileges prior to installation of this patch.
Next, download the file ECR_462259.zip on the target system, extract the zip file containing this current patch to a temporary folder. The zip file contains two files:
Win32/strgxi2.dll
Win64/strgxi2.dll
The files will be manually copied to the target system and replace the existing versions.
The destination location of each file is listed below here under “Files Changed in this Patch”. For each file, rename the original version that exists on your hard drive (add “_original” to the filename), and then copy the new version of the file from the patch to that location. The purpose of renaming the old files instead of deleting them is to create a backup version of the deliverable files.
Copy win32/strgxi2.dll to ..\Program Files (x86)\Common Files\AspenTech Shared\ as strgxi2.dll
Copy win64/strgxi2.dll to ..\Program Files\Common Files\AspenTech Shared\ as strgxi2.dll
This will complete the installation.
Note: This Field Test has been tested to ensure that it has not had an adverse effect on any closely related functionality. However, it has not been through AspenTech’s full Quality Assurance procedure.
Issues Addressed by this Patch
Defect ID Description
423740 Issue checking for license with Aspen Report Writer within a virtual environment
413480 Dongle not recognized within Excel 2016
452747 V11_ASW not working with standalone dongle locked license
Files Changed in this Patch
Install Location Filename File Version or Modified Date
..\Program Files (x86)\Common Files\AspenTech Shared\ Strgxi2.dll 2018.11.1.517
..\Program Files\Common Files\AspenTech Shared\ Strgxi2.dll 2018.11.1.517
Post Installation Verification Steps
Install the Dongle locked standalone license file.
Launch the SLM Configuration wizard, check that “Ignore local keys” is unchecked in “advanced settings
If Ignore local keys is checked, uncheck it then click Apply Changes to initializing the standalone license.
Opening Excel 2016 and enable the FAST AFR V11 Add-in.
Keywords: FAST add-in, AFR license check failed,
References: None |
Problem Statement: How can I diagnose if my tags and database in an Aspen Online project are working correctly? | Solution: In an Aspen Online project, Tag validation should be performed:
During the configuration of a new project
When tag names, tag types and/or CIM-IO attributes have been modified in the AOL project
When changes occur in the historian, e.g. tag renaming or deletion
To run – Click the Validation button in the Diagnostic portion of ribbon. Two options:
Validate all relevant tags – tags that read from/write to historian
Validate only as needed – tags that are relevant and not labeled as valid
If users have only added tags to the project and there are no other changes, they can validate tags as needed
There is also a useful tool to perform Consistency checks for variables and tags on the Data Server. It appears as the Check Consistency button in the ribbon. It is very helpful to check when the project is not running correctly. Within the same tool, there is a checkbox for option to ask AOL to fix the problems at the bottom of the dialog box; USE WITH CAUTION, since AOL may delete data if selected. If the checkbox is not checked, AOL will only report problems. Report section will contain all found consistency problems.
Data Server performs some of these consistency checks when it starts, and will stop if these checks fail
Lastly, the case history system also represents a place for model files in various status to be saved under the Hist folder for troubleshooting purposes. The user can control what files are saved by specifying filters in this field. For each model, the user can control how many subfolders are saved
Keywords: aol, diagnosis, troubleshoot, validation, consistency
References: None |
Problem Statement: How does Aspen Flare System Analyzer (AFSA) defines the composition when I specify the Molecular Weight? | Solution: For vapor only systems it’s often useful and fast to define the composition on each PRD by specifying the molecular weight of the fluid.
To define a composition from the Molecular Weight flare applies the following steps:
Scans for the selected Fluid Type.
Searches, from the available Components that match this Fluid Type, for those whose molecular weight are closest to the specified value, one above and one below.
Solves for the following equations:
MW [specified] = X1*MW[1] + (1 - X1)*MW[2]
and
X2 = 1 - X1
Where:
MW [specified] is the value that the user enters
MW[1] & MW[2] are the molecular weights of the components that AFSA selected on step 2.
X1 & X2 are the mole fractions of the components chosen by AFSA
With the equations above, AFSA solves for the respective mass fractions, which are displayed on the composition forms
Here is an example of this calculation:
Using the information from the screenshot above let’s follow the steps ASA applies.
The selected fluid type is HC, which means than only hydrocarbons will participate on this analysis, if any component such as H2O were present on the list, they would not participate in the analysis.
The specified MW is 50, and from the list, the components with the most similar values (higher and lower) to this are Propane (MW=44.097) and n-Butane (MW=58.124).
X1 = (MW[spec] – MW[2]) / (MW[1] – MW[2])
X1 = (50 – 58.124) / (44.097 – 58.124)
X1 = 0.57916
X2 = (1 – 0.57916)
X2 = 0.42083
These are the values that are displayed on the composition form.
Keywords: Composition, Source, Components, Molecular, Weight, PSV, PCV, Valve
References: None |
Problem Statement: Two issues are seen in the PCWS web page:
Under the Online tab, the Manage section is not visible to click on:
Under the History tab, although there is data visible for all other sections, when clicking on AW Maker, KPI Manager, or Tag Group Manager, the following “Permission denied” message is displayed: | Solution: When configuring Manage, the software checks through all of the online applications APC data services provided under the Configuration tab. If there are no hosts identified, there will be none to check and thus, create permission issues for certain sections of the web page.
To solve this issue, add a running APC ACO application host under the Configuration tab with a Good status (green) and hit Apply to save changes. Refresh the web page to see the changes.
If the user does not want to use the host, they can deselect the check box for Online applications to disable it and it will still overpass the “Permission denied” issue.
Keywords: PCWS, production control web server, apc, web, manage, permission denied, AW, maker, watch, KPI Manager, Tag Group Manger, data services, configuration, host
References: None |
Problem Statement: When using the HYSYS Line Sizing Manager, the calculated line Velocity doesn't match Stream Actual Vol Flow for certain streams. What causes this issue and when does it occur? | Solution: The Line Sizing Manager in Aspen HYSYS allows you to perform sizing calculations using stream data as reference and design/rate piping diameter based on certain criteria, such as maximum pressure gradient or maximum velocity.
However, the analysis that the Line Sizing Manager performs can provide incorrect results when working with a stream that has a single component and is close to bubble point conditions. The line sizing analysis simulates the fluid over a small finite length of pipe. In these types of streams, small changes in pressure can lead to full vaporization, and full vapor ends up being used for the sizing calculations.
The above statement can also be true for multicomponent mixtures if all the components in the stream have very similar bubble points.
If density does not change due to pressure drop in the Line Sizing Manager, calculations should be valid; otherwise, these calculations could be incorrect.
For this same reason, this tool should not be used for compressible gas flow, since this will present large density changes when pressure drops. The Line Sizing Manager should not be used for flashing flow or any type of compressible flow region.
In the attached example, we illustrate how to identify this situation. The simulation has three material streams, all composed of a single component (ammonia) and at equal Pressure conditions. Each stream has a different Vapor Fraction specification: one of them has 50% Vapor (50-50), the second one is at bubble point conditions, and the last stream is at dew point conditions.
An analysis has been created for each stream using the Aspen HYSYS Line Sizing Manager in order to compare the calculated velocity from this analysis with the “real” velocity of the stream using the calculated pipe diameter and the stream’s flow.
A spreadsheet operation shows the results of this comparison. The Diameter and Velocity results that were calculated for each Line Sizing analysis have been copied. In the spreadsheet, we use the formula Vol Flow = Area * Velocity to calculate the Flow that was used for the analysis and compare it with the Stream’s Act Vol Flow. For the case of stream 50-50, you can see that this calculated Flow is indeed different from the stream value.
As stated before, stream 50-50 has only a single component, and slight changes in Pressure will end up fully vaporizing the stream. Therefore, the Line Sizing Manager ends up using an incorrect value for the analysis.
Keywords: Line, Pipeline, Error, Difference, Velocity, Flow, Compare
References: None |
Problem Statement: How does Model Scheduling works in Aspen Online projects? | Solution: In an Aspen Online project, Model execution scheduling is used so model calculations can be specified to be automatically performed at desired times of the day and/or at a desired frequency every day or based on the steady-state condition of the plant. This can be configured on the Models | Model name | Specifications | Schedule sheet. In said sheet you can:
Set how often is a project/model being run by Aspen OnLine
Schedule can be the same for the whole project, or be different for each model in the project
Can specify fixed intervals or several fixed times of the day
Make sure to check the checkbox – otherwise configuration below the checkboxes will be ignored
To schedule automatic model executions for a model, follow these steps:
In the Client GUI, open the Models | model name | Specifications | Schedule sheet
Select the Fixed time schedule checkbox to automate model execution at specified times during the day.
Select the Fixed-interval schedule checkbox to specify model execution at fixed intervals during the day. For example, a model may be scheduled to execute every 2 hours during a day.
For Aspen Plus EO models driven by steady-state detection, these two options should not be selected.
In Aspen Online, there are two ways to schedule a project – project-wide vs model-specific:
Project-wide schedule is useful when the user wants to set up specific run sequence for models (e.g. when user wants to always run a specific model first)
Model-specific schedule is useful when the user wants to run models at regular intervals or fixed times
At most 1 model may be running at any given time. Other model(s) will wait until the current model finishes running. If the wait time is greater than 10 min, the model run will be skipped. The model Specifications section also contains the Time specifications.
Timeout – maximum amount of time allowed before AOL terminates a model run. This is needed for:
Model takes taking too long to converge
Model hangs hanging due to invisible pop-up or inability of the relevant simulator to get a license
Look ahead interval – for dynamic models
Wait times – delays to avoid simulator crashes during model execution and accessing results for Aspen HYSYS and Aspen Plus
Also useful for debugging purposes (e.g. set longer wait time before closing model to debug HYSYS models with interactive service)
Keywords: aol, schedule, project, model, run
References: None |
Problem Statement: Which pre-requisites do I need to set up and install Aspen Online? | Solution: Aspen Online requires having an Existing Data Historian (e.g. IP.21) which serves as the DCS Input data. It can be on the same machine or a different machine
Server can be shared by multiple machines with Aspen OnLine installation
Existing simulation models (e.g. Aspen Plus simulation models(*.bkp), HYSYS simulation models(*.hsc)). The models must be fully solved and converged for them to be solvable (robust in terms of convergence)
Software Requirements:
Aspen Engineering Suite
Aspen CIMI-IO Interfaces (If using CIM-IO and IP.21)
Starting with V11, download the CIM-IO Mini Suite from support website
Microsoft Excel
AOL Server Readiness – Aspen OnLine service needs to be running
Open the Services window
Windows Key + R to launch run dialog, type in services.msc
Make sure the following services are running:
Aspen OnLine V11.0
Aspen CIM-IO Manager
If Aspen OnLine V11.0 service is not running, set Aspen OnLine V11.0 startup type to Automatic (Delayed Start)
Stop and restart the service afterwards
AOL Server Readiness – Ensure Sufficient Shared Memory
Aspen OnLine requires a higher Shared Memory Limit than the default value (768) to operate correctly
Increase the SharedSection’s last value to 4096 in the registry (8192 for ACM family) if the value is less
Restart the machine
Keywords: aol, deployment, prerequisite, install
References: None |
Problem Statement: Why the mass balance in the Delayed Coker is not accomplish? | Solution: The mass balance in the Delayed Coker is not the same as the outlet stream is not taking in count the coke formation in the reactor.
As shown below, the user can check the mass balance by taking in count the coke formation in a spreadsheet
Keywords: Delayed Coker, Mass, Balance, Formation
References: None |
Problem Statement: How to find the glass transition temperature in liquid? | Solution: There is this parameter in Aspen Plus/Properties.The glass temperature for polymers (and it's a rough approximation using Van Krevelen model , it's the average of the Tg of the segments).
The glass transition corresponds to the transition from the solid state to the liquid state (or the reverse one). It is basically a kinetical phenomenon. It refers to the so-called "structural relaxation". If the structural relaxation has time enough to occur during the observation time, the material behaves as a liquid. If the structural relaxation cannot occur during experience time, then the material behaves as a rigid -or semi rigid- solid.
What is exactly structural relaxation?
There is no exact answer to this question.
It corresponds to the structural rearrangements that allow the material to reach the equilibrium state that corresponds to the actual temperature. But the nature of these rearrangements remains confuse. Diffraction studies do not show significant differences. The specific aspect of polymers is the existence of long chains that are not directly broken by thermal motion. On the other hand, mineral glasses (oxides, fluorides, chalcogenides) do not contain isolated molecules, but rather consist in a tridimensional packing of anions and cations.
It is possible to propose a simple structural model that accounts for most features of glass transition. It is based on the hypothesis that vacancies do exist in the liquid state, and that their number increases with temperature. Simple relations account for thermal expansion, heat capacity, density. It gives a simple answer to the Kauzmann paradox and leads to a general expression of the viscosity vs temperature relation.
Glass transition may be more simple than generally assumed.
Keywords: glass transition temperature, Aspen Plus, glass temperature
References: None |
Problem Statement: After creating Process tank in model and saving changes APS gives me an error below.
Then everything's fine, but after closing and reopening my process tank becomes crude.
Similar error can be observed with properties, when adding Properties to the model through the Model->Properties and trying to save. | Solution: Entries were added manually to TANKS (or PROPRS) table so the X_SEQ number was incorrect.
You try to add a new tank on the flowsheet (or property in the model fromAPS interface) but as the X_SEQ is already there, it won't be possible.
To solve the issue please go directly to dbo.ATORIONKEY table and change the PROPS LAST_ID entry to the appropriate one from last TANKS ID.
Keywords: Violation
ATORIONKEY
Duplicate key
TANKS
PROPS
References: None |
Problem Statement: Do Acid Gas Fluid Packages support high concentrations of H2SO4? | Solution: Unfortunately, in Aspen HYSYS the Acid Gas fluid package can only treat H2SO4 as a trace component to model the effect of heat stable salts, so its concentration should be low (usually hundreds to thousands ppmw). High concentrations of sulfuric acid are not supported for this property package.
If the user wants to simulate the process at those concentrations there are three workarounds:
1.- Model it in Aspen Plus as shown in the following article Is it possible to model a sulfuric acid process?, use the Electrolyte NRTL as the property package and use the chemistry tool to generate all the neutralization reactions as shown in the following article How to model electrolytes and salts in Aspen Plus
If the user wants to keep working in Aspen HYSYS, please select one of these options:
2.- Perform all the properties and reactions inside Aspen Plus based on the first comment, export it to Aspen HYSYS as shown in the following article How do I import a fluid package from Aspen Properties or Aspen Plus files in to Aspen HYSYS?
3.- Use an OLI property package that allows to simulate electrolyte systems and the reactions but it will require an additional license but you have to purchase the "engine" from OLI Systems as mentioned in the following article Do I need a license to access the OLI Electrolyte property package?
Keywords: H2SO4. Acid Gas, High, Concentrations
References: None |
Problem Statement: How do I set up and manage Aspen Online projects? | Solution: The Aspen Online product does not work with one single standard file, but with a folder structure containing several varying files. Firstly, in order to start using Aspen OnLine, the first step is to create a new project or open an existing project.
How to create New AOL Project:
Click “New” on Start Using Aspen OnLine Dialog (a list of projects currently registered on the server is shown)
Specify project name and location accordingly if needed
The project needs to be in a location accessible by all accounts; desktop is not valid
Project names must be unique on each server
An Aspen OnLine project shows up as a folder in the file system
Do not place projects under a user-specific folder
Each Aspen OnLine project will contain one or more simulation models. However, if a model is running in RTO mode, all other models in the project will be ignored.
User can have multiple projects on the same Aspen OnLine server machine
Aspen OnLine is a client-server application; the user can remotely connect to a project from another machine
Note: Only one user at a time can check a project out for editing (changing project configuration)
The Aspen OnLine Project Manager is one component of Aspen OnLine. The Aspen OnLine Project Manager allows you to manage Aspen OnLine project files. Aspen OnLine project files are the files that can be modified or executed through the Aspen OnLine Client GUI.
Open the Project Manager by clicking Manage Projects in the File menu.
Use the Server name field to specify the server computer running the Aspen OnLine server application. When you specify a computer, the Aspen OnLine Project Manager connects to the Aspen OnLine server on that computer and displays the list of registered projects on that computer. All the commands below operate on projects running on this server.
Command Description
Register Register an existing Aspen OnLine project on the server computer. In order to modify or execute a project, it must first be registered.
Rename Rename an existing Aspen OnLine project on the server computer.
Clone Create a copy of the selected Aspen OnLine project on the server computer.
Change password Set or change the password for access to a project. If a password has been set, it must be provided to modify the project. It is not required to view the project.
Unregister Unregister an existing Aspen OnLine project on the server computer. None of the project files are deleted. However, an unregistered project cannot be modified or executed. You may want to use unregister to keep an archive of earlier versions of a given project, or before making a copy of a project, or because a project no longer needs to be modified or executed. If a password has been set, the password must be provided to unregister a project.
Delete Delete all files (including simulation files) associated with a project.
When you close the Aspen OnLine Project Manager, projects in this window remain active on the server.
AOL Project Folder Structure
ConfigData*.*df files (on V11, .mdb on V10 and earlier) – contains project configuration information
RunInfoData*.*df files (on V11, .mdb on V10 and earlier) – contains run-time tag values
Offline – Contains simulation model files
Online - Will be populated during Offline-to-Online operations and during project execution
Hist – Archive simulation files during project execution for troubleshooting purposes
Keywords: aol, project, manager, online
References: None |
Problem Statement: What do the checkboxes on the Run-Time ribbon of Aspen Online do? | Solution: The checkboxes on the Run-Time ribbon enhance and aid in the online run of the model. They can be seen as two different sections: the resolve Steady State section and the read/write section.
SSD print – generate steady-state detection report, checked by default
If Resolve SS is selected, the steady-state detection program will rescan the configuration database for changes before the next steady-state detection
By default data server checks for changes in configuration information every five cycles
After the new configuration information is rescanned and absorbed, the Resolve SS checkbox will be automatically cleared
If Force steady is selected, AOL will treat the system as if it is at steady-state for the current cycle
Skips steady-state check for current run
Automatically cleared afterwards and not applied for the next cycle
Other checkboxes:
End lineout
If selected, the optimizer will end its lineout period immediately.
Autorestart on failure When selected, the Watchdog program will restart the optimization program if it fails.
Write Suppress for SM models
Write suppress capability for EO Models has been present in AOL for decades; write suppress for SM Models is introduced in V10
Suppress the writing of tag values from model output variables to historians (Read suppress can be seen as a similar tool)
Outputs are sent to files in the folder <Project folder>\Online\OutputToFiles which can be picked up by in-house tools
Can be useful for testing purposes
Can also be used to satisfy some companies’ IT policies
Read supress: if active, no values are read from the DCS. An initialization script is used to initialize the project when this mode is active.
Keywords: aol, checkbox, ss, run-time
References: None |
Problem Statement: Why is there a grayed-out fin when using Plate-fin kettle? | Solution: When working with Plate Fin type exchangers, the exchanger types available are Standard axial flow, simple crossflow, multi-pass crossflow or Plate-fin kettle.
Plate-fin kettle exchangers are kettle reboilers, in which a crossflow plate-fin exchanger is used instead on a tube bundle. The parting sheets are vertical. The cold stream has vertical fins, open at the top and bottom to permit boiling in upflow and return of unvaporized liquid to the pool in which the exchanger is immersed. The hot (condensing) stream flows horizontally. The exchanger is defined as being horizontal, with the condensing stream inlet at end A. The condensing stream has distributors. The program calculates the flowrate of the internal recirculation, and overall stream outlet conditions.
With this configuration in mind, the Plate-fin kettle type of exchangers only allow for one X-flow fin number, since the stream is only going crossflow through a single fin. On the Input | Exchanger Geometry | Layer Types section, if you try and specify more than one X-flow fin, EDR will display the selection with a red color:
The correctly specified X-flow fin selected is fin number 2. Fin number 1 is not selected in that page. This disables the Fin 1 to be further specified on the Input | Exchanger Geometry | Fins section.
If you desire to use different fins for crossflow streams, the exchanger would not be a Plate-fin kettle, but a Multi-pass crossflow one.
This also means the Fin type selected on the Input | Exchanger Geometry | Layer Types section will need to be different to disregard the EDR error (red color on section). If more than one fin wants to be added to the exchanger, one of the fins used can remain being X-flow fin, but the other will need to be specified as a Multipass X-flow.
Keywords: Plate, fin, kettle, EDR, layer
References: None |
Problem Statement: Can I estimate missing properties of a new Database Component in Aspen Flare System Analyzer? | Solution: When you create hypothetical components in Aspen Flare System Analyzer (AFSA), the estimate button allows to calculate all the unknown properties that have not been manually entered.
However, if the user is creating a Database component (On the Navigation Pane | Databases | Components Database Editor) this Estimate button is not available.
From the usage point of view, handling a new Database Component and a new Hypocomponent is different, when defining a Database Component, it is expected from the user that all the component data is manually entered. Therefore, no Estimate option is available in this form.
As a workaround, if not all the information is available and the user wants to use the Estimate capabilities built into AFSA, the user can follow the procedure on KB 80108 and create a new hypothetical component by entering the known component data. All the unknown properties should be calculated from the Estimate button and them manually entered on the Database Component form.
Keywords: Estimate, Database, Missing, Unknown, Default, Additional, New
References: None |
Problem Statement: Is it possible to set in APS that day of schuduler starts at 3 am? | Solution: Option Beg of Day Offset could be useful in that case. You can find it in Model Settings.
This is the number of hours that the refinery uses to move their schedule forward to the next day.
With default 0 value in the Beg of Day Offset field schedule starts at midnight.
Once you define 3, it denotes that the roll forward occurs at 03:00 am everyday.
Keywords: Start date
Roll forward
Settings
References: None |
Problem Statement: We’ve installed Aspen Unified PIMS and can successfully log in, but not able to see icons on portal page. I can’t choose and migrate existing model | Solution: You need to log in AUP with the user, who performed the installation/configuration of AUP first. New user can’t give themselves rights, it has to be done under the administrative account.
You can verify which account is currently in use. To do that please use “User Info” button on the top right.
If you found out that it is not Admin user, please log in using correct account to grant access rights to the current user.
1. Once you’ve logged in under Administrator, you can click “Roles” tab
2. Click on Plus “+” icon to add line
3. Choose “Administrator” (or “Creator” if applicable)
Administrator Site Role allows user to manage Site and Model Privileges, create, delete, edit, view, copy Model, migrate Models, create and import Snapshot. Creator can create and copy Model, migrate Models and import Snapshot
4. Set the options to search for a user or group.
5. Select the desired domains. Click Search to begin looking for matches. A table appears with possible matches.
6. Click to select the desired person/group. Click Add Administrator. Your selection appears on the Site tab.
Repeat that for each user to allow full access to AU features. Now all users should be able to see all icons.
Keywords: AUP
Aspen Unified
icons
migrate model
roles
access
References: None |
Problem Statement: Where are private and public Aspen SQLplus web reports saved? How can this location be changed? | Solution: Public and private reports are saved to XML files on the Web Server. The registry value that specifies the path of these files is the Reports value under registry key
HKEY_LOCAL_MACHINE\Software\AspenTech\InfoPlus.21\SQLplus\Report
The default path is:
C:\ProgramData\AspenTech\SQLplus
Modifying this registry will affect the location where reports are saved for all users, so make sure any users requiring access have NTFS permissions to the new directory.
Note: Please note that after the installation of an SQLplus cumulative patch (e.g. 2006.5.6), the Reports value of the above mentioned registry key is reset to the default path.
KeyWords
xml
errors saving reports
Keywords: None
References: None |
Problem Statement:
When displaying a Data Point on a Graphic created with Aspen Process Graphic Editor or Aspen Process Graphic Studio, normally the Data Point showed is going to be retrieved from IP_INPUT_VALUE. Nevertheless, for some Data Points the values required to be presented must have already passed through the Data Compression Algorithm, and in consequence, it is required to search for the value within the History Repeat Area of the tag. | Solution:
1.- Open the Properties of the Data Point and go to the Data tab.
2.- In order to display values from the History Repeat Area, the following syntax must be used in Name: TagName 1 IP_TREND_VALUE, Where "TagName" is the name of the tag. And under Attribute select <VALUE>.
For example:
Note: For Aspen Process Graphic Editor the structure is similar.
3.- Publish the graphic and you should be able to see the value retrieved from the History Repeat Area.
Keywords:
Aspen Process Graphic Editor
Aspen Process Graphic Studio
Repeat Area
References: None |
Problem Statement: Why I can see Epsilon MAX iteration setting changes when loading model in V10/V11 PIMS AO
. | Solution: In PIMS AO versions before V10, the “Epsilon MAX Iteration Using Epsilon” default value is 30, while in V10 and beyond versions, Epsilon MAX iteration default values is changed to 10, since we found for many models having the default value at 30 delays unnecessarily convergence due to epsilon not being removed.
If in versions before V10, Epsilon MAX iteration is set to default value 30, when you migrate the model to V10/V11, it will automatically change to 10. If a user has specified a different number of max epsilon iterations than default value, this number would remain the same in V10 and later versions.
Keywords: None
References: None |
Problem Statement: The Aspen Cim-IO Manager service will not start with “Error 1053: the service did not respond to the start control request in a timely fashion.” | Solution: This error can occur for different reasons including, the license server is not accessible, or the Cim-IO Manager service is not registered properly. In this case the Windows services file was not accessible because the name was changed to SERVICES.TXT. To resolve the issue rename the services.txt file to SERVICES without the “TXT” extension.
KeyWords:
not starting
Keywords: None
References: None |
Problem Statement: We use SQL model and import events using Import Interface (Integration -> Import -> Events). APS will save 260 new imported events for more than one minute. Sometimes we need to import and save more than 500 events. Could you please suggest how to improve performance in that case? | Solution: Try to activate bulk events writing in CONFIG table. You can do it by entering “Y” in the column VALUE_ of row BULK_EVENT_WRITE (create it if necessary). It is N by default. In that case APS writes out each of the event tables one record at a time.
That option speeds up the writing of the event tables. Instead of writing the eight tables out one record at a time, a bulk write of each of the eight tables is performed.
It is highlighted that function is not recommended if your network goes down frequently.
Keywords: Slow performance
Save
CONFIG
References: None |
Problem Statement: Is there any recommended procedure to distribute the heat loss in a FCC model? | Solution: It is unusual for users to provide heat loss estimates for entry in the Calibration Environment. Often, users leave all heat loss terms zeroed and allow any resulting heat balance error to be handled in the heat of cracking offset.
Recommendations:
The user may set a Flue heat loss term to account for an unusually low flue gas temperature in the plant data, this may be required to converge the model.
For two-stage regenerators it may be worth entering heat loss terms for both regenerator stages. So, as an approximation it can be assumed that the heat loss in the regenerator is in the range 1-4% of the total heat generated by burning coke.
Notes:
Heat loss can be allocated between different sections based on the surface area of each
Adjusting the Stage 2 Bed Heat Loss can help in matching the Stage 1 Regenerator Bed Temperature (which is calculated during calibration).
Reactor heat losses are less important and are usually substantially less than regenerator losses.
Keywords: FCC, Heat Loss, Distribution, Procedure
References: None |
Problem Statement: For some reason we see not the usual stream details in simulation mode, but a pop-up window "Combination Tank/Stream ... and property VOL is not in TREND_SCREENS" as below
All of my trends in the model are WGT. If I look in the TREND_SCREENS table, none of the trends are in VOL, only WGT. | Solution: Possible root of that issue could be that originally the trends were added in VOL, but later changed to WGT.
APS has in memory the previous data and it is not overwritten because it is a different property.
Please delete the TREND_BASE.DTA and TREND_BASE.DTAB from the working folder. These ones are Binary files created in APS working folder during the simulation. They will be regenerated after next simulation and saving.
Keywords: Trends
TREND_SCREENS
Binary files
References: None |
Problem Statement: What type of reports can I generate from an Aspen Online project run? | Solution: Aspen OnLine has the capability of generating a number of log files, each of which focuses on different things to report:
Run Log: RunLog_0.log is located in the project folder. Contains information for all the input and output variables at the time of model execution.
Generally good first place to check to diagnose model run issues
Unsuccessful run – no output variable section
Event Log: Accessible via the log reader button on the Run-Time\Status tab next to Aspen OnLine engine’s Loading status entry. Contains license checking information
Engine Log: EngineLog.log is in the project folder (click the log reader button next to Aspen OnLine engine’s Running status entry). It contains debug information for formulas if message level is set to debug. It also records all abnormalities during project execution with time stamps. Contains:
Steady-state detection failures
Data validation failures
Run-time calculation errors and warnings
CIM-IO Related Logs: Two log files in the project folder – SsdLstIO.log and EngLstIO.log.
SsdLstIO.log contains log for communication between data server and CIM-IO
EngLstIO.log contains log for communication between AOL engine and CIM-IO.
For CIM-IO logs, set Debug print level (up to 10) on the Project Configuration \Specifications form. Search for strings “invalid” or “error” to pinpoint problems.
The report level and generation can be modified. By default, log files have a maximum size limit of 1MB. Bigger log file sizes are recommended for troubleshooting for more information to be presented, but will make project run slower; whilst smaller log file sizes are recommended for normal project execution.
Adjust Message level for more detailed logging
Summary by default and can increase to Detail or Debug
Debug print level controls level of output for the interface between AOL and CIM-IO Interfaces (0 lowest, 10 highest)
Aspen Online also generates the Data Server report. To review, click the log reader button next to Data Server’s Running Status entry. It contains overall report for inputs, outputs and status for steady-state and deviation.
SSD Point Summary tab - information for steady-state detection results on each tag
Average Problems tab - tracks all average tags that have bad quality
Deviation Summary – displays only tags with deviations greater than tolerance
Sections – view deviation summaries in each tag section
Keywords: aol, log, files, report, run
References: None |
Problem Statement: What are the different tag types available on Aspen Online? | Solution: In the Aspen OnLine context, a tag is an identifiable and accessible collection of information. These collections hold:
Information originating from the plant,
Information being sent to the model and being returned from the model, and
Information entered by the user and being presented to the user.
Tags are used to hold, manipulate, and display all data in Aspen OnLine. Aspen OnLine tags can be categorized as Plant (DCS) or Internal Application Tags, depending on their source and use.
Plant (DCS) tags are tags that:
Actually reside in the plant information management system (IMS) or the distributed control system (DCS), and
Provide plant data as input to the Aspen OnLine application.
The tag name used in Aspen OnLine is the same as the tag name in the DCS or IMS. When connected to these tags, Aspen OnLine retrieves the values and attributes associated with these tags. They are global tags and are referred to as DCS tags in the Aspen OnLine configuration system.
Internal application tags are tags that:
Allow entry of input data other than Plant DCS/IMS tags, or
Provide the means to display model-calculated results, or
Provide the means for further data manipulation or calculations within Aspen OnLine.
The value of any internal application tag can be sent back to an information management system (IMS) for further data analysis and trending. A tag needs to be created for these purposes in the IMS. The tag name used in Aspen OnLine and in the IMS must be the same.
The Tag type specify the purpose of the tag. There are 7 different tag types:
Internal application tags
Manual – user specified value
Formula – define a tag with a value that is a function of other tags
Local GUI – tag value coming from model output variables
Average – tag value is the average value of another tag
Steady State Detection (SSD) – tag value is the steady-state detection results of another tag
Signal – hold project run-time information; many are pre-defined in AOL
Plant (DCS) – tag value coming from historian
Validity ranges and options to handle out-of-limit data are specified on the Tags | Data Validation sheet.
Check the Data Validation checkbox under the model’s specification sheet
Can specify lower and upper limit for each tag
Option to clamp tags when they are out of bounds
If a tag is not clamped and its value is out of bounds, the quality of the tag will be labeled as “exceeded limit”, and considered as bad
Initialization tag
Set initialization tag under Tags\Initialization sheet
Automatically load current plant value as default and allow the value to be modified by user input
Average tag
The usage of a rolling average value reduces impact of noise. Optionally, you can define an average tag to receive the rolling average value of another tag.
Average period – the number of historical values we used to create the average for the Average output tag. Calculated with less values when project has fewer available historical values.
Tags Tag UOM sheet
The Tags sheet has columns for UOM String, Physical Type and unit Units. UOM string can come from historian or be entered by the user.
User can use the Tag UOM form to set up a mapping from the UOM String to a physical type and unit combination. Update will find Tag form entries with the same entered UOM string that satisfies the specified options and update the corresponding physical type and units.
Keywords: aol, tag, type, online, uom
References: None |
Problem Statement: Why am I getting input error 1050 on Aspen Shell and Tube? | Solution: Aspen Online product can be run either from another Server (other machine different than the local one) or on the Local Machine. The first Aspen OnLine component to start is the Aspen OnLine service. If being ran on the Local machine, user requires to be logged in to a System account or using an Admin User.
It should automatically work by default. However, there can be problems with the User restrictions due to the account login permissions on Windows.
To check this and troubleshoot:
Go to the Services on Windows and locate Aspen OnLine Service (for the Version which is experiencing problems)
Do a right click on the Service and click on the Properties option. On Properties, go to the Log On tab
This Log On tab has two options:
Log on as Local System account: the Local System Account selection has extensive privileges on the local computer, and acts as the computer on the network. This account has access to most system objects and does not have a password, so if running AOL as a Local Service, this is the preferred option.
This Account. If This Account is selected and account doesn’t have Admin privileges, Aspen OnLine Service will not be able to start. Also, if the User is Password protected, the same Windows Log In Password needs to be added here (Note if Windows Password is updated, the password would need to be updated here.
After setting the correct Log On option, the AOL service must be restarted.
The first Aspen OnLine component to start is the Aspen OnLine service. The Aspen OnLine installation sets this service to start automatically after the server machine is rebooted. First it will check for an Aspen OnLine license.
Note: If service Aspen OnLine V11.0 is not running after the reboot of a machine (likely due to the machine being very busy during startup and the service being unable to start within 30 seconds), you may want to set the Startup type for the Aspen OnLine V11.0 service to Automatic (Delayed Start)..
Keywords: Aol, service, login, run
References: None |
Problem Statement: When trying to connect the model using the Aspen Unified PIMS V11 Excel Add-in, the following error shows up: “Cannot link worksheet. Ensure the workbook is not in compatibility mode.” Error shows even when workbook is not in compatibility mode. | Solution: To solve this error, you will need to modify the file named AddinHome.cshtml in the next path: C:\Program Files (x86)\AspenTech\Aspen Unified\Web\Views\ExcelAddin
Remove the commented CDN lines in the file. The attachment in this article contains the modified file.
This issue will be fixed in V12.
Note: Please make sure you are using a supported version of Microsoft Office.
Keywords: AUP, Add-in, PIMS
References: None |
Problem Statement: APS crashes, when I click Model | Pipeline | Routs in some models without pipelines even. | Solution: It could be caused by corrupted PL_LOCATIONS table data. Please check if that table has ‘’ entries after db upgrade.
That should be corrected. Please change it due to the example from our DemoDSS model. You need to specify UNASSIGNED row. Then you should be able to use Pipeline menu without issues.
Keywords: Crash
Pipeline
Route
References: None |
Problem Statement: On Aspen HYSYS the pipe segment, the user can add the outside (external) insulation thickness and properties. Is there any way to add inner layer insulation properties for a Pipe Segment in Aspen HYSYS? | Solution: No, there is no way to add multiple inner and/or outer layers of insulation for a Pipe Segment in Aspen HYSYS.
To add multiple inner and/or outer layers of insulation for a Pipe Segment users will need to use the pipe segment or complex pipe within the Aspen Hydraulics subflowsheet.
Please follow these steps:
1. Enter to the Aspen Hydraulics subflowsheet
2. On the Heat transfer ribbon of the pipe segment/Complex pipe select the option of Estimate HTC/Heat Transfer Set
3. Specify the medium and wall conditions, and click in Add layer for the outer and/or inner depending on the require needs
4 Select the desire insulation type and specify the thickness
5.To view the results, go to the Performance tab |Insulation Page for Distance, Bulk Fluid Values and calculated temperature differences for Fluid / Inner - Outer / Ambient and the Ambient temperature set.
Keywords: Pipe, Insulation, Internal, External, Aspen Hydraulics
References: None |
Problem Statement: How does #LIMITS work in APS? | Solution: In APS, keyword #LIMITS can be used in Units excel file to define modifications to tank limits.
It is a known issue that in the released versions #LIMITS keyword does not update MIN/MAX limits in property dialog box.
However, #LIMITS do work for the tank limits on trend screens. So that’s why we could see the discrepancy between property dialog and trend screen values.
This issue will be resolved and improved in later versions.
Keywords: None
References: None |
Problem Statement: What services are provided with the 24x7 Customer Care Service? | Solution: Customer Care Service:
Under the AspenTech Premier Plus support, customers can access Customer Care 24 hours a day, 7 days a week.
Our customer service mainly deals with non-technical issues such as:
User registration for AspenTech customer support website access
Support website usage issues and questions
Software release media downloads or shipments
Software license key or dongle exchanges
Temporary or emergency license keys
Software usage log upload and reporting
Customer name or email domain changes
Customer Feedbacks
University Academic License Agreement (aspenONE for Universities Program)
Outside Local Business Hours:
For a non-Critical issue reported outside the local business hours, a case will be created, and an AspenTech representative will be assigned to work with the customer during the following business hours to resolve the case.
For a Critical issue that results in data loss or a general system down situation in a manufacturing environment, AspenTech will immediately assign our technical consultant available, sometimes from a different geographic region, to assist the customer on a best effort basis. If the customer has reached Customer Care, our Customer Care representative will ensure that a technical consultant is engaged to assist the customer.
During weekends or public holidays, our Customer Care is available to work with the customers on the range of non-technical issues listed above, including license key or emergency license issues. For a Critical issue that results in data loss or a general system down situation in a manufacturing environment, our Customer Care representative will ensure a technical consultant is engaged to assist the customer and the AspenTech management is notified, so that all the resources available at the time can be gathered to assist the customer.
Keywords: Customer Care, Premier Plus, 24x7 Customer Care Service, Non-technical
References: None |
Problem Statement: How to use #PL_DST keyword to set up Daylight Savings Time in APS? | Solution: In APS, keyword #PL_DST can be used to indicate that period lengths which are to be calculated using daylight savings time (DST).
To define period lengths as DST values:
1. Enter the keyword #PL_DST in cell A7. This keyword must be in cell A7.
2.
Keywords: None
References: the system generated value found in B7 in the column B cell associated with Period Length. This causes Period Length to be calculated using DST. The B7 value is system calculated. A DST compliant Period Length will be populated at Cell B7 during ‘Simulation’/’Publish All’ operation if the keyword “#PL_DST” exists in the PREP sheet.
3. Change the value for Period Length B5 as shown in the screen shot below.
4. This will allow users to use the correct “Period Length” in their Excel calculations. |
Problem Statement: What services are monitored by the Aspen InfoPlus21 Health Monitor, AllIP21ServicesRunTest and how to add, or remove services? | Solution: The AllIP21ServicesRunTest monitors services listed in ..\AspenTech\InfoPlus.21\db21\etc\ServicesList.cfg. The Services List contains required Aspen InfoPlus21 services and optional services.
Example; Service Name;Display Name
Aspen Process Data Service;Aspen Process Data Service
Aspen InfoPlus21 Administrators can edit the ServicesList.cfg file to add or remove services as needed.
After making changes stop/start TSK_HLTH
KeyWords:
IP21 health monitor
Ip21HealthDef
Keywords: None
References: None |
Problem Statement: How to configure the correct driver in PIMS for a TLS 1.2 enabled database server?
When trying to connect to the database server, the user is getting the following error: [DBNETLIB]ConnectionOpen (SECDoClientHandshake().]SSL Security error | Solution: Aspen PIMS can connect to a database server with TLS 1.2 enabled. For this you will need to install "Microsoft OLE DB Driver for SQL Server". This driver supports TLS 1.2 security but you have to be using the correct version of the SQL server database driver. There are different versions of the "Microsoft OLE DB Driver for SQL Server" database driver and PIMS does not support all versions. You must use version 18.0.2 or 18.1 of the "Microsoft OLE DB Driver for SQL Server" driver to use with PIMS. Using the incorrect version will make PIMS crash.
To get the correct version, use the following link and download the x64 installer. The x64 installer will also install the 32bit version needed for PIMS: https://docs.microsoft.com/en-us/sql/connect/oledb/release-notes-for-oledb-driver-for-sql-server?view=sql-server-ver15#previous-releases
If there is a previous version of the "Microsoft OLE DB Driver for SQL Server" driver installed, then uninstall it before installing the correct one. You can uninstall the driver using Control Panel.
Also, when using these versions, the user must clear/remove any value in the parameter Extended Properties on the All tab on the database driver dialog (Model Settings -> General -> Output Database tab. Click the ellipsis button (...)).
Check MS OLE DB Driver Version:
Go to Model Settings -> General -> Output Database tab. Click the ellipsis button (...) and verify that the dialog has just two authentication choices: Windows Authentication and SQL Server Authentication. If it has more like the Azure Active Directory authentication methods, then it is the wrong version of the driver.
Or check the version on the msoledbsql.dll in the folder C:\Windows\System32. Right-click on the .dll and go to the details tab. The version should 18.1 or 18.0.2.
WRONG VERSION:
If the database driver dialog looks like the one below, then it is the WRONG version of the "MS OLE DB Driver for SQL Server"
The later versions of "Microsoft OLE DB Driver for SQL Server" added support for Azure Active Directory authentication. PIMS currently does not support Azure Active Directory authentication in V11.
Keywords: SQL, Results database
References: None |
Problem Statement: Why do formulas inserted into an Aspen Calc formula have “.function” after them?
Problem Statement:
Some Aspen Calc formulas that include references to other Aspen Calc formulas include “.Function” after the name of the referenced formula. | Solution: Aspen Calc supports several formula types including, CalcScript, VBScript, Excel, COM Object, EXE. When creating a VBScript formula in Aspen Calc Insert Formula must be used to call another Aspen Calc formula so the bindings can be set correctly. Aspen Calc adds “.function” to a formula called from within a VBScript formula.
KeyWords:
VB Script
aspencalc
Keywords: None
References: None |
Problem Statement:
How to perform custom calculation based on the attribute values within Aspen Basic Engineering (ABE)? | Solution:
Being able to perform custom calculations in ABE could be very useful as we often have plenty of equipment data imported to ABE that can quickly be used to produce preliminary sizing results. Users can define a calculation procedure in an Excel Spreadsheet and apply it to ABE through Bridge application. Alternatively, users can write the calculation procedure in a script form directly to ABE. This article provides an example of the second option, in which users write an AZMethod script to calculate vessel volume given tan-tan length and diameter.
[?Class=ProcessVessel, DisplayName="Set Vessel Volume",
Interactive=true?]
AZMethod SetVesselVolume ()
set ClassView = ClassStore.FindClassView("VesselProcessSpecification") 'Navigate to VesselProcessSpecification ClassView to grab the necessary attributes
set VesselCV = self.View(ClassView)
Length = VesselCV.VesselTanTanLength.Value("m") 'Get tan-tan length and the correct unit
Diameter = VesselCV.VesselDiameter.Value("m")
if not IsNull(Length) and not IsNull(Diameter) then
Volume = (3.1417*Diameter^2)*Length/4 'Calculate the volume
VesselCV.VesselVolume = Volume
else
Server.SendWarningMessage "Insufficient Data“ 'In case tan-tan length and diameter are missing, issue message
end if
End AZMethod
This script needs to be compiled and installed to run in ABE. The compilation and installation is required only once and fairly straightforward. For more information on this procedure, please refer to the following article:
"How to use KB scripts in ABE?" - https://esupport.aspentech.com/S_Article?id=000062079
Keywords:
Data manipulation, KB script
References: None |
Problem Statement: If Regulatory Prop Constraints and Spec Targets are Defined at the Same Time, Which Property Will MBO Choose as the Bassline of the Optimization? | Solution: Using VOC as an example, If the setting is checked and if the spec targets are specified at the same time, regulatory spec is -27.5 (max) and a spec target is set at -28.5. Which one will MBO choose?
If the Regulatory Prop Constraints setting is checked, MBO will take that as the limit. So the max VOC will me -27.5 in this case.
Keywords: None
References: None |
Problem Statement:
How to prepare a relief systems design documentation in the "Safety Analysis" for Hysys & Aspen Plus V11 | Solution:
Starting in V11, within the Safety Analysis environment, you can use ABE Datasheets to prepare documentation of the design basis for any PSVs, rupture disks, and storage tanks. The Safety Analysis environment provides standardized relief systems calculations and data consistency across the final report deliverables, making it faster and easier to complete a pressure relief analysis.
ABE Datasheets offers a light-weight, single-user experience to create datasheets quickly and easily. The technology also offers a server-based, multi-user experience so that companies can have a centralized repository of their relief systems design documentation. To get started, from the Safety Analysis environment, on the Home ribbon tab, click Datasheets. The Datasheets button is only available when Aspen Basic Engineering is installed on your machine.
For more details, please refer to the following KB:
How do I create a PSV Excel Datasheet in Aspen HYSYS or Plus V11?
https://esupport.aspentech.com/S_Article?id=000065633
Keywords: None
References: None |
Problem Statement: How can I use Sensitivity Analysis to study the effect of mass/mole flow of a feed stream on the mass/mole fraction, activity coefficient and pH of a product stream? | Solution: This article demonstrates how to use sensitivity analysis in Aspen Plus and how to obtain properties such as mole fraction and activity coefficient for various components. As an example, a pure sulfuric acid stream and a pure water stream are mixed to obtain an acidic solution stream. The objective is to vary the flow rate of the sulfuric acid stream (H2SO4) to demonstrate how to can obtain the mole fraction and activity coefficient of the acidic solution stream (ACIDMIX) using Aspen Plus.
In the simulation environment, under the Model Analysis Tools tab in the Navigation Pane (located on the left-hand side of the screen), click the Sensitivity Analysis button. You could also select Sensitivity from the Analysis button in the ribbon.
Select new and click ‘OK’ to create a new analysis.
Select New and create a new manipulated variable in the Vary tab. In this case, as an example we mix an acid stream and a water stream to get an acidic solution stream. You could do this manually or drag and drop this from the stream window. For doing it manually, select Variable (user input), Type (Mass-flow), Stream (Name from flowsheet), Substream (Mixed), Component and Units (user input). Also, add the variable limits – Start and End points as well as number of points or the increments.
Under the Define tab, select the parameters you are interested in studying. In this case, it will be the mole fractions of the component of interest and the activity coefficient.
For example: For the mole fraction of sulfuric acid (H2SO4) in the solution (stream ACIDMIX). Select Type (Mole-Frac), Stream (ACIDMIX), Substream (Mixed), Component (H2SO4)
For obtaining a property such as the activity coefficient of each component, we need to define property sets. Click on Property Sets in the Navigation Pane. Click on New, change the name to ‘GAMMA’ and click OK.
Once created, click on the newly created property set ‘GAMMA’ and under the Properties tab, select ‘Search’. Search for ‘Activity coefficient’ or ‘Gamma’ and click OK.
Under the Qualifiers tab of the Property set, select the phase (Liquid) and the component (H2SO4).
Note that a Define can link to only one value reported in a Property Set.
Go back to the Define tab in the Sensitivity Analysis and create a new variable called GAMMA, Type (Stream Prop), Stream (ACIDMIX) and Prop Set (GAMMA)
Similarly, a property set could also be created for pH and used in the sensitivity analysis. Please note, that if the "Electrolyte" template is selected, a property set is already created for pH and only needs to be added to the "Define" tab on the sensitivity analysis like the activity coefficient.
5. Under the Tabulate tab of Sensitivity Analysis, click on Fill variables.
6. Run the simulation and view the results of the Sensitivity Analysis.
The following articles may also be of interest to you for more information on sensitivity analysis:
Manipulating mole or mass fraction in a sensitivity block -
https://esupport.aspentech.com/S_Article?id=000055652
How do I set up a Case Study in Aspen Plus? -
https://esupport.aspentech.com/S_Article?id=000084293
Example: Using a Sensitivity Analysis to tabulate Phase Equilibrium results -
https://esupport.aspentech.com/S_Article?id=000057260
Keywords: None
References: None |
Problem Statement: How to create and interact with a comment in A1PE | Solution: Comments and notes are useful when you want to keep a track of all the events happening on the plant for each tag.
Please find the following steps to create and edit comments inside AIPE.
1. Inside A1PE, on a plot expand the annotation panel and click the New (+) icon under Notes.
2. Choose the “Annotation” option. The annotation is added to the center of the plot; you can move it to a desired location as shown in the screen capture below.
3. To convert this annotation into a comment you just need to select the annotation and then click on the Pencil (inside the annotation panel) to edit. It will open a window so you can convert it into a comment maker.
4, Now you can write a comment, choose the exact time of the event and the plant area. On the Advanced options you can choose the urgency and the event type.
This comment will be saved in the database that belongs to the tag. Anytime that you open a new plot that belong to this tag you will be able to see the comments.
This applies for V9.x , V10.x and V11.x systems.
Keywords: A1PE
Comments
Annotation
Event.
References: None |
Problem Statement: How to set up a sensitivity case scenario in a batch process? | Solution: In Aspen Plus the user can create different Model Analysis Tools such as Sensitivity Analysis, Optimization and Data Fit. For further information, refer to the following articles:
Using a sensitivity analysis to change the feed stream to a block
Optimization Example for Minimizing Steam Use
Using Data-Fit Capabilities in Conjunction with Reactors
Unfortunately, if the flowsheet is qualified as Batch only Data Fit will be available.
The workaround is to use BatchProcess block in a continuous process flowsheet to create a continuous – batch process to enable all the Model Analysis tools.
Note: Only the variables that are in the continuous flowsheet could be manipulated.
Keywords: Case study, Analysis, multiple cases, Batch, Continuous
References: None |
Problem Statement: Why is the Sound Power Level (SPL) value reported zero for certain pipes in my Aspen Flare System Analyzer flowsheet? | Solution: AIV/SPL calculations are done based on the vapor portion of flow only. The vapor criteria is based on upstream flow of the Pressure Relief Devices (PRDs). Hence, for the case of flashing liquid at the PRDs, SPL calculation for pipes downstream of these PRDs will show zero. This behavior can be changed in AIV settings: Go to Calculation Settings > Open AIV tab > Toggle the option under Mixed Phase and Liquid Source Considerations to "Use Overall flow" and specify vapor fraction greater than 0%.
Another possible reason why SPL is calculated zero is the presence of knockout (KO) drum. Per API 521 section 5.5.12.2 paragraph 2: "The fatigue evaluation should extend to a vessel such as a knockout drum, unless new noise sources are located in the piping downstream of the drum." The first paragraph in EI T2.7.1 also states the same. Hence, the program is implemented accordingly to not transmit SPL across the KO drum. Pipes after a KO drum will report SPL result as zero.
Keywords: Sound Power Level (SPL), AIV, noise, Flare System Analyzer
References: None |
Problem Statement: Why Sometimes Variable Bounds Defined in Non-Linear Equations are Not Considered in the Matrix Analyzer | Solution: This happens mostly with Q variables. The reason is because Q variables are often defined in multiple places in the model. For example, if the Q variable is referring to a quality of a stream, then they are generated from R rows. If the Q variable represents material composition, they are generated from composition recursion R rows and depooling structure E rows. So there are at least two places, which are R rows and Non-Linear Equations, for the user to define Q variable bounds.
See the example below:
Because this variable is defined in an R row first, so the “New variable” check box is not going to be checked. Although there is a min value of -1 and max value of 105 defined, these bounds will not be considered in the calculation. The model might have more serious problems like infeasibility. See the final matrix analyzer:
The lower and upper bound are not the numbers we specify in the Non-Linear Equation section.
The reason is because the R row used to generate the Q variable will free up the Q variables without any min/max bounds. This is why in Non-linear equations, the min/max for the Q variables are greyed out. They will not be used because they were freed up from the R rows before.
The workaround is to add the desired min/max bounds in table BOUNDS like the following:
You will see in the final matrix analyzer the variable bounds are updated:
Keywords: None
References: None |
Problem Statement: What are the pre-requisite of using the setting “Build Crude Unit Swing Cut Quality Gradients” setting work in PIMS-AO? | Solution: First, the algorithm for this setting is proprietary to AspenTech. The math behind the scenes cannot be disclosed to anyone.
The setting is only available in PIMS-AO. It is in XNLP Settings -> Advanced.
This setting is defaulted to be turned off. In normal crude unit structure, PIMS will optimize how much of a swing cut goes up or down. The entire swing cut has one set of properties and those constant properties are used to adjust the stream above and below are appropriate for the swing allocation.
If this setting is turned on, PIMS adjusts the properties of the up and down portions of the swing cut. In table ASSAYS, you will need to provide the final vapor temperature (FVT) data for the swing cut itself, the cut below the swing cut and the two cuts above the swing cut in the I rows. If this information is not defined, you will receive Error E687: Missing FVT Data for Gradient Quality Calculation in Table XXX Cut YYY. Once you have the necessary information in table ASSAYS, PIMS uses the cut points of the streams around the swing cut to determine the gradient for a property. The matrix structure to calculate properties are also different.
The following is an example of this setting. The model has NK1 as a swing cut that goes up to WN1 (Whole Naptha) and down to KE1 (Kerosene) in SCD2 and SCD3. The matrix structure in the matrix analyzer is different from the traditional crude unit structure.
If SPG of WN1 is recursed and calculated from the matrix, you are going to see two new columns: xCD2NK> and QdSPNK2. These two variables are calculated nonlinearly based on derivatives, and the product of these two variables are going to be the gradient that is taken into consideration when calculating the final property of the cut WN1. The “d” in the Q variable means there is gradient calculation considered when recursing on the property. “SP” is the first two tags for SPG. The matrix analyzer will create 2 rows for these two columns:
This E row calculates the value of the driver column xCD2NK>.
When recursing on the actual SPG of the cut, the swing quality gradient is taken into the equation as above.
Keywords: None
References: None |
Problem Statement: What database tables are updated when add/edit Products from Products Dialog box in MBO? | Solution: Here is an example below showing the DB table changes if you add a product through the product dialog box in MBO. Note this is when you don’t make any other changes to your schedule (no Gantt changes, events, etc).
1. Add a new product called “DUMMY”, and copy the specs from another existing product. Click OK and save changes to the database.
2. The following data tables will be edited after adding the “DUMMY” product to the model
Table BLENDS
Table MATERIAL_ATTRIB
Table MODEL_LOG
Table SPECS
Table PRODUCTS
Table COMPOSITION
ATORIONKey is a summary of the last primary key used in selected database tables. Because adding a new product will make changes to “MATERIAL_ATTRIB”, theoretically speaking, ATORIONKey also has changes in its values.
Table ATORIONKey
The above data tables in your DB should change.
Keywords: None
References: None |
Problem Statement: Is possible to create an Aspen Properties Database with hidden parameters, but unrestricted access? | Solution: When using the Aspen Properties Database Manager, in "Backup Database Wizard" for a security database just created, you can set the option “Give access to Aspen Plus/Aspen Properties Calculation Engine”.
This will hide parameters from GUI and Engine report for any user (inside or outside, including the user who created the database) but grant unrestricted access for engine calculations.
Note: the security is added to the database level and cannot be implemented to a specific databank within a database. So, all (not just some) parameters are hidden.
For detailed information on how to implement additional security measures, please refer to the articles below:
How do you create a database with extra security?
How do I customize a proprietary Aspen Properties database?
Keywords: Database, Secure, Hidden, Security.
References: None |
Problem Statement: Why am I seeing different numbers in PIMS Submodel Calculator and APS SMC? For example, in PIMS I see coefficient is 2575.6102. When saving to SMC file and opening it through APS interface, coefficient appears as 2575.6104. The fourth decimal place is different in PIMS and APS. In this instance, this is very minor because the difference is small relative to the overall number. However, if the number was 0.0002 and APS changed it to 0.0004 then this would be significant. | Solution: The numbers change due to conversion from float to double and double to float. Because of this, we expect numbers to change slightly in 6th to 7th significant digits. This behavior will not change a number of 0.0002 to 0.0004.
Keywords: Orion, SMC
References: None |
Problem Statement: When running a full project evaluation, the following error comes up: ERROR> 'STL- #' - COULD NOT SELECT BEAM OR COLUMN | Solution: A possible root cause of this errors could lie on extreme specifications entered fo the Civil elements, such as using an unrealistic value for the Horizontal acceleration (g) in the General Civil/Steel Specs in the Project Basis View. The subsequent errors let the user know that it is impossible to design civil foundation for such a high value of seismic acceleration.
To get rid of this error messages simply specify a more coherent value for the horizontal acceleration.
Note: Make sure that the value of 2 g specified for the horizontal acceleration does not refer to the UBC zone instead, as the horizontal acceleration for a UBC zone 2B is equivalent to 0.20 g.
Keywords: Error STL, Horizontal acceleration, Beam, Column, Pipe Rack, Seismic Data, UBC Zone.
References: None |
Problem Statement: Why do I see a flash failure error in Blowdown when modeling a full liquid pure component case? | Solution: This issue is specific to pure component systems modeled at full liquid initial condition.
Calculation for blowdown of pure component system with full liquid spec as initial inventory has been known for being difficult to solve. The convergence typically fails whenever the system reaches the line separating the liquid and vapor in the phase diagram.
A workaround that has helped resolve this problem in most of the cases is mixing the inventory with a small fraction of an inert component such as nitrogen. To obtain best results, users should test the modified system in different amounts of the inert, and also vary the solver time step under the Run Control tab.
Keywords: : BLOWDOWN, full liquid, pure component, flash failure
References: None |
Problem Statement: How to solve "Output Error in OpenOutputDatabase for field" message in Aspen PIMS? | Solution: To solve this message, follow the steps:
Perform model cleanup. Model > Cleanup Model(s), select the model and click OK
Exit PIMS
Manually delete or rename Results.mdb in the model directory
Manually delete PMLOG11.mdb in the upper directory (above the model directory)
Relaunch PIMS
Keywords: PIMS, warning
References: None |
Problem Statement: Why Do We Not See the Full Decimal Places Shown in the Submodel Sections of PIMS Full | Solution: Report and SDMAP.xls?
Solution
Sometimes we don’t see the full decimal places reported in the full solution report and sdmap file. For example, you might see a value that should be “0.0005” but reported as “0”. This might cause problems if the report or file is going to be queries later. How do we resolve this?
In PIMS, go to Reporting -> Miscellaneous. Change “Submodel Value Less Than Filter” value to a smaller number. This number will filter out any value that is less than this number to be reported as 0.
Keywords: None
References: None |
Problem Statement: Why does E608 Occurs when You Turn On Automatic Infeasibility Breaker in PIMS?
In V11, sometimes when you have a VPOOL table set up and modify some components in the virtual pool in a case, you will see the following error message stopping you from running the model:
*** Error E608. Only 81 of the 82 Components in VPOOL VP1 are in Table SELL. | Solution: As an example, if we declare a virtual pool VP1 in table VPOOL with 82 components. All these streams are purchased streams in table BUY. Then we proceed to a case to modify 81 out of 82 components except for 1 stream named HCS. Then you will see the above error message show up. Why is that?
When you set your infeasibility breaker to “Apply Penalties to Case Changes Only”, then the infeasibility breaker will only apply to whatever modification changed in table CASE. The setting could be found at XNLP Settings -> Penalties. If stream HCS wasn’t changed in table CASE, this will cause a problem because all components in VPOOL must go to same destinations. Distress sales structure is applied to all other components but HCS. This will cause the streams in the same virtual pool not going to same destinations. Thus you see the error.
The workaround is to add HCS to be modified as a sales in the case so that all streams in the virtual pool goes to same destinations. Or HCS could be deleted from VPOOL. The same idea applies to other tables related to virtual pooling. Although structure might be built in the back end like distress purchase/sales, we need to make sure the same structure is explicitly defined in the model as well.
Keywords: None
References: None |
Problem Statement:
Why is specific gravity property not transferred from HYSYS to Aspen Basic Engineering (ABE)? | Solution:
ABE PipingSystem class contains attributes to hold density and specific gravity values as shown below
However, when viewing the values for these attributes after a simulation import or data transfer, we may find that SpecificGravity values are missing.
The corresponding HYSYS mass density property is reported in the default Properties page of a stream. Specific gravity in HYSYS, however, is not reported by default. Due to this reason, it's not mapped to the corresponding attribute in ABE in the data transfer process. Hence, we do not see the value reported in ABE. There are two ways to workaround this challenge:
Have HYSYS report specific gravity value
Specific gravity is simply a correlation derived from mass density. If we're discussing specific gravity relative to water, it's mass density of the fluid divided by mass density of water. Put simple, it's a conversion with a fixed factor being water mass density. Hence, we can report specific gravity by changing unit of mass density. HYSYS fortunately provides this option in the built-in unit sets, so we can complete the conversion by simply switching the unit in Unit Sets:
Note that this workaround will report specific gravity in place of mass density. If you'd like to keep both properties to transfer to ABE, please continue to read the second method below.
The other alternative is to perform the conversion from ABE side. This conversion calculation can easily be done with a simple AZMethod script to convert the transferred mass density value to specific gravity and then populate result into specific gravity attribute. You can refer to the following article in which vessel volume is calculated based on dimension attributes. The result is then populated to the "VesselVolume" attribute. The main difference you would need to customize for our case includes targeting class PipingSystem, and specifying a classview that contains both attributes that report mass density and specific gravity.
Keywords:
Missing data, Incomplete Simulation Import, Datasheets field not populated
References: None |
Problem Statement: How to copy/paste PIMS AO internal tables from table grid? | Solution: In PIMS AO, internal tables are created based on corresponding model structures and they are listed in the model tree “Internal Tables” section to validate model structure or for users reference to add additional constraints according to the existing ones. It is not able to copy the internal tables from table grid in released versions.
One workaround to copy/paste internal tables is to generate data validation report and get the data from there.
In Run>>Data Validation, select Validation Summary and click OK to generate validation report.
In the data validation report, you could search and copy internal tables.
Keywords: None
References: None |
Problem Statement: What is the maximum tag name that can be entered into Aspen Cim-IO Transfer record IO_tagname field? | Solution: There are three groups of Aspen Cim-IO transfers Io, IoLong, IoLL with different IO_Tagname lengths.
The IoGetDef, IoGetHistDef, IoUnsolDef, IoPutDef, IoPutOnCosDef, have a 39 character IO_TAGNAME limit.
The IoLongTagGetDef, IoLongTagUnsDef, IoLongTagPutDef, IoLongTagPOCDef, have a 79 character IO_TAGNAME limit.
The IoLLTagGetDef, IoLLTagUnsDef, IoLLTagPutDef, IoLLTagPOCDef, have a 255 character IO_TAGNAME limit.
KeyWords:
tag name
address
Keywords: None
References: None |
Problem Statement: The utility to create CIM-IO logical device CIM-IO IP.21 Connection Manager is not installed with APC Online, but only installed with InfoPlus.21. | Solution: Edit cimio_logical_devices.def to add or remove logical devices. This article introduces how to create CIM-IO interfaces and create logical devices with these interfaces.
1) Invoke the CIM-IO Interface Manager and click Create a new one link to add CIM-IO interface.
2) At step Interface, input the OPC DA server name and click Discover, select the OPC DA Server that you want to connect. Click Next buttons and Finish button at last step.
3) At CIM-IO Interface Manager, check whether the interface is started with Green indicator. Write down the interface name, it’s I_OPC_1 at follow screenshot.
4) Open the file cimio_logical_devices.def under folder C:\Program Files (x86)\AspenTech\CIMIO\etc in Notepad, add a line with format “LogicalDeviceName NodeName ServiceName”.
See follow screenshot as example, NodeName is your server name of APC Online, ServiceName is the Interface Name at CIM-IO Interface Manager, and the LogicalDeviceName will be used in Configure Online Server of DMC3 Builder. If you can’t save and overwrite the file, please save it in a temp folder and copy it back to replace.
5) To verify the CIM-IO configuration, please invoke CIM-IO Test API and press 9 to test Get function. Input logical device name (IOOPC in this example), tag name and other settings. You will get the tag value and statue if it’s well configured.
Keywords: CIM-IO, APC, Logical Device, OPC
References: None |
Problem Statement: What are the compiler requirements for resolving “nmake” error in ACM V11? | Solution: ACM needs to access right compiler while generating procedure code for fortran subroutines.
If you receive an error “nmake ran with errors” message, then please make sure following compilers are present in the machine:
Visual Studio C++ 2017
Intel Parallel Studio XE 2017 Update 5 Composer edition for FORTRAN Windows with ACM
Note, we tested with full version of Visual Studio not the Build Tool. So, if you have problem with Build Tool, then most probably you need to install Full version of Visual studio.
For other versions of ACM, please review Compatibility notes in Help menu.
Key Words
Procedure, Fortran, Compiler
Keywords: None
References: None |
Problem Statement: Accessing a specific sub-flowsheet using VBA may throw some errors since the name may not be recognized | Solution: Sub-flowsheets in HYSYS are defined with two pieces of unique information – Name and Tag:
Users may call sub-flowsheets in VBA by making using of their tags with the following syntax:
Dim HySubFlowsheet As Flowsheet
Set HySubFlowsheet = HySubFlowsheets.Item(“Tag”)
Version
V11
Key words
HYSYS, Automation, VBA
Keywords: None
References: None |
Problem Statement: If the node name defined for a device in the CimIO_Logical_Devices.Def file on the Aspen InfoPlus21 server does not match node name of the Aspen Cim-IO Server then Store and Forward will not forward data. | Solution: Follow these steps to determine is the node names are different;
1) Aspen InfoPlus21 server;
Open the Cim-IO\ETC\CimIO_Logical_Devices.Def file.
Identify the line that contains the details for the device.
The second column contains the node name of the Cim-IO server
EX: OPCDev1 NODE1 OPCDev1
Make a note of the node name
2) Aspen Cim-IO Server;
Open the Cim-IO\Log\CimIO_MSG.Log
Review the message headers.
EX: 10-DEC-2019 13:39:15.030, Logged by OPCdev1 on node OPCNode1:
Make a note of the node
If the node names do not match then the the configuration must be adjusted using one of the following solutions.
Solution1:
Change the node name in the CimIO_Logical_Devices.Def file on the Aspen InfoPlus21 server to match the node name of the Aspen Cim-IO server.
Solution2:
Add the Cimio_Nodename.txt file on the Cim-IO server:
• Create a file named ..\AspenTech\CIM-IO\etc\cimio_nodename.txt on the Cim-IO interface server.
• Add the node name found in the CimIO_Logical_Devices.Def file on the IP21 server. [Make sure the case of the node name matches].
• Enter a carriage return following the node name in the cimio_nodename.txt file and save it.
• Complete a Clean Start of the Aspen Cim-IO Interface Per KB,
How do I perform a clean restart of an Aspen Cim-IO Interface with Store and Forward?
KeyWords:
nodename
server name
NIC
forwarding
store & forward
Keywords: None
References: None |
Problem Statement: How do I setup vessel pressurization and depressurization scenarios using Event Scheduler in HYSYS Dynamics? | Solution: HYSYS Dynamics can be used to study vessel pressurization and depressurization scenarios.
In this example, a feed stream composed of light hydrocarbon components including methane, ethane, propane, n-butane and n-pentane is fed into a tank. Peng-Robinson equation-of-state (EOS) is used as the fluid package to define the properties of different components. Event Scheduler is used to setup two scenarios, one involving pressurization of the tank and the second involving depressurization of the tank. For more information on Event Scheduler, please use the help guide by pressing ‘F1’ on Aspen HYSYS and searching for ‘Event Scheduler’. The following articles also contain helpful information on Event Scheduler:
https://esupport.aspentech.com/S_Article?id=000049818
https://esupport.aspentech.com/S_Article?id=000054401
Scenario 1: Pressurization of tank
Description: Once this schedule is triggered, both the pressure controller and level controller are turned into manual mode and their operating points (OP’s) are set to 0, effectively closing both outlet valves, which results in pressure build up in the tank. Once the pressure reaches the desired set value (20 barg), the integrator is stopped.
Scenario 2: Depressurization of tank
Description: Once this schedule is activated, the flow controller is turned to manual mode, and its OP set to 0, closing the inlet valve. The pressure and level controllers are turned back on and set to open completely, and once the pressure reaches the desired value (10 barg), the integrator is stopped.
Steps to run the attached steady state file in Dynamics
Open the attached file. Go to the Dynamics tab in the Ribbon. Click on Dynamics mode.
A dialog box will appear asking whether you are sure you want to switch to dynamics. Select ‘yes’.
Go to the event scheduler tab and activate the Pressurization schedule by clicking Start.
Run the integrator and observe the changes to the vessel pressure in strip charts.
For instructions on how to create and customize strip charts, please see the following articles:
https://esupport.aspentech.com/S_Article?id=000089851
https://esupport.aspentech.com/S_Article?id=000070914
https://esupport.aspentech.com/S_Article?id=000081879
The integrator automatically stops when the pressure reaches 20 barg. The vessel pressure is shown in the graph below in red, the vessel liquid level percent in green and the feed mass flow in blue.
Go to event scheduler tab and activate the Depressurization schedule by clicking Start.
Run the integrator and observe the changes to the vessel pressure in the strip charts. Again, the integrator automatically stops once the desired pressure is reached – 10 barg.
Keywords: Event Scheduler, Pressurization, Depressurization, Events, Strip Chart, Dynamic Run, Time
References: None |
Problem Statement: The Aspen InfoPlus.21 Administrator will not expand, or is slow to expand the Aspen InfoPlus.21 data source. | Solution: On the Aspen InfoPlus.21 server open a Command Prompt and verify that PING and NSLOOKUP return the correct Node Name and IP address.
If the node name or IP address are not correct then verify the following:
Check the C:\Windows\System32\drivers\etc\Hosts file and verify that all entries are correct.
Verify the configuration of all Network Card(s).
Verify the DNS configuration is correct
Contact the IT group responsible for the network and have them resolve the ping and nslookup issues.
KeyWords:
tsk_admin_server
IP21
Keywords: None
References: None |
Problem Statement: Is the Aspen Calc AutoBinding setting in Options a system or user setting? | Solution: AutoBinding is a user setting that automatically binds CalcScript parameters to Aspen InfoPlus.21 tags when you create or modify calculations. Before you do so, you must ensure that the names of the parameters match the names of the tags and enable automatic binding before you create or modify a calculation.
KeyWords:
auto binding
Keywords: None
References: None |
Problem Statement: What to check if you encounter the error “XLP Case Stacking” in PIMS-AO? | Solution: XLP Case Stacking Error Message is one of the messages that could have multiple root causes. Here is a list of general guidelines you should try after you receive the error message:
1. Check if your PIMS is at the latest version. If not, please install the latest patch. This is a known issue that was fixed.
2. Check if this is a modelling issue. The way to check is run our Volume Sample model and see if the error shows up. If it does, then you will definitely need to install the latest patch listed in step 1. If it doesn't, we need to proceed to check within the model.
3. Turn off AO and run the model in DR. Sometimes the error message is pointing to table CASE. There might be some errors with the syntax of some cases. DR will point to the row and column where you have the syntax error in your CASE file which is more helpful.
4. This error message is not documented in the help file because it's not related to back-end calculation. If the problem is not within table CASE, DR will also give you real error messages. Pointing to the row/column that you have not edited correctly.
Keywords: None
References: None |
Problem Statement: Aspen HYSYS Amines fluid package is no longer supported by versions V10 and V11, however version V10 is still capable of using it but it will recommend to change the fluid package to Acid Gas. Since version V8.3 the Acid Gas Cleaning functionality was introduced to Aspen HYSYS, which offers expanded capabilities and a tighter integration with Aspen HYSYS, thus finally in V11 Amine package was completely removed from HYSYS.
Nevertheless, sometimes it will be necessary to use old simulations, from versions V9 or previous, that are using DBR Amines fluid package in versions V10 or V11. But, is it possible to use those simulations in the newer versions? The answer is yes and depending on the version you are using the solution will be a little different. | Solution: When the user tries to open a simulation that is using DBR Amines in HYSYS V10, the following message will appear.
If the user accepts to change the fluid package to Acid Gas, it will automatically convert the fluid package into Acid Gas Chemical Solvents fluid package, and everything that was using the DBR Amine will now be using the Acid Gas package. In version V10, if the user wishes to continue using the DBR Amine package, just close the window that is suggesting to switch the fluid package and continue working with DBR Amines.
In the other hand, in version V11 it will be different, as V11 will not know he fluid package and at the moment the user opens the simulation it will show warnings about failures loading the fluid package and it will ask to replace it. After selecting OK in all messages, Aspen HYSYS will automatically go to the Properties Environment, where the user must select a new fluid package to substitute DBR Amine. Then add a new one using Acid Gas Chemical solvents and use the component list that contains the amine components. Also delete the DBR Amine.
Then go to the Simulation environment and using the Fluid Package Manager tool select the new fluid package in all streams, unit operations and flowsheets in which DBR Amine was used.
This way it is possible to use simulations that were created in versions V9 or previous and which are using DBR Amines in versions V10 and V11.
Keywords: DBR, Amine, Acid Gas, Chemical Solvents, Fluid Package
References: None |
Problem Statement: Triple steps is only applicable for Single-Step (V10.0 or ealier) and Test (V11.0) mode, but not for Multi-Step or Calibrate mode. The noted is missed for DMC3 Entries Dictionary in DMC3 Builder or PCWS help document. | Solution: There's a note for DMCplus Entries Dictionary of entry STMVPATTERN:
But the note is missed for DMC3 Entries Dictionary of entry, we'll update the note in V12.0 release.
Keywords: Step Pattern, SmartStep, DMCplus, DMC3, Triple Step
References: None |
Problem Statement: Sample Macro: Automation of BLOWDOWN with VBA | Solution: As with other parts of HYSYS, BLOWDOWN can be accessed and automated with VBA code. The following example shows how users can access variables and results of a BLOWDOWN unit.
Private Declare Sub Sleep Lib "kernel32" (ByVal dwMilliseconds As Long)
Public Sub TestBlowdownProfile()
'assumes that there is a running instance of HYSYS V10 with a BLOWDOWN case already open in it
Dim hyApp As HYSYS.Application
Dim hyCase As SimulationCase
Set hyApp = CreateObject("HYSYS.Application.V10.0", "")
hyApp.Visible = True
Set hyCase = hyApp.ActiveDocument
Dim utils As UtilityObjects
Set utils = hyCase.UtilityObjects
Dim varUtil As Variant
For Each varUtil In utils
If LCase(varUtil.TypeName) = "blowdownutility" Then
Dim bdUtil As BlowdownUtility
Set bdUtil = varUtil
AccessBlowdownResults bdUtil.BlowdownOp
End If
Next
End Sub
Public Sub AccessBlowdownResults(bloOp As BlowdownOp)
If bloOp.RunEndedStatus <> bresCompleted Then
bloOp.RunBlowdown
Do
bloOp.Application.DoEvents
DoEvents
Sleep 100
Loop While bloOp.RunEndedStatus = bresRunning
End If
Dim bloFS As Flowsheet
Set bloFS = bloOp.OwnedFlowsheet
Dim ops As Operations
Set ops = bloFS.Operations
Dim varOp As Variant
For Each varOp In ops
Select Case LCase(varOp.TypeName)
Case "blovessel"
Dim bloVessel As BlowdownVessel
Set bloVessel = varOp
AccessBloVesselResults bloVessel
Case "bloorifice"
Dim bloOrifice As BlowdownOrifice
Set bloOrifice = varOp
AccessBloOrificeResults bloOrifice
End Select
Next
End Sub
Public Sub AccessBloVesselResults(bloVessel As BlowdownVessel)
Dim times() As Double
Dim pressures() As Double
Dim vapTemps() As Double
Dim liqTemps() As Double
Dim innerWallVapTemps() As Double
Dim innerWallLiqTemps() As Double
Dim outerWallVapTemps() As Double
Dim outerWallLiqTemps() As Double
Dim innerWallTopTemps() As Double
Dim outerWallTopTemps() As Double
Dim innerWallBtmTemps() As Double
Dim outerWallBtmTemps() As Double
times = bloVessel.ResultTime.Values
pressures = bloVessel.ResultPressure.GetValues("bar")
vapTemps = bloVessel.ResultGasTemperature.Values
liqTemps = bloVessel.ResultLiquidTemperature.Values
innerWallVapTemps = bloVessel.ResultCylinderInContactWithGasInnerWallTemperature.Values
innerWallLiqTemps = bloVessel.ResultCylinderInContactWithLiquidInnerWallTemperature.Values
outerWallVapTemps = bloVessel.ResultCylinderInContactWithGasOuterWallTemperature.Values
outerWallLiqTemps = bloVessel.ResultCylinderInContactWithLiquidOuterWallTemperature.Values
innerWallTopTemps = bloVessel.ResultTopEndInnerWallTemperature.Values
outerWallTopTemps = bloVessel.ResultTopEndOuterWallTemperature.Values
innerWallBtmTemps = bloVessel.ResultBottomEndInnerWallTemperature.Values
outerWallBtmTemps = bloVessel.ResultBottomEndOuterWallTemperature.Values
End Sub
Public Sub AccessBloOrificeResults(bloOrifice As BlowdownOrifice)
Dim times() As Double
Dim downstreamPressures() As Double
Dim downstreamTemperatures() As Double
Dim massFlowRates() As Double
Dim upstreamPressures() As Double
Dim upstreamTemperatures() As Double
times = bloOrifice.ResultTime.Values
downstreamPressures = bloOrifice.ResultDownstreamPressure.GetValues("bar")
downstreamTemperatures = bloOrifice.ResultDownstreamTemperature.Values
massFlowRates = bloOrifice.ResultMassFlowRate.Values
upstreamPressures = bloOrifice.ResultUpstreamPressure.GetValues("bar")
upstreamTemperatures = bloOrifice.ResultUpstreamTemperature.Values
End Sub
Keywords: None
References: None |
Problem Statement: How to perform a pump speed variation controller? | Solution: Aspen HYSYS allows the user to control different outpouts based on process variables. To perform a pump speed variation controller, please follow these steps:
1. On the Curves ribbon of the Rating Tab, enable the "Use Curves" option and select the desire Gas Fraction basis
2. Click in "Add Curve" and enter the volume flow vs head vs % efficiency data.
3.Create a PID controller where the PV is the outlet stream pressure of the pump and the OP is the speed of the pump.
4. Configure the controller, the action will be reverse as if the pressure of the outlet stream increase the pump speed must decrease. Also, configure the controller OP Port where the user must specify the minimum and maximum speeds that the pumo can handle (normally based on pump curves or from vendor)
5. Configure the tuning parameters to control the pressure, if the user doesn't know what tuning parameters should use please follow the steps for an auto tuning where tuning parameters for the PID controller will be based on gain and phase margin design as mentioned in the following article: Aspen HYSYS Dynamics Autotuning Method
Keywords: Speed, Variation, Control, Pump
References: None |
Problem Statement: Why does the Rating tab of a heat exchanger is grayed out in Dynamic mode? | Solution: When the user is working in a dynamic simulation, Aspen HYSYS will grey out the information in the rating tab and now the crucial geometry and/or heat parameters will now be located in the Dynamics Tab. So, the user can make all the necessary changes of the heat exchanger and evaluate different scenarios.
Keywords: Heat Exchanger, Geometry, Rating, Grey out
References: None |
Problem Statement: Is possible to have multiple simulations linked to the same Aspen Simulation Workbook (ASW) file? | Solution: Once you have enabled ASW on MS Excel, you can link as many simulations as you need, following two approaches:
From Excel ASW ribbon | Simulations,click on the “+” symbol and browse for the desired file.
From the ASW Organizer | Configuration | Simulations, click on the “+” symbol and browse for the desired file.
Note you can connect and make visible all the linked files simultaneously as well, if needed.
For additional information, please refer to the articles below:
How to enable ASW in MS Excel?
Copy and paste variables from Aspen HYSYS
Jump Start: Aspen Simulation Workbook in Aspen HYSYS V8
Best practices in using Aspen Simulation Workbook (Things to avoid when using ASW)
How to Move or Rename a Simulation associated with Aspen Simulation Workbook
Keywords: ASW, Multiple simulations, Connect, Visible, Simultaneously.
References: None |
Problem Statement: How to plot the Residue Curves for a ternary mixture? | Solution: A residue curve describes the change of the composition of the liquid phase of a chemical mixture during continuous evaporation at the condition of vapor–liquid equilibrium (open distillation). Multiple residue curves for a single system are called residue curves map.
Residue curves allow testing the feasibility of a separation of mixtures and therefore are a valuable tool in designing distillation processes. Residue curve maps are typically used for examining ternary mixtures which can't be easily separated by distillation because of azeotropic points or too small relative volatilities.
Aspen Properties provides two options to plot the residue curves:
Aspen Distillation Synthesis Ternary Diagram (recommended): state-of-the-art feature for the synthesis and conceptual design of distillation processes enables the user to locate all the azeotropes and automatically compute distillation boundaries and residue curve maps for ternary mixtures.
Conceptual Design of Distillation Columns in Aspen Plus
How are distillation boundaries calculated in Aspen Plus "Distillation Synthesis" ?
Once you plot the ternary diagram, you can use the toolbar button Add Curve (graphically or by value) to add the residue or distillation curve.
Analysis Residue (legacy): older feature which allows you to generate a simpler ternary map for 3 selected compounds, showing only the phase envelope, tie lines, and azeotropes.
Note: Aspen Distillation Synthesis includes additional features, that’s why is recommended. When you run the command for the older Analysis Residue feature, a message will appear informing you about Aspen Distillation Synthesis:
Keywords: Distillation Synthesis, Ternary, Residue Curve, Distillation Curve.
References: None |
Problem Statement: How to set an intermediate or final equation of a calculator as the target variable in a Design Spec and how to access to the Design Spec Target in a Sensitivity block | Solution: To set an intermediate or final result of a calculator as the target variable in a Design Spec, the Design Spec cannot access as it can be a Fortran expression. So, set it as a value is the simplest expression possible by defining the expression as a Parameter type since by definition it is a value that could be share with other blocks.
Notes:
The parameter should be initialized in a Calculator (Fortran) block, and then it can be accessed and used elsewhere in the flowsheet.
Attached is an example where a Calculator Block is used to get the concentration of product, simultaneously a Design Spec is used to vary the flowrate to achieve the target value. Then, a Sensitivity is used to vary the concentration of product and plot the flowrate necessary.
KeyWords
Calculator, Design Spec, Sensitivity Analysis, Link, Parameter
Keywords: None
References: None |
Problem Statement: Is it possible to automap and transfer only material streams data from Aspen HYSYS to ABE using the Web Mapper? | Solution: It is not possible to automap and transfer material streams data to ABE using the Aspen HYSYS Web Mapper if the model only contains material streams and no unit operations; although after following the standard workflow to transfer data to ABE no warning / error message will pop up and the user will get a notification telling them that the data was successfully transferred, the material streams will not be automapped (i.e., no workspace objects will be automatically created to map the flowsheet streams against them), as show in the images below:
What needs to be done is to add a unit operation model to the Aspen HYSYS flowsheet (which does not necessarily need to be neither solved nor fully defined with its inlet / outlet / energy streams).
Now, the Web Mapper will be able to create workspace objects to map them against the flowsheet objects and bring the streams data to ABE.
Keywords: Web Mapper, Automap, Transfer Data, Material Streams, Unit Operation, Workspace Objects, Flowsheet Objects.
References: None |
Problem Statement: How can I control the size of a text box in order to correctly fit the space of a text? | Solution: As mentioned in the article How can I add text to the PFD? the user can insert a description of the process in the PFD but in some cases the default size of the text box doesn't fit the text.
To size the text box, follow these next steps steps:
1. In the Flowsheet/Modify Tab, click Size
2. Click on the desired text box to fit and drag either of the blue squares to the required position
Keywords: Size, Text Box, Fit, PFD
References: None |
Problem Statement: What are specific examples that are a good basis for employing custom attenuation for a device or fitting? | Solution: By default, the Override Standard Attenuation and Custom Attenuation check box is cleared.
The Custom Attenuation field provides additional flexibility for situations where the geometry of an unit operation is approximated / modeled in a way that does not fully capture the AIV attenuation for the actual configuration.
In cases where the piping is simplified such that the automatically calculated SPL / attenuation does not correspond to the actual characteristics of the piping, we recommend that you specify a value in the Custom Attenuation field. For example, unit operations such as tees and swages are often modeled as point models but have real geometry. The Custom Attenuation field lets you take credit for AIV attenuation in these fittings.
If the user is specifying piping exactly as it exists in the plant and you are satisfied with the built-in calculations provided by Aspen Flare System Analyzer, then we recommend that you clear the Override Standard Attenuation check box. AIV calculations are more conservative when this check box is cleared.
Keywords: AIV, Custom, Data, dB, D/t
References: None |
Problem Statement: How to figure out the required tables in Aspen Petroleum Scheduler (APS) and Aspen Refinery Multi-Blend Optimizer (MBO) models in the version you run? | Solution: In APS/MBO, the required tables to construct a complete APS/MBO model are listed in TABLENAMES in OrionDBGen.mdb. To get the list of tables specifically for your version, you can go to C:\Program Files (x86)\AspenTech\Aspen Petroleum Scheduler and search for OrionDBGen.mdb.
V11 APS/MBO OrionDBGen.mdb>>TABLENAMES:
Keywords: None
References: None |
Problem Statement: Are the new Column Analysis ‘Custom Trays’ for rating calculations available in Aspen HYSYS V11? | Solution: Custom trays for rating calculations are only available in Aspen Plus V11 for RadFrac columns and not available in Aspen HYSYS.
To know more about custom trays in Aspen Plus V11, please refer to KB Article: ‘RadFrac with Column Analysis now supports custom trays for rating calculations.’
Keywords: Custom Trays, Rating Calculations, Column Analysis, RadFrac, Columns.
References: None |
Problem Statement: What generates the message "The required relieving capacity is less than 30% of the rated valve capacity" and how do I fix it? | Solution: This warning is caused by an over-sized relief valve (i.e. installing a valve that is significantly larger than it needs to be for a particular scenario) and this condition can result in the valve opening and shutting rapidly, which can damage the valve and/or valve piping. It is a common and well-accepted best practice in relief valve sizing to avoid selecting a relief valve that is grossly-over sized, therefore, the Safety Analysis Environment triggers this warning at 30%.
Besides the warning suggestions (use an smaller orifice or splitting the flow across multiple PSVs), you can follow one of these options to remove the warning:
Option 1.- Turn off the warning in the General Setup Tab of the Preferences Manager, modify the percentage for the warning or uncheck the warning box to remove this.
Option 2.- If none of the standard orifice sizes is adequate, add a custom orifice size, as mentioned in the article How to change orifice sizes for PSV's in the Safety Analysis Environment
Option 3.- If the valve will handle multiple scenarios, add a PRD to focus in the bigger diameter. To checl how to model it please refer to the article How to use the Rating mode for a PSV
Keywords: Relief Capacity, PRD, Percentage, Orifice
References: None |
Problem Statement: When trying to use the workbook to see the composition of every single component, the compositions of some components are reported as XXX instead of showing a value as you can see in the following image: | Solution: By default in Aspen HYSYS, the Workbook groups all the component lists of all Fluid Packages in one general component list known as Master Component list. Therefore the workbook will report a composition as XXX for the components that are not loaded to the fluid package that is used by the stream.
If you look again at the image you can see that propane appears as XXX for the streams 1 to 4, but in the last two streams it is reported with a value, which means that this component is not loaded to the fluid package that streams 1 to 4 are using, but it is loaded in the fluid package of the streams 1-2, 2-2, 3-2 and 4-2. And the same happens with Ethylene, which is reported in the streams 1 to 4 and does not appear in the streams 1-2 to 4-2.
The fluid package can be added to every stream going to Workbook tab and select the option Setup, in the composition tab clicking on Add the Fluid package can be selected to be shown for each stream. This make more visible how the change of fluid package is generating that some components are being reported as XXX.
Note: Besides, although the components are present in the component lists of specific streams, these components can be reported as XXX. This happens because Workbook has a problem when using component lists and Fluid Packages created with Aspen Properties, and even though the fluid packages associated to Aspen Properties are not used the fact of using Aspen Properties can cause problems in the Workbook.
Keywords: Workbook, Composition, Fluid Package, Component list, xxx.
References: None |
Problem Statement: Why does Petroleum Assay characterization result for FlashPoint not match with my Whole Crude input even though I select "Match Whole Crude Properties" option? | Solution: The algorithm to match bulk properties shifts the property curve up and down in order to find the solution. This can sometimes temporarily bring the values outside the predefined limits for the property. This issue often occurs because the Max. value used to indicate the property's upper limit is not high enough for whole crude matching to successfully fit the property to the target value. In this situation, we recommend that you increase the Max. value on the Property Details dialog box for the property; this step will often improve the accuracy of your results. Follow the steps below to change the limits:
1. While you're in the Properties Environment, go to Customize tab > Select Property Library.
2. Open FlashPoint from the Property drop down menu.
3. The Property Details window should open. Look for the "Max. value" entry, and change this value to 600 (the default should be 400).
4. Make sure to check the box "Update all assays" at the bottom left. Then hit OK.
5. Go back to your Assay and recharacterize (using the Match Whole Crude option), it should now match your FlashPoint input
Keywords: None
References: None |
Problem Statement: Does AFSA calculate an adjusted Likelihood of Failure(LOF), etc. for "Custom Curves" & "Custom Attenuation" in AIV calculations? | Solution: LOF applies exclusively to Energy Institute calculations, all other calculations have a binary accept/reject choice based on an SPL threshold (fixed for API method, variable for Carucci-Mueller and custom curve). This applies for custom curve option as fixed threshold value which comes from the D/t vs. dB curve.
AFSA interpolates a limit dB value from the curve based on the D/t for the particular pipe (e.g. for a pipe with a D/t of 27 with the curve given above, the limit value would be 125.6666666666667 dB, so if the SPL in the pipe were 125 dB, it would not be flagged, and if it were 126 dB, it would be flagged as a violation).
Keywords: LOF, AIV, Custom, D/t, dB, SPL
References: None |
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