question
stringlengths 19
6.88k
| answer
stringlengths 38
33.3k
|
|---|---|
Problem Statement: Can we model differential condensation in HEATX block in Aspen Plus? | Solution: Heat transfer calculation in case of differential condensation is not supported with Aspen Properties. So, when HEATX block is used in either short-cut or rigorous mode, it does not consider the effects of differential condensation as it uses Aspen Properties.
Only way to implement this would be to use BJAC properties in standalone EDR.
Key Words
Differential Condensation, Properties, BJAC
Keywords: None
References: None |
Problem Statement: When simulating plate exchanger, EDR has access to vendor plate exchanger models such as APV, Alfa Laval and Trantor. But the plate models in the list is outdated. For example, there will be APV C series exchangers out soon, but what is available in EDR are SR14 exchangers, which are two models old. Could I edit the vendor plate data in the plate databank of plate exchangers? | Solution: We add a new feature in V11 which allows the customer to edit vendor plate data and add/update any plate model into customized database.
1. Go to Plate/ Input/ Exchanger Geometry/ Plate Details, and click on “Plate Databank”
2. In the plate databank, select the manufacturer, plate, Chevron Angle, etc. Then click OK.
3. Now you could edit vendor plate data. Make sure you enter a new plate name or manufacturer name. Click Save. Now the user-specified plate data is saved to a customized database.
4. Now both Manufacturer data and the saved user data are available in the plate databank. Next time when you want to use this user-specified plate data again, just select the name you specified for that plate data in step 3 (for example, User), and you will retrieve the data.
5. You can also delete the saved user-specified plate data.
Key Words
Plate exchanger
Plate databank
User data
Keywords: None
References: None |
Problem Statement: What is the cause of non-stop integration issue when multiple bed is running in cycle? | Solution: Usually multi-bed operation is synchronized with Cycle Organizer. Under the “Control” option, user can assign either time driven or event driven option. The non-stop integrator issue happens mostly in the case when stop criteria is event driven. The root cause is that the stop criteria is never satisfied.
To diagnose the problem, it is useful to make a plot of variable of interest and monitor is dynamic run pattern. Also check if a time driven option can be used instead.
Key Words
Integrator, Cycle Organizer, Variable
Keywords: None
References: None |
Problem Statement: Which vaporizer type could be suitable for ‘Dry evaporator type screw chiller' | Solution: It can be modeled when vaporizer type is chosen as 'forced circulation'
A sample case is attached for a reference.
Keywords: None
References: None |
Problem Statement: How to create material pool for blend components in MBO? | Solution: To create material pool for blend components in MBO, please refer to the following two methods.
Method 1: Visualize the blend components pool trend.
1.Created a new material, e.g. COMPONENT.
2.Created material service events against the component tanks, e.g. THCL and TLCN, for the model horizon.
3.Created a PROD_SERVICE material pool PCOMP with basis ID “COMPONENT”.
4.Trend the PCOMP pool by volume.
5.Reload Simulator/Refresh Trends. And you can trend the components material pool in the chart of PCOMP.
Method 2: To schedule blending events for blend components pool, you may want to create virtual pool by using INIT worksheet in MBO
1. Add USE_MBO_INIT in CONFIG table.
2. Add a virtual pooling tank.
For example, TALKP represents the pool of two component tanks TALK and TALK1, which are used for component ALK.
3. For component ALK, change the tank to TALKP.
4. In Units>>INIT worksheet, add following structure to load TALKP inventory and property values at the beginning of the horizon.
Keywords: None
References: None |
Problem Statement: When I open Aspen Plus or Aspen HYSYS, the following error message shows up:
apedconnectionerror.log
Failed to initialize the Aspen Properties Enterprise Database.
Using the configuration file from C:\ProgramData\AspenTech\APED VX.X\casasecd\config.aem
Please use the Aspen Properties Database Configuration Tester to diagnose and fix the problem. | Solution: The error message indicates that our APEA built-in databases are not correctly configured in your machine. In order to fix this, please do the following:
1. Go to the shared folder: C:\ProgramData\AspenTech\APED VX.X (replace X.X with your Aspen Properties version)
2. Run DeleteDBInstance.bat. as administrator (right click and select as admin). This batch file will drop any database from restoring that is incomplete. It also deletes the instance of LocalDB you own and the folder named by your Windows logon.
3. Open the Start Menu, Open the Database Tester with a right click and select Run as administrator from All Programs | AspenTech | Aspen Properties or and click on Restore databases directly. Check that there are no errors.
Note: The database is created for each user, so each user that wants to use localDB for the APED, needs to have admin rights.
Now Aspen Plus and Aspen HYSYS should open normally without the error message.
Keywords: APED, initialization, APED connection error
References: None |
Problem Statement: How to model internal dividing redistribution in Aspen Plate Fin exchanger? | Solution: In some cases, a stream is only present for a fraction of the length of a set of layers and then exits the core, which leaves that set of layers empty. To avoid having empty layers in a fraction of the exchanger, a second stream can be diverted from another set of layers to occupy the empty region. This second stream must then pass through a redistributor in the second set of layers (Layer Type) to divert part of its flow, and the first set of layers must have an inlet intermediate distributor to take this inflow into the otherwise empty layers.
In summary, the stream is initially in a single set of layers and ends up in two sets. This is what we call “dividing redistribution”.
The attached example tries to simulate an internal dividing redistribution like the one shown below:
Where Stream 2 (Hot), leaves the exchanger at some point, so Stream 1 (also Hot) is divided to occupy the empty layers.
Keywords: Redistribution, distributor, plate fin, EDR
References: None |
Problem Statement: Why do i see a difference between the closing inventory between APS and MBO for the Component Rundown tanks? | Solution: This can happen because the COMP_RD table was not synced with APS and did not have the latest published values. This can be resolved by refreshing the data in the COMP_RD table with the latest published values from APS.
To sync the data in COMP_RD table with APS, you can follow the below steps:
(1)Clear all the data in _ZSTRMS & COMP_RD tables
(2)Open the model in APS and ReloadSim/SimulateAll/Publish All <== Note down Tank Material Balance for the component rundown tank.
(3)Close APS, open the model in MBO and select the Event screen
(4)Click on 'Model->Component RunDowns...' and then click on 'Copy from APS'
(5)Go to Tank Material Balance and select the component rundown tank
(6) You can see that tank material balance is same in both APS and MBO
Keywords: None
References: None |
Problem Statement: How to specify penetrations and distances for nozzle projections in Shell and Tube Mechanical? | Solution: When specifying the nozzle location, there may also be intent on specifying a penetration distance for the nozzle. Let’s take this scheme as example:
Nozzle in this case has 12” out of the tank and 15” as penetration. To achieve this first we review the nozzle being specified under Nozzles-General:
Once nozzles are reviewed, location can be further specified on Input | Exchanger Geometry | Nozzles-Details-Ext.Loads | Penetr/Proj/Distances Tab, where Penetrations and Projections are stated on their respective columns for the corresponding nozzle:
With this, the Code Calculations will report the specified Nozzle Projection:
The Setting Plan also displays both Projections numbers in one single value. Even if the Setting Plan and Drawings themselves do not show the 15 projection, it is used on the calculations:
Keywords: nozzle, projection, location, Penetr/Proj/Distances, Distance Nozzle CL, EDR
References: None |
Problem Statement: How to retrieve diffusion coefficient of species in liquid mixture along the length of Plug Flow Reactor ( PFR)? | Solution: For this purpose, property set DMX can be utilized. DMX reports diffusion coefficient of a component in liquid mixture.
First please create a property set with DMX and in “Qualifier” tab select phase as “Liquid”.
Then from PFR > Report > Properties, select the property set (DMX).
Now once the flowsheet is solved, we should be able to see the component diffusion in
Profile Result > Properties form.
Key Words
Diffusion, Component, Plug Flow Reactor
Keywords: None
References: None |
Problem Statement: I need to convert a PRO//II file to Aspen Plus file. How could I do it? | Solution: You could use the PROII to Aspen Plus convertor.
1. Open PROII to Aspen Plus convertor under C:\ProgramData\Microsoft\Windows\Start Menu\Programs\Aspen Plus.
2. In the toolbar, make sure Aspen Plus is selected from the list.
3. Click “open” button on the top left corner, navigate to the file you want to convert, and click Open. The original file appears in the left pane. Messages (including those about objects you might have to convert manually) appear in the right pane.
4. Push the green triangle to convert the file. When the process is completed, Conversion complete appears in the right pane, and the converter saves a backup file and opens it in Aspen Plus.
5. Examine the messages in the right pane and modify the converted file as needed to deal with unconverted or incompletely converted objects. You can use the Show output from filter above the pane to limit the messages shown to specific types.
6. Check in the converted file:Ensure all Pro/II components are correctly mapped to Aspen Plus components.
Ensure all Pro/II property packages are correctly mapped to Aspen Plus methods.
Ensure all Pro/II materials streams and unit operations were created in Aspen Plus.
7. See Troubleshooting Pro/II to Aspen Plus conversions if you encounter any issues.
Key Words
PROII
Aspen Plus
Convertor
Keywords: None
References: None |
Problem Statement: What is the difference in the Aspen Capital Cost Estimator (ACCE) M and N feature? | Solution: The M feature suppresses the bulks and essentially runs ACCE as Aspen In-Plant Cost Estimator. The N feature suppresses the bulks (volumetric model), but allows for other ACCE features such as multi-contractors.
See table below for more details on what each of these option includes and suppresses:
A = Allowed, S = Suppress, I = Ignored, NC = Not Created, SC = Some files created
Feature M M Notes N N Notes
Equipment volumetric model S Installation bulks such as volumetric piping, instrumentation, civil/steel are not estimated unless specified using the installation bulk addition forms. S Same as M.
Area level bulks S Area level bulks such as pipe system testing hours, misc. concrete, instrument freeze protection, area lighting and grounding, portables etc. are not estimated. S Same as M.
Engineering workforce input I All other engineering workforce input is ignored. A Allows engineering workforce input. (If you don't need this you can delete engineering using the contractor forms.)
Drawing types and drawing counts I All input regarding changes to drawing types or drawing counts in the engineering calculations is ignored. A Allows drawing count inputs.
Construction workforce input I Modifications to CWF#1 are allowed. All other CWF input is ignored. Modifications to crew mixes or craft names are not allowed for any CWF. A Allows multiple construction workforces to be specified. Allows craft rates to be specified. Allows crew mix and craft name adjustments.
Power distribution I Power distribution system inputs are ignored and substation/transmission line bulks are not estimated. I Same as M.
Panel board I Panel board input is ignored and panel boards are not estimated. I Same as M.
Process control I All process control input is ignored and process control line items (OPC,CTL) are not estimated. I Same as M.
Project execution schedule setting I All the settings to adjust project execution schedule are ignored and schedule is not created. A Allows project execution schedule.
Contractor input I All contractor input except the first contractor is ignored. Project level error is generated if multiple contractors are specified. A Allows multiple contractors.
Scope (Conset ) input I All scope/conset input is ignored and the case is treated as single contractor run. A Allows conset specifications.
Area level design specs I All area level design specs are ignored.(No adjustments to specs by area allowed.) A Allows area level design specs.
Unit rate estimation I If detailed unit rate estimation is selected, error message is generated and file is ignored. A Allows unit rate estimation.
CCP report NC The CCP report is not created. Instead the reporter is launched after evaluation is complete. A CCP report is generated.
External files SC The external indirects/pro-ratables file, instrumentation control systems file is ignored because external indirect costs and control system costs are not estimated. A All external files are allowed.
Keywords: M, N, feature, suppress bulks, bulks, suppresses, volumetric, delete, remove
References: None |
Problem Statement: How to calculate the enthalpy of water using Steam Tables reference state? | Solution: ASME Steam Tables use the triple point of water (0.01 C and 611.657 Pa) as the reference state for the enthalpy calculations, which is different from the reference state used by Aspen Plus (Ideal Gas @ 25 C and 1 atm).
An alternative to estimate an enthalpy of water in Aspen Plus equivalent or similar to the enthalpy reported in ASME Steam Tables, is to calculate the enthalpy of water at the triple point and subtract it from the enthalpy of the stream calculated by Aspen Plus.
The attached example attempts to estimate the enthalpy of saturated liquid and saturated vapor at a specific temperature (20 C) using the approach described above. The file includes the following:
- Two streams, one representing the saturated liquid and the other the saturated vapor.
- Property Set “MASSENTH” to retrieve the mass enthalpy of each stream at the desired units.
- Property Set “REFERENC” to calculate the enthalpy of water at the triple point (0.01 C and 611.657 Pa, specified under Qualifiers)
- A Calculator block to compute the new enthalpy using the different reference state.
Keywords:
References: state, ASME steam tables, enthalpy |
Problem Statement: How is objective function OBJFN calculated in PSCP? | Solution: In PSCP, the objective function is calculated by following equation:
Objective Function =
Sales Revenue (T. Demand)
+ Exchange Revenue (T. Exchange)
– Purchases (T. Supply)
– Exchange Costs (T. Exchange)
– Inventory Drawdown (T. Inventory)
– Operating Costs (T. Operation)
– Transportation Costs (T. Transport)
– Inventory Holding (T. Inventory)
– Inventory Penalties (T. Inventory)
– Feasibility Penalties (Model Infeasibility Breaker Settings)
– Miscellaneous Costs (Miscellaneous tables)
Keywords: None
References: None |
Problem Statement: How can I create T.Exchange in PSCP? | Solution: We can create T.exchange to represent exchange contracts in refinery/terminal transportation and trigger the model to deliver a material at one node, and receive material in exchange at a different node.
The material received may be the same as, or different from, that delivered. You may also define pricing differentials and delivery and receipt time windows as necessary. Use input table Exchange to incorporate product.
Keywords: None
References: None |
Problem Statement: What is the difference between any and span keywords in PSCP? | Solution: In PSCP, we can use predefined keywords “Any” and “Span” for nodes/periods in multiple tables.
Keyword any is used to specify the value valid for all unspecified nodes/periods. In other words, use keyword any to identify a default value that is used when a specific value is not otherwise specified.
Keyword span is to indicate that the limit spans all unspecified nodes/periods rather than applying to a specific nodes/periods.
Keywords: None
References: None |
Problem Statement: How do I create a PSV Excel Datasheet in Aspen HYSYS or Plus V11? | Solution: Starting in V11, Datasheets are transferred into Aspen Basic Engineering (ABE) which should be installed along with Aspen Plus and/or HYSYS. From the ABE environment, datasheets may be exported to Excel via the steps below:
Part I - Connect to the Workspace
1) After the PSV calculations have been finalized from the Safety Analysis environment in Aspen HYSYS/Plus, click the Datasheets button from the Home tab.
2) The ABE V11 Project Selection window will appear. If there isn't an existing Workspace, then select Create a New Workspace and provide a name for it.
Part II - Map the PSV
3) Once the Mapper form has loaded, ensure the desired PSV is selected and click the Transfer button.
Note: If using an existing workspace, ensure the PSV is being mapped to the appropriate Workspace Object before clicking Transfer.
4) A notification confirming a successful transfer of data should appear. Click OK to dismiss the popup.
Part III - Add a New Datasheet
5) Click the Explorer button in the ribbon bar.
6) After the Explorer finishes loading, click the Add New Datasheet button in the top-right corner.
7) In ABE, AspenTech has provided several pre-built datasheet templates. In this example, we will use the AZ Safety Pressure Valve template. Select it and then click Next.
8) Choose the PSV Object and then click Create.
9) The new datasheet will now be created. You may click the Open button to view it.
10) Once the desired datasheet has loaded, click the three dots in the top-right corner to find the Export to Excel option.
11) The datasheet will be exported to Excel and saved to the local Windows Downloads folder.
Keywords: Safety, datasheets, PSV, Aspen Basic Engineering, ABE, Explorer, Mapper, Excel, HYSYS, Plus, V11
References: None |
Problem Statement: Some workflows shared diagrams which may need different notes depending on the case. So, how can one set up notes label for a PFD only? | Solution: In the Drawing Editor there is an option to create note labels on a single PFD under Label | Create on this diagram only. This note label will be only visible on this PFD.
Keywords: Notes Label, Create on this diagram only, PFD.
References: None |
Problem Statement: How can I access parameters, such as AIT and FLASHPT, from the pure component databanks? These parameters are listed as present in the Pure Component Databanks, but not visible from Aspen Properties/Plus. | Solution: There are some parameters available in the Aspen Properties Databanks that are not used by any property method. These parameters can be accessed through the Database Manager – Aspen Properties.
They can also be accessed in the user interface by typing the name of the parameters on the Customize | User Parameters form (in the Properties environment) as shown in Knowledge Document 86043.
AIT: Auto ignition temperature
ANILPT: Aniline point
DHLSF: Heat of fusion at the normal freezing point
ENT: Absolute entropy of formation at 298.15 K
FLML: Lower flammability limit
FLMU: Upper flammability limit
FLASHPT: Flash Point
MOC-NO: Motor octane number
RI: Refractive index at 298.15 K
ROC-NO: Research octane number
SVRDIP: Second virial coefficient
TPP: Triple point pressure
To view the parameters in the Aspen Properties Database Manager:
From your Start Menu, open the Database Manager – Aspen Properties Vxx
Select the Database APVxxx
Go to “Selected Compounds”, click on “Find compounds” and add the desired compounds
Go to “Properties and Parameters” and select “Pure”
Select the Compound, Databank and Properties to be displayed
Keywords: AIT, FLASHPT, FLML, FLMU, Database Manager, Databanks, Pure Parameters.
References: None |
Problem Statement: How can I create capacity constraints in PSCP? | Solution: To create capacity constraints in PSCP, there are two types of tables we need to use:
Defines Limits – CapacityRows
Defines Capacity Constraint:
CapInventory - defines inventory capacities
CapSupply - defines capacities applied to supply columns
CapDemand - defines capacities applied to demand columns
CapSegment - defines capacities applied to segment columns
CapTransport - defines capacities applied to transport columns
CapOperation - defines coefficient entries in the capacities rows for operation vectors
CapCollector - specifies how to add entries to the collector columns of other non-collector capacity rows
Keywords: None
References: None |
Problem Statement: How do I turn off all installation bulks in my ACCE project? | Solution: You can choose to deactivate the volumetric model in an ACCE project in the Project Basis View | General Project Data form. Here you will find the option Suppress default equipment/area/project bulks option.
When M is selected, ACCE will function just like Aspen In-Plant Cost Estimator (AIPCE). The M option suppresses the equipment volumetric model (installation bulks) and most of the system developed area and project bulks. This will ignore Engineering and Construction (crew mixes, craft names) Workforce, Power Distribution and Process Control, Panel board, Contracts, Project Execution Schedule as well as all area design basis option to develop estimate and reports.
When the M option is selected, the user will not see the normal Evaluate Project dialog box pop-up when first initiating a project estimate run. Instead, the estimating evaluation progress window will show immediately and evaluate the project, and no CAP_REP.CCP report will be generated. You will only be able to run the reports out of the Aspen Icarus Reporter.
Deactivating the M selection will allow everything to go back to normal.The N option suppresses equipment volumetric model bulks and most of the system developed area bulks. Multiple contractors and consets are still allowed and standard ACCE estimates and reports (CCP) will be generated for 'his option.
For more details on the differences between the M and N option in ACCE, please review article What is the difference in the Aspen Capital Cost Estimator (ACCE) M and N feature?
Keywords: CAP_REP.CCP, Suppress default equipment/area/project bulks, General Project Data, Suppress, Turn off, Installation bulks, Remove installation bulks, Volumetric.
References: None |
Problem Statement: How does ABPD calculate time for Evacuate and Pressurize operations? | Solution: Aspen Batch Process Developer (ABPD) uses the Ideal Gas model to calculate the amount of gas needed to Pressurize/Evacuate a vessel from one initial pressure to a final pressure:
Where:
M = the mass of gas required
V = the free space in the unit
Pf = the final pressure of the unit
Pi = the initial pressure of the unit
MW = the molecular weight of the gas
R = the universal gas constant
T = the temperature of the unit
Then, the program calculates time as:
Where:
toperation = the operation time
M = the mass of the gas
Ṁ = the average transfer rate of the gas
The average transfer rate of the gas can be specified by the user, or the program will use a default value, but in either case the value is in a volume basis, so the program needs to convert it to a mass basis flow using the Ideal Gas model as well:
Rho = M/V = (P*MW) / (R*T)
Where:
Rho = Density
M = Mass
V= Volume
P = Final pressure of the unit
MW = Molecular weight of the gas
R = Universal gas constant
T = Temperature of the unit
Note: Please notice that the program uses the final pressure, Pf, to calculate the density of the gas, which will have an impact on the calculated time of the operation.
Keywords: Evacuate, Pressurize, Time.
References: None |
Problem Statement: How to use different MIP types in PSCP model? | Solution: MIP is normally specified by using the MipType field in the Supply, Demand, Transport, Operation and Collector tables. There are 4 types of MIP structure we can set up in PSCP model:
Threshold
The Min field is treated as a lower threshold activity limit. This activity must either be zero (0.0) or less than the Max value.
Linkage
Forces a more expensive transaction to limit theSolution before a less expensive transaction of the same type (material, transport mode, submodel operation, or capacity) can be included in theSolution. The activity of this column must be zero if the activity of a more expensive linked variable is less than its Max value. This variable must have a Min value of zero and a non-zero Max value. The more expensive linked variable must also have a non-zero Max value.
LotSize
The activity of the column will be a multiple of the value specified in the MipFactor field. Min and Max provide the basis for lower integer and upper integer variables, respectively. The actual Min will be raised to the next higher multiple of the MipFactor, and the actual Max will be lowered to the next lowest multiple of the MipFactor.
LotCost
This MIP type is similar to MipFactor in that the activity is continuous, but the model pays for each lot through MIPCost.
Keywords: None
References: None |
Problem Statement: How to verify Aspen Multi-Blend Optimizer has been successfully installed? | Solution: This Tech Tip provides a description of the check points to review and ensure Aspen Multi-Blend Optimizer was installed successfully.
Open Aspen Refinery Multi-Blend Optimizer
From Start Menu in your computer Open MBO, you will be asked to Specify a Working Folder, is important that the final user has all the necessary read and write rights on this folder, the working folder will contain the files associated with the current model for example Log files, after selecting this folder click on Ok
The following behavior should be observed
Open a Model
Open a standard model
Once you have open MBO, open a demo model to make sure the installation is properly done, to do that, go to menu File| Open Model and browse for the Demo.mdb model located in C:\Users\Public\Documents\AspenTech\Aspen Refinery Multi-Blend Optimizer\Access
A login Dialog box will come up, use the following login information to make open the model, then click Ok, note there is no password required for this demo model, in your model that might be different.
The following behavior should be observed
Open your model
Once you have made sure that a standard model opens properly, try with your model. remember that to open an MBO model in a newer version you have to make a Database Upgrade process.
Working with Access Database
If you are working with an Access Database you should follow the steps listed in the Open Standard Model section, considering the following variations:
Login Information: This will depend on the way your model is setup, the options are to use Windows Authentication or use your regular login User Identifier and Password.
Working with SQL or Oracle Database
If you are working with a SQL Database you should follow the steps listed in the Open your Model working with Access Database section, considering the following variations:
DSN File: The file you will be looking for is a DSN file instead of an mdb file.
Run a Model
Run a standard model
Once you have opened a standard model make sure you can run the model by clicking on the Optimize icon , the following should be shown:
The following will be shown:
Note that the progress bar should reach 100%. Finally, a HTML Report will be shown as follows:
Run your model
Once you have made sure that a standard model runs properly, repeat the same steps on your model.
Reporting Options
Refinery Wizard
To test the Aspen Refinery Report enable the memory cache option by clicking the corresponding icon , then, go to Menu Events | Publish and select Publish All, then choose the optimize option
Finally the HTML Report will be prompted again. Once you reach that point go to the Event Tab
The Report Wizard will be enabled . click on this icon, an excel file will be opened, choose a Blank workbook
Go to the Aspen Refinery Report tab and make sure you have the following options available and that the icon Disconnect appears as in the following image:
When this revision process is finished click on the Turn Off Memory Cache icon .
Aspen Report Writer
Report Writer is an Add-In that will be helpful for pulling information from Results DB, is important that this Add-In is properly installed to check that this is installed open an excel file and make sure that you can observe the ADD-INS tab as in the following image:
Integration Check List
Excel Integration Utility
Excel Integration Utility is an Add-in that is very useful to import information to your database, make sure you can observe the Aspen_EIU tab as in the following image:
Note that there is a Status icon , click on it an connect to APS or MBO
The status should change as follows:
General Recommendations
If any of the above described behaviors is not observed is important to properly attend the problem.
If you have any question on these steps, contact support for assistance.
Keywords: None
References: None |
Problem Statement: What is causing the runtime error to appear in Aspen HYSYS Blowdown Utility? | Solution: Small difference in time-step is a lot of unnecessary data. Changing the value to a big difference in time-step, such as 1,50,100 will get rid of the error message. This is because it will run to the halt time.
If it needs to run to the halt pressure, then you need to increase or decrease the halt time.
Keywords: Blowdown, Runtime, Error
References: None |
Problem Statement: How can I make table snapshots show properly in PIMS AO? | Solution: In PIMS-AO, we can view tables from model tree in a quick method. Directly clicking on the table tab will show up snapshot of the table.
If the tables are not shown up properly in PIMS-AO, click View>>Restore Table Grid will restore table view.
Keywords: None
References: None |
Problem Statement: I have created a custom pipe spec with a flange class of 150. However, when I apply it to a pipe with a control valve, the control valve flanges are still estimated as class 300. How do I change my control valve flange class to 150? | Solution: There is an option to set the Control valve minimum class to 150. Its default is 300, which is why control valves will still have 300 class flanges even with 150 specified on the custom piping specs.
In V9:
This option is available from the component Options | Pipe - General Specs form.
In V10:
This option is also available as a global specification from the Project Basis View | Piping Specs | General form.
Keywords: Control valve, flange class, pipe specs, custom, general
References: None |
Problem Statement: By default, OPCs contain a document number rather than a name (on some projects, it could be a description instead). How can one set up attributes to enable OPCs to contain something other than the Document Name? | Solution: In the CLE (Class Library Editor) one can check the Class View used in this label which is “New Sheet Connector”. The Class View available in the Standard Data Model is named as “GraphicDefinerSheetConnectorNew”. Then, create a copy of this Class View and include the attributes that you would like to see, such as Document Name, within this customised label for connecting PFDs. Including this Class View in the customised label
Once it is done and the label has been compiled and included in the Symbols and Templates folders in the Workspace Libraries, on the MSD right click on the sheet connector and select the “Select a Shared Diagram” option from the context menu. You can then select the other MSD document name you would like to connect to (the Online Help also provides additional information on this).
Keywords: OPC, Document Name Attribute, New Sheet Connector.
References: None |
Problem Statement: Some workflows require to show an item object in dashed lines to differentiate from initial scope. So, how can I show future items and lines as future scope in the Drawing Editor? | Solution: There are plenty of type of lines which may be selected from Drawing Editor. Just right-clicking on the equipment and selecting Properties | Format | Style, one can find a “Future” line which shows dashed lines in grey colour.
Doing this helps to differentiate between initial and future scopes on equipment.
Keywords: Future, Scope, Format, Style, Line Properties.
References: None |
Problem Statement: How can I modify the *.appdf file being used by my Aspen Plus Dynamics model to either update the component list or choose a different property method? | Solution: Whenever it comes to updating the *.appdf file of an Aspen Plus Dynamics model to either add / remove components from the component list or use a different property method, a means of doing so is by importing an updated *.aprbkp file into the Aspen Plus Dynamics model.
It is also a useful workflow to get to update *.appdf files when opening a dynamic model in a newer version of Aspen Plus Dynamics (keep in mind that *.dynf files are upward compatible, but *.appdf files are version-specific).
To update an *.appdf file using an *.aprbkp file, please follow the steps below:
1) Open the Aspen Plus steady-state model you used to jump straight to dynamic mode and go to the Properties Environment or start a new Aspen Properties model. Either way, the files must be the exact same version as that of the Aspen Plus Dynamics model.
2) Make the necessary changes to the model in terms of components, property method, physical properties correlations, pure components or binary interaction parameters.
3) Go to File | Export | Export a document and save your model as an *.aprbkp file.
4) Open your Aspen Plus Dynamics model and double-click on the ‘Configure Properties’ form. Next, use the ‘Import Aspen Properties file’ option and browse to the location were the *.aprbk file was saved in. Then click on the ‘OK’ button.
5) The *.appdf file will get updated.
Keywords: Aspen Plus Dynamics, Update, Modify, Component List, Property Method, appdf, aprbkp.
References: None |
Problem Statement: How can I plug more than 500 tubes in Aspen Shell & Tube Exchanger? | Solution: Aspen Shell & Tube Exchanger (EDR) has a limit of 500 for the number of plugged tubes you can model. However, there is an easy workaround you can try to overcome this limitation.
The program allows you to specify the number of tubes in the exchanger, but internally it also has an algorithm to calculate the maximum number of tubes that can fit in a particular shell. When the input for the number of tubes and the calculated number of tubes don’t match, EDR shows a warning message:
This message states that the program will use your input to calculate tubeside heat transfer and pressure drop:
However, the program will still use the calculated number of tubes to build the tube layout:
Thus, this is as if the remaining tubes were “plugged”, because they are part of the tube layout, but they are not being considered for tubeside heat transfer and pressure drop calculations.
Using this approach would allow you to model more than 500 “plugged” tubes.
Take the attached file as an example. The calculated number of tubes is 1068 and the input is 560, so only 560 tubes will be used for heat transfer and pressure drop purposes, while the full 1068 tubes will be used in the tube layout, which means that 508 tubes (1068-560=508, >500) are “plugged”.
Keywords: Shell and tube, plugged tubes
References: None |
Problem Statement: If one would like to edit the Expansion Template found in the Drawing Editor’s Symbol Library | Primary Expansions, where should these modified: using the Graphic Definer or Drawing Editor? | Solution: The Expansion Templates are created and may be modified in the Drawing Editor and not using the Graphic Definer. Although, one can edit an existing Expansion Template in the drawing editor to see the Class View selected for it.
Keywords: Expansion Template, Primary Expansion, Edit.
References: None |
Problem Statement: How to change the Units of a Product shipment event from VOL/Day to VOL/Hour in APS? | Solution: By default, the UOM of any Event is set from the Events Default tab in the APS Settings Window.
Refer Screenshot:
So the Unit can be changed from the Events Default Tab from VOL/Day to VOL/Hour as shown below:
Once changed in the Settings dialog box, when an event is open you can see the event showing the Unit as VOL/Hour
Note - After changing the Unit settings in the Settings dialog box, the Model must be saved
These settings usually get stored in the CONFIG table for the event default settings
Keywords: Event Unit , Default settings, Product Shipment
References: None |
Problem Statement: How to setup SMC files on PIMS and APS: A detailed guide | Solution: SMC stands for Sub Model Calculator, which is another mode of adding APS logic, but is a popular link with PIMS, where we can export PIMS submodel behavior into APS. The first step to using this functionality has to be from the PIMS side, where an SMC file has to be created (.smc). This file will store data regarding a given PIMS submodel hence the same calculations can be performed in APS. Both applications will be consistent.
Use the following steps to create an SMC file:
At first a matrix must be generated. Run the model and get an optimized case in PIMS
Once this step is done the user can access Submodel Calculator from the Data Assistant:
3. Next step is to choose with which PIMS submodel we would like to work and later on export to SMC file:
4. Once the submodel is chosen, submodel calculator will appear:
As APS is a simulation tool and not optimization we need to deliver squared (number of columns= number of rows) matrix so APS will be able to calculate variables based on an input. In the submodel calculator view we can see if the current submodel structure is squared or not:
4 COLS
3 ROWS
The user would need to have a basic understanding of PIMS terminologies to perform this operation. As an example here (Volume Sample model, SKHT submodel) we have 4 columns (variables) and 3 relevant rows (constraints). Since we know that the feed value KE1 to this submodel in APS will be taken from the upstream unit and will not be unknown/variable, we can fix it by giving any value (this value will be updated in APS to the proper one in a given simulation run):
The “Use” column seen determines the rows that will be exported to APS, in the SMC file that the user is about to create.
5. Change SKHTKE1 column from variable to a fixed value. Now the submodel is squared:
3 COLS
3 ROWS
6. Create the SMC file of this squared matrix from File-> Save, and save as type “.SMC”
Mapping the SMC file in APS before use:
After exporting the SMC file from PIMS,
In the APS model go to Model-> PIMS sub models
2. Locate the submodel exported from PIMS in the left pane:
3. Note that there are four main tabs in the dialog opened:
Summary: Summarizes the SMC with the mapping done in APS, identifying the inputs and outputs of the SMC
Submodel: Is a snapshot of the PIMS submodel that was used to create this SMC
PIMS Prop Calc: SMC also captures static values/relations stored in PIMS from the PCALC and the BLNPROP tables.
Build Ref: Mapping tab between the PIMS and APS tags
It is the best practice to carry only the original property within APS. The SMC unit in APS is set up to enable mapping to be indexed/reverse indexed when needed.
4. Open the Build Ref tab of the Submodel dialog, to begin the mapping process in APS:
Each property can be assigned PIMS-to-Orion function and an Orion-to-PIMS function which allows the entry of an Excel function, ABML (Aspen Blend Model Library) function, or UBML (User Blend Model Library) function to be used for handling the indexing. For ABML and UBML the same function name is used for both the PIMS-to-Orionand Orion-to-PIMS function.
5. Map PIMS material (product/feed stream) tags to their corresponding steam IDs when incorporating PIMS submodel into your APS model. Once the properties are mapped, it is possible to transfer values from the model to the PIMS Submodel Calculator (.smc) file and conversely. Map all feed or product streams referenced in WBAL or VBAL rows in the .smc file.
6. In the Streams section, enter the desired PIMS material tag in an available row, and then enter the corresponding stream ID in the adjacent column
7. Click the OK button to save your modifications
8. Repeat for all streams referenced in WBAL or VBAL rows
At the end of Step 8, the following mapping should have been complete:
Properties PIMS and APS
Streams
Feeds to the SMC unit, mapping between the WBAL/VBAL rows and APS stream VOL/WGT
Keywords: None
References: None |
Problem Statement: When using Acid Gas cleaning option in Aspen HYSYS, some tray efficiencies are higher than 1, which is not reasonable. | Solution: When calculating tray efficiencies, HYSYS uses Murphree efficiency theory:
When the denominator of this definition of Eff (i,j) is close to zero, the efficiency can change arbitrarily from negative infinity to infinity. When xi,j and yi,j are small, the uncertainties are larger. So the tray efficiency could be larger than 1 from numerical point of view. There is no real physical meaning. This should not affect the general results. If we limit the upper bound to 1, for some flow patterns it may affect the convergence. We just need some flexibility on this to help convergence in some situation.
From Aspen HYSYS V11, a warning message will be given in the trace window after the acid gas column is converged:
Some of the calculated CO2 or H2S efficiency values in column (*column name*) are greater than 1.0. When the component is near the equilibrium region, the value in the Murphree equation for efficiency calculations can be greater than 1.0. While the efficiency is typically between 0.0 and 1.0, the upper limit was relaxed to 1.25 to improve convergence for some cases; separation will not be impacted significantly since its driving force is close to zero in the component equilibrium region.
Keywords: Tray efficiency
Acid gas
Murphree
References: None |
Problem Statement: How do we back up our APS/MBO database model? | Solution: There are two types of common model dbs. One is in Microsoft Access, and the other one is SQL server. If your model is in Microsoft Access, you can directly copy and paste the model file to a different location on your machine/or any other location. If your db model is in SQL, then a backup process needs to be done. Please look at the following procedure:
First, log into your SQL server database using your server string and password:
In the left hand side panel, right click on your APS/MBO db, and select option all tasks -> back up.
After that, a new dialog box will appear and ask you for the backup options. Choose the correct database and give the backup file a name. The file path will also be shown. Take note of the file path and click OK.
Once it says backup successfully, you can go to the file path and collect the .bak database file.
If you are using Units.xls file, dlls, smc, or any other tools in your model, please zip everything together as the model folder. If you are going to try the same model on a higher version like V11, you will probably need to perform a db update when you open the model in APS/MBO. This is discussed in another KB article. Please search “How to perform a DbUpdate in APS/MBO”.
Keywords: None
References: None |
Problem Statement: How to create material pool for blend components in MBO? | Solution: To create material pool for blend components in MBO, please refer to the following two methods.
Method 1: Visualize the blend components pool trend.
1.Created a new material, e.g. COMPONENT.
2.Created material service events against the component tanks, e.g. THCL and TLCN, for the model horizon.
3.Created a PROD_SERVICE material pool PCOMP with basis ID “COMPONENT”.
4.Trend the PCOMP pool by volume.
5.Reload Simulator/Refresh Trends. And you can trend the components material pool in the chart of PCOMP.
Method 2: To schedule blending events for blend components pool, you may want to create virtual pool by using INIT worksheet in MBO
1. Add USE_MBO_INIT in CONFIG table.
2. Add a virtual pooling tank.
For example, TALKP represents the pool of two component tanks TALK and TALK1, which are used for component ALK.
3. For component ALK, change the tank to TALKP.
4. In Units>>INIT worksheet, add following structure to load TALKP inventory and property values at the beginning of the horizon.
Keywords: None
References: None |
Problem Statement: When I open Aspen Plus or Aspen HYSYS, the following error message shows up:
apedconnectionerror.log
Failed to initialize the Aspen Properties Enterprise Database.
Using the configuration file from C:\ProgramData\AspenTech\APED VX.X\casasecd\config.aem
Please use the Aspen Properties Database Configuration Tester to diagnose and fix the problem. | Solution: The error message indicates that our APEA built-in databases are not correctly configured in your machine. In order to fix this, please do the following:
1. Go to the shared folder: C:\ProgramData\AspenTech\APED VX.X (replace X.X with your Aspen Properties version)
2. Run DeleteDBInstance.bat. as administrator (right click and select as admin). This batch file will drop any database from restoring that is incomplete. It also deletes the instance of LocalDB you own and the folder named by your Windows logon.
3. Open the Start Menu, Open the Database Tester with a right click and select Run as administrator from All Programs | AspenTech | Aspen Properties or and click on Restore databases directly. Check that there are no errors.
Note: The database is created for each user, so each user that wants to use localDB for the APED, needs to have admin rights.
Now Aspen Plus and Aspen HYSYS should open normally without the error message.
Keywords: APED, initialization, APED connection error
References: None |
Problem Statement: How to model internal dividing redistribution in Aspen Plate Fin exchanger? | Solution: In some cases, a stream is only present for a fraction of the length of a set of layers and then exits the core, which leaves that set of layers empty. To avoid having empty layers in a fraction of the exchanger, a second stream can be diverted from another set of layers to occupy the empty region. This second stream must then pass through a redistributor in the second set of layers (Layer Type) to divert part of its flow, and the first set of layers must have an inlet intermediate distributor to take this inflow into the otherwise empty layers.
In summary, the stream is initially in a single set of layers and ends up in two sets. This is what we call “dividing redistribution”.
The attached example tries to simulate an internal dividing redistribution like the one shown below:
Where Stream 2 (Hot), leaves the exchanger at some point, so Stream 1 (also Hot) is divided to occupy the empty layers.
Keywords: Redistribution, distributor, plate fin, EDR
References: None |
Problem Statement: How can I do “milk run” modeling in PSCP? | Solution: In PSCP, “Milk Run resembles the delivery route of a milkman who loads his wagon completely and then drops off deliveries along a fixed route. It is used to model barging services and assumes limited number of barging vessels, which includes time for vessel to return to starting node. Travel times are defined as the cumulative time to travel to each terminal in sequence.
Milk Run transportation arcs in the PSCP matrix are defined between one loading port and each delivery port. This structure prevents material loading at the delivery ports. The travel times in the Distance table are the cumulative times based on the route the ship actually travels (not the time it would take from the loading port to each terminal). The return leg is not defined as a transportation arc, but the total voyage time is defined as a MipFactor constant in the Collector table for the Milk Run collector variable.
To create Milk Run structure in PSCP model, you can follow the workflow below:
Define the several possible routes in table “Modes”. These same modes are used in the Transport, CapTransport and Distance tables.
Define which transportation arcs are included in each Milk Run. Only one loading port is defined for a Milk Run. All other ports are for material delivery only. Each arcs is defined between the loading port and a single delivery node to prevent loading at delivery ports.
Define the travel time between nodes for each route in table “Distance”. Travel times are cumulative in the order the ship travels between nodes. Travel times are NOT the travel time from the loading port directly to each node.
Entries in the CapTransport table are used to collect the material shipments to each terminal into the same Capacity variable that is then used as the Milk Run collector variable in the Collector table.
In the “Collector” table:
Define as many “ship collector variables” as the number of ships available (Each one has Max = 1 to limit each ship to one route at a time)
Define as many “Milk Run collector variables” as routes.
MipType – Milk Run
MipFactor – Number of days needed to complete the entire trip
MipLink – One of the Ship “collector variables”
Keywords: None
References: None |
Problem Statement: How to use the Indexed Viscosity method in Aspen HYSYS | Solution: For certain fluid packages Aspen HYSYS provides different options of Viscosity method
Note: To choose the Indexed Viscosity method the user can drop the list of the Indexed Viscosity option
Aspen HYSYS uses the following methodology to calculate the kinematic viscosity (cSt) of the stream:
1. Calculates the Indexed viscosity for each component i, iv(i) = A*log10(log10(visc(i)+C))+B;
Where: visc(i) is kinematic viscosity (cSt) of component i.
2. Calculates the Indexed viscosity of the stream = Sum(x(i)*iv(i));
Where : x(i) is mass fraction of component i.
3. Calculates the kinematic viscosity (cSt) of the stream =10^(10^((IV-B)/A))-C; ^ = exponent.
The following example can clarify the calculations.
In the attached HYSYS file, there are two components: C10 and C15.
Kinematic viscosity of C10, visc1 = 0.9985 cSt
Kinematic viscosity of C15, visc2 = 2.559 cSt
With Indexed Viscosity method selected with A = 30, B = 40 and C =2 (the numbers here are totally arbitrary):
iv(1) = A*log10(log10(visc1+C))+B = 30.35
iv(2) = A*log10(log10(visc2+C))+B = 34.56
Indexed viscosity of Mixed stream, IV = x1*index1+x2*Index2 = 32.88
Kinematic viscosity of Mixed stream = 10^(10^((IV-B)/A))-C = 1.793 cSt
The excel file has the corresponding calculations.
Notes:
1. Please choose constant C such that visc(i)+C is >1. Log10(Log10(visc(i)+C)) becomes indeterminate otherwise.
2 Constants A and B do not effect the calculated viscosity. They affect the index viscosity only. This is the nature of the equations. Choose A and B wisely to match index viscosity. Choose C wisely to match kinematic viscosity.
Keywords: Indexed viscosity, Kinematic viscosity
References: 1. Twu, H.C. and Bulls, J.W., Viscosity Blending Tested, Hydrocarbon Processing, April 1981. |
Problem Statement: Is the Safety Analysis ‘Chemical Reaction’ scenario capable of sizing a PSV to protect a system against undesired runaway reactions? | Solution: We do not have any direct support for runaway reaction calculations inside the Safety Analysis environment. The ‘Chemical Reaction’ scenario type in the Safety Analysis environment serves as documentation only. The user will have to provide a relief stream and required relief rate, and then Safety Analysis will calculate the required orifice size and (if desired) perform line-sizing calculations. So, the ‘Chemical Reaction’ scenario works pretty much as a ‘User Defined’ scenario.
The best way to do this is probably a dynamic simulation.
There are some shortcut methods in the ‘DIERS’ literature for runaway reaction calculations. However, even a shortcut method will need fairly detailed information about the system and the kinetics of the runaway reaction in order to calculate an estimated vent size requirement. This kinetics are not necessarily straightforward to derive from first principles or knowledge about normal operation; often relief-focused calorimetric studies are needed to properly account for potential side and/or decomposition reactions.
Anything more rigorous will necessarily involve a dynamic simulation where capacity is determined on a trial-and-error basis, due to the complexity of the energy and material balances in the system. Both Aspen Plus Dynamics and Aspen HYSYS Dynamics have PSV models available for dynamic modeling, which might turn out to be of great help for this purpose.
Keywords: Chemical Reaction Scenario, Safety Analysis, Runaway Reaction, Dynamic Simulation, Aspen Plus Dynamics, Aspen HYSYS Dynamics.
References: None |
Problem Statement: How to resolve when in Aspen Petroleum Scheduler/Orion, on invoking an event's User Calc , you are unable to see the Template data ? | Solution: The screenshot shown in the above statement belongs to a User Calc for Crude Run known as Optimize, User Calcs are customized utilities usually deployed for automation of a task,
This issue of not being able to see the template/data in the User Calc window is due to Restriction set to the User Calc executable/Folder.
This issue can be resolved by giving the User the permission to Read/Write the Folder where User Calc and the APS Model reside.
On setting the Security permission for the User Calc folder, this issue will get resolved.
Once the permission is set, kindly re-open the APS application and invoke the User Calc again.
Keywords: User Calc, Crude Run, Optimize, Orion
References: None |
Problem Statement: When registering a project from a previous version of Aspen OnLine in V10, if the project name contains a hyphen or other special character, the migration may fail with error [Microsoft][ODBC Text Driver] Syntax error in FROM clause. | Solution: Aspen OnLine uses Microsoft database technology, and certain special characters are not supported. AspenTech recommends only using alphanumeric characters for project names and beginning all project names with a letter.
Rename the project folder using only alphanumeric characters, then repeat the registration process.
Keywords: AOL, ODBC text driver, error
References: None |
Problem Statement: During FCC calibration, how to adjust sulfur content so that the the calculated H2S match the expected value? | Solution: When performing the FCC calibration in software, the option to specify wt% sulfur in coke is not available in Coke and Sulfur Balance and the default value is 5 wt% shown on the result of FCC calibration | Analysis | Mass Balance tab. So if user want the calculated H2S match the expected value, how to adjust sulfur content so that obtain the expected value?
1, User can specify the SOx content in the Flue gas on the Operation | Regenerator page in calibration.
2, If the user wishes to match the H2S exactly with the expected or measured value, they can increase or decrease the flue gas SOx as needed. If the SOx content is increased, the H2S by difference will decrease. Conversely, if the SOx content is decreased, the H2S by difference will increase.
Note: we typically calculate H2S by difference because the measurement for that is typically poor whereas the measurement for the sulfur in the liquid products and the SOx content in the flue gas tend to be good, and so people don't typically measure the sulfur in the coke, but rather the SOx in the flue gas (which is the combusted product of the coke.).
Since the model must sulfur balance, the degree of freedom is the H2S. If the user isn’t sure about the SOx in the flue gas, then it is available to move that up or down to match the desired H2S, please see below snapshot.
Key Words
FCC calibration, Wt% feed sulfur in coke, SOx content in the flue gas
Keywords: None
References: None |
Problem Statement: What is the suitable property package selection for GDU in Aspen HYSYS? | Solution: Basically, the interaction parameters for TEG and water in the PR property packages are based on data from the Union Carbide glycol handbook at 1 atm. Although the entire composition range was used in the fit, these Property Packages are more applicable to higher glycol
concentrations (glycol > 80 mass%) and higher temperatures.
(see https://esupport.aspentech.com/S_Article?id=000029035 for more detail).
Peng-Robinson model is suitable to handle the properties for the process. The Peng-Robinson package is the model in HYSYS that Aspentech have made the most enhancements to, it has the largest applicability range in terms of temperature and pressure and largest binary interaction parameter (BIP) database. It also applies some special functionality to particular BIPs. H2S, CO2, and H2O are among those receiving special treatment. For example, the BIPs for the pairs of H2S-H2O and CO2-H2O are treated as functions of temperature. This helps the model to better
represent the behaviour of systems containing these components. There could be some concerns for the glycol dehydration for which there doesn't seem to be a clear status on which model is best. Peng-Robinson should give sensible results.
Apart of using only one Fluid Package, you could also use both Glycol and Peng Robinson in one simulation. The most practical approach is to use Peng Robinson for the contactor and the Glycol
package for the regenerator.
The TEG-Water binary interaction parameters in PR receive special treatment and Peng Robinson has given accurate results when modelling this type of systems. This fluid package is recommended to be used on the contactor and the surrounding units in the
simulation.
The Glycol property package contains the necessary pure component and binary interaction parameters for components commonly encountered in natural gas dehydration process. The property package is tuned to represent accurately, the phase behaviour of these components, especially that for the TEG - water binary system. The fluid package should be applicable between 202 C to 206 C and 1 to 2 atmospheres, which are the conditions for a typical glycol regenerator.
As with any fluid package, it is suggested to follow some engineering approach when selecting a fluid package to be used in the simulation.
Keywords: Aspen HYSYS, Fluid Package, GDU
References: None |
Problem Statement: In Aspen Advisor/AORA While trying to launch a SQL Server based model, how to resolve the error message, ”Login failed for user ‘advisor3?
(Refer Screenshot for error details) | Solution: The Aspen Operations Reconciliation and Accounting System (Aspen Operations Accounting), formerly known as Aspen Advisor, performs plant performance analysis and yield accounting functions.
In Aspen Operations Accounting, a model of the processing plant is used to track material receipts, shipments, internal movements, and inventories.
The model can be closely representative of the physical plant or more virtual depending on the tracking and reporting requirements.
After the database tables have been created, you build the model by adding various global and equipment objects to be used within the model.
The model can be a MS Access, SQL or Oracle based model.
In the screenshots shown in problem description,
Root Cause: The customer is trying to launch a SQL based model, however there is no user named ‘Advisor3’ configured in the Model Database.
Solution
“Advisor3” user name is an Inbuilt – Hard coded user name and has an associated password with Advisor application
This Username with the same password must be configured to Access Advisor application. To solve the issue, please create a new user named: Advisor3 in the SQL database.
Once done, re-open the model and the problem should be resolved.
Keywords: AORA, Advisor, User Login, Advisor3, Login Failed
References: None |
Problem Statement: When there is a firewall between the Aspen InfoPlus.21 server and Aspen Process Explorer clients, certain ports need to be opened to allow communication (see also knowledge base article: How do I connect Aspen InfoPlus.21 client applications to an Aspen InfoPlus.21 server across a firewall?).
In some cases, even after this configuration, some customers may experience that the first connection attempt between Aspen Process Explorer and Aspen InfoPlus.21 might be quite slow, but subsequent attempts are faster.
Other symptoms are:
Aspen Process Explorer clients and the Aspen InfoPlus.21 server can produce deny messages in the log file of the firewall on closed ports - especially when Aspen InfoPlus.21 is located outside of the firewall.
In the TSK_APEX_SERVER.OUT file on the InfoPlus.21 server, you get SRVR_CALLBACK::CLNTTCP_CREATE FAILED messages. | Solution: The reason for these symptoms is because the Aspen InfoPlus.21 server needs to make callbacks to the clients to support asynchronous requests. Because Aspen InfoPlus.21 is outside of the firewall, these callbacks fail. After a certain timeout, Aspen InfoPlus.21 will default to using synchronous communication instead.
Below is the sequence of events, to explain in detail how the procedure works:
An Aspen Process Explorer client sends a request to the portmapper on the InfoPlus.21 server through port 111 asking for the port number that TSK_APEX_SERVER has registered. This is the same port number that is configured by writing -n xxxx in the command line parameters for TSK_APEX_SERVER, where xxxx is the port number (for further information on how to assign the port number to Aspen Process Explorer clients see knowledge base article: How do I connect Aspen InfoPlus.21 client applications to an Aspen InfoPlus.21 server across a firewall?).
The Aspen Process Explorer client makes a connection to TSK_APEX_SERVER through this port.
The Aspen InfoPlus.21 server requests a port from the Aspen Process Explorer client portmapper for callbacks.
The client portmapper assigns a random port and the Aspen InfoPlus.21 server will use this port to perform asynchronous replies.
The Aspen Process Explorer client sends an asynchronous history request to the Aspen InfoPlus.21 server.
The Aspen InfoPlus.21 server gathers data and tries to send it back to the client through the assigned port. This fails since the firewall blocks this port.
Aspen InfoPlus.21 will try this send for a time, but will eventually timeout from sending these unsuccessful asynchronous history requests. It will automatically switch over to use synchronous communication to send the data.
In summary, the delay and deny messages are caused by the random port assignment used for asynchronous requests. However, Aspen InfoPlus.21 will switch over to use synchronous replies if the asynchronous replies fail. Therefore, the Aspen Process Explorer client will eventually receive data.
As you can see above, communication on port 111 is needed for communication between client and server applications. Thus when there is a firewall between the Aspen InfoPlus.21 Server and Aspen Process Explorer clients, port 111 must be open.
On the InfoPlus.21 server you possibly resolve such firewall and performance issues by including NobleNet Port Mapper Service (PORTSERV.EXE), PORTMAP.EXE and infoplus21_api_server.exe in the firewall restrictions list.
Process Explorer users can choose to disable the private firewall on the client machine to allow the asynchronous communication to occur, and the delay while the timeout is occurring will disappear. If the client firewall needs to be enabled you may add the PORTSERV.EXE and PORTMAP.EXE executables into the exception list of the client Windows Firewall configuration.
Other users, if they have chosen to place Aspen InfoPlus.21 outside of the firewall, will simply experience this delay. It is more typical that Aspen InfoPlus.21 would be placed inside the firewall, where the asynchronous replies would succeed, because ports would not then be blocked for outgoing traffic.
Another option is to force synchronous communications on the client system. This can be accomplished by one or other of the following options:
A) Disable the NobleNet Portmapper Service on the Aspen Process Explorer client machine(s). This will force synchronous replies from Aspen InfoPlus.21. DO NOT disable the NobleNet Portmapper Service on the Aspen InfoPlus.21 machine.
B) A registry setting can be used to disable asynchronous communication on the client machine. The following registry key is:
For 32-bit Process Explorer running on a 64-bit version of Windows (Wow6432Node):
[HKEY_CLASSES_ROOT\Wow6432Node\CLSID\{710B32A1-7277-11D1-932C-00805F0F1C84}\Options]
DisableAsync=True
-or- for any other combination of software/Windows:
[HKEY_CLASSES_ROOT\CLSID\{710B32A1-7277-11D1-932C-00805F0F1C84}\Options]
DisableAsync=True
Keywords: deny
extremely slow
denied
firewall
References: None |
Problem Statement: Process for validating PIMS model during an upgrade | Solution: This article describes the process for upgrading the PIMS model to a higher version and validate the user's workflow after an upgrade.
General Description of the process:
Check Non-Default Model Settings
Make sure you have a list of Non-default model Settings, right click on Model Settings and select Print option. Use your printed pdf to configure your model settings after the upgrade process.
Summarize your Workflow
Summarize and document the workflow used by PIMS users. The document recommended best practices and functionalities used by users to configure in the newer version after migration.
Make a Model Backup
Before you go to a newer version make sure to have a backup in case something is changed or modified, especially when they are being upgraded from versions previous to V8.8.
Open your model in the newer version
In general terms there are no upgrading steps necessary when opening a model in a newer version of PIMS, though, for models that are being upgraded from a version previous to V8.8 you will find the following dialog box:
Starting from V8.8 PIMS has a number of significant changes in the way various tables are handled. A number of tables have been eliminated from the system and are so noted in the following discussions.
When a model is first opened with a new version of PIMS, a number of changes are automatically made to the model. These changes are required to bring the model into the correct format. The first is that the tree structure (discussed later) is created from tables SETUP, RECURSE, TABLIB, PIMSLP, SERVERS, REPORT, and SKEDLINK. If the system detects an incorrect table TABLIB, you will be prompted to either continue the conversion or abort the conversion. The table TABLIB can then be edited outside of PIMS and then converted successfully.
Configure your Non-Default Model Settings
Once you have upgraded PIMS make sure to setup your Non-Default Model Settings.
Verify your Workflow
Verify the workflow you follow can be properly followed in the new version of PIMS. If you note that your workflow is not delivering the same results, contact support. Is recommended to not deploy a newer version of PIMS without having this step check.
Notes:
If your model has warning or error messages, a version upgrade will most likely not solve them, if you find model warnings during the upgrade process is important to attend them.
Keywords: None
References: None |
Problem Statement: Cases created in versions prior to V9 in which Saturate with Water extension was used instead of the “Stream Saturator” unit operation might have problems with the extension not being displayed on the flowsheet, although it might still resolve saturation streams. | Solution: Since V10, we no longer deliver Saturate with Water extension with HYSYS. The best option is to replace this old extension with the new Saturator unit operation: delete the extensions and add the new Stream Saturator.
You can find more information about the new unit operation in KB How to specify the relative humidity of a process stream in Aspen HYSYS?
If you still want to use the old extension, you will need to re-register it with HYSYS V10.0. The extension is still available on support website Saturate Extension Unit Operation.
We recommend to use the new unit operation Saturator that is available in Aspen HYSYS (released in V9.0). The new unit op is created and maintained by AspenTech so we will able to address any concerns you have regarding the new unit operation.
Keywords: Custom, Extension, Saturate
References: None |
Problem Statement: Can a user monitor the PID controller variables response in Aspen HYSYS Dynamics? | Solution: The response of the Process Variables (PV), Setpoint (SP), and Output (OP) can be seen on the Monitor tab of the controller. The behavior of process variables can be monitored in a graphical format while calculations are proceeding.
The Monitor tab displays the PV, SP, and Op values in their relevant units versus time. Users can customize the default plot settings using the object inspection menu, which is available only when you right-click on any spot on the plot area.
Keywords: PID controller, Process Variables (PV), Setpoint (SP), Output (OP), Monitor
References: None |
Problem Statement: What are the changes in dock scheduling in V11 compared to the previous versions? | Solution: A Dock Scheduling license is now only checked out if a user opens a DS screen. Previously a license would be checked out if voyage data is found in the model irrespective of DS usage. Use the Integration | Voyages command to add, update and delete voyages. The DSIMPORT_VOYAGES and DSIMPORT_CARGOS staging tables are used to quickly perform the new voyage integration procedures. Importing and updating DS cargo and events for any voyage is now supported directly from the interface from the Dock Scheduling Integration menu option. Access rights to Dock Scheduling can now be set using the DSS column in the GROUPS table.
Entering a zero in that column restricts access to DS. A missing value or any other value allows access to DS screens and specific DS data. ADMIN group users will always have DS access. If a user does not have access rights, the Dock Scheduling node on the navigation tree will be disabled and therefore access regarding viewing and any interactions will not be allowed. Properties can now be associated with non-crude product receipt cargo event types. On the Event Detail dialog for a non-crude receipt event, there is a new Property area Props where you can add/edit/delete properties associated with the Cargo Material. How properties are saved when OK is clicked is determined by the new Synchronize non-Crude Receipt Properties setting found on the DS Settings dialog box. If this setting is selected, changes to the properties’ list in the Event Details dialog box (ex. properties added or deleted) would be reflected to other events. No changes to properties’ values will be copied/reflected across events in the group.
NOTE: Any changes to API/SPG on an event in a group, will always be reflected in all other events in that group when OK is clicked. If DS units and APS units for the non-crude receipt event are different, API/SPG will be used to convert the UOM. This converted UOM will be used to calculate the event quantity if needed. SPG is used to convert the UOM if both API and SPG are provided. See the table descriptions for specifics on how DS properties are handled in the CARGO_PROPS and ATORIONEventProps tables. Linking voyages together is now supported using the following options: On the Voyages dialog, a Start Link and Stop Link options have been added where you can supply the voyage ID to establish the links. Two new options, Start Link and Stop Link, have been added to the shortcut menu associated with a voyage on the Gantt chart. Rightclick and select the option and then click on a vessel to establish the link. The Link - Thickness of link line option has been added to the Dock Scheduling Gantt Options dialog box that lets you specify the thickness of link lines on the Gantt chart. STARTLINK and STOPLINK fields have been added to the VOYAGES and _VOYAGES tables. Demurrage calculations are not affected by the Start/Stop links during optimization. Information has been enhanced to include calculation of demurrage excluding links using the Demurrage without Links display field in the Optimize Demurrage dialog box. Additional columns have been added to the dialog to display start and stop link information. If links are broken after optimization, a message will appear after OK is clicked.
The Auto Adjusting feature does not take start and stop links into account. If links are broken during dock adjustment, a message will appear.
For a common model between APS and MBO that has Dock Scheduling voyage data, MBO now allows loading and simulating Product Receipts and Product Shipment event types. This allows calculation of tank inventories and properties within MBO. You are also allowed to now change tanks and Prep and Post values times on Product Receipt and Product Shipment events from within MBO. Note that MBO will not optimize these Dock Scheduling events. They will be considered fixed.
Copy a voyage to create a new voyage You can now use the Copy and Paste shortcut commands associated with the Voyage Gantt chart to create a new voyage. Select the desired voyage to copy by clicking and dragging to cover a specific area on the Gantt that contains the desired voyage(s) and then pasting your selection on the Gantt to create a copy. ETA and Lay window times will be adjusted. Docking time, departure time and event time will be calculated. The other time variable remains the same as well as the Dock of the original voyage. Note: Copy/Paste can be done only on horizontal scale, meaning that a copied Voyage(s) on a DOCK1 can only be pasted on DOCK1 at separate times. For vertical movements, use the existing drag and drop feature.
Prep and Post Hours The Prep (Hours) and Post (Hours) fields have been added to the DS Cargo Details and Event Details dialog boxes to allow you to add preparation and recovery times associated with the event. The APSFLOWEVENTS, _APSFLOWEVENTS, CARGO and _CARGO tables have been updated to include the PREP and POST fields. Note the following as related to the Prep/Post fields: Hours entered in the Prep/Post fields on the DS Cargo Details dialog box affect the Voyage schedule. Entries made in the DS Crude Receipt and DS Product Shipment event dialog boxes do not affect the Voyage schedule. These values affect the availability of the tanks in APS, but not voyages. The DS Cargo Details dialog box now allows empty or blank values such as for the Cargo ID.
Changes Trend Tolerance Calculation A change was made in regard to how the Trend Tolerance % setting found under the Model Settings is applied. Previously, the calculation was applied to the MIN and MAX values directly. Doing so caused trend violations to appear unreasonable when the MIN value was zero. A change was made so that the entered percent is applied to the difference or range between the MIN and MAX values. Regardless what the MIN and MAX numbers are, the violation tolerance can now be reflected reasonably. Publishing Change - _EVENTS and EV_DAILY_DEST_TANKS for Pipeline Product Shipment events For event type 36 in the _EVENTS table, the calculation used to determine the WEIGHT value has changed: For Beginning Line-fill events, the SPG of the batch is used For Product shipment receipt events, the SPG of the source tank is used Previously, in the _EVENTS table, the SPG of the destination tank was used to determine the WEIGHT value. The change to the WEIGHT value seen in the _EVENTS table also causes a change in the WEIGHT value in EV_DAILY_DEST_TANK table for type 36 events.
Engine Modifications/Calculation changes Below are additional changes in V11 that may cause value to appear differently in V11.
Most of the differences (on the order of 1.0e-5) are mainly due to round off small differences on the order of 1.0e-6 or 1.0e-7 in the upstream(s). However, there are differences, mainly caused due to valid changes to logic for the existing features in APS.
1.
Keywords: None
References: : Wrong baseline pipeline fill is set when pipeline is rolled forward v11 Type of differences: In V11, some of the tanks does not have composition or properties as compared to results in V10.1. Issue: Due to an issue with Roll forwarding logic, the Simulation logic made delivery of very tiny pipeline batches into wrong tanks. Fix: Resolved the issue of delivering tiny PL batches to wrong tanks, resulting to differences when compared to results in V10.1.
Reference: APS fails to publish crude tank weight for the first day of publishing Type of differences: In V11, for crude tanks, data for WGT/SPG at the model start(midnight) has been published and the same was missing in V10.1. Issue: Data for WGT/SPG and compositions are not published at start of the models, publish was only publishing starting from 10 seconds period. Fix: Resolved the issue and hence one can see more records in V11 compared to V10.1.
3. Reference: Crude unit feed compositions are wrong if crude tank goes negative Type of differences:
Active Crude charging tanks (negative) caused differences in _CRDRUNS, resulting into all sorts of differences in downstream/tanks/parameters etc. Issue: Existing logic for mixing streams into a tank, has an issue where it mixes one stream at a time resulting into invalid results when the tank is negative. Fix: The mixing logic was changed to do pre-mixing when a tank is negative at the beginning of a transfer event and when the transfer has multiple sources
4. References associated with Weight Based pipeline movements: a. Slow performance in opening model, creating event, click save, switching event screen, publish results etc. b. Not able to reload simulator - APS crashes or Excel giving error Waiting for another OLE application. Type of differences: Many of the process tanks has very big differences in properties and WGT Issue: Issue with the SPG calculation Fix: In V10.1, the incorrect specific gravity (spg) was used to calculate the volume of material placed in the pipeline for weight based pipeline shipments. With the re |
Problem Statement: How do I resolve an Unexpected exception: object reference not set to an instance of an object error? This error may occur from the File | Print menu. | Solution: Go to File | Export Case
Select .mdb | .xls | .xml format
Click Browse
Change the Save as type to .xml
Choose a location and provide a File name
Click Save
Click Next (do not check the Clear all existing data before export button)
Click Next through the remaining Export Wizard forms to accept the default selections
Choose a location and provide a name for the Export Definition File
Open a new Flare file
Go to File | Import Case
Change the file type to .XML and then locate and select the .XML created in the steps above
Click Open
Click Next through the remaining Import Wizard forms
Locate and select the newly created Definition File
Once the file has finished importing, return to File | Print
The error should now be resolved
If you are still receiving the error after performing these steps, then please contact AspenTech Support.
Keywords: Error, object reference, print
References: None |
Problem Statement: How to use Advanced Analytical data in Molecular Characterization? | Solution: This document provides instruction on how to use advanced analytical data in molecular characterization as part of Aspen Assay Management features.
User can prepare the analytical data from a Fourier Transform Ion Cyclotron Resonance Mass Spectrometer (FT-ICR MS) or a Gas Chromatograph – Time-of-Flight Mass Spectrometer (GC ToF MS). The format is a the result after the user has processed their spectra by carbon number and hydrogen deficiency. Aspen Asset Management will parse in their data, normalize it, and use it to assign a molecular composition to their crude sample.
Keywords: Advanced Analytical, Molecular Characterization
References: None |
Problem Statement: What are the lists of pure component databanks in Aspen Plus? | Solution: Databank Contents Uses
PURE35 Data from the Design Institute for Physical Property Data (DIPPR) and AspenTech Primary component databank in Aspen Plus
AQUEOUS Pure component parameters for ionic and molecular species in aqueousSolution Simulations containing electrolytes
SOLIDS Pure component parameters for strong electrolytes, salts, and other solids Simulations containing
electrolytes and solids
INORGANIC Thermochemical properties for inorganic components in vapor, liquid, and solid states Solids, electrolytes, and metallurgy applications
AP-EOS
Pure component and binary interaction parameters used in the CPA equation of state property method Mixtures containing hydrocarbons and polar/associating chemicals
NIST-TRC Data from the National Institute of Standards and Technology (NIST) Thermal Research Center (TRC) Vast range of components
ETHYLENE Pure component and binary interaction parameters for components typically found in ethylene processes for use with the SRK property method Ethylene process
simulation
COMBUST Pure component parameters for components typically found in combustion products, including free radicals Simulations containing
combustion products
POLYMER Chains of repeating monomer units Polymers processes
SEGMENT Individual monomer groups or segments Polymers processes
INITIATOR Property parameters and thermal decomposition reaction rate parameters for polymer initiator species. Polymers processes
ELECPURE Pure component parameters for some components
commonly found in amine processes. Amine processes
FACTPCD FACT species (components referenced in a specific
pure orSolution phase for use only with the Aspen/ FACT/Chemapp interface in Aspen Plus) Pyrometallurgical processes
PPDS Physical Property Data System databank of the National Engineering Laboratory Link to PPDS databank
NRTL-SAC Pure component parameter XYZE containing segment representations of common solvents Calculat ions using
NRTL-SAC property
method
HYSYS Pure component and binary parameters needed by
Aspen HYSYS property methods Models using Aspen
HYSYS property
methods
BIODIESEL Pure component parameters for components typically found in biodiesel production processes Biodiesel processes
Keywords: Aspen Plus, Databanks, Pure, Components
References: None |
Problem Statement: As below shown, for one Scenario, ignore the source 22-BDV001 and 22-BDV002, these sources automatically are considered as Zero Flow source, but why also has vapor fraction indicated after run? | Solution: This is because it is checked this option: Calculate ignored sources with zero flow.
1, If selected, sources that have been ignored to be treated as if they have a zero flow, this will result in the back pressure being calculated and limit checked against the source MABP even if the source has been ignored. And you can see mass flow shown 0, but pressure has value.
2, If unchecked this option, all ignored sources result will be directly showed n/a.
Keywords: AFSA, Zero Flow Source, Ignore.
References: None |
Problem Statement: How to resolve the problem that Variable change in Excel are not displayed in Aspen Plus? | Solution: This can occur for one of two reasons:
If you put an equation in a cell, the equation will take priority over any attempt to enter a new value on the form in Aspen Plus.
ASW expects you to change specified variables from Excel.
To fix, close the form/dialog box in Aspen Plus; then, open it back up; you will now see the value is consistent with Excel.
Another way to force an update, is to click the Refresh button in the Workbook group of the ASW ribbon.
Keywords: Aspen Plus, ASW, Variables, Shown
References: None |
Problem Statement: When I export a split plate-and-frame economizer, APEA assigns a utility after the mapping procedure. How do I remove the utility and connect the appropriate process stream instead? | Solution: The first step is export the simulator data using the Send to APEA button.
Map either the hot or cold side to a plate-and-frame heat exchanger. Note, it is not necessary to map both sides.
Go to View | Process Flow Diagram.
After the PFD loads, right-click the inlet utility stream and select Delete. Repeat for the utility out stream.
Click the Draw Disconnected Streams button in the top bar.
Select the inlet process stream from your simulation.
For the inlet process stream, click in the blue space first and then click on the inlet flange (it will change color when the mouse pointer is correctly positioned on it).
Click the Draw Disconnected Streams button in the top bar again.
Select the outlet process stream from your simulation.
For the outlet process stream, click the outlet flange first (it will change color when the mouse pointer is correctly positioned on it) and then click nearby in the surrounding blue space.
At this point, the plate-and-frame exchanger should be correctly set up as an economizer with process streams on both the hot and cold sides.
Keywords: Utility, economizer, plate and frame
References: None |
Problem Statement: I am getting an error while using the AFR V10 converter. When I click on the Load Data button on the converter an error message comes up saying COM class factory for component with CLSID {00021A20-0000-0000-C000-000000000046} failed due to the following error: 800702e4 The requested operation requires elevation. (Exception from HRESULT:0x800702E4) | Solution: This issue with the converter not working might be based on a permissions issue that is seen commonly on Windows7/Server 2008. The likely issue is permissions restriction through the User Account Control (UAC). The workaround is to run the Converter as an Administrator on the machine that is experiencing this issue.
Key words
Converter, Administrator rights
Keywords: None
References: None |
Problem Statement: Can I use the available icons of unit operations in Aspen Plus for models I built in Aspen Custom Modeler (ACM)? | Solution: If you want to use the icon of a unit operation model in Aspen Plus for your ACM model, you can attach the ‘Dynamics’ library to your ACM simulation file and then copy the icon you want to use from the ‘Dynamics’ library models and paste it on the ACM model folder.
1) Attach the ‘Dynamics’ library to your ACM simulation file.
2) Double-click on the unit operation folder that has the icon you want to use for your ACM model. Right-click on the icon and select the ‘Copy’ option.
3) Paste the icon on your ACM model folder. Once done, you may right-click on the occurrence of the ACM model on the flowsheet and select the ‘Exchange Icon’ option.
Keywords: Icons, Aspen Plus, ACM, Unit Operations, Dynamics, Library, Attach.
References: None |
Problem Statement: How can you view the list of controllers in the simulation when using Aspen HYSYS Dynamics? | Solution: The list of all the controllers installed in the simulation are summarized in the Control Manager. This can be accessed from the Dynamics ribbon tab, in the Tools group.
The controllers are grouped as PID, MPC, DMC, Ratio and Split controllers by individual tab. The user can change the controller mode (Off, Manula, Auto) and setpoint values directly from the control manager. The controller can also be opened by a left mouse double-click on the controller name. The control manager makes it easier to access each controller in a complex flowsheet containing a large number of controllers.
Keywords: Control Manager, Dynamic Simulation, Controller
References: None |
Problem Statement: Is it possible to print a plot directly from a stream analysis in Aspen HYSYS? For example, the Dew point and Bubble Point curve from the Envelope Utility? | Solution: Utility plots are not accessible through report manager data sheets. To print a plot from one of the utilities in Aspen HYSYS, open the stream analysis and select Print Plot after right clicking on the plot area.
Keywords: print, plots, chart, graph
References: None |
Problem Statement: I observe Aspen Petroleum Scheduler crashing, what should be checked? | Solution: When APS is crashing some of the following options could be involved, please try the following suggestions and if that does not solves the issue create a dump file following the instructions in KB Article How do I collect a crash dump for aspenONE Engineering Products? That can be found in this link https://esupport.aspentech.com/S_Article?id=000031299 , and contact support to send the gathered information.
Excel Add-Ins and Office dll files that can make APS crash when they are not properly installed.
Some excel Add-ins are known to make APS crash, if a crashing behavior is observed try to deactivate all excel Add-ins.
Microsoft dll that are related to VBA can make APS crash when they are not properly installed or have multiple versions installed and register, for example FM20.dll can have multiple versions installed and registered. This is known to make APS crash.
Office Installation has been changed or deleted. If office has been upgraded or reinstalled or somehow modified, please make sure that the installation is properly set and that the requirements are met, you can check the supported platforms for the supported versions of APS in this link http://home.aspentech.com/en/platform-support. Once you have make sure the requirements are met and the installation is properly done please reinstall APS.
Operative System has been updated or reinstalled, if the OS has been upgraded or reinstalled or somehow modified. please make sure that the installation is properly set and that the requirements are met, you can check the supported platforms for the supported versions of APS in this link http://home.aspentech.com/en/platform-support. Once you have make sure the requirements are met and the installation is properly done please reinstall APS.
Note: Is important to send the following information to support:
APS version you are working with.
Clarify if this is a recent installation or if APS was working properly before observing the crash.
Please consult any of the suggested changes with your IT Personnel.
Operative System version you are currently working with.
Office Version installed in the computer that is presenting the crash.
Keywords: None
References: None |
Problem Statement: Why regressed reaction parameter is out of bound while regression converges? | Solution: The reason is that, In Data Fit, the regressed reaction parameters unit is same as the Global unitset of the simulation case.
For example, here the range and unit of activation energy is 20-30 and Kcal/mol, respectively.
However, when the regression is converged, the value of regressed activation energy is 44468.5 which appears to be out of range of 20-30. The unit of this regressed parameter is by default English (Btu/Ibmol). Please note that 44468.5 Btu/Ibmol is equivalent to 24.7 Kcal/mol.
Key Words
Data Fit, Activation Energy, Regression, Unit
Keywords: None
References: None |
Problem Statement: How to link a user subroutine dll file into Aspen Plus file? | Solution: Please follow the steps to connect a dll file into Aspen Plus file:
Please create a note pad file with a “.opt” extension. In the note pad file, please paste the link of the dll file location. Here in the screenshot the dll file and note pad file is in the same folder named “User routine Link”
Then open the Aspen Plus file and please go to Settings > Linker Option , and paste the path of the “.opt file”. Then please hit “Apply” > OK.
Key Words
User Subroutine, dll, Aspen Plus
Keywords: None
References: None |
Problem Statement: How do I Modify the Aspen Online (AOL) Engine Execution Cycle for an Aspen Plus Equation Oriented (EO) Project? | Solution: The cycle time for the Aspen Online engine is the time between 2 model execution cycles. Once the Aspen Online evaluates that the plant is steady, the AOL engine will begin the model execution.
Users can control the duration between each model execution cycle thereby controlling how frequently the optimizer is run. This can be done via Project Configuration| Models| EO Options| Ramp tab.
Line-out period – this sets the duration between cycles for an optimization model if the optimization set points are implemented
No ramp wait time – this sets the duration between cycles for the model if the optimization set points are not implemented
As shown in the screenshot above, the No ramp wait time is set to 5 minutes. As a result, the model execution from start of cycle 1 to start of cycle 2 is 5 minutes (15:38:35 to 15:43:40)
If this number is not changed, the default interval between execution cycle will be 2 minutes if set points are implemented and 1 minute if not. For Sequential Modular projects, Aspen Online provides functionality to schedule the model runs based on either time interval or specific number of runs.
Keywords: AOL, no ramp wait time, Line-out period, model cycle time, execution delay
References: None |
Problem Statement: Why does the Vapor Percent level is shown as 100% for Vessel Holdup calculations? | Solution: Vapor percent level is like a level gauge measurement. Each phase percentage level is estimated as the level from the bottom of the vessel.
So if there is vapor, it will be 100%.
Keywords: Vessel, Dynamics, Holdup, Percent Level
References: None |
Problem Statement: How to run a case study in Aspen HYSYS | Solution: 1. In the Home tab, select the Case Studies option and click on Add
2. In the Variable Selection Tab, add the independent and dependent variables by clicking the respective Find Variables option to open the variable navigator. You can also drag and drop the desired variables from any HYSYS stream or unit operation.
3. In the Case Study Setup tab, specify the range of the independent variables as mentioned in the following article How can I specify specific sets of conditions when running a case study? and click Run.
Note: If you uncheck the Reset after run option, the values given to your independent variables will be the values used in the last run of the case study.
4. To see the results, click on the Results tab or click the Plots tab to obtain them in a graph.
Keywords: Case Study, Independent, Dependent, Variables
References: None |
Problem Statement: How To: See the Aspen OnLine (AOL) Simulator Model run from the GUI instead of Simulator Engine using AOL Interactive Service | Solution: The Aspen OnLine Windows service executes the simulator model from the simulator engine and therefore runs the model in the background. If the model fails to run, users can set Aspen OnLine to run the model interactively from the GUI by using the Aspen OnLine Interactive Service. This can be used as a troubleshooting aid.
1. Close any open Aspen OnLine Project client GUI – unload the data server (steady state detection {SSD})
2. Go to Local Services and stop the Aspen OnLine Service
3. Go to C:\Program Files (x86)\AspenTech\Aspen OnLine VX.X and locate the AOLServiceInteractive.exe executable
4. Right-click on the AOL interactive service executable and run as Administrator
5. Launch the Aspen OnLine GUI and open the project you want to run
6. Load the SSD and then the Aspen OnLine engine
Now the project and model execution will be interactive. In the snapshot below, the process model is in Aspen Hysys Dynamics and the interactive service allows us view the model running and the strip charts updating in real time:
To stop running in interactive mode, unload data server, close Aspen OnLine client GUI, exit interactive service GUI, restart Aspen OnLine local windows service then open your AOL project as usual.
Keywords: AspenOnline Interactive service, Aspen OnLine client gui, interactive service
References: None |
Problem Statement: The Submodel Calculator (SMC) allows you to simulate one or more Aspen PIMS submodels independently of the rest of the model. After specifying the necessary variables and the properties to square the resulting matrix, it will calculate the rest of the variables and report total activities.
Common applications of this tool are Aspen PIMS model tuning and generation of submodels simulation files for Aspen ORION.
Another possible application is to allow process engineers to analyze the material balance generated by Aspen PIMS for a given unit and compare it to the data from other sources. In this case, it is probably best to use SMC either from within Aspen PIMS or through automation (to provide a customized user interface), as the rest of the model is not relevant for this kind of analysis.
How can you run SMC through VBA automation? | Solution: Attached is an Excel File configured to run SMCthrough VBA automation. The input SMC file is called SKHT.smc and is a representation of the Aspen PIMS Volume Sample model SKHT unit.
Note 1: The VB Code is in Module1. Use Alt-F11 to go directly to the VBA macro editor to review it or edit it.
Note 2: Experience with VBA is required to modify or edit the code. AspenTech does not provide support on VBA.
To run this example:
Open the file PimsSubModelCalculator_SKHT.xls.
Select Enable Macros; if you want to save changes select No when asked whether to open as Read-Only.
In sheet Input, make sure that in cell A2 the path points to a current Aspen PIMS model (it does not have to be the Volume Sample model).
In cell A12, enter the full path to the submodel calculator file, including the .smc file name.
In cells B15, B16, enter the input data (SUL of KHT feed, KHT Feed flowrate).
Click the Execute PIMS VBA Macro
The results will be written to Sheet Output in the same format as the original SMC output. If you want to totalize feeds and yields for example, you have to add some logic in MS Excel (SUMPRODUCT() function or better, in VBA. An example of possible Ms Excel logic to clarify the results is shown in columns H to M.
Relevant VBA Code explanation:
You have to define an InputRowColumnValuesArray(1, 2) As Variant: (1,2) indicates two sets of input data, with 3 pieces of data each (starts from 0). An OutputTableValuesArray(0, 0) As Variant is also required to store the output data.
For this particular SKHT.smc file, only two input values are required:
Sulfur of the feed: first you need to identify that the SUL is the matrix coefficient of the intersection of row ESULKHT and column SKHTKE1, indicated in the first two InputRowColumnValuesArray(0, 0) and (0, 1) variables. The actual SUL value is taken from cell B15 in the Input sheet and multiplied by -1, [Range(B15) * (-1)]
KHT Feed Flowrate: This is represented by the activity of column SKHTKE1, therefore you have to specify the variable InputRowColumnValuesArray(1, 0) = ActivityRow. The input value is taken from cell B16 in the Input sheet.
The simulation of the SMC file is done using the Aspen PIMS VBA Automation function EvaluateSubmodelCalculator(), as indicated below
The results are written by looping through the Output values Array. With the structure below, you don't need to know beforehand how many rows and columns are in the results.
To adapt this report for another SMC file:
Open the relevant Aspen PIMS model, go to Model | Data Assistants | Submodel Calculator, select the submodel(s) that you want to include (to select several units, use Ctrl + the submodels).
Click the Resolve button, so that it will import the relevant property values.
Square the matrix, i.e. define the necessary column activities (blue cells in first row) so that you have an equal number of columns and rows.
Once the matrix is squared, click Calc: the resulting column activities will be shown.
Go to File | Save As and save it as an .smc file. This will be your input file for the report.
In the VBA code, adjust the InputRowColumnValuesArray(ROW, COLUMN) section to capture all the relevant input information, i.e. change the names of the relevant rows and column, add additional input arrays, etc.
Keywords: Submodel Calculator
VBA Automation
EvaluateSubmodelCalculator()
smc file
References: None |
Problem Statement: Why do some values in my datasheet/report have an asterisk next to them? | Solution: The asterisk indicates that the value is user specified, rather than calculated by HYSYS. (In HYSYS these numbers show blue rather than black). To turn off this feature press the Format/Layout button on the Report Manager window (if printing a report) or Select Datablock window (if printing a single datasheet), and then uncheck the 'Indicate User Specified' checkbox.
Keywords: Asterisk, Indicate User Specified
References: None |
Problem Statement: Automation GetOrionDataCache fails after selecting option Export Blends in Menu Simulate| Publish | Export Blend | Solution: Automation GetOrionDataCache fails after selecting option Export Blends in Menu Simulate| Publish | Export Blend
This is by design. Export Blends is related with blends only. We are doing a simulation with blend event time periods only and are not taking other time periods into account. Hence GetOrionDataCache values will not be correct if it is maintained for Streams. Simulate All needs to be done with memory on cache on to establish proper results.
Keywords: None
References: None |
Problem Statement: How do I add new attributes on a datasheet? | Solution: To add a new attribute on a datasheet:
1. Open the Datasheet Definer, connect to a workspace and open the datasheet you want to add an attribute in (e.g., 'AZ Shell and Tube Heat Exchanger').
2. Click on the Datasheet button and go to the Class Views tab to check the Object Class View name (e.g., ‘PIP VEDST003’ for Shell and Tube Heat Exchanger). Close the Datasheet Definer.
3. Open the Class Library Editor application. Open the Class Library from: WorkspaceLibraries\DataModel folder.
4. Expand the Included Libraries folder from the Workspace pane, go to the Class Views folder and search for the Class View specified in the Datasheet Definer (‘PIP VEDST003’).
5. If it exists, expand the node you want to add the attribute in, right-click on the first attribute listed and select the Insert Attribute Before option.
6. Enter a name for the attribute and click on OK.
7. Select any attribute from the listed below, (e.g., ‘SizeBundleDiameter’) right-click on it and select Open ShellAndTubeHeatExchanger to open the Composite View linked to this Class View.
8. In the Composite View window, add an attribute following the same procedure described in steps 5 and 6.
9. The new attribute will also have to be created in the Class level. Open the ShellAndTubeHeatExchanger class (right-click on any attribute from the composite view level and select the Open ShellAndTubeHeatExchanger option) and insert an attribute. Now, the new attributed is created in the Class View, Composite View and Class levels.
10. Once you have created the attribute in these three levels, go to the Class level, select the attribute and drag and drop it to the same attribute from the Composite View. After that, select the ‘Synchronize All’ option. The Class attribute will be mapped against the Composite View attribute. Do the same to map the Composite View attribute against the Class View attribute.
11. Save the *.azcs file replacing the original one. Accept the option for checking for errors.
12. Compile the Library by clicking on the ‘Make Class Store’ button.
13. Reload the workspace from the Administration application and open the Datasheet Definer. Connect to the workspace and open the datasheet.
14. Highlight the field you want to add a new attribute in, click on ‘Add – Value’.
15. Map the value against the new attribute created from the CLE by clicking on ‘Field | Browse’. Change the View to the Class View the new attribute was added in (e.g., ‘PIP VEDST003, Page1, NewAttribute’).
16. Save the *.xlms file in the WorkspaceLibraries\Datasheets folder and click on Generate Template, saving the *.zft file in the WorkspaceLibraries\Templates folder. Reload the workspace from the Administration application.
17. Open the datasheet in the Datasheet Editor and find the new field defined for the created attribute.
Keywords: Attribute, Datasheet, Class Library Editor, Class, Class View, Composite View, Compile.
References: None |
Problem Statement: What are the color coding represent in the spreadsheet in Aspen Plus? | Solution: Below are the color coding representation in the spreadsheet:
Italic blue values are default values in input fields where you have not entered a value
Bold blue values are values you have specified
A bright blue outline indicates the field you are currently editing
Black values are results or non-editable values
Gray values on a light gray background are disabled because of other specifications
Keywords: Aspen Plus, Color Code, Spreadhseet
References: None |
Problem Statement: How do I export column hydraulics results to KG-Tower? | Solution: First, please make sure that both Aspen HYSYS and KG-Tower are installed on the same computer.
In Aspen HYSYS V8.8 and older versions, the ‘Tray Sizing’ utility is available to perform design and rating calculations for trayed / packed columns. All you need to do is to click on the Tray Sizing | Export | Export to KGTower button, then select the trays to be exported, as well as the KG tray / packing information. Next, click on the ‘Export’ button as shown below:
The KG-Tower application might not be automatically launched. However, a ‘.kgt’ file should be generated in the save path specified (as shown in the image above). This ‘.kgt’ file should open in KG-Tower.
Now, as of Aspen HYSYS V9 onwards, you cannot create ‘Tray Sizing’ objects, instead we recommend the ‘Column Analysis’ tool to perform column hydraulic calculations. Click on the Column Analysis | Export to Vendor button and select the column sections to be included in the exported ‘.kgt’ file, as shown in the image below:
Keywords: KG-Tower, Hydraulic Results, Tray Sizing, Column Analysis.
References: None |
Problem Statement: Is there an example of a script to retrieve stream’s properties for an equipment using the Query Editor in Explorer? | Solution: The attached file contains an example script which can be used in the Query Editor in Explorer to retrieve mass flowrate.
The starting point to test the script is to put a Process Vessel on a PFD, connect two streams and give each stream a total mass flowrate (e.g. via a mass balance insert). This script considers the data in CaseID 4, so you may need to change or remove the CaseID in lines 59, 67, 68 and 74). You will also need to update the script to put the OID of your vessel in line 16. The file can be edit in Notepad++ to find the line numbers.
The purpose of the script is to report some properties of the streams attached to the vessel. It loops through each stream in the “TerminatedPipingSystems” attribute of the vessel and assigns each object therein to a variable called Stream. Then try to retrieve properties of the object in the Stream variable.
Keywords: Script, Query Editor, Stream’s Properties, Example File.
References: None |
Problem Statement: How do I create a continuous equipment list in ABE? | Solution: Continuous Equipment Lists are similar to Summary Sheets, but they list the information for all class members in a continuous list on a single page, instead of generating additional pages to contain all the related information.
1. Open the Datasheet Definer aplication and connect to a workspace. Create a new workbook from 'File | New | Blank worbook'.
2. Click on the 'Datahseet' button and enter a name for the continuous list. Change the 'Use' option to 'Summary'.
3. Go to the Class Views tab and choose the Object Class View for the document.
4. Add a value field and map it against the 'Item Number' attribute from the 'Field' option.
5. Define the rest of attributes as needed in the continuous list.
6. After mapping all the attributes, select one by one and define a wildcard for them by clicking on the 'Set Object' button.
7. Click on the 'Set Repeat Area' button under the Editing section and highligh the repeating fields as well as the expansion direction.
8. Save the *.xlms file in the WorkspaceLibraries\Datasheets folder and click on 'Generate Template', saving the *.zft file in the WorkspaceLibraries\Templates folder.
9. Reload the workspace and open the Excel Datasheet Editor. Open a continuous list. You will see all the objects from the defined Class View populating the list. Try adding additional objects by typing in the last 'Item Number' row. It should create the object and add an additional row to the list.
Keywords: Continuous List, Set Repeat Area, Attribute.
References: None |
Problem Statement: What is the difference between the two options for Characterizing Assay? | Solution: The Characterize button has two options for conventional characterization for input assays:
Match Assay Cut Properties which is the the Default option, will use all the available data during the characterization, but properties of product cuts are matched most closely. This implies that whole crude properties may not be matched. This option is used when characterizing assay data that contains a self-consistent set of properties for the whole crude, as well as for all the product cuts. For example, when entering a new set of crude assay data or updating an existing crude with new complete lab assay analysis.
Match Whole Crude Properties option, all the available data is used during the characterization, but properties of the whole crude are matched most closely, thus sacrificing the accuracy of the product cuts.
Keywords: Petroleum Assay Manager, Characterize, Match Assay Cut Properties, Match Whole Crude Properties
References: None |
Problem Statement: How Eventscoll Automation codes are used with Pipeline Events | Solution: You can use Orion.Eventscoll object to expose different methods, this methods can be applied to different types of evets, for example, Pipeline Events. You can find attached a workbook with the following automation examples:
Create PL Crude Receipt
Create PL Crude Shipments
Create PL Product Shipment
Keywords: None
References: None |
Problem Statement: In Aspen Petroleum Scheduler and Aspen Multi-Blend Optimizer, how to define different categories to group User Tools, how can I reassign a Tool to a different category and how to rename a category? | Solution: This Tech Tip provides a description on how to define different categories to group User Tools, how to reassign a User Tool to a new category and how to rename a category.
For this example, we will use the demo model located in C:\Users\Public\Documents\AspenTech\Aspen Petroleum Scheduler\Demo\Access
The next steps are to add a new Tool in a New Category
Right click on User Tools and select the option Add New
In this case I will select an AccessFunction command type though it can be done for the other types, fill all the required information. Then click on Ok.
The result will be shown as follows:
The following steps are to reassign a Tool to a new category, note I have added a second test function.
Select the tool you want to reassign and right click on it, then select the option Properties as shown
In the category section add the new category name
The result will be as follows:
How to rename a Category
Make sure the category you will rename only have one Function as in this example, then right click on the Function and Select Properties as show
In properties you require to change the Category Field to the new name in this case I will name it New Category Rename
The result is as shown
Note: If you only have one function assigned to a category and you reassign it, the category will be automatically removed.
Keywords: None
References: None |
Problem Statement: What is the effect of the submerged surface area on the heat transfer coefficient for a shell side condenser? | Solution: First, we should review the impact of the submerged surface area on heat transfer. Upon increasing the submerged surface area, the vapor mass flux increases (most of the times only slightly) due to a reduction in the vapor phase flow area. However, the result of this change in the vapor mass flux on the overall shell side heat transfer coefficient (HTC) is not that direct.
The overall HTC is the combination of the vapor single-phase term, liquid single-phase term, condensate shear term and gravity condensate term, all together. The most direct effect is on the condensate shear term, which will increase by an increase in the vapor mass flux (caused by more submergence).
On the other hand, we also have the effect of the mixture mass transfer on the shell side HTC. An increase in vapor mass flux (due to an increase in submergence) will increase the mass transfer resistance, and as a result it will reduce the overall shell side HTC.
Thus, we have a couple of counter-affecting factors that make a conclusion difficult. Depending on the significance of each of the above mentioned factors, the shell side HTC may increase or decrease by changing the submerged surface area.
For more information you can consult the following KB articles:
How to fix operation warning 1325? Also applicable to operation warning 1326 and 1327
How to interpret Operational Warning 1325 is regarding how Aspen Shell & Tube Exchanger?
Keywords: Submerged surface area, heat transfer coefficient, shell side condenser
References: None |
Problem Statement: How to reload simulator and simulate all in APS V11 and other versions? | Solution: First, log into your APS model. Make sure that you have already done DB update before you attempt to open the db. If not, please refer to KB article 1548.
Make sure to point to the correct folders for: dlls, smcs, ubml, and Units.xls. Or otherwise the simulation will run into errors.
Check model settings or look at Gantt chart to decide on model start date:
Navigate to simulator -> reload simulator. You will need to wait for a while depending on the size of the model and how complicated the external tools and automation are.
After reload simulator is finished, click on simulate all, and it will simulate everything for the next 30 days in your model. It will show you a dialog box with how much percentage the model has simulated. Wait for the percentage to go to 100% and data will be written back to Excel.
After that, you can see the trends change in the large & small trend charts.
Keywords: None
References: None |
Problem Statement: How to run database upgrade script against your SQL server database APS/MBO model? | Solution: This is a continuation of KB article 1548. You need to perform DB update first for your SQL server model. This article is a detailed explanation for step 7 in that article.
First, restore the SQL database by following detailed steps in another KB article “How to restore SQL server database for an APS/MBO model?”.
After you have restored the database and generated the .dsn file, we are ready to upgrade the database schema. Please follow the steps listed in KB 1548.
After you validate your database, and clicked update, on the right-hand side, you are going to see “Please run the script on the database to complete update”. Now we are going to find that SQL script and run it against our desired database. This is step 7 in KB 1548.
Find the SQL script in the file path in the red text. In the example above, it says the db update script is located on my desktop and called DBUpdate.sql. Lets un that script and update the database:
Make sure to choose the correct database to run against. On the top left corner, there is a drop down menu to let you choose which database you want to run the script against. In my example, the database is called “BP_Whiting_Production…”.
Press F5 to execute the script after you choose the correct database.
If there are no errors, then the update should be done. Go back to new version of APS and open the model. You will be able to open it.
Keywords: None
References: None |
Problem Statement: What are the general steps to check if event reconciliation is the same in V11 compared to old versions? | Solution: Petroleum Scheduler calculates the difference between the simulated and the measured tank volume at the end of reconciliation period. If this difference exceeds either the absolute or the relative limit, the trend of the tank volume will be highlighted. The measured and simulated tank volume may differ significantly at an earlier time and will not be considered out of balance as long as the two volumes converge at the end of the reconciliation period.
In performing event reconciliation, you should split the events that cross the end time of the reconciliation. If this is not done, Petroleum Scheduler assumes that the error is the same in the portion of the event past the end of the reconciliation period.
For example, if half of an event extends across the boundary and the error is 1000 bbls, then Petroleum Scheduler will assume that there is another 1000 bbls of error associated with the other half of the event on the other side of the boundary.
There are two ways Petroleum Scheduler tries to adjust the event volume to achieve a match of the volume at the end of the reconciliation period.
First method – lump the difference into the last event
Second method – attempt to determine the beginning and the end of the events from the plant dataFirst Adjustment Method
In the first method where the error is lumped into the last event, if the last event cannot accommodate this error or has been marked as reconciled, Petroleum Scheduler will lump the remaining error into the next to the last event. This process continues until the entire error has been accounted for or all the relevant events have been exhausted.
Second Adjustment Method
In the second method, the data must be sufficiently dense to provide several points between each event. Also the noise in the data must be smaller than the tolerances provided. Use the filter tolerance to help Petroleum Scheduler parse the plant data into events. If there are missing events or events not in the correct order in the model, the algorithm will not be correct. In this case, you should manually override the values generated by Petroleum Scheduler or use the lumping method instead.
Follow the below steps to perform event reconciliation:
To perform event reconciliation:
From the Model Accuracy node on the model tree, right-click on the desired tank reconciliation screen.
Select Event Facilities to access the Event Facilities Manager dialog box to add trends to the tank volumes to be reconciled.
Click OK to return to the Model Accuracy Interface.
Run event reconciliation by clicking on the toolbar.
Alternatively, click Reconcile | Auto Reconcile | All Tank Trends.
The Simulating dialog box appears indicating reconciliation is occurring.
Select all the events on the Gantt chart.
Right-click and select Multiple Event Editor to view the changes.
Manually override the calculated values as needed.
Select the Rec option to prevent Petroleum Scheduler from recalculating the values, if desired.
Keywords: None
References: None |
Problem Statement: When I include overtime in the general rates, it adds extra hours and dollars.
When I manually input overtime as a library item, it adds the dollars in.
If overtime is input in the general rates, would it be double-dipping by putting in extra hours and dollars? Or is Icarus simply showing what the extra hours are and calculating the dollars in the overtime section? | Solution: When you include overtime in the general rates, it adds extra dollars and labor hours by design. When you input overtime as a library item, only dollars are added.
Therefore, if you input overtime in both general rates and as a library item, it is not double-dipping as the Icarus cost engine does not take into account user entered costs (library or quoted items).
3 things to remember concerning overtime:
1. The default overtime is set to 0 hours.
2. The default standard work week is 40 hours.
3. Overtime rate percent standard = 150% (time and a half).
Here is how the Icarus cost engine generates the overtime rate:
((standard time rate + overtime rate)/ total number of hours) = total overtime rate.
For information on how Icarus Calculates the Overtime Premium, please refer to the Icarus User's guide, Chapter 3
How IPM Calculates the Overtime Premium
The overtime premium formula uses the following variables:
A - Hours, Direct Field Labor
B - Average Craft Rate
C - Overtime Rate (% STD) as set in General Wage Rates
D - Work Week per Shift, Overtime (hours)
E - Work Week per Shift, Standard (hours)
F - Overtime Premium
The overtime premium formula is: F = A * B * (C-1) * (D / (E + D)).
Here is how overtime works:
The overtime rate percent standard (C): Specifies overtime pay expressed as a percentage of standard pay (for example, time and a half = 150%).
Keywords: overtime, over time
References: None |
Problem Statement: How to verify Aspen PIMS has been successfully installed? | Solution: This Tech Tip provides a description of the check points to review and ensure that Aspen PIMS was installed successfully.
Open PIMS, from Start Menu in your computer Open PIMS
Open a PIMS Model
a. PIMS AO Sample Model Once PIMS is opened, go to Menu Model| Open…, then select a DR Sample Model. browse the following address C:\Users\Public\Documents\AspenTech\Aspen PIMS\Pims\Volume Sample make sure that the AO Icon is enabled
b. PIMS DR Sample Model, Once PIMS is opened, go to Menu Model| Open…, then select a DR Sample Model. browse the following address C:\Users\Public\Documents\AspenTech\Aspen PIMS\Pims\Volume Sample make sure that the AO Icon is not enabled
Run a Model
Run Sample Models to verify they can be properly opened.
Run a Sample AO Model,
Repeat the actions described in step 2.a.
Click on Model Execution Icon , or press F5 key.
Make sure Stack All Cases is selected as in the following image then click Ok
The following Result should be expected, the Optimization Process Overall Progress should be completed, any other behavior is not expected and should be addressed. Note that is important to run at least 3 cases.
ii. Run a Sample DR Model
1. Repeat the actions described in step 2.a.
2. Click on Model Execution Icon , or press F5 key.
3. Make sure Stack All Cases is selected as in the following image then click Ok
The following Result should be expected, the Optimization Process Overall Progress should be completed, any other behavior is not expected and should be addressed. Note that is important to run at least 3 cases.
b. Run your model to verify it can be properly open.
Report Writer Installation
1. Report Writer is an Add-In that will be helpful for pulling information from Results DB, is important that this Add-In is properly installed to check that this is installed open an excel file and make sure that you can observe the ADD-INS tab as in the following image:
General Recommendations
If any of the above mentioned behaviors are not observed is important to properly attend the problem.
If you have any question on these steps contact support for assistance.
Keywords: None
References: None |
Problem Statement: When registering a project from a previous version of Aspen OnLine in V10, if the project name contains a hyphen or other special character, the migration may fail with error [Microsoft][ODBC Text Driver] Syntax error in FROM clause. | Solution: Aspen OnLine uses Microsoft database technology, and certain special characters are not supported. AspenTech recommends only using alphanumeric characters for project names and beginning all project names with a letter.
Rename the project folder using only alphanumeric characters, then repeat the registration process.
Keywords: AOL, ODBC text driver, error
References: None |
Problem Statement: Why is the API[Petrol] giving different results compared with the API density reported in the stream properties? How is API[Petrol] calculated? | Solution: Mass density may be displayed in API units (please refer toSolution 116594), but the value reported will not match with the API[Petrol] value. The [Petrol] designation indicates that the property is calculated using Aspen HYSYS Petroleum Refining. The reason the two representations of API gravity are not the same is due to the different calculation methods used for each property.
The API mass density (100.7 in the screenshot above) is calculated with the following expression:
API = 141.5 / SG (actual conditions) - 131.5
where SG (actual conditions) is the specific gravity at the stream temperature and pressure
While the API[Petrol] (75.02 in the screenshot above) follows this equation:
API = 141.5 / SG (60/60) - 131.5
where SG (60/60) refers to the mass density of a liquid at 60 F over the mass density of water at 60 F (based on the API definition).
Note the SG (60/60) property may be added from the Petroleum section of the Correlation Picker.
As a result, API[Petrol] is independent of the stream conditions and will only change due to compositional differences. On the other hand, the API mass density is reported at process temperature and pressure and will change according to the current stream conditions.
Keywords: API, Petrol, Refsys, molecular weight
References: None |
Problem Statement: How can add / attach libraries to Aspen Custom Modeler (ACM)? | Solution: Libraries can be attached to ACM on two different levels:
1) Local Level: On the Simulation Explorer, left-click on the ‘Libraries’ folder. Next double-click on the ‘Open Library’ icon (on the ‘Contents of Libraries’ pane). Now browse to the location where the ACM library (*.acml file) is located and click on the ‘Open’ button.
The recently added library will only be available for the simulation file you imported it into, but if you either start a new ACM model from scratch or open another existing model, the recently added library will not be available.
2) Simulation Level: Go to the ‘Tools’ menu on the ribbon and click on the ‘Settings…’ option (at the very bottom of the list). Next, go to the ‘Libraries’ tab and browse to the location where the libraries you want to attach to new simulations is located.
The recently attached libraries will be available for all new ACM models and can be removed if desired on the same dialog.
Keywords: Libraries, Add, Attach, Local Level, Simulation Level,
References: None |
Problem Statement: How can I set up the Windows compatibility mode of the ABE applications? | Solution: Users may set up the Windows compatibility mode of all ABE applications to run for, which is not mandatory but might turn out to be convenient to avoid that problems arise when attempting to use, for example, the ABE Excel-based applications (e.g., Excel Datasheet Editor).
To do so, go to: C:\ProgramFiles\AspenTech\BasicEngineeringVXX.X\UserServices\bin.
Note: In the path above ‘VXX.X’ refers to the ABE version you have installed on your machine (e.g., V10.0, V11.0).
Right-click on the ABE *.exe file for which you want to set the Windows compatibility mode (e.g., ‘AZExplorer.exe’) and click on the ‘Properties option’.
On the ‘Compatibility’ tab, under the ‘Compatibility mode’ section, check the ‘Run in compatibility mode for:’ box and select the Windows version you want the ABE application to run for.
Keywords: Windows Compatibility Mode, Aspen Basic Engineering, ABE, Applications.
References: None |
Problem Statement: After migrating to a newer version, or run the same model on a different machine, how do we transfer the Gantt chart preferences in an event screen of an APS/MBO model from the old machine to the new one? | Solution: Unfortunately, the Gantt Chart preferences settings are not stored in any of the APS/MBO database tables. It is stored in the machine’s registry. Basically, the user needs to export the registry settings of the Gantt Chart section of the old machine and import to the new machine. Let’s look at how this could be done:
In old version of APS/MBO, log into your model, and edit the “Gantt & Trend Chart Options” on the top left corner of the event screen:
In this example, I changed the Gantt bar thickness from 2 to 8 for better visualizing the events. Feel free to change any other settings in the dialog box.
Next, go to Start -> search regedit, run the Registry Editor and navigate to Orion Scheduling -> Gantt View.
Here, in the Data column, you will see the value that you have changed in the bracket. If you changed anything else from the Gantt chart options, you can navigate to different folders to find exactly what you have changed.
Next, export this registry by right clicking on the folder, and select “export”.
Save it to your machine and open the machine with new version of APS installed and go to regedit:
Import the registry just exported.
Now open APS, you should be able to see your Gantt chart options exactly the same as previous version:
Keywords: None
References: None |
Problem Statement: Are there any guidelines for converting an Aspen HYSYS case from steady state to dynamics? | Solution: Pressure/flow stream specifications are made on the Specs page of the Dynamics tab of any material stream. Dynamic specifications for unit operations are also generally found on the Dynamics tab of the unit operation property view. The following table contains some rules that will help guarantee a consistent, properly specified flowsheet every time.
Dynamic Specifications
Boundary Streams
Insert a valve on all boundary streams (feed/product streams) within the Flowsheet that are not connected to conductance devices (i.e., heat exchangers, coolers, heaters)
Pressure Specifications
Place a pressure specification on all boundary streams (feed/product streams) within the Flowsheet.
Distillation Columns
Distillation columns with condensers require an extra specification around the condenser. Make a flow specification for the reflux flow.
Valves
Use the pressure/flow relationship as the dynamic specification for a valve.
K value
Use the overall K value as the dynamic specification for coolers, heaters, and heat exchangers and LNG exchangers.
Pressure gradients
Be sure to account for pressure gradients throughout the Flowsheet. Moreover, be sure to specify reasonable pressure drops/rises in the Flowsheet. Pressure differentials are the driving force for flow through the process Flowsheet.
Column Internals Analysis (New V9.0)
Use the Column Internals Analysis to estimate the column geometry and pressure profile.
Mixers
Use the Equalize All option as the pressure specification for mixers.
Tees
Remove Use Splits as Dynamic Flow Specs on tees.
Rotating Equipment
(Pumps, Compressors, Expanders)
Use Efficiency and either Head or Pressure Rise as dynamic specifications for rotating Equipment. Compressor and Pump Curves, if available, make excellent dynamic specifications.
Hold-ups
Be sure to properly size equipment with hold ups.
Note:
Dynamic specifications can only be modified when the integrator is stopped. Once the integrator is started the value of the dynamic specification can be changed (its value appears in blue), but the choice of dynamic specification cannot be changed.
Keywords: dynamic specifications, sizing, pressure spec, flow spec etc;
References: None |
Problem Statement: Can I connect my Aspen Plus model to ASW if they are from different versions? | Solution: You can have different versions of ASW and Aspen Plus installed on your machine and still connect your process model to ASW.
For example, if you have the ASW V9.0 add-in installed and activated on your machine, and Aspen Plus V10 installed as well, you can still have ASW V9.0 connect to your Aspen Plus V10 model.
What you need to do is to go to the Organizer | Configuration | Simulations form and set the 'Version Option' to 'Exact Version' and type in 'V10.0' right on the 'Version String' field, as shown in the image below:
Basically, you are telling ASW which Aspen Plus version to use to launch the simulation file.
Keywords: Add-in, Organizer, Configuration, Version String.
References: None |
Problem Statement: How to Use DMCplus Model to Create the SmartStep Seed Model? | Solution: Files in this KB are the built-in files that come with DMCPlus installation.
The following dataset is used for illustration purposes and is not based on real plant data.
Use DMCplus to create a model with first order curves for these relationships.
1) Open HGP-SeedStep1.dpp.
2) In the model’s folder you will find model HGPSeed1 which is a skeleton structure for your seed model.
3) For the relationship in the table above, use curve operations to add
a) For steady-state variables, insert a “First Order” model.
b) For the ramp variables, insert a “Zero Model” and then Rotate it to the steady state gain (slope).
When ready, we will skip forward in time
4) Close the project.
5) Open HGP-SeedStep2.dpp. This is the completed seed model with all relationships entered.
6) Examine to model and then export the model as HGPSeed1.mdl.
7) Close the project.
Keywords: DMCPlus, Seed Model, SmartStep
References: None |
Problem Statement: What is the procedure of creating custom calculations using Aspen Watch Maker? | Solution: 1) Launch Aspen Watch Maker via either the link pinned to the Start menu or Start | Programs | AspenTech | Aspen Manufacturing Suite | APC Performance Monitor | Aspen Watch Maker.
2) Select Tools | Tag Maintenance… to bring up the Tag Maintenance window.
3) Add Tag button to add the Aspen Watch Tags using the DCS Tag names as the I/O Address. Make sure all of the tags are getting a value. Then press OK to exit the Tag Maintenance window.
4) Select Tools | Group Configuration… to bring up the Group Configuration window.
5) Press New, enter a group name (for instance “HGP”) into the New Group dialog box, and press OK.
6) Select any tag specific to the HGP unit that can be either under Miscellaneous Tags or PID Loops, then select an Available Tag and “move” it into Selected Tags.
7) Press Save to save your configuration.
8) Repeat this as needed.
9) When finished, press Close to close the Group Configuration window.
10) Select Tools | Custom Calculations… to bring up the Custom Calculation List window.
11) Select New to bring up the Custom Calculation Configuration dialog window.
12) Set these values:
i) Application: Tag Group: <name>
ii) Name: TOTALPROFIT
iii) Abbrev: TPR
iv) Scope: General
v) Method: Average
vi) Alarm Type: Alarm-Low-Percent
vii) Priority: Low
viii) Description: <enter something appropriate>
13) Press Edit… to launch the Formula Configuration dialog window.
14) Enter the formula into the Formula box in the Formula Configuration dialog window. For example, the below formula can be used with the built-in DMCPlus column.
DC3Top * DC3TopPrice + Tank1Flow * Tank1FlowPrice – DC2Feed * DC2FeedPrice – DC3Steam * 24 * DC3SteamPrice + (DC2Vent + DC3Vent – Furn1Fuel * 0.28 * 24) * 0.18 * FuelGasPrice
15) Press Test to populate the List of variables. Try changing values for the variables in the List of variables to verify that the correct result is being calculated and shown in Result.
16) Press OK to close the Formula Configuration dialog window and return to the Custom Calculation Configuration dialog window.
17) Click anywhere in the first row under Variable Binding to launch the Variable Binding dialog window for the first variable.
18) Set these values:
i) Application: PID Loop
ii) Category: Attribute
iii) from the Variable/Tag list, select: FC-D3TOP
iv) from the Attribute/KPI list, select: PV
19) Press OK to close the Variable Binding dialog window
Keywords: Custom calculation, Aspen Watch
References: None |
Problem Statement: How can we change the working folder when ACM models are stored on a drive with no write privileges? | Solution: 1 - Start up the Windows registry editor. To do this go to the Windows START button, click on RUN and then type REGEDIT in the dialogue text box.
2 - Once the registry window opens, find the registry key:
Computer\HKEY_CURRENT_USER\Software\AspenTech\Aspen Custom Modeler\36.0\Simulation
3 - Change the value for the WorkingDirectory to a location where you have write privileges and close the registry.
4 - Start ACM.
Note 1: If you want to keep the acmf file in a folder where you don't have write access (not advisable), Go to the TOOLS pull-down menu in ACM, click on SETTINGS | PREFERENCES and select allow setting the working folder, and then Go to the FILE pull-down menu and click on SET WORKING FOLDER. Change the working folder to a place where you have write access.
Note 2: If you want to keep the ACMF file in a folder where you have write access, then no other changes are needed (or simply uncheck the allow setting working folder option if it is checked - by default this is unchecked).
Key Words:
Working Directory, acmf
Keywords: None
References: None |
Problem Statement: How to add a User Tool/ Interface in APS for ease of access of the Scheduler? | Solution: In APS , the Scheduler needs to sometimes refer external applications like a calculator/report/any other custom utility.
In order to do this, the Modeller/ Administrator can assist in adding this Tool in APS.
In the APS GUI, on the left hand side there is a navigation pane , in the navigation pane, there is a section named as Tools
These user -defined tools (commands) are macros, functions, and executables that can be accessed from the Tree view.
You can add the following types of user-defined tools:
AccessMacro
AccessFunction
ExcelMacro
Executable
Here are the steps to follow:
1)In order to add a utility to this section, there are categories (if predefined)
So click on the Interfaces folder and right Click to Add New Interface
2) In the Tool Properties Window > Click on the command type option and from the Drop down , you can select as Executable if it is a .exe
3) Once the type of file is selected, specify the path of this file that is the Executable file folder.
4) The Description column is for the name of the utility that is seen in APS GUI
5) Once done, click Okay and you will notice that the utility is now a part of the APS GUI
This utility can be invoked at any point of time from the Tools section in APS and user does not have the need to navigate for using this utility from elsewhere.
Similarly other interfaces/reports can be added under the tools section.
Keywords: None
References: None |
Problem Statement: Where can I find CPDIEC Fluid package? | Solution: You could find the CPDIEC in Fluid package form by clicking on Edit Properties edit as
in the below snapshot.
1
Please note that only Electrolyte NTRL fluid package from Aspen Properties could be
used in Hysys to get elements of CPDIEC.
In order to see the FP Electrolyte NTRL, you will need to add the component from Aspen Properties. Then, you will be able to see the Electrolyte NRTL FP in Aspen Properties as well.
Keywords: Aspen HYSYS, CPDIEC, Electrolyte NTRL, Fluid Package
References: None |
Problem Statement: How do I insert rows and columns in the Aspen HYSYS spreadsheet? | Solution: To insert a Row/Column in spreadsheet click on the Edit Rows/Columns on the Spreadsheet tab.
Keywords: Insert, row, column, spreadsheet
References: None |
Problem Statement: I have multiple versions of Aspen Process Economic Analyzer (APEA) loaded on my machine and I want to link a particular version of APEA with Aspen HYSYS. How can I use Aspen HYSYS to load a preferred version of APEA?. | Solution: You have to unregister the version of APEA that you do not want to use and re-register the version you want to open when you link from the HYSYS interface.
If you have both versions 9.0 and 10.0 of APEA on your machine, and you want to link to v10.0 and do not want to link v9.0 of APEA, you have to unregister the APEA v9.0 and then register version v10.0 from the command prompt.
Open the Administrator Command Prompt and type
regsvr32 /u C:\Program Files (x86)\AspenTech\Economic Evaluation V9.0\Program\Sys\AspenIcarusTask.ocx
regsvr32 C:\Program Files (x86)\AspenTech\Economic Evaluation V10.0\Program\Sys\AspenIcarusTask.ocx
Once you unregister one version and register another version, whenever you link APEA from Aspen HYSYS it will link to the registered version.
Keywords: register, unregister, multiple version, Icarus, link Hysys
References: None |
Subsets and Splits
No community queries yet
The top public SQL queries from the community will appear here once available.