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Problem Statement: How do I return from the Blowdown sub-flowsheet to the main flowsheet? | Solution: Go to the Flowsheet/Modify tab and click the Go to Parent button.
Keywords: Blowdown, flowsheet
References: None |
Problem Statement: I would like to automate the Health Summary Report for a selected Aspen InfoPlus.21 system. | Solution: Before you start, please first follow the instructions included within the Aspen SQLplus Reporting help. Aspen SQLplus Reporting page can be accessed by following this URL in the IE browser on the Web server:
http://localhost/SQLplus/Report.aspx?IsPublic=true&ReportName=HealthSummary [localhost]
Before configuring the automatic emailing of reports, the Automating Reports help topic explains that, you must first configure the Aspen Simple Mail Transfer Protocol (SMTP) Service as described in the Configuring the E-mailing of Reports help topic.
To automate the Health Summary report for selected Aspen InfoPlus.21 systems proceed as follows:
1 Select the Health Summary public report for the selected system. The report definition is displayed in the right pane.
2 Click Automate to invoke a page that allows configuring the automatic generation of the Health Summary report.
3 Select the desired Aspen InfoPlus.21 system in the Data Source field.
4 Enter a report name in the Automated Report Name field.
5 Select the Change of State tab.
6 Enter IP21SystemHealthTests IP_REPORT_TRIGGER into the InfoPlus.21 Field, and then press the Add button.
7 Select the E-mail tab, and then create an email list by adding email addresses.
8 Select the Result Limit tab, and then select the Delete report results radio button.
9 Enter the desired number of days (for example, 1 day), and then click OK to finish automating the report.
Keywords: Health Monitor
SQLplus Reporting
References: None |
Problem Statement: In the Aspen InfoPlus.21 Manager under the File menu option, there is an option to 'Restore Group Configuration'.
Below this, there is an option to 'Replace' or 'Merge' Current Configuration.
Under Merge, there is an option to 'Overwrite' or 'Keep' Existing Tasks.
What do these all mean? | Solution: The Restore Group Configuration option is used to reinstate the list of defined IP.21 tasks in the IP.21 Manager along with the start up order of the tasks.
At some point, the list of tasks was saved or should have been saved using the File | Save Group Configuration option into a file with an .ipg extension. This is commonly done after a change is made to the startup order of the tasks, or if a new task is added, or if an upgrade is about to be performed.
There are 3 options available to restore:
1. File | Restore Group Configuration | Replace Current Configuration
This option totally replaces the existing configuration with that from an available .ipg file.
2. File | Restore Group Configuration | Merge to Current Configuration | Overwrite Existing Tasks
The 'Merge to Current Configuration' option combines the existing configuration with that from an available .ipg file. Meaning that if there are any 'unique' custom tasks (e.g. Aspen Cim-IO tasks) that appear in either configuration (current or .ipg file), then they will now appear in the new merged configuration list.
The 'Overwrite Existing Tasks' option means that if there are any 'common' tasks between the two files, the existing tasks are overwritten using the information in the referenced .ipg file selected for restoring.
For example, TSK_DBCLOCK would be in both the existing list of defined tasks and the .ipg file being restored. This task, amongst other things, defines the database memory allocation value via the 'command line parameters'. It is quite possible that the number defining memory allocation in the current Tsk_Dbclock configuration is different to the Tsk_Dbclock value in the .ipg file
The 'Overwrite' means that the new configuration will contain the value seen in the .ipg file
3. File | Restore Group Configuration | Merge to Current Configuration | Keep Existing Tasks
The 'Merge to Current Configuration' option combines the existing configuration with that from an available .ipg file. Meaning that if there are any 'unique' custom tasks (e.g. Aspen Cim-IO tasks) that appear in either configuration (current or .ipg file), then they will now appear in the new merged configuration list.
The 'Keep Existing Tasks' option means that if there are any 'common' tasks between the two files, the existing tasks are NOT overwritten using the information in the referenced ipg file selected for restoring.
For example, TSK_DBCLOCK would be in both the existing list of defined tasks and the .ipg file being restored. This task, amongst other things, defines the database memory allocation value via the 'command line parameters'. It is quite possible that the number defining memory allocation in the current Tsk_Dbclock configuration is different to the Tsk_Dbclock value in the .ipg file
The 'Keep' means that the new configuration will contain the value that was in the existing configuration.
Keywords: None
References: None |
Problem Statement: How can I bypass the login prompt that requests username and password when launching the PCWS web page? | Solution: Follow these steps to change the internet settings so that it automatically logs in without prompting for the username and password:
1. Open Control Panel and select Internet Options for the Internet Properties dialog box to open.
2. Under the Security tab, select Local Intranet, and click on the Sites button.
3. Click on Advanced.
4. Add the PCWS URL to the zone:
5. Back on the main dialog box, click on Custom level.
6. Scroll down to User Authentication and select the bubble for Automatic logon with current user name and password. Hit OK and apply the changes.
7. Optionally, you can repeat steps 2-6 for Trusted Sites under the Security tab for good measure.
Keywords: PCWS, production control web sever, web page, skip, bypass, avoid, without, login, logon, sign in, sign-in, prompt, user, add, trusted, sites, local, intranet
References: None |
Problem Statement: What needs to be done in order to migrate from a Framework Security server to a Local Security server? | Solution: In order to migrate from a Framework Security Server to a Local Security server please do the following:
1. On the Framework Security server open AFW Tools and switch to the 'Transfer AFWDB Data' tab.
2. Export the Roles and Applications by clicking the 'Export' button. A drive and path can be placed in front of the filenames (e.g. C:\PFWAPPL.XML) if desired. An Exported Successfully message should appear if the export was successful.
3. Locate the PFWROLE.XML and PFWAPPL.XML files and copy them to the Local Security system.
4. On the Local Security system open AFW Tools, switch to the 'Transfer AFWDB Data' tab, and make sure the path to the files is correct.
5. Click the 'Import' button and look for an Imported Successfully message.
6. Open AFW Security Manager and verify that the roles and applications are listed correctly.
Keywords: Microsoft SQL Server
SQL Server
Oracle
Microsoft Access
Access
.MDB
AFW Database Migration
133288-2
References: None |
Problem Statement: A customer is looking for a | Solution: to automate the Aspen Extractor stop/restart procedure when having to reboot the APRM/IP.21 server.
Questions:
1. Is it a must to disable the Extractor Scheduler prior to stopping the Aspen IP.21 Database and Aspen related services or will it be enough to just stop the Aspen Extractor Service?
2. Are there any concerns of missing data or data gaps if Aspen Extractor service is stopped abruptly while the Extractor Scheduler is in processing status?
3. If it’s advisable to disable the Extractor Scheduler prior to stopping the Aspen Extractor Service, are there any API calls or commands that can be used instead of doing it from the Extractor Administrator GUI?
This knowledge base article answers the above questions and provides a procedure to safely stop and restart the Aspen Extractor server.
Solution
It is always advisable to disable Extractor Scheduler before stopping the Extractor service. If you have to wait for data flag to turn on, then you may stop your IP.21 database before stopping the Extractor. Otherwise, you should stop the Extractor before stopping IP.21.
There is no API call to disable Extractor Scheduler nor any KBA on the API. But you could write a script to issue a database call to update the Extractor database to disable all Extractor configurations.
In the Extractor database, there is a table called ExtractorServerConfigAssign that contains a State column. Each row in this table is equivalent to one Extractor configuration. Setting the state column to Disabled will mark the configuration as disabled. Extractor Administrator UI actually just performs the same update to the table. After you disable all configurations, you should wait a reasonable time (5-10 minutes) before you can stop the Extractor service.
Below is a sample code to disable/enable the Extractor configurations:
'
Keywords: None
References: None |
Problem Statement: How to initialize the vessel temperature profile for dynamic simulation? | Solution: A vessel can be configured to account for heat transfer between vessel fluid and surrounding environment. A detailed heat loss model includes inside vapour and liquid phase heat transfer coefficients, outside heat transfer coefficient, and heat conduction through the metal wall and insulation.
HYSYS calculates the temperatures of vessel fluid, inner wall, outer wall, outer insulation and heat flow.
It is generally recommended to initialize the temperature profile after entering the detailed heat loss parameters. HYSYS assumes the vessel is lined out when determining the initial temperatures. When the dynamic simulation is first started with heat loss data, the initialization helps to stabilize the simulation.
Figure 1: Temperature profile before initialization.
Figure 2: Temperature profile after initialization of temperatures.
Keywords: Heat transfer, Vessel, Temperature Profile
References: None |
Problem Statement: aspenONE Process Explorer (A1PE) returns the following error: Server is unable to acquire SLM_RN_PME_IP64_PRDSRV license, and no value shows. | Solution: Make sure that IP.21 server is running under a granted license status
Open the IP.21 Admin
Right click over the server name | properties and then check license status.
If IP.21 is running with a license denied or grace period mode it will cause this problem in A1PE.
If the license status is Granted then do the following:
Run the command IISReset in a command prompt with Admin privileges on the server which has A1PE installed. It could be possible that AspenProcessDataAppPool is not running, this IIS Pool contains the application used by A1PE to read values from IP.21 server, that can be the reason why you can open A1PE but not see any data.
If after doing IISReset the problem persist, Open IIS (from windows start menu), select application pools and verify that AspenProcessDataAppPool is running with the proper Admin account.
Keywords: Server is unable to acquire SLM_RN_PME_IP64_PRDSRV license
A1PE
License status
AspenProcessDataAppPoolx86
IISReset
References: None |
Problem Statement: How do I find heat of fusion for a chemical? | Solution: Follow the steps below
Search for the chemical in Aspen Plus properties environment or Aspen Properties (KB 000096832)
Click the Retrieve parameters button
A pop up window appears. You can select copy pure component parameters to input if you would like to see the parameters on input forms as well
In the Methods/Parameters/ Results/Pure Components, look for HFUS parameter
Keywords: Heat of melting, chemical properties
References: None |
Problem Statement: VBA Automation does not explicitly reports Unit Operations and/or Process streams status. | Solution: The easiest way to acknowledge the calculation status of a piece of equipment or stream in a simulation is by accessing its Status bar. This can be accomplished by making use of the below BackDoor command:
Dim hyApp As HYSYS.Application
Dim hyCase As HYSYS.SimulationCase
Dim b As Object
Dim test1 As BackDoor
Dim test2 As TextVariable
Set hyApp = GetObject(, HYSYS.Application)
Set hyCase = hyApp.ActiveDocument
a = hyCase.Flowsheet.Operations.Count
For i = 0 To a - 1
Set b = hyCase.Flowsheet.Operations.Item(i)
Set test1 = hyCase.Flowsheet.Operations.Item(i)
Set test2 = test1.BackDoorVariable(:status.1).Variable
Next i
Key words
HYSYS, Automation, VBA, Adjust
Keywords: None
References: None |
Problem Statement: How do I specify distillation temperature corresponding to x% EVAP [Petrol]? | Solution: The x% EVAP [Petrol] is found under the calculator tab in the Workbook. This is often used to obtain the % corresponding to a distillation temperature. By default, the value is <empty>.
The x% EVAP correlation is available under the Petroleum correlation type on the Correlation Manager. The Distillation Temperature can be specified here. The output will be x% corresponding to the given temperature.
From the Composition Basis drop-down list, you can select one of the following options: Volume (default), Mass or Mole
You can also select distillation type as D86, TBP, D2887, D1160
Keywords: x% EVAP, petroleum correlation, specify distillation temperature, Workbook
References: None |
Problem Statement: Why is the number of identical items field not adjusting my quoted item? | Solution: The software requires 2 fields to be entered correctly for this to work:
1. The 'Quantity adjustment option' field must be set to 'Y'.
2. The 'Unit of measure' field must be set to 'Items'.
Keywords: quoted, identical items, unit of measure, ITEMS, quantity adjustment, quantity
References: None |
Problem Statement: How do I add a Motor Operated Valve? | Solution: Solenoid valves are created via Instrument Installation Bulks:
Start with a Plant Bulk Pipe component
Go to Options | Instrumentation
Select the Control Valve location (pipe line number, enter 0 to install on given pipe)
Must specify an On/Off valve
Select “Remote ControllType” as “M”
Keywords: Motor, operated, valve, solenoid
References: None |
Problem Statement: What is the default productivity in the Economic Evaluation products, and what does it include? | Solution: The Economic Evaluation products use a default productivity of 100 percent. The 100 percent productivity assumes a 42 minute work hour due to breaks and delays.
You may override the default 100% productivity from the Project Basis View | Basis for Capital Costs | Construction Workforce | Wage Rates form. You may use the Productivity all crafts input field to set all crafts at once. Alternatively, you may click the curved red arrow in the Craft wage rates field to set the productivity on a craft by craft basis.
Examples of calculating productivity percentages:
If you want to specify a 45 minute work hour, enter a productivity of 107.14% (calculated by diving 45 minutes by 42 minutes).
If you want to specify a 38 minute work hour, enter a productivity of 90.48% (calculated by dividing 38 minutes by 42 minutes).
Note that 42 minutes is in the denominator, not 60 minutes, due to the default. Also, the productivity values are entered as percentages, not decimals.
Keywords: productivity, percentage
References: None |
Problem Statement: Is it possible to estimate parameters for two isomer molecules which cannot be found in the database? | Solution: If the desired isomers are not available in any of the Aspen Plus data banks, it will be necessary to directly define them to keep on working. But, if only the structure for each of the isomers is drawn without any additional parameters entered, the results will be the same for each of them because Aspen Plus breaks the molecule into its functional groups to do the estimation. For example, Fumaric and Maleic acid have different molecular structure but the same functional groups:
Fumaric acid: Maleic acid:
For the components to have different properties, some different parameters need to be added. After defining the non- databank isomers with the User Defined wizard and drawing the molecules, specify available data for each one of them, such as normal boiling point, vapor pressure and heat capacity data (i.e. fumaric and maleic acid have different properties). This will give more information to Aspen Plus to do a more accurate estimation for each one of them.
For more information about how to define a conventional non-databank component, please refer toSolution number 24028.
Keywords: Isomers
Cis-isomer
Trans-isomer
References: None |
Problem Statement: Why is the escalation cost not appearing on my report? I added escalation index values (Project Basis View | Escalation) and selected Accumulated as the method. | Solution: When accumulated is selected as the method, only the forward escalation (present to future) is reported as a lump sum. The forward escalation values are entered in the ESCALATION INDICES section. Once Escalation Indices are provided, then a lump sum Escalation Cost will be reported in the Non-Field Cost Summary.
The past to present escalation update, from values entered in the USER BASE INDICES section, will not be accumulated and reported in a lump sum. They will still be spread into each component, which is the same result as when the method is set to Spread.
Keywords: escalation, accumulated, report, user, base, index
References: None |
Problem Statement: Can I zoom in on the ACCE input forms? The data entry is small and difficult to read. | Solution: Yes, it is possible to zoom in on the forms to make them larger and easier to read. Hold down he ctrl key on keyboard and scroll using your mouse wheel or touch pad.
Keywords: zoom, forms, small
References: None |
Problem Statement: Why are there no warnings flagged for Sound Power Levels (SPL) when using E.I. Guidelines (2008e) as screening criteria for acoustically induced vibration (AIV) calculations? | Solution: Aspen Flare System Analyzer (AFSA) does not flag a warning if E.I. Guidelines (2008e) screening criteria is selected and the Likelihood of Failure (LOF) is less than 0.5.
When the calculated results for AIV-SPL are greater than 155 dBa and the result is not being flagged (i.e., font is not red; there is no “warning message” associated with AIV-SPL in the Error Messages/ Results Problems), it implies that the Likelihood of Failure is less than 0.5.
Warnings will only be flagged only when the Likelihood of Failure is greater than or equal to 0.5.
Keywords: AIV, E.I. Guidelines (2008e), Likelihood of Failure (LOF)
References: None |
Problem Statement: Was the gProms born from ACM? What is a conversion tool? | Solution: Both ACM and gProms originated in Imperial College, London and have common roots. However, that does not mean we can convert easily between them. We have no way to reconcile these two products.
Keywords: gProms, ACM, Aspen Adsorption, Aspen Custom Modeler
References: None |
Problem Statement: How to create the connection of the Aspen Adsorption with the Comsol? | Solution: It need to use 3rd party tool. It is should be possible using Excel as a bridge application. Currently, after build the model in Aspen Adsorption, with installation of Aspen Simulation Workbook, Excel can be used as input and output interface of Aspen Adsorption.
Keywords: gProms, Aspen Adsorption, Comsol
References: None |
Problem Statement: Are the Escalation Values applied to User-Entered Costs? | Solution: All user-entered costs (quoted cost items, quoted equipment costs, library items, material/labor lump sum additions, project indirects, etc) are assumed to be valid at the User base time point.
The User Base Indices (UBI) only applies to the system generated costs which are adjusted to User cost values (at the User base time point).
The Escalation Indices (EI) will apply to all cost values. This means that the system generated costs will first be updated to the User cost values based on the UBI and then the EI will apply to update all (system as well as User, both at the User base time point) costs to a future projected cost.
For more information on how escalations are calculated please refer to Knowledge Article:
How is Escalation calculated for Icarus products?
https://esupport.aspentech.com/S_Article?id=116180
Keywords: Escalation Indices, EI, UBI, user-entered costs
References: None |
Problem Statement: How RPLUG calculates the heat transfer to environment in Aspen Plus Dynamics? | Solution: When “Model equipment heat capacity” is chosen, the heat transfer between the fluid and the material of the reactor is calculated with the mass of the material and heat transfer coefficient. The heat transfer between the fluid and wall is calculated according to:
Q_flux_wall = U_wall*(Ti - T_wall),
Where,
T_wall is the the temperature of wall
Ti is the temperature of fluid
The temperature of wall can be same as process stream temperature or calculated according to the thermal fluid temperature on shell.
In order to calculate the heat transfer to the environment, user must submit the ambient temperature Tamb and the overall heat transfer coefficient U_env. This coefficient involves the heat transfer phenomena from the wall to the environment.
About the energy balance of equipment, the area to calculate the wall temperature considers the inner diameter. The heat loss to the environment is calculated considering the temperature of the fluid, the wall temperature, environment temperature and the respective overall heat transfer coefficients (Uwall and Uenv).
The heat transfer area is determined using the number of tubes, the inner diameter and reactor tube length:
PI*Diam_*NTube*L
where,
Diam_ is the inner diameter of tubes on reactor,
NTube is the number of tubes (it was specified on Aspen Plus User Interface)
L is the length of the reactor.
Please review the code in the RPlugPDE model in Aspen Plus Dynamics and the Aspen Plus Dynamics V10 On-line help.
If you search for HeatOptEqp in RPlugPDE, you will see the code relevant to heat transfer options.
Keywords: Heat transfer, Rplug, Twall, etc
References: None |
Problem Statement: What are the various unit operations in Aspen HYSYS that facilitate heat transfer modeling? | Solution: Aspen HYSYS features a variety of unit operations to facilitate heat transfer modeling. Users can use the following unit operations from Model Palette to model heat transfer.
Heater/Cooler: The Cooler and Heater operations are one-sided heat exchangers. The inlet stream is cooled (or heated) to the required outlet conditions, and the energy stream absorbs (or provides) the enthalpy difference between the two streams. These operations are useful when you are interested only in how much energy is required to cool or heat a process stream with a utility, but you are not interested in the conditions of the utility itself. The difference between the Cooler and Heater is the energy balance sign convention.
Heat Exchanger: The Heat Exchanger performs two-sided energy and material balance calculations. The Heat Exchanger is very flexible, and can solve for temperatures, pressures, heat flows (including heat loss and heat leak), material stream flows, or UA.
Fired Heater: The Fired Heater (Furnace) operation performs energy and material balances in steady state or dynamic modes to model a direct Fired Heater type furnace. This type of equipment requires a large amount of heat input. Heat is generated by fuel combustion and transferred to process streams.
LNG exchanger: The LNG (Liquefied Natural Gas) exchanger model solves heat and material balances for multi-stream heat exchangers and heat exchanger networks. TheSolution method can handle a wide variety of specified and unknown variables.
Air Cooler: The Air Cooler unit operation uses an ideal air mixture as a heat transfer medium to cool (or heat) an inlet process stream to a required exit stream condition. One or more fans circulate the air through bundles of tubes to cool process fluids. The air flow can be specified or calculated from the fan rating information.
Plate Exchanger: The Plate Exchanger unit operation solves heat and material balances for two stream plate heat exchangers. Plate heat exchangers consist of plates packed in a frame. Two streams, one hot and one cold, flow in alternate channels between these plates. Plate unit operations can solve for heat loads using either a basic heat and material balance or a rigorous calculation based on geometry.
Keywords: Heat Transfer, Heater, Cooler, Heat Exchanger, Fired Heater, LNG Exchanger, Plate Exchanger, Air Cooler
References: None |
Problem Statement: How can I set the condenser temperature for a Radfrac column if I'm not using a Partial-Vapor-Liquid condenser type? (Note: only the Partial-Vapor-Liquid condenser type allows temperature to be specified on the Condenser tab of the Radfrac input form.See article How do I set the condenser temperature in a Radfrac column?) | Solution: It is possible to set the condenser temperature using a design specification inside the column. The design spec (dependent) variable would be the stage 1 (condenser) temperature. The vary spec (independent) would be condenser duty. Note that the condenser duty would need to be one of your operating specs from the main column setup.
The specs can be found in the navigation pane under:
Dependent: Blocks | <Column name> | Specifications | Design Specifications
Independent: Blocks | <Column name> | Specifications | Vary
Please see attached example file illustrating the described setup.
Keywords: condenser, temperature, radfrac
References: None |
Problem Statement: Is it possible to skip installation of the SQL Express Engine? | Solution: You need to change the registry to tell the installer to skip installation of the SQL Express engine on the client machine. This is needed for customers whose IS policy prohibits installation of any SQL engine on the client PC.
1. For 2006.5, merge the attached ( MSDE_fool_installer.reg) registry into the client registry entries using the registry editor.
2. For V7.X - V8.8, create the following registry entry:
Use the DWORD type when creating the entry.
32bit OS:
[HKEY_LOCAL_MACHINE\SOFTWARE\AspenTech\Setup]
NOSQLExpress=dword:00000001
64bit OS:
[HKEY_LOCAL_MACHINE\SOFTWARE\WOW6432Node\AspenTech\Setup]
NOSQLExpress=dword:00000001
Keywords: aped
SQL Server Express
References: None |
Problem Statement: How to change the Unit Basis for a project in Aspen Capital Cost Estimator? | Solution: In this example we show how to change the units for the Wire Size to mm2.
When you have a project there is a Unit Basis library associated to it, for example US_IP:
This unit basis doesn't have mm2 by default so you need to change the specification for this.
The way to do this is by closing your project and then going to the Library Tab on the Palette and select the Basis for Capital Costs Folder. Expand the Inch-Pound folder and right-click on US_IP. Choose the option Duplicate:
This will allow you to customize this unit basis. On the window that shows up, give the new unit base a name and click ok:
Now, the menu for this library will show up and you can go to Units of Measure Customization Input. Then go to Special Units > Wire Size Units and select M (for mm2) and click on OK:
Close this unit basis and open your project. Right click on Basis for Capital Cost and choose Select. On the window that shows up, choose the Unit Basis you just created and click OK:
Note: When you select 'OK' there will be a window notifying the user about the changes in the current project. Changing the setting may affect your project definition and evaluation if any of the following specs are different from those used in the new basis: Country Base, Currency Definition, and Units of Measure of Customizations. Power Distribution system may be in conflict, if previously defined. In addition, all area links will be removed from project and need to be respecified. This will break all PD, PB, PC, and CS area links!
Warning 1: warning when project have previously defined PD, PB, PC Warning 2: Warning when project Do NOT have previously PD, PB, PC
Now you will see the units in mm2:
Keywords: Unit basis, library.
References: None |
Problem Statement: Is there a way to specify API 650 standards for my process vessel? | Solution: Yes, you may specify the Vessel Design Code in the Project Basis View | Basis for Capital Costs | Design Basis | Equipment Specs. There you can specify ASME, which refers to ASME code, Section VIII. Note that ASME code, Section VIII complies with API 650 standards.
Keywords: API 650, API, 650, vessel, ASME
References: None |
Problem Statement: What does the Accessories cost field in the Customer External Files | Civil Material mean and how does it work? | Solution: The Accessories cost field in the Customer External Files | Civil Material refers to Anchors and Embedments costs in user currency per unit volume of concrete. These items are generated for certain equipment foundations and can be viewed in the Evaluation Report. For example, if a project scenario contains a distillation column, then some quantity of Foundation Accessories (COA 452) will be generated. The base year for this cost data should also be provided.
The application of the Accessories cost is as follows:
Assume you have set $100/CY for this item and have a concrete volume of 10CY. The Icarus cost engine will now calculate your Foundation Accessories to be $1000 (or more depending on your basis year set for pricing). It will then back-calculate the number of accessories needed to reach the total of $1,000.
Useful tip:
Once the concrete volume is known, the user may tweak the $/CY value to reflect their own estimated cost for the accessories.
Keywords: Customer External Files, Civil, Accessories, Anchors, Embedments
References: None |
Problem Statement: How to handle MPI related errors in PIMS when using parallel processing? | Solution: In V9, V10 and V11, PIMS replaces MPICH2 with Microsoft MPI (MSMPI), which should be in “C:\Program Files\Microsoft MPI\Bin\”. Users may need to uninstall MPICH2 or disable MPICH2 service from task manager if it exists on the machine before. In the registry, please also confirm MPIExecDirectory does exist for MSMPI.
Meantime, please check if Windows Firewall blocks some of PIMS executables. To unblock, please go to Control Panel, Windows Firewall, Exceptions tab, Add Program and add the following executables.
1. C:\Program Files(x86)\AspenTech\Aspen PIMS\CaseParallel.exe
2. C:\Program Files(x86)\AspenTech\Aspen PIMS\MultiStartParallel.exe
3. C:\Program Files(x86)\AspenTech\Aspen PIMS\PIMSWin.exe
4. C:\Program Files\Microsoft MPI\Bin\mpiexec.exe
Keywords: None
References: None |
Problem Statement: When an EO script (from model manager) is copied to notepad, it loses all the cariage returns (as shown below). Is there a workaround? | Solution: This problem is observed in older builds of notepad like version 1709. In newer builds like 1809, the problem is not observed. Easy workaround is to copy the script to Wordpad or MS Word
Keywords: Equation oriented, global scripts, local scripts
References: None |
Problem Statement: When grouping several trends in one trend plot, how can I display all the titles for each of the trends?
For example, in the plot below, how can include T011 and T012 in the plot title. | Solution: To display more than one line of title to show several trends, go to Gantt & Trend Chart Options (or access through Gantt > Preferences) and in the Graphic Features tab, uncheck the option “Show only one trend title for each Y-axis for multiple trends”.
Click “OK” to apply changes. Now you should see all the trend titles.
Keywords: Gantt chart, APS, MBO, graph
References: None |
Problem Statement: In several of the heat exchanger input forms, there are options for specifying cladding. Included in those options, there is a Cladding location field with SHELL, TUBE or BOTH as available selections. What does the cladding location option include when specified for a heat exchanger? | Solution: The Cladding location tells Icarus which pieces to clad. It specifically refers to the Tubesheet, but also entails ancillary items. Note that tubes are never clad.
The TUBE option will clad one side of the tube sheet as well as the channel(s) and heads that are in contact with the tube side material.
The SHELL option will clad one side of the tube sheet and the shell. For a U-TUBE exchanger, it will clad the head that sees the shell side fluid.
The BOTH option will essentially clad the entire exchanger with the exception of the tubes.
Keywords: floating head, fixed head, TEMA, clad, heat exchanger, clad, cladding,
References: None |
Problem Statement: Sometimes when storing PIMS model in a OneDrive folder, users might get errors related to files not being opened when running the model. These errors might vary for each user but if you are working with a model that is stored in OneDrive and are getting these types of errors, you can try the | Solution: described in this article.
Example of error: ERROR. COULD NOT OPEN FILE...
Solution
To solve the issue, you will need to pause OneDrive syncing while you are using PIMS. To do right click on the OneDrive cloud icon on the notification area. This will display a list of options. Click on “Pause Syncing”.
You can also choose to pause syncing for 2, 8 or 24 hours. This way it will automatically resume syncing after the selected time has passed.
Keywords: Cloud, update, model directory
References: None |
Problem Statement: I specified the distance to the Motor Control Center (MCC) on the area electrical specification (Area Specifications | Area Electrical | Distance to Motor Control Center) as 500 ft. Now I am receiving a warning which states the SPECIFIED DISTANCE TO MCC MAY GENERATE OVER SIZED WIRE/CABLE. However, equivalent distances have also been specified for the instrumentation junction boxes, but no warnings for these lengths were generated. Why? | Solution: Electrical wire is a much higher voltage than instrument wire (480/460 volts for electrical wire compared to 24 volts for instrument wire). Due to the lower voltage, the Icarus cost engine does not check voltage drops on instrument signal wire. It does, however, calculate voltage drops on electrical wire and adjusts wire sizes, as needed.
The warning is a reminder to check whether the length specified is correct and to make sure that the estimator understands that the wire is sized for both required amperage and the voltage drop.
Keywords: voltage, resistance, electrical, voltage, control, cable, ohm, MCC
References: None |
Problem Statement: How to define Min% and Max% in Blends in MBO？ | Solution: In MBO, it is a good practice to define reasonable Min%, Max % and Threshold for all components. This would guide the optimizer to search in a more practical and limited space and help with convergence.
To define MIN% and MAX% in blends, users should go to Model>>Product and under Components, Min% and Max% of component allowed in the blended product can be entered.
Keywords: None
References: None |
Problem Statement: What are the file formats in Aspen Plus simulations? | Solution: File Type Extension Format Description
Compound *.apwz Binary Compressed file which contains the model (the BKP or APW file) and external files referenced by the model. You can add additional files such as supporting documentation to the APWZ file
Document *.apw Binary File containing simulation input, results and intermediate convergence information
Backup *.bkp ASCII Archive file containing simulation input and results
Template *.apt ASCII Template containing default inputs
Attached video file describes about the different file types elaborately..
Keywords: File, Formats, Aspen Plus
References: None |
Problem Statement: How to create submodels to replace PIMS internal structure for CRDTANKS and CRDALLOC tables? | Solution: In PPIMS model, CRDTANKS and CRDALLOC tables are used to define tank beginning inventory and allocation to crude units. PIMS takes care of the internal structures for both tables.
In some cases, users would prefer to set up submodel tables to replace the PIMS internal structures for crude tanks so as to add custom constraints into the model. Following model is an example to create submodel tables.
This is the Volume PPIMS Sample Model with crude tank related tables.
T. CRDTANKS:
T. CRDALLOC:
T. PERIODS:
T.PINV
Ideally, PIMS will internally create two submodel tables Sdp1 and ST01 for T.CRDTANKS and T. CRDALLOC tables.
To manually create submodel tables for corresponding constraints, we can set up following tables.
In order to avoid duplicate tags, we change the crude tags ANS, NSF to lower case ans and nsf in T. BUY to represent the purchase quantity of ANS and NSF.
Followings are the changes made in the tables:
ST01 represent crude T01, which calculates crude unit feed rates based on crude purchased quantity and tank inventory.
The RHS of composition recursion rows are calculated according to crude tank open inventory and initial crude tank composition.
For example, in RansT01:
RHS= T01 open inventory * ANS percent% in T01/Period length= 20*60/30=40
Sdp1 depools ANS and NSF from T01 to calculate the feed rates of ANS and NSF to crude unit CD1.
Additional structures:
Keywords: None
References: None |
Problem Statement: What are the various available specification types for a heat exchanger in Aspen HYSYS? | Solution: The available specification types for a heat exchanger include the following (these can be added via the Specs Page)
Specification Description
Temperature The temperature of any stream attached to the Heat Exchanger.
Delta Temp The temperature difference at the inlet or outlet between any two streams attached to the Heat Exchanger.
Minimum Approach Minimum internal temperature approach. The minimum temperature difference between the hot and cold stream (not necessarily at the inlet or outlet).
UA The overall UA (product of overall heat transfer coefficient and heat transfer area).
LMTD The overall log mean temperature difference.
Duty The overall duty, duty error, heat leak or heat loss. The duty error should normally be specified as 0 so that the heat balance is satisfied.
Duty Ratio A duty ratio can be specified between any two of the following duties: overall, error, heat loss, and heat leak.
Flow The flowrate of any attached stream (molar, mass or liquid volume).
Flow Ratio The ratio of the two inlet stream flowrates.
Subcooling Subcools the LNG or heat exchanger to the temperature of any of the attached stream. Select the stream you want to use from the Stream drop-down list.
Superheating Superheats the LNG or heat exchanger to the temperature of any of the attached stream. Select the stream you want to use from the Stream drop-down list.
Keywords: Heat Exchanger, Product stream temperature, Minimum temperature approach, Overall UA, LMTD, Degrees of subcooling / superheating, Delta Temp
References: None |
Problem Statement: How to do Aspen MBO model validation and find missing data? | Solution: Apen MBO model validation is a crucial step to troubleshoot model infeasibility and convergence issues. In MBO models, almost more than 50% infeasibilities come from missing or bad inputs.
Users need to check if there are missing data in the model:
Verify all tank properties exist
Populate reasonable Defaults for each property, if missing
Copy From _STRMS in APS, only the ones you trust
Verify derived properties
Avoid “Default from PROPS”
Use Model -> Validate Model to look for missing data
Followings are common places to look for missing data:
Beginning Inventories
Component Rundowns
Tank Property Change Events
TANK_PROPS table
Keywords: None
References: None |
Problem Statement: What are the various mathematical/logical in Aspen HYSYS that automate tasks and support engineering calculations? | Solution: Following mathematical/logical operations are available in Aspen HYSYS to automate tasks and support engineering calculations.
Balance: The Balance operation provides a general-purpose heat and material balance facility. The only information required by the Balance is the names of the streams entering and leaving the operation. For the General Balance, component ratios can also be specified.
Adjust Operation: The Adjust operation varies the value of one stream variable (the independent variable) to meet a required value or specification (the dependent variable) in another stream or operation.
Set: The Set is an operation used to set the value of a specific Process Variable (PV) in relation to another PV. The relationship is between the same PV in two like objects; for instance, the temperature of two streams or the UA of two exchangers.
Recycle: The Recycle installs a theoretical block in the process stream. The stream conditions can be transferred either in a forward or backward direction between the inlet and outlet streams of this block. In terms of theSolution, there are assumed values and calculated values for each of the variables in the inlet and outlet streams. Depending on the direction of transfer, the assumed value can exist in either the inlet or outlet stream.
Spreadsheet: The Spreadsheet applies the functionality of spreadsheet programs to flowsheet modeling. With essentially complete access to all process variables, the Spreadsheet is extremely powerful and has many applications in HYSYS.
Keywords: Mathematical/Logical Operations, Balance, Adjust, Set, Recycle, Spreadsheet
References: None |
Problem Statement: How do I add costs for a Close Circuit Television (CCTV) system? | Solution: The option to add a CCTV system is found under Project Basis View | Basis for Capital Costs | Design Basis | Electrical Specs. This option is also available in the Area Specs | Area Electrical. Change the option from N to Y to include it.
CCTV is part of the Communication and Alarm Systems section. Other options include:
Public Address General Alarm Systems (PAGA)
Telephone System
Area Networking (LAN)
Radio Systems
Access Control
Intrusion Detection
Meteorological
Keywords: CCTV, communication, alarm
References: None |
Problem Statement: Cim-IO store file does not forward and tags do not update after communication is restored. This behavior can be caused by multiple network cards or a difference in configuration between the Cim-IO client and Cim-IO Interface server. | Solution: On the Aspen Cim-IO client server [Aspen InfoPlus.21], check the file ..\AspenTech\CIM-IO\etc\cimio_logical_devices.def and note the NODENAME referenced for the given Aspen Cim-IO interface.
EX; LogicalDevice NODENAME Service
On the Aspen Cim-IO interface server, check the ..\AspenTech\CIM-IO\log\CimIO_MSG.log file and note the NODENAME in the messages.
EX; Logged by service name on node NODENAME:
If the NODENAME does not match when comparing the messages to the cimio_logical_devices.def file then follow the steps below to resolve the issue.
Create a file named ..\AspenTech\CIM-IO\etc\cimio_nodename.txt on the Cim-IO interface server.
Add the NODENAME noted in step 1. [Make sure the case of the NODENAME matches].
Enter a carriage return following the NODENAME in the cimio_nodename.txt file and save it.
Stop and restart the Cim-IO Store & Forward processes on the Aspen Cim-IO server. This may require a Clean Start
Keywords: cimio_nodename.txt
nodename.txt
store and forward
multiple network cards
References: None |
Problem Statement: How do I get temperatures for different % true boiling points (TBP) in Workbook? | Solution: If the desired temperatures are for 0%, 5%, 10%, 30%, 50%, 70%, 90%, 95%, 100%, these variables can directly be added from the Calculator variables option.
However, if you want to get boiling point temperature for a percent (%) not available in the above option, one workaround is to follow the following steps:
Select the entire flowsheet (if it is too large, you can select portions of the flowsheet which are of interest )
From the Ribbon, under Home, go to Stream Analysis and Petroleum Assay. Close the dialog boxes that open after creation of the analyses.
Then, go to Workbook, Setup and add Petroleum Assay as a Workbook tab.
From Setup, under the Petroleum Assay tab, add true boiling points which are of interest. These include as an example - 1%, 15%, 95% and 99% TBP which are not available under the Calculator variables of the Workbook.
Keywords: Workbook, TBP %, Calculator variable, Petroleum properties
References: None |
Problem Statement: Which property value will PIMS use for transferred stream in destination local model if there are multiple property values defined? | Solution: In MPIMS models, streams can be transferred between local models to reflect the practical refinery/petrochemical materials distribution.
It is common properties for these transferred streams are defined/recursed in source plant as well as destination plant. MPIMS will take the following hierarchy to pick properties:
1. If a material xxx is transferred from A to B and its properties are recursed in A, then the recursed property values of xxx are used for xxx in destination plant B(from the solved values in A). In another word, if transferred stream properties are recursed from source plant, then destination plant will always use these recursed values for transferred streams.
2. If there are no recursion for transferred streams in source plant and you want to use the static/constant property from source plant, following setting can control it:
Override Transferred Static Qualities Select this option to override the static quality in a destination plant with the static quality from a source plant. This applies to a situation where there is a stream in a local model that has a static (fixed) quality and that stream is transferred to another local model which also has a fixed quality but with a different value. Setting this option overrides the destination plant static quality with that of the source plant. This only applies when using the XLP matrix generator. By default, this option is not selected.
Keywords: None
References: None |
Problem Statement: How do I adjust Scaffolding costs? | Solution: Scaffolding costs may be adjusted from the Contracts | Contractors form in the Project Basis View. Right-click on the desired contractor and select Edit. In the next form, you will see an option for Scaffolding. You may adjust the cost directly by entering a USD amount or by entering a % of DFL.
Keywords: Scaffolding, costs
References: None |
Problem Statement: Which P&ID related items may I locate in shared directories? | Solution: Note these settings may be made from Tools | Options | Preferences | Locations tab | Other Location Specifications
The following items may be set to shared folders:
PIDDir
PIDDrawingsDir
PIDIconsDIR
The following items may not be set to shared folders:
PIDBitMapDir
PIDDrawingsSysDir
Keywords: P&ID, shared, local
References: None |
Problem Statement: In the BJAC databank, there are 5 types of Fuel Oil:
Fuel Oil Number 1 (k=11.0)
Fuel Oil Number 2 (k=11.0)
Fuel Oil Number 3 (k=11.0)
Fuel Oil Number 6 (k=11.0)
Fuel Oil Number 6 (low range)
What is the difference between the Fuel Oil Number 6 (k=11.0) and Fuel Oil Number 6 (low range)? | Solution: Fuel oil number 6 (k=11.0) has a temperature range of 150-900 F, whereas Fuel oil number 6 (low range) has a temperature range of 80-200 F (299.8 -366.4 K). Low range refers to the temperature range over which the properties are curve-fitted.
k=11.0 is the crude oil characterization factor. The K Factor (also known as UOP K Factor or Watson K factor) is a measure of parafinicity of the crude oil. A characterization factor of 11.0 indicates a hydrocarbon compound predominantly naphthenic in nature.
The temperature ranges can be found under Customize Tab | Chemicals Database and selecting Databank BJAC.
Keywords: BJAC databank, fuel oil, low range
References: None |
Problem Statement: Can I save the customized Recap of Design and apply that list for subsequent runs in Aspen Exchanger Design & Rating (EDR)? | Solution: The Recap of Design screen summarizes the basic geometry and performance of all designs reviewed up to that point. The side-by-side comparison allows you to determine the effects of various design changes and to select the best exchanger for the application. You can customize what information is shown in the Recap by clicking Customize.
This customized list can be saved and applied for subsequent runs by following the steps given below:
1. Select the variables to create the custom list and then enter a name into the Recap list name input and then click the Save List button.
2.For subsequent runs, you can select your customized list from the Available recap lists drop-down box.
Keywords: Recap of Design, EDR, Shell & Tube, Air Cooler, Plate Fin, Fired Heater, Plate
References: None |
Problem Statement: How to use KEEPLOCL setting to preserve local model constraints in global model matrix? | Solution: In MPIMS and XPIMS models, select KEEPLOCL option to preserve any local model structure that intersects with local model purchase and sales vectors in the local table ROWS, RATIO, or MIP. The purpose of this feature is to keep any linear-programming structure, with some exception, that you have added to local PURC and SELL vectors in table ROWS. The system still strips from the local model PURC and SELL columns any entries pertaining to group limits. All column entries are retained except entries in OBJFN, MINOBJ, VBAL, WBAL, ABUY, and ASELL.
You may need to consider turn on KEEPLCL if you have PURC/SELL vectors or related structures entered in table ROWS, RATIO or MIP in local models and would like to keep these constraints in the global model matrix.
Keywords: None
References: None |
Problem Statement: This knowledge base article describes how to solve the Report Writer error:
The macro `AspenRpt.xla!ATMenuRunReport' cannot be found. | Solution: 1. Press ALT + F11 to open the VBA editor and compile, click OK on the compile error dialog
2. This will automatically invoke the reference window, Uncheck Missing: AspenRpt
3. Now go to Tools |
Keywords: ARW error
Macro AspenRpt.xla cannot be found
Aspen Report Writer error
References: s
4. Click Reference and select C:\Program Files\AspenTech\Aspen Report Writer\AspenRpt.dll
5. Click OK to close the Reference window
6. Override AspenRpt.xla (Ctrl+S) |
Problem Statement: Can I include effects of radiative heat transfer for a pipe in Aspen Flare System Analyzer? | Solution: Yes, users can include effects of radiative heat transfer for a pipe in Aspen Flare System Analyzer (AFSA) by enabiling the Enable External Radiative HTC option on the Calculation Settings|General Tab.
Also, users require to select ‘Yes’ for External Radiative HTC option on the Heat Transfer Parameters Tab of the Pipe operation to include the effects of radiative heat transfer in addition to the effect of convective heat transfer. Enter the material fractional emissivity to be used for the calculation of the external radiative heat transfer coefficient on Emissivity field.
External HTC is from the ESDU 69004 standard. See the ESDU web site link for more details.
Keywords: External Radiative HTC, Emissivity
References: None |
Problem Statement: What is the liquid maximum velocity exponent and multiplier? These options are found in the Line Sizing Model section of the Project Basis View | General Piping Specs: | Solution: These parameters are used to calculate the maximum allowable velocity. The liquid maximum velocity multiplier, A, defaults to 100 ft/s. The liquid maximum velocity exponent, B, defaults to 0.5 They are used in the equation shown below with liquid density to calculate Vmax. This equation, as well as the ones for vapor and steam, may be found in Chapter 18 of the Icarus
Keywords: Pipe, multiplier, exponent, velocity, max, allowable, liquid, density
References: Document (Help | Documentation). |
Problem Statement: When opening a v10 case file and in v11 and trying to upgrade the CAP library case file GML_V11-0.CASX, you might get the below error message: | Solution: This error message is caused because sometimes the RLIBMGR could be corrupted in the upgrade process. To resolve this, follow the below workaround:
From the command line, run:
COPY RLIBMGR C:\Program Files\AspenTech\Aspen Caps\Shared Libraries\GML_V11-0.CASX
COLLECT
LINK
Then proceed with the upgrade.
Keywords: None
References: None |
Problem Statement: How does combine layers work in LNG Exchanger during dynamic modelling? | Solution: With the Combine layers check box selected, individual layers (holdups) carrying the same stream in a single zone is calculated using a single holdup.
Each layer type is included in several sets, usually only the same layer type carrying the same stream in a single zone, so this option is used to make each same layer type using single holdup.
Combined Layers:
Not Combined Layers:
The Combine Layers option increases the speed of the dynamic solver, and usually yields results that are similar to a case not using the option.
Keywords: LNG Exchanger, Combined Layer, Set
References: None |
Problem Statement: VBA automation can access all setting inputs for an Adjust UnitOp. However, how can a spreadsheet cell be connected to the Target value? | Solution: The easiest connection would be to connect the Spreadsheet cell to Adjust’s User Supplied Target Value cell (instead of making use of the SpreadSheetCell Object option). The code below shows a sample code based on the Sweet Gas Refrigeration Plant.hsc sample file. The Adjuster’s Target Value cell is linked to the ‘Heating Value’ Spreadsheet’s cell A9.
Dim hyapp As HYSYS.Application
Dim hycase As SimulationCase
Public Sub SpreadsheetTest()
Set hyapp = CreateObject(HYSYS.Application, )
hyapp.Visible = True
Set hycase = hyApp.ActiveDocument
'access the RealVariable from somewhere in the flowsheet
Dim adjust As AdjustOp
Dim targetVar As RealVariable
Set adjust = hycase.Flowsheet.Operations.Item(ADJ-1)
Set targetVar = adjust.TargetValue
'access the spreadsheet
Dim spreadsheet As SpreadsheetOp
Set spreadsheet = hycase.Flowsheet.Operations.Item(Heating Value)
'access the target cell (x, y are 0-indexed, not 1-indexed)
Dim cellA9 As SpreadsheetCell
Set cellA9 = spreadsheet.Cell(0, 8) 'A9
'if you want to add it as an import set it as the ImportedVariable
cellA9.ImportedVariable = targetVar
'if you want to add it as an export, set it as the ExportedVariable
'cellA9.ExportedVariable = targetVar
End Sub
Key words:
HYSYS, Automation, VBA, Adjust
Keywords: None
References: None |
Problem Statement: What are internal model structures for CRDMIX table? | Solution: CRDMIX table in PIMS is used to specify that receipts contained in table RECEIVE are actually a mix of crudes. This forces the system to build the appropriate structure to cause the affected crudes to travel to the common destinations in the ratio of the receipt.
For example, MIX crude is mixed by 20% ans and 80% nsf and crude tank T01 contains the MIX crude, which feeds logical crude unit 1.
In the internal submodel, ST01, additional rows/columns are added to feed MIX in crude tank T01. The composition of MIX crude in composition recursion rows are identical as those in CRDMIX Table.
Keywords: None
References: None |
Problem Statement: What are the differences between two warning messages in Aspen MBO during optimization? | Solution: During MBO optimization, you may receive following two messages when receiving an incompleteSolution, which provides slightly different indications about what is the issue and how to do next step troubleshooting.
1. Infeasible nonlinear problem
In this case, MBO algorithm has detected that there is not enough progress towards making the problem feasible for a number of iterations, despite all the convergence strategies implemented in the algorithm.
2. Maximum XSLP iteration exceed
The convergence criteria are not yet met, but the logic in the algorithm detects that there are still chances to reduce infeasibility and progress towards convergence. However, the maximum number of iterations is reached and MBO are forced to stop.
Keywords: None
References: None |
Problem Statement: What is the meaning for W918 and how to solve it in PIMS? | Solution: In PIMS model, W918 reflects the issue that material balance VBAL/WBALxxx code does not match volumn code yyy in submodel Szzz.
In submodel Szzz, column yyy has -999 placeholders in E, G, L or R rows and a 1.0 in a VBALxxx or WBALxxx material balance row. The material balance row stream code xxx does not match the feed column code yyy and stream yyy does not have properties PCALCed from stream xxx. In this case, the stream properties from yyy are used to replace the -999 placeholders, but they may not be the correct properties if they are not related to the material balance stream xxx.
You can ignore this warning if stream yyy has recursed properties that are identical to those of stream xxx when calculated from duplicate recursion structures in the same submodel that includes the recursion structure for stream xxx.
Even if both streams xxx and yyy have identical fixed properties, a modeling best practice is to change the submodel column from yyy to xxx to match the material balance row. However, if two columns are needed to represent fixed properties for the same feed stream, then the warning message will appear for the column having the stream code that does not match the material balance row and the warning can be ignored. In this case, consider an alternative model structure since it is not good practice to have multiple stream codes with identical fixed properties representing the same stream since errors will be introduced if any of the properties are not identical between the two streams.
If the column code yyy is a stream with properties PCALCed from the stream code xxx on the material balance row, but the entries in table PCALC are not 1.0s, the properties may still be wrong, but no warning message will be provided.
To solve this warning message, ensure that the column name and the material name on the VBAL/WBAL row are both as intended and spelled correctly. If they are as intended, consider restructuring your model according to normal best practices. You can also try PCALCing the feed pool’s qualities to the dummy column tags.
Keywords: None
References: None |
Problem Statement: How does Aspen Capital Cost Estimator determine pipe lengths for a pump? | Solution: ACCE uses the equations described below where:
HDFT = Feet of head
GPM = Gallons per minute
Note these lengths are for Installation Bulk Piping which may be modified from the Options menu in the Pump component.
The drains are a set length at 15' and are independent of the flow and head.
In this example, assume the pump produces 500 GPM at 75' head.
Keywords: Pump. pipe, length
References: None |
Problem Statement: How do I view and modify the index file? When I double-click it, nothing happens. | Solution: Before you can view and modify the index file, first you have to select one. To select an index file, go to the Project Basis View and right-click on Index. Choose select to display the available options. Once the selection has been made, you may now double-click Index and view/modify the percentages.
Keywords: Index, project, basis, view
References: None |
Problem Statement: Why are output XML and BMS files not updated after Aspen BCI mapping table changes? | Solution: The changes in the excel BCI mapping tables need to be saved in the excel file. Meantime, we may also need to Refresh Tables in order to make the changes loaded to Aspen BCI if you see the discrepancies between BCI mapping tables and output files.
Keywords: None
References: None |
Problem Statement: How can I create a Pressure-Entropy (P-S) curve for a pure component? | Solution: The Analysis tools in Aspen Plus/Aspen Properties can be used to evaluate different thermodynamic properties and their dependency on each other.
Even though there is not a one-click option to create a Pressure-Entropy curve, the same Analysis tools can be employed to create one.
This example attempts to do the following: Create a Pressure-Entropy envelope for a pure component using the PTENVELOPE analysis
Description
The model uses water and SRK as the Property Method
A Property Set was created to calculate Entropy (S) of the pure component:
The P-S envelope will be created with two analysis, one for the bubble point curve (VF=0) and one for the dew point curve (VF=1).
A first PTENVELOPE analysis is created for the bubble point curve (VF=0):
Flow and a vapor fraction are specified. The Property Set is added in the Tabulate tab:
Run the simulation. Then move to the Results:
Create a Custom plot to show entropy on the X-axis and pressure on the Y-axis:
Create a second PTENVELOPE analysis to represent the dew point curve (VF=1)
Flow and vapor fraction are specified. Add the Property Set to the Tabulate tab:
Run the simulation. Then move to the Results:
This time, instead of creating a Custom plot, click on “Add Curve” and select the VF=0 curve:
Select the same variables:
To marge the Y-axis into a single axis, click on Y axis map, then click on Single Y Axis:
- The final curve should look like this:
The example file is attached
Keywords: Entropy, pressure, curve, envelope, PTENVELOPE.
References: None |
Problem Statement: When using Parametric Analysis in Aspen PIMS, users can define different types of variables using TYPE column. This article explains and exemplifies all the available types. | Solution: Table PARAOBJ defines the variables to be analyzed and the changes for the evaluation. There are five types of variables that can be defined in table PARAOBJ for Parametric Analysis. The following table shows an example of all these types.
TYPE 1 – Default if TYPE is blank. Indicates the item to be varied will be the value in the intersection with the objective function row, normally a COST or PRICE.
In the example, PRICE of products URG and DSL is being varied, as well as the COST of crude ARL
TYPE 2 – Indicates the INITIAL, FINAL, DELTA and STEPS columns will be used to vary the MIN bound of the specified variable.
In the example, we are varying MIN amount of ARL as well as the MIN capacity of Cat Cracker.
TYPE 3 – Indicates the INITIAL, FINAL, DELTA and STEPS columns will be used to vary the MAX bound of the specified variable.
In the example, we are varying MAX capacity of Dist Hydrotreater and MAX amount sold of URG
TYPE 4 – Indicates that the INITIAL, FINAL, DELTA and STEPS columns will be used to FIX the value of the specified variable or to set the MIN and MAX bounds of the specified variable equal.
In the example, we are varying FIX of process limit, which is the Reformer Severity, as well as the FIX amount of purchased crude TJL.
TYPE 5 – Indicates that the INITIAL, FINAL, DELTA and STEPS columns will be used to vary the SPEC of the specified blend specification (MIN spec or MAX spec is determined by the row name.)
In the example, we are varying the minimum DON in URG, as well as the maximum SUL in URG.
Note: Columns DELTA and STEPS can be used to define the difference to vary for each case or the amount of cases to analyze respectively.
After completing table PARAOBJ, you will also need to provide table DISPLAY. This table defines the variables to plot against the input variables for allSolution Analysis Tools.
Keywords: PIMS AO, analysis tools
References: None |
Problem Statement: The following warning message may appear in the CimIO_MSG.log file on the Aspen Cim-IO server if it’s V11.0.1 or later and Aspen InfoPlus21 is V10.1 or less.
27-MAR-2020 13:04:41.198, Logged by CIMSERV_ST on node SERVCIM:
Warning, CIMIO client node [SERVIP21] v15.1.1.35 NOT compatible with CIMIO server aspenONE v11.0.1 or later. Contact AspenTech support for the latest CP/ECR supporting CIMIO aspenONE v11.0.1 | Solution: The warning message indicates that the Aspen Cim-IO client system will not provide Store & Forward traceability through fields in IoDeviceRecDef record. Due to the new store and forward queue the following fields are no longer updated with timestamps indicating store and forward activity. [IO_FWD_ASYNC_STATUS, IO_FWD_ASYNC_START, IO_FWD_ASYNC_END, IO_FWD_UNSOL_STATUS, IO_FWD_UNSOL_START, IO_FWD_UNSOL_END, IO_STR_ASYNC_START, IO_STR_ASYNC_END, IO_STR_UNSOL_START, IO_STR_UNSOL_END]
Keywords: Compatible
Not compatible
Store & forward
References: None |
Problem Statement: How relief valve unit operations works in steady state? | Solution: The example file shows how the Relief Valve works in Aspen HYSYS.
Here are some important points about relief valve in HYSYS
1. In addition to defining the feed stream 1, the outlet stream 2 , pressure should also be defined. If the outlet stream pressure is not defined 'Unknown Product Stream Pressure' warning is shown.
2. Relief valve automatically calculates the mass flow rate for feed stream 1 if the relief valve size is entered and outlet pressure is defined. Refer to the attached image file below.
Note that, relief valve generates an error message for consistency error, if sizing information is entered as well as the flow rate is defined for the feed stream 1
3. In the attached example, the set pressure for relief valve is 110 psia and full open pressure is 95 psia. In the Set Pressure field, specifies the pressure at which the Relief Valve begins to open and in the Full Open Pressure field, specifies the pressure at which the Relief Valve is fully open.
The feed stream1 pressure is set at 120 psia and outlet stream 2 pressure is set at 90 psia. The sizing information is also entered as shown above in the screenshot. The feed flow rate is not entered, it gets calculated automatically from the sizing and back pressure (outlet stream 2 pressure) information.
4. If you reduce the orifice size or increase the outlet stream 2 pressure towards feed stream 1 pressure, the feed stream 1 flow rate will go down.
5. Sometime the user has the information about the flow rate but no information about the outlet stream pressure, in that case an adjust block may be used as shown in the attached case file. The outlet stream 2 pressure may be adjusted to achieve a flow rate or orifice size may be adjusted to achieve a flow rate.
In the attached example an adjust block ADJ-Pressure is added to relief valve to reduce the flow from 8600 lb/hr to 1000 lb/hr. An adjust block ADJ-Sizing is added to show how it will be implemented.
6. Please note that relief valve will show in yellow border line when it is open and show in black if it is closed on the PFD.
Keywords: relief, relief valve, valve
References: None |
Problem Statement: What is the picketed weir option in the tray internals design section? | Solution: The picketed weir option adds pickets to the outlet weir of the tray. This lowers the effective weir length, which in turn increases the weir load (gpm/ft). Picketed weirs are helpful in situations of low liquid rates across tray decks by promoting even liquid distribution.
The amount of picketing may be adjusted on the Picketed/Swept-back Weirs form.
Keywords: Weir, tray, picket
References: None |
Problem Statement: How is PO period (Payout Period) calculated shown in Cash flow spreadsheet? | Solution: The payout period is calculated in the 'Cashflow' spreadsheet as:
(last negative NPV period number) - (last negative NPV value) / (PV of cashflows value at the first positive NPV period).
For example, if NPV becomes positive in period number 1, the payout period is calculated as:
PO = D1 - D116 / E109 (all cells refer to Cashflow spreadsheet), please see below screenshot:
PO = 1 - (-7723659.36 / 7782033.45) = 1.99
Note: The PO period calculation includes EPC and startup durations. The cash-flow analysis starts at period 1, so EPC and startup durations are considered from the beginning of period 1 and on.
Keywords: PO Period, Payout period
References: None |
Problem Statement: For the Aspen Hydraulic subflowsheet, I want to be able to add multiple pipe segments on the same unit operation, but it does not show me the Append segment option, as in the Aspen HYSYS main flowsheet pipe segment. How can I append the different segments in the same block using Aspen Hydraulics? | Solution: Within the Aspen Hydraulics subflowsheet, the append segments option is NOT available for the Aspen Hydraulics Pipe Segment. Instead, use Aspen Hydraulics Complex Pipe Segment, in this unit operation the append segments option is available under the Design | Data form.
Additional information: If you would like to append fittings, use the Aspen Hydraulics Pipe Segment, in this unit operation the append fittings option is available under the Design | Fittings forms.
Keywords: Pipe segments, Pipe fittings, Segment, Fitting, Add, Aspen Hydraulics.
References: None |
Problem Statement: In the PCWS > History > Inspect page, there's a CCF Snapshot to get historical CCF file. Please note that, the CCF snapshtos are generated base on current CCF file structure, include the calculations and variables. | Solution: The help change is in the PCWS Web Help Inspector Page topic.
Item 7. in the list of features discusses the CCF Snapshot. This information should include the following:
The CCF that is downloaded is always based on the latest available CCF to guarantee that the database record structure matches the current production configuration file. The values in the configuration file are updated with the current or historical database values (as requested in the Timestamp setting). There is no way to retrieve data into a previous version CCF because that would require keeping track of obsolete or outdated records for each controller in the database whenever a controller re-deploy occurs. That is not part of the function of the product.
Keyword:
DMCplus, CCF, Snapshot, Inspect
Keywords: None
References: None |
Problem Statement: Is it possible to use the Column Internal Analysis feature in Aspen HYSYS Dynamic Mode? | Solution: The Column Internal Analysis feature allows you to analyze different column internals configurations. Unfortunately, this analysis tool is not available in Aspen HYSYS Dynamic Mode. When users select the Internals tab in the Column Property view while in Dynamic mode, they will be presented with the following message, Sizing and rating of trays and packing is not available in dynamic mode.
In Dynamic mode, the pressure profile of the column is calculated using dynamic hydraulic calculations. In steady state (SS), by default it is user specified. However, in SS the column’s pressure profile can be calculated using the Column Internal Analysis feature. Use the Column Internals Example KB (link below) to learn how to update pressure drops in your column using results from the hydraulic calculations.
https://esupport.aspentech.com/S_Article?id=000057301
Keywords: Column Internal Analysis, Column, Pressure Profile
References: None |
Problem Statement: How to increase the diagnostics of a calculator block? | Solution: You can increase the Calculator defined variables Diagnostics message level to 8 in Control Panel or History file on the Block Options | Diagnostics sheet; this will print the value of all input and result variables in the Control Panel and History file.
Key Words
Calculator
Diagnostics
Control Panel
History file
Keywords: None
References: None |
Problem Statement: What is the limitation of “Estimated Mass Transfer Coefficient (MTC)? | Solution: If MTC values are not constant and other available methods fail, you can use “Estimation” method.
In this method, MTC values will be calculated as a function of supplied isotherm. Usually this approach does not provide most accurate value, rather this can be used as initial rough guide. You can fine tune the value by adjust it manually until the breakthrough curve matches the experimental measurements.
Key Words
Isotherm, Mass Transfer Coefficient, Estimation
Keywords: None
References: None |
Problem Statement: How do I set the condenser temperature in a Radfrac column? The option is greyed out. | Solution: The condenser type must be set to Partial-Vapor-Liquid on the RadFrac Specification | Configuration tab. This will unlock the condenser temperature input.
If your condenser is not a partial-vapor-liquid type and you still need to adjust the condenser temperature, then please see article How can I set the condenser temperature for a Radfrac column if I'm not using a Partial-Vapor-Liquid condenser type?.
Keywords: Radfrac, condenser, temperature
References: None |
Problem Statement: My column converges, but an outlet stream does not. How do I fix this? There is a warning which states the temperature of the stream can not be found at the specified conditions. | Solution: To resolve this issue, open the column and go to the Flowsheet tab. On this form, change the Transfer Basis for the problematic stream to T-P Flash. This should allow the stream to converge. The choice of T-P Flash means the temperature and pressure values will be transferred across the boundary from the column sub-flowsheet to the main flowsheet.
Keywords: transfer, basis, temperature, column, converge, flowsheet
References: None |
Problem Statement: The following message below appears every time that I try to open Aspen Plus, Aspen HYSYS or Economic Evaluation with the Statement
'Please wait while Windows configures Economic Evaluation Vx.x' | Solution: This configuration message appears every time you open Economic Evaluation, or Programs linked to it (Aspen Plus, Aspen HYSYS), due to a corrupt installation process when the AspenONE Engineering software package was installed the very first time. Hence, the following procedure has to be followed in order to correct this:
1) Go to Start | AspenTech | Uninstall AspenTech Software (V8 and below)
Go to Start | Aspen Configuration | Uninstall AspenTech Software (V9 and up)
2) Uninstall ‘Economic Evaluation – ver Vx.x’ (Select this product from the list, as the screenshot below shows):
3) Once this program is removed (uninstalled). Then go to location C:\ProgramData\AspenTech\
Locate folder: Economic Evaluation Vxx - then delete it
4) Proceed to re-install (Economic Evaluation) if you need it - if so once again using ‘Admin Rights’ (right-click on Setup file from AspenONE Engineering media provided).
5) Then, the first time that you open Aspen Plus, Aspen HYSYS, or Aspen Economic Evaluation after re-installation, do this using ‘Admin Rights’ as well for each product.
6) Now all programs (Aspen Plus, Aspen HYSYS, Economic Evaluation) will open without showing this message anymore.
Keywords: Economic Evaluation, Windows Configuration, Uninstall.
References: None |
Problem Statement: After setting the affinity in the Aspen infoPlus21 Manager in V10.1, the affinity settings are reset after 15 minutes. | Solution: If the Aspen InfoPlus21 system was upgraded from a prior version the affinity settings were configured using batch file and query that executes on a schedule. For reference, here is a link to the legacy process for setting affinity. https://esupport.aspentech.com/S_Article?id=000076419
Remove affinity.bat, TSK_Affinity, and any QueryDef, CompQueryDef record that executes the affinity.bat file .
Keywords: CPU
References: None |
Problem Statement: How many vessels and what type of orientations can be modeled for a Fire Emergency Scenario in Aspen HYSYS/Plus Safety Analysis? | Solution: In Aspen HYSYS/Plus Safety Analysis, users can select up to 3 vessels in the Number of Vessels field and can select Horizontal, Spherical, or Vertical (incl. bottom head & no bottom head) as the orientation of the vessel under fire. The default value is Horizontal.
The Head Type can be selected as well based on the orientation selected. If a horizontal or vertical vessel is selected, 2:1 Ellipsoidal, Hemispherical, or Flat options are available. The default value is 2:1 Ellipsoidal. If a spherical vessel is selected, no head type is available to select.
For more information on the equations and example benchmark calculations for emergency scenario required relief loads, please use this link.
Also, the F1 Help Menu session Equipment Calculations: Partial Surface Area and Partial Volume describes the equations for the partial surface area and partial volume calculations implemented in the Safety Analysis environment.
Keywords: PSV Sizing, Fire Emergency Scenario, Safety Analysis, Vessel Orientation, Head Type
References: None |
Problem Statement: What can I check if my PID controller is not taking action to control downstream pressure? | Solution: Below are a few ideas for settings to check. Please also feel free to contact AspenTech Support for further assistance.
Ensure the proper action, direct or reverse, is selected.
Check the Tuning Parameters. Some values may cause the valve to respond too slowly with respect to process conditions.
Ensure the Mode is set to Auto.
Ensure a proper SP and PV range is provided.
Ensure the overall flowsheet has an appropriate pressure gradient. HYSYS Dynamics, unlike Steady State, requires DP to establish flow. You may have to open some valves manually (change % open from 0 to an arbitrary starting value).
Keywords: Dynamics, pressure, flow, controller, tuning, valve
References: None |
Problem Statement: How do I check the temperature profile of a pipe segment? | Solution: After the pipe has converged, go to the Performance tab and click the View Profile button. This will length profile data for the pipe segment, including temperature.
Special note: the number of segments shown in the profile may be modified on the segment itself (Rating tab | Design | Increments).
Keywords: Pipe, profile, temperature
References: None |
Problem Statement: In a Shortcut Dryer Type, there is no way to add the Exit Stream Moisture Content. | Solution: This issue can happen, if the component to be considered as moisture under Simulations | Setup | Solids | Solid Characterisation is not specified.
To specify Water as the Moisture component, select it and move it to the right for the appropriate substream:
Once user specifies this moisture component, it will be possible to specify the required moisture content in the Dryer input as below:
Keywords: None
References: None |
Problem Statement: Is it possible to set a volumetric flow specification for a stream in Aspen HYSYS Dynamics? | Solution: Yes, this can be set via the Material Stream Dynamics tab | Specs form. You may make the selection in the Flow Specification section.
Keywords: Volumetric, flow, dynamics
References: None |
Problem Statement: Can I perform Flow Assurance in Aspen HYSYS Pipe Segment? What are the Piping Flow Assurance studies I can perform? | Solution: Yes, Aspen HYSYS Pipe Segment allows users to perform Flow Assurance studies to check the physical structures of a pipe against the predicted wear caused by the type of fluid it is carrying to estimate the functional viability of the pipeline over time.
Users can predict the formation of hydrates, the rate of corrosion, and the physical erosion along the length of pipeline is extremely important during pipeline design and maintenance.
Following are the available flow assurance options
CO2 Corrosion: Predicts pipe wall corrosion rate caused by the presence of CO2 in a hydrocarbon pipeline.
Erosional Velocity: Calculates the erosional velocity: the continuous impact of particles (liquids or solids) on the pipe wall surface.
Hydrate Formation: Performs hydrates formation calculations in the pipe segment that can reveal locations along the pipeline where these restrictions can occur.
Slug Analysis: Predicts slug properties for horizontal and inclined two-phase flows in each pipe segment.
Wax Deposition: Calculates the Wax Deposition rate on a pipe segment.
Keywords: Pipe Segment, Flow Assurance, CO2 Corrosion, Erosional Velocity, Hydrate Formation, Slug Analysis, Wax Deposition
References: None |
Problem Statement: Aspen Simulation Workbook (ASW) built-in functions to fetch various attributes of a loaded simulation case | Solution: There are few built-in ASW formulas or functions to fetch various attributes of the simulation case.
ASW Active Simulation:
“ASWActiveSimulation” returns the name of the active simulation
ASW Get Table / Model variable Attribute:
“ASWGetTableVariableAttribute” returns the given attribute of the variable reference by the specified Excel range;
“ASWGetModelVariableAttribute” returns the given attribute of the referenced model variable
Note: Name or Variable ID should be from the Organizer window
ASW Simulation Attribute:
“ASWSimulationAttribute” returns the given attribute of the named simulation
Example : Connected, Disconnected, Results Available, Results available with warnings, etc.,
ASW Simulation Last Solve Time:
“ASWSimulationLastSolveTime” returns the time of the last solve of the named simulation
Note: Cell should be formatted with Date/Time format
ASW Simulation Path:
“ASWSimulationPath” returns the full path name of the given simulation
Keywords: ASWActiveSimulation, ASWGetTableVariableAttribute, ASWGetModelVariableAttribute, ASWSimulationAttribute, ASWSimulationLastSolveTime, ASWSimulationPath, ASW, Excel, ASW Functions
References: None |
Problem Statement: Why cannot a user select the files to be compared on the File Comparison screen of the Aspen Version Comparison Assistant (AVCA)? | Solution: On the File Comparison screen, users can select the files that they want to compare, as well as view file information and previous comparison information.
However, when the file names are different users cannot select the files to be compared. Ensure that the files to compared have the same file names in the two versions.
Keywords: AVCA, File Comparison
References: None |
Problem Statement: Even though Heat Capacity is listed as a property that can be modified by making use of Tabular properties, its calculation inside the Simulation environment depends on the Enthalpy calculations. | Solution: Since Heat Capacity is a reflection of Enthalpy, the Enthalpy field can be modified inside the properties environment to get the desired information. For this, the user can
- Go into Fluid Packages > Tabular > Options and activate the ‘Use HYSYS’ tick box for both Enthalpy(L) and Enthalpy(V)
- On the Information dropdown, select the phase of interest and the desired component to be modified. Press the Cmp.Prop.Detail button to access the data used to correlate Enthalpy
- Add the required data on the Table tab and ensure that the regression equation is suitable (note: in order to generate Enthalpy figures, the user can make use of the dH = cp * dT formula)
- Press the Regress button to proceed updating the data
Upon going back to the Simulation environment, the simulation should now reflect the new Heat capacity figures
Note: In order to make use of either phase Enthalpy Tabular option the user will need to mark both phases as available for modification.
Key words
HYSYS, Tabular Properties, Heat Capacity
Keywords: None
References: None |
Problem Statement: Aspen BCI and BMS system mapping is important configuration to make the output files generating correct format and information for Honeywell automated in-line blend control system. | Solution: The table below lists the mapping between BCI table and BMS system. Column Names are the columns in BCI tables which are used as labels assigned to corresponding information in BMC system.
Keywords: None
References: None |
Problem Statement: For the hydrocracker feed characterization, I have a question about the fingerprint bias factors. Specifically for the light, medium and heavy component ratios - what are the basis for the cuts? Are there temperature cut-offs for each one? | Solution: There aren't any hard-coded limits to the biases, but it is possible you could make them so large that they could cause an issue. For the cut point biases, the default cut points are 400F, 650F, and 1000F. So anything boiling less than 400F is light lump, anything between 400F and 650F is medium, 650+ is heavy with 1000+ corresponding to vacuum resid. The biases are subtracted from the base cuts. So if you had a 10F bias for the light cut point, it would treat anything boiling below 390F as light and the 390-400F material would be considered as medium. Typically, the biases are in a range of 0 to 50F, so there is no issue. If you put a 250F bias on the heavy cut point, that would effectively mean that there is no medium material as 400F would then be the cut between medium and heavy (unless you also had the bias on the light cut - from the previous example, if that were still 10F, then the 390-400F would still be considered medium, but that would be the only medium material if the heavy cut point bias was 250F).
In regards to the WABP biases - it would be prudent so that when the bias is applied the WABP still falls within the boiling range. For instance, if your light and heavy biases were both 0, then the medium WABP should be between 400F and 650F. If your medium WABP by default is 530, you wouldn't want to have a medium WABP bias of more than 130F or less than -120F because that would mean the weight average boiling point of a fraction would be outside of its boiling range.
For the C-sub-A bias, the main thing is that you don't want the C-sub-A to be less than zero or more than 100 (probably a more realistic upper bound would be 50-60% for an FCC cycle oil, and probably considerably less for a VGO or other types of oils).
Keywords: hydrocracker, feed, basis, cuts, heavy, medium, light
References: None |
Problem Statement: Can I plot more than one variable after running a case study? | Solution: The Case Study plotting options depend on which Case Study Type is selected under the Case Study Setup tab. When Case Study Type is selected as ‘Sensitivity’ analysis, plot options allow up to two dependent variables and the option to select all the independent variables on the same plot.
When Case Study Type is selected as ‘Nested’ or ‘Discrete’ analysis, it is possible to ‘Plot All’ results across each Step by selecting ‘Plot All.’ However, plot options allow only two dependent variables at a time.
All plotting options are visible in the Plots tab of a Case Study after running the case study. Under the Results tab of a Case Study, there is a button provided to ‘Send to Excel’ which will export all the resulting data from the case study to a Microsoft Excel table.
For more information on running a Case Study in HYSYS, visit the following KB articles:
How to run a Case Study? How to Create a Case Study?
What is the difference between Sensitivity and Nested Case Study Types?
Keywords: Case Study, plot variables, Display Properties
References: None |
Problem Statement: How do Halt Conditions work in BLOWDOWN? | Solution: In BLOWDOWN, two different Halt Conditions can be set-up in the Run Controls tab, the Time and the Pressure. This can be seen simply as 'IF/THEN' logical statements running in parallel. For example:
'IF the BLOWDOWN analysis time is greater than the <900 seconds>, THEN pause the BLOWDOWN analysis run’
-or-
‘IF the pressure of the vessel is greater than the <10 psig>, THEN pause the BLOWDOWN analysis run'
That is the reason why BLOWDOWN completes calculations whenever either of the specified halt conditions is met. The model will not necessarily meet both halt conditions.
Keywords: BLOWDOWN, Halt Conditions, Halt Time, Halt Pressure, Run Controls, Depressurization, Stop, Stopped
References: None |
Problem Statement: Why is the Model Pressure drop option disabled for pipes (Blowdown and vapor/liquid outlet lines) when using Single Vessel Blowdown template? | Solution: The Model Pressure Drop check box is selected when users want to model the pressure drop across the pipe. If this check box is cleared, then the pipe is modeled as a vessel. In the single vessel template, the pipes before the orifice are modeled as open-ended vessels. Blowdown does not model pressure drop for vessels and obtains the mass flow rate in the system using the procedure in the following reference: Haque, M. A., S. M. Richardson, and G. Saville. Blowdown of pressure vessels. I. Computer model. Process Saf. Environ. Protect 70.B1 (1992): 3-9. Thus, this option is disabled.
If users would like to model the pressure drop in the Blowdown lines, there is a variation of the single vessel template (Single Vessel: Pressure drop considered upstream and downstream of the blowdown orifice) which is available through this KB.
https://esupport.aspentech.com/S_Article?id=000066751
Keywords: Model Pressure Drop, Single Vessel Blowdown
References: None |
Problem Statement: How can we report Bulk Modulus? | Solution: Bulk Modulus is not a property that is directly reported in Aspen HYSYS. However, it can be calculated either in the Aspen HYSYS Spreadsheet for any given stream or by using a User Variable with the calculations you want, which will then be available for all streams.
The attached zip file contains a HYSYS case with the user variable. Furthermore the word document shows an explanation of the equation from page 5 of Fluid Mechanics with Engineering Applications by Daugherty, Franzini and Finnemore, 8th Edition, the equation for Bulk Modulus (Ev) that can be re-arranged to:
Ev = -v1 * (P2 - P1)/(v2 - v1).
Where v is the specific volume (1/Density) and P is the pressure. The important thing to remember here is that since we are trying to get the derivative (or the slope), you will need to keep the delta P small.
In this User-Variable routine, it takes the stream current operating conditions as the initial pressure and density to feed in the above equation. The differential is calculated between this conditions and the next 100 kPa increment conditions (add 100 kPa to the current pressure and evaluate density at the new increment). You can open the code inside HYSYS and modify the increment amount if necessary.
Before a user variable can be used, it must first be imported into the case, this is done as follows:
1. Go to Customize | Import and Export User Variables.
2. Press the Select File button and navigate to the .huv file on your computer (You may need to change the file filter, if it is currently set to .hvv).
3. Select it and press Save.
4. The user variables in the selected file should now appear in the right-hand list box, select the user variables required, the Import button should become activated.
5. Press the Import button - the selected user variables should now appear in the list boxes on the left-hand side. These show their names and the type of object they apply to.
6. Press OK.
Now go to the user variables page of an object that the user variable applies to...
Stream = User Variables Tab
Operations = Design Tab ... User Variables page
Flowsheet = Flowsheet Menu ... Flowsheet user variables option Simulation Case = Simulation Menu ... Simulation user variables option
The user variable may already appear in the list - if it doesn't, press the green tick button, it should now appear.
To enable the user variable check the checkbox next to its name. To see the code for the user variable, double click on its value, or press the cross and pencil button.
Keywords: Bulk Modulus, user variable, .huv
References: None |
Problem Statement: Is there a way to add more intervals to the Heat Exchanger Performance table? | Solution: When an exchanger is using Simple End Point heat exchanger method. (This can be viewed on Design|Parameters page). The exchanger Performance Tabular Results will only show the inlet and outlet points (end points) results.
When an exchanger is using using Simple Weighted heat exchanger method which has default intervals defined as 5 on the Parameters page. he exchanger Performance Tabular Results will display results for the defined intervals. User can change the intervals if needed on Design|Parameters page.
Keywords: Heat Exchanger, Performance Tabular Results, Simple End Point, Simple Weighted
References: None |
Problem Statement: This article explains how to generate an XML output file when recipes are submitted through Blend Controller Interface (BCI). XML generation is only applicable for Honeywell BPC-MBO recipes. | Solution: Prior to generating an XML file, enter the XML file name using the RREP Input field found under the Program Options dialog box.
The XML output format does not support custom data sections (e.g., custom Booleans, custom reals, or custom text). A warning will be generated when the recipe is submitted. To output custom data to an XML file, you will need to use the SpareValues table.The BlendOrderID type needs to correspond to the value selected from the Model Settings dialog box and then you will need to enter the desired information into the SpareValues table. Additional procedural information can be found below.
To generate an XML file:
Open the Model Settings dialog box.
Select Honeywell BPC – BMO Recipes as the Control File Format.
Select Generate XML File.
If you have custom data values (e.g., custom Booleans, custom Real or custom text) to export, you will need to use the SpareValues table to include these values to the XML file.
Select which value to use as the Blend Order ID from the SpareValues BlendOrder ID dropdown list. A summary of what needs to be added to BlendOrderID field follows:
Selected value What needs to be entered in the BlendOrderID field in the SpareValues table
[AB_BLN_EVENTS].[SEQ]
Default Enter the event sequence number to indicate to which blend order the spare values belong.
BCI Product Enter the BCI product code; indicates the spare values belong to the blend order which has the same BCI product code.
MBO Product Enter the MBO product code; indicates the spare values belong to the blend order which has the same MBO product code.
Enter the location for the XML file. You can also click … to select the desired location.
Select or enter any other setting options.
Click OK to close the Model Settings dialog box.
Right-click on a desired recipe and click Select Recipe. Repeat this for each recipe you wish to submit.
Click Run | Submit Recipe(s) from the main menu to submit the recipe and generate the file. The status window displays success or additional information regarding any errors.
You can find XML file in specified location.
Keywords: MBO, BCI, recipes
References: None |
Problem Statement: What is the Aspen Process Economic Analyzer Options question when I open ACCE? | Solution: This option allows Aspen Process Economic Analyzer (APEA) to be run inside of ACCE. APEA allows the user to connect to Aspen Plus or HYSYS to import the equipment from the simulation file. If you are not planning on doing so, then feel free to leave this feature turned off.
Keywords: Aspen Process Economic Analyzer
References: None |
Problem Statement: What are Boundary Nodes? When are they added to the Aspen Hydraulics subflowsheet? | Solution: When building the flow network in Aspen Hydraulics, HYSYS automatically adds Boundary Nodes to all the inlet and outlet streams in Steady State mode.
The Aspen Hydraulics Boundary Node controls whether a boundary is considered a pressure, flow, pressure and flow, or <none> specification. This boundary type specification is a system wide specification that can be edited on the Constraints tab of the Aspen Hydraulics Sub-Flowsheet.
You cannot manually add or delete Boundary Nodes. They are automatically added and removed as you change the topology of the flowsheet. You cannot break connections between internal streams and Boundary Nodes.
Key points about Boundary Nodes:
1. Boundary Nodes are never added before or after other unit operations (such as Valves, Swages, and Tees).
2. Boundary nodes are added when stream connections are made or broken, such that a stream is connected to a Pipe Segment at a boundary.
3. Boundary Nodes are not added to the flowsheet in Dynamics mode.
4. The Boundary Node icon on the flowsheet displays the type of system constraints applied:
P indicates that a pressure constraint is enforced.
F indicates that a flow constraint is enforced.
PF indicates that a pressure constraint and a flow constraint are enforced.
A blank icon indicates that no constraints are enforced.
Keywords: Aspen Hydraulics, Boundary Nodes, Constraints
References: None |
Problem Statement: How do I define a hypothetical component (hypocomponent) with Molecular Weight over 1000 on Aspen Flare System Analyzer? | Solution: Aspen Flare System Analyzer does not allow you to create a component with Molecular Weight greater than 1000. For more information on the maximum molecular weight allowed for a hypothetical component, please see the link below:
https://esupport.aspentech.com/S_Article?id=000091203
However, there is a workaround for defining components with larger molecular weights. These components may be defined as hypothetical components on HYSYS. Please see the link below how to add a hypothetical component on HYSYS:
https://esupport.aspentech.com/S_Article?id=000030160
Once this is done, please import the component in Aspen Flare System Analyzer. Please see the link below on how to import stream data from Aspen HYSYS into Aspen Flare System Analyzer:
https://esupport.aspentech.com/S_Article?id=000032095
Keywords: Hypothetical component, hypocomponent, molecular weight, 1000
References: None |
Problem Statement: How can I report properties for a nonconventional component? | Solution: To report non-conventional properties follow the steps below:
1. Change the Stream Class to a non-conventional type (e.g. MIXNC) over the Simulation environment in Setup | Stream Class.
2. Look for the non-conventional component property using the <add properties> button at the end of the results form (e.g. HCOMB).
Also, you can make use of a Property Set to achieve this. The advantage is that the non-conventional component property can be accessed through a Calculator block and/or in a Sensitivity analysis as a Stream-Prop. The steps to do this are listed below:
1. Change the Stream Class to a non-conventional type (e.g. MIXNC) over the Simulation environment in Setup | Stream Class.
2. Add a new Property Set and change the Substream type to NC to calculate the properties for nonconventional components.
3. Search for the non-conventional property set (e.g. HCOMB) and select it.
4. If necessary, setup the Qualifiers tab.
5. Run the simulation and consult the Stream Results summary to add the property to the report using the <add properties> button.
Note: By default the property is requested for all substreams though it gives a blank for other substreams where it does not apply.
Keywords: Non-conventional, property sets, heat of combustion.
References: None |
Problem Statement: How can I restore the Flowsheet or Model Palette on Aspen Plus if I am unable to see it? | Solution: Flowsheet
If you accidentally closed the Flowsheet, please go to View and select Flowsheet
Model Palette
If you accidentally closed the model palette in the Simulation Environment, please make sure it is visible under View | Model Palette
If you still cannot view it, it is likely because the model palette is floating – it is open in a separate tab. The model palette can be viewed by clicking on the Aspen Plus icon, and multiple tabs will open. One of them will be the Model Palette tab.
To restore it back to its original position, please right click on it to make sure it is ‘dockable’
Please dock it at the bottom of the screen
Keywords: Flowsheet, Model Palette, Missing, accidentally closed, dock,
References: None |
Problem Statement: Why is the “Column Design” tab not visible? | Solution: In V9, Column Hydraulic Analysis was introduced to replace Legacy Hydraulics (tray and pack sizing and rating) to evaluate the pressure profile in a Column.
When opening a file built in V9.0 or older version in V10 and latest versions, the following message will appear:
If “Use Legacy Hydraulics” is selected, the “Design Column” tab will not be available (won’t appear).
The file must be upgraded to use Column Hydraulics in order to access the Design Column tab.
If the message is not displayed, please follow the steps:
Open the file and go to File | Options | Upward Compatibility
Check the option “Show new sizing and rating upgrade dialog.
Click on Apply and OK
Close Aspen Plus file and save changes.
Open again the file. Now the message should appear.
Keywords: Column Design, Upgrade Column Hydraulics, Use Legacy Hydraulics, Column Internals
References: None |
Problem Statement: How many workspaces can be created in the Administration Tool using the feature of using local databases? | Solution: Since the introduction of local databases in ABE V8.8, you can create as many workspaces as you require using a database type of MS SQL LocalDB. Please note that this type of local database is only useful when you are creating small projects in ABE that only a single user can access. For bigger projects, you must use another type of database, such as: Oracle or SQL Server type (refer to KB 142043 for further details on how to create a workspace using an SQL Server).
In order to create a new workspace using this type of database, simply select the MS SQL LocalDB option from the Select a Database Type: drop-down list when creating a new workspace from the Administration tool, as the screenshots below show:
Now the new workspace has been created and can be used immediately:
Keywords: Local Database, Workspace, MS SQL LocalDB.
References: None |
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