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Problem Statement: How do we add Aspen DMC plus online controller to Aspen Watch Maker | Solution: The below procedure describes in details of procedure to add Aspen DMC plus online application to Aspen Watch.
The below procedure needs to be carried out in Aspen Watch server after ensuring both servers are physically able to communicate.
1. From the Windows Start menu, click Programs | AspenTech | Aspen Manufacturing Suite | APC Performance Monitor | Watch Maker (APC)
-or-
o From the Windows Start screen, search for Watch Maker, and then select the Watch Maker (APC) shortcut.
o From the main menu of Aspen Watch Maker, click File | Install Database Configuration.
o Click Yes in the User Account Control dialog to run the Install Database Configuration utility as Administrator, in order to give the script sufficient privilege to run successfully.
2. After the Install Database Configuration utility starts, press ENTER to accept the Yes [Y] default and start the database configuration.
There is very little interaction required, other than deciding whether to continue with the procedure. You may see a significant amount of informational text scroll by if this is an upgrade.
Watch the window for the message Aspen Watch database configuration successfully completed.
3. After the database restarts at the end of the procedure, press any key to exit the Install Database Configuration window.
Also exit the Aspen Watch Maker program.
Note: If you receive an error, look in one of the following files for more information:
o PROGRAMDATA\etc\cfg\awlog.txt
o PROGRAMDATA\etc\cfg\upgrade.out
...where PROGRAMDATA, for typical installations, is...
C:\ProgramData\AspenTech\APC\Performance Monitor.
4. Exit InfoPlus.21 Manager, and then reopen it to update the list of Defined Tasks.
5. Confirm that the following Aspen Watch Performance Monitor tasks are listed under Running Tasks:
TSK_ACP1 TSK_IQ1 TSK_MSC2
TSK_ADAP TSK_IQ2 TSK_MSC3
TSK_ADM1 TSK_IQ3 TSK_PID1
TSK_ADM2 TSK_IQ4 TSK_PID2
TSK_AW01 TSK_IQ5 TSK_PID3
TSK_AW02 TSK_M_IODEV1 TSK_RTO1
TSK_AW03 TSK_M_IODEV2 TSK_RTO2
TSK_AW04 TSK_M_IODEV3 TSK_RTO3
TSK_AW05 TSK_M_IODEV4 TSK_RTO4
TSK_AWTG TSK_MSC1
6. If the Select Data Source dialog box displays, do the following:
o In the Select Data Source dialog box, click the Machine Data Source tab.
o Select the SQLplus machine data source for the local Aspen Watch computer. (The Data Source Name is usually SQLplus on localhost.)
o Click OK.
7. From main menu of Aspen Watch Maker, click Actions | Add...
8. Click Browse, and then navigate to each directory, PROGRAMDATA\app\<appname>, to locate and double-click (see next step) a DMCplus Controller application CCF file, where...
o PROGRAMDATA is located as follows:
C:\ProgramData\AspenTech\APC\Performance Monitor
...and where...
o <appname> is the name of your Aspen DMCplus Controller application.
9. Double-click the CCF file that you want to add to the Aspen Watch database.
10. The Controller Name field is automatically updated with the folder name containing the CCF file.
If the application name differs from the, change the name here.
11. From the Application Type drop-down list, select either DMCplus.
12. From the Collection Task Name drop-down list, select one of the external task names.
13. From the Cim-IO Device Name drop-down list, select the Cim-IO device name that provides access to the Context Cim-IO Server for the selected application. (Notice that the node name is provided for you.)
Then click OK.
14. The Start Collecting dialog box prompts you to start the data collection process for this application.
Click Yes to start data collection.
After starting data collection, it might take few minutes to successfully start collection and eventually, the Run Status should be changed to Success
15. Repeat Steps 7 through 14 for each CCF file.
Keywords: Aspen Watch Maker
Add controller to Maker
Add application
DMC plus controller to Maker
References: None |
Problem Statement: What is the Basic Engineering Design Data (BEDD) datasheet for? | Solution: The Basic Engineering Design Data (BEDD) datasheet is a central datasheet which contains the information concerning the site, climatic conditions, utilities, etc., that pertain to a process plant or site.
The data on the BEDD datasheet is transferred to other datasheets to fill out information, for example, for the Site Data and Utilities Conditions.
To specify BEDD for a workspace, follow the steps down below:
1) In the ABE Explorer, click on Edit | BEDD Management… This will open the BEDD datasheet.
2) Enter the necessary data and once done, close the BEDD datasheet.
From now on, the data entered in the BEDD datasheet will be available to other datasheets created in the workspace.
Keywords: Basic Engineering Design Data, BEDD, Datasheet, Workspace, Explorer.
References: None |
Problem Statement: How to make a 2-D model work in Aspen Adsorption? | Solution: When you switch Spatial dimension to 2-D, Aspen adsorption may stop working.
Please follow this workaround to make 2-D model working:
1.Change specification to 2D model and double click on the specification settings
2.Go to Analyze and then click on use specification tool
3.A new window with Specification analysis will show up, click on close
4.Go to the Configuration Block/Stream and initialize the bed
5.Go to initialization or dynamic mode and run the simulation. It should work well.
Key Words
Spatial dimension, 2-D, Adsorption
Keywords: None
References: None |
Problem Statement: My backup (.bkp) file is very large which is slowing down the user interface. I do not think that the file should be so big. Is there anything that I can do to reset it and make it smaller? | Solution: The ADS portion of a backup file can accumulate orphan records. The ADS section stores some results such as the new stream results, column analysis results, and batch results. We are working to resolve this issue in the Aspen Plus User Interface, but as a temporarySolution, we have created a batch file that can be used to strip out this portion of the file. The input will remain intact, but the results stored in this section will be lost.
Note: ThisSolution requires Strawberry Perl for Windows: install Padre, the Perl IDE (easiest option).
Recommended procedure will overwrite the parent file, so save a copy if you want both before-and-after files:
Download the attached stripads.bat file and put it in a new directory.
Put a copy of the bloated backup file in the same directory.
Two options, both will remove the ADS section of the file:
Drag and drop the *bkp file onto the batch file from within Windows File Explorer
Run via command prompt: stripads backupfilename.bkp
Open the modified backup file in Aspen Plus User Interface to make sure that it runs as expected.
Keywords: None
References: CQ00767200, CQ00769091
Fixed in Version
V10 CP2, V9 EP19 |
Problem Statement: When the user would use IAS type isotherms? | Solution: Regular isotherms like Langmuir are based on assumptions that isotherm parameters are regressed against mixture data. However, sometimes user rather have only pure component adsorption data. In that case using IAS option lets the user simulate competitive, multicomponent adsorption using only pure component isotherm parameters.
So, if the user has Langmuir 1 parameters for several pure species, then selecting IAS Langmuir 1 will help to capture the mixture adsorption behavior more accurately:
Key Words
Langmuir, IAS, Multicomponent
Keywords: None
References: None |
Problem Statement: Example of dealing with multiple process options / Workaround for mixer not solving when one feed stream is undefined | Solution: One possibleSolution here is to use a Tee to split the feed between the possible options and then set a Tee split specification to direct the feed to the required option. A mixer can then be used to combine the products from the different options for further processing. However a trick must be used when combining the product streams from the two options since the HYSYS mixer won't solve if any of its feed streams are undefined.
The attached HYSYS V11 case shows such a system. It illustrates two possible process options for a de-ethaniser column. It also shows the potential problem. [To see the problem ignore 'SPRDSHT-1' by ticking the Ignored checkbox.] The column that has zero feed flow will not solve, so its outlet streams are undefined. This means that the feed stream to the mixer has undefined compositions and flows. This causes the mixer not to solve, and hence any downstream operations will also be unsolved.
If the undefined mixer feed stream has a flow of zero set manually then the mixer does solve (effectively ignoring the unknown stream). Hence the workaround to the mixer not solving is to use a spreadsheet to set zero mole flow on the unsolved stream. When the stream is going to be calculated by the column then set the flow to -32767 (the HYSYS <empty> value) HYSYS then effectively ignores this specification and uses whatever flow it calculates. The spreadsheet uses an If Then Else function to decide based on the tee splits what value to export to the mixer feed stream flow rates.
Keywords: Multiple Process Options
Mixer unsolved
Spreadsheet
References: None |
Problem Statement: What is a quoted equipment and how to define it in Aspen Capital Cost Estimator? | Solution: Quoted equipment items can be used for unique, special, non-standard and proprietary types of process equipment, and it is typically used for on-off items which won’t be used commonly in next projects.
The quoted equipment items are unknown to the system, so a Code of Account (COA) must be provided. If the COA provided is in the range of 100 to 299, the engineering will be developed based on its class, if not, it will be treated as a bulk and the system will allocate 15-20% of cost to engineering.
Note: The COA number 292 stands for proprietary equipment
Steps to define a quoted equipment:
1. Add a project component to the area of interest
2. In the ICARUS Project Component Selection window select Quoted Equipment
3. The mandatory input required for quoted equipments are the Item description and the Code of Account (red cells). The Total cost per unit (blue cell) is not available for this product, this is only for AICE product. Use Material cost per unit (yellow cell) and Labor hours per unit (green cell) in order to allow ACCE to perform its calculations.
Note: The item class and item type are used for engineering costs and reporting and the component weight is used for freight and potential structural loads.
4. Click OK to finish defining the quoted equipment
Keywords: Quoted equipment, proprietary equipment, component, not available, introduce, industrial equipment
References: None |
Problem Statement: Although BLOWDOWN provides with multiple graphic and table reports, users are also able to retrieve results in VBA | Solution: The attached VBA code provides the required syntax need to call for different sides of the result reports from BLOWDOWN
Version
V10
Key words
HYSYS, Automation, VBA, BLOWDOWN
Keywords: None
References: None |
Problem Statement: How to get Benzene content property on material stream in Aspen HYSYS V11? | Solution: Open HYSYS simulation in Aspen HYSYS V11
Click on Simulation environment
Open required material stream, Worksheet tab, Properties page
Click on Append New correlation button (Green colour plus sign), GC.
Select GC, A C6 Benzene which reports Benzene content property in stream.
Keywords: Benzene content, A C6 Benzene Wt Pct, etc.
References: None |
Problem Statement: Where can I find the Calculated Equivalent Length in the Line Sizing tab of the PSV form over the Safety Analysis environment in Aspen HYSYS and Aspen Plus V11?
This value is reported on V10 and previous versions. | Solution: Starting in V11, Safety Analysis environment line sizing use Aspen HYSYS Hydraulics for more accurate calculations, and the Calculated Equivalent Length have been removed.
Nevertheless, if the simulation is changed to Rating mode it will be possible to Edit Pipes & Fittings to get the L/D and the K value, among others. Also, if a step forward is taken to Aspen Flare System Analyzer, it will be possible to find the equivalent length over there.
Keywords: Equivalent Length, Line Sizing, PSV, Safety Analysis.
References: None |
Problem Statement: Limitations of Freundlich adsorption isotherm | Solution: Freundlich isotherm may have a good fit in certain ranges, but at zero and infinity it is non-physical. Freundlich isotherm violates certain thermodynamic constraints. The slope is infinite at the 0 concentration limit, which could cause numerical calculation problems. It also hits no max loading as you increase the concentration or pressure.
If Freundlich isotherm causes problems in your adsorption model, you could try more robust isotherm such as Langmuir. Use the Freundlich isotherm and generate some points in your region of interest, then re-fit the data to a Langmuir isotherm (not Langmuir-Freundlich as that also has the infinite slope at 0 issue).
Key Words
Adsorption
Freundlich isotherm
Langmuir isotherm
Keywords: None
References: None |
Problem Statement: How to increase work space for large Hysys EO model? | Solution: Hysys EO flowsheet with large component list and complex recycle operation may take much longer time to converge. So, in message panel following error on insufficient work space may show up and solver will stop:
+---------------------- ERROR ----------------------+
Insufficient WORK SPACE during FACTORIZE
phase of LU decomposition.
The current size = 40811214
the minimum size = 22569882
+
Keywords: None
References: None |
Problem Statement: Usually Microsoft Access database for APS/MBO models are easy to open. You can direct point to the .mdb file. But if the model is in SQL server, how do we open the model? | Solution: First, when a SQL APS/MBO model is being transferred, the model is usually backed up to a .bak file. The user who receive the model needs to restore the database in his/her SQL server. Here are the steps:
1. Copy and paste the .bak file to the following location: C:\Program Files\Microsoft SQL Server\MSSQLxx.SQLEXPRESS\MSSQL\Backup
2. Log into SQL Server Management Studio, in the left hand panel, under databases, right click and select “Restore database”.
3. In the dialog box, choose “Device” as source, and click on the “…” button to the right. In the dialog box, click “add”. Choose the desired .bak file and click OK.
4. It will tell you when the restore process is complete. After it’s completed, click OK again on the main menu. It’s going to read the file and tell you restore success.
5. You are going to see the new database is listed in your SQL server.
6. Next, we need to create the “bridge” .dsn file in order for APS/MBO to open the model. The applications cannot open the model directly from SQL server, that’s why we need to go to ODBC data sources and create a file DSN for the database.
7. Choose File DSN and click on Add, select SQL server.
8. Click Next, and name your model. The example I chose is “Sample”.
9. Click Next and Finish. Now it’s going to prompt you to create a new data source to SQL server, in the Server text box, enter your SQL server:
10.Click next and use Windows Authentication to log in.
11. It will prompt you to select a database within that server. Click on the dropdown and select the database we just restored.
12. Click OK all the way to the end.
After these steps, you will be able to open the .dsn file just created in APS/MBO. This will be your model stored in your SQL server database.
Keywords: None
References: None |
Problem Statement: What is an Equipment Model Library and how to define it in Aspen Capital Cost Estimator? | Solution: The Equipment Model Library or EML is intended to store custom equipment items, for which you create component specification forms. This library can store a generic equipment item that comes in discrete sizes, such as an extruder, or an equipment item that follows a continuous cost-capacity relationship such as linear, semi-log or log-log.
In a project, you can add an item from the EML as a component and fill out the form that you earlier created. This comes to be very useful to add proprietary equipment that is commonly used, for which size-price relationship data is well-known, but is not included in the ACCE components library.
The following are the steps to define an Equipment Model Library:
1. In the Libraries tab of the palette window go to Cost Libraries | Equipment Model Library and expand the folder of the units of measure of your interest, then Duplicate any of the preset files.
2. Provide a File Name and optionally a File Description for your new equipment model library.
3. In the Library window you Add, Modify, Copy, Delete and/or Escalate your items. For this example, the item A1 was added.
4. After clicking the OK button, the Develop Equipment Library Model will display. There you will be able to specify your new equipment providing different costs for different size values, as well as specifying the sizing calculation method (linear, logarithmic, semi-logarithmic or tabular).
Note: For more information about Equipment Class and Equipment type please refer to the article What information should I enter in the Equipment/Item Class and Equipment/ItemType fields when adding a User model in the Economic Evaluation products?. For more information about the Codes of Accounts (COA), refer to the Aspen Icarus V11
Keywords: User Library, Libraries, Proprietary equipment, User defined
References: Guide chapter 34
5. (Optional) There is the possibility to specify alternative materials of construction for the equipment model and impact the price by an escalating factor. For this example, if the centrifugal pump is built in A516 the price will be 1.4 times the price that it would be for SS.
The following are the steps to load an Equipment Model Library into the project:
6. Add a new project component to any desired area and select the Equipment model library project component.
7. In the Select an Equipment Model Library File window select the library that you have just created or the one that is of your interest.
8. In the Select an Equipment Model Library Item window select the item that you need for your project. In this example, as we only created the item A1 this is the only one that will appear on this list.
9. When clicking in the OK button, the new component will be added to your area. The last step is to provide the size value to allow the engine to calculate the cost from the sizes and costs using the calculation method selected when defining the item.
Note: The smallest and the largest equipment provided to the EML will define the minimum and maximum limits for the sizing parameter. |
Problem Statement: How do I remove motor control centers from my estimate? | Solution: You may disable motor control centers from the Project Basis View. Go to the Power Distribution form, right-click on your Unit Substation and then choose Edit.
You will find an option for Motor control center required. There is a drop-down and you can choose the - option to exclude cost and installation.
Keywords: None
References: None |
Problem Statement: Is it possible to modify the system-calculated design for one of my components and apply my own custom rules? How can I do that? | Solution: The Custom Model feature will help you if you are looking to modify some design with your custom rules.
This is an example of the application of these custom rules: Assume that you have a vertical vessel component, and you want to use your own method to calculate the base material thickness, from the design pressure, temperature and other inputs of your components; you could then use the custom model to do this calculation. Attached is an example spreadsheet created to calculate this thickness, which is to be used with a Vertical vessel model.
A custom model is configured in the form of an Excel worksheet which needs to be located at C:\Users\Public\Documents\AspenTech\Shared Economic Evaluation VX.X\API Custom Models.
In this folder you can find a file named General Model Template.xlsx which can be used as a starting point to create new Custom Models.
Locate the attached model here and open it.
You will notice 3 sheets in this Excel file: Input, Custom Rules and Output:
In Input you will name what input information you want to retrieve from the component form. Each input has it unique name (e.g. CpDesignGaugePressure) and you can find a list for all these names in the Application Programming Interface (API) and Object Definitions guide (Open in Help | Documentation, attached as reference).
Once you have retrieved the input information, you can setup all your calculations in the Custom Rules page.
Finally you can copy your results to the Output spreadsheet which has a similar structure as the Input sheet (also uses the unique names from the API
Keywords: User Custom Model, Customize, Proprietary, Model.
References: Guide).
When you are done setting up your model spreadsheet, you can use the Custom Model feature in our component by right-clicking a component and selecting Custom Model.
A list will appear with all the available Custom model files. Select the one you want to use and click on Run
The model spreadsheet will open for you to review the results. Finally click on OK in the Custom Model list to transfer the model results to the design/input form in the Economic Evaluation software. |
Problem Statement: How to resolve the “.NET Framework” error while trying to new Layer on existing gas bed? | Solution: Please follow these steps to create a new Layer set range to get rid of this error:
Go to Variable Find
Type “LayerSet” and hit “Find”.
Right click on the bed name and select “Properties”
Modify the range of Layer as needed. Hit Apply and OK.
This will now enable to add more Layers without the .NET error.
Key Words
Layerset, .NET, Gas Bed
Keywords: None
References: None |
Problem Statement: Why a window which says ‘Clipboard copy is not implemented’ frequently pops up in Aspen Energy Analyzer? | Solution: It is found that the problem is caused by on-line dictionary programs like Bing Dictionary. As the dictionary program uses clipboard frequently when it is activated, there are conflicts with these two programs. The problem will disappear if you close the dictionary programs.
Keywords: AEA Clipboard
References: None |
Problem Statement: How can I define the color and style of the material streams in my Aspen Plus model? | Solution: There are two very easy ways to change both color and style of material streams in the flowsheet:
1) Right-click on any material stream in the flowsheet and select the ‘Color and Style…’ option.
The ‘Color and Style’ window will appear and you will be able to set the outline color, weight (width) and style of the selected material stream. Finally, click on the ‘OK’ button.
2) Expand the ‘Stream Groups’ folder (which is located under ‘Setup’ folder) and select the default stream group (feeds, products, initial, tears) that your target stream(s) belong to.
You will be redirected to a format form which the exact same options from the ‘Color and Style’ window of the optioned described above. Finally, click on the ‘Stream-Groups’ folder and make sure that the checkbox located under the ‘Format Active’ column is ticked.
Keywords: Color, Style, Material Stream, Stream Groups, Format Active.
References: None |
Problem Statement: How can I find the breakdown of the functional groups used by Aspen Plus when doing an estimation calculation based on molecular structure? | Solution: It is possible to get information on the functional groups and the number of occurrences that Aspen Plus uses when trying to do an Estimation. To obtain such values follow the instructions below:
Increase the Diagnostic Message Level to at least 6 for Physical Properties (SetUp | Specifications | Diagnostics)
Run the Estimation
Click on the History report button on the Home tab.
The generated file will be a text report, with the breakdown values available there:
3 UNIFAC
NO. OF COMPS = 2
J NSEQ NO OF GROUPS
1 1 3
2 2 4
NO. OF GROUPS = 7
J GROUP NO NO OF OCCUR
1 1015 4
2 1010 3
3 1005 2
4 1065 1
5 1055 1
6 1015 1
7 1010 1
For the example above, the History file is reporting:
Estimation method – UNIFAC
Number of components – 2
The first component is using 3 functional groups
The second component is using 4 functional groups
Number of Occurrences for each functional group
You can review what is the functional group that corresponds to each GROUP NO by going to Components | Molecular Structure | (select a compound) | Functional Group tab
Note: using V11, the Structure sheet is now integrated into the left side of the Functional Groups sheet, allowing you to reference this picture when specifying functional groups.
In this window you can select the estimation method and select a Group number from a dropdown list. During the selection you can see what is the functional group that corresponds to each GROUP NO.
For additional information, refer to the article Perform Component Properties Estimation using Aspen Properties and Aspen Plus
Keywords: Molecular Structure, Functional Groups, Estimation, UNIFAC, Joback, UNIQUAC.
References: None |
Problem Statement: How can I access pure component temperature dependent parameters in Aspen Custom Modeler? | Solution: Pure component property parameters can be retrieved using physical property procedure calls. For temperature dependent parameters, you need to use the procedure pParamT.
This example attempts to do the following:
1. Retrieve the PLXANT parameters (T-dependent) for two components.
2. Use the retrieved parameters in ACM to calculate vapor pressure of each component.
Description:
- The model uses Aspen Properties.There are only two components in the component list: N2 and O2:
- A custom model named “VapPres” was created to achieve the two goals described above using the following code:
- The retrieved parameters, along with the results, are shown in the “AllVariables” table of the custom model:
- Example file is attached
Keywords: ACM, parameters, pparamt, temperature dependent
References: None |
Problem Statement: How do I configure the mapping of component in MBO to APS stream when using Copy from APS? | Solution: In order to configure the mapping of the component in MBO to the APS stream for the Copy from APS functionality, you'll need to change the ID in the database table _ZSTRMS. If you don’t want to change the name of the stream, you can create a dummy stream and send all the properties via the POST worksheet.
Keywords: None
References: None |
Problem Statement: How can are the model accuracy trends scale is setup in Aspen Petroleum Scheduler? | Solution: Accuracy Screens trends scaling will be defined by the information in the Event View Trends Min/Max Y- Values. If these values are not defined, APS will automatically calculate the min/max Y – values.
We can see observe this behavior that is by design in the following example for CCU Hvy Naphtha Trend that has no values defined and APS is automatically calculating:
In the Model Accuracy Trends, we would observe the following:
To modify trend scale values, you can enter Trend List Dialog box by right clicking on the event screen and then enter the desired values on the Min/Max Y-Values as shown in the following screenshot where we are adding new Min and Max Y-Values for CCU Hvy Naphtha trend:
In the Model Accuracy Trends, we would observe the following:
Keywords: None
References: None |
Problem Statement: How to resolve “Unable to read Basis” error while opening HYSYS V7.3 file in HYSYS V10? | Solution: Open HYSYS V7.3 simulation in Aspen HYSYS V10
Un-register Gas Properties extension from Aspen HYSYS V10, by clicking on Aspen HYSYS V10 file, Customize, Register extension, select Gas Properties extension, click Unregister extension, it resolve the error message Unable to read Basis.
Keywords: Unable to read basis, Gas properties extension
References: None |
Problem Statement: When you change the default directory in Aspen Capital Cost Estimator, the folders order is not respected when saving. | Solution: Verify that the Default Project Directory folder is not duplicated in Alternative Project Directories. If so, Remove the duplicate folder from the Alternative Project Directories, since the program will display these folders in the same order over the Palette window.
If the previous step does not work, try verifying that there are not more than one PROJECTS.OBI files in the folder that you are defining as the default. If so, delete all of them and reset that folder as the default.
Keywords: Default, directory, save, order, change, drive
References: None |
Problem Statement: Where is the Configure Database Wizard in Aspen Manufacturing Suite V8? | Solution: In AMS V2004.2 two tools were introduced for mass population: the OPC Address Scanner and the IP.21 Configure Database Wizard. The Configure Database Wizard allowed you to create tags in InfoPlus.21 corresponding to tags discovered in a data acquisition device. It did this by importing an XML file previously generated by the OPC Address Scanner tool and required a suitable XSLT stylesheet module to transform the input file into an intermediate XML file.
There were some nice features of these tools, the OPC Address Scanner could be configured to be executed periodically on the command line to report new tags or updates to existing tags. The wizard itself could also configure CIM-IO records.
These tools have had considerable problems though, the XML file generated by the scanner could run to 100’s of MB in size. The wizard was complex to set up and required a great deal of coaxing to be made to work successfully. The whole process was invariably time consuming and frustrating.
With AMS V8, the Configure Database Wizard is no longer installed (although it is currently spuriously referred to in the IP.21 help file – this is a known issue). The menu item that used to appear under the Action menu in InfoPlus.21 Manager has been removed. The OPC Address Scanner still remains, at least in V8.0.
The Configure Database Wizard can be considered deprecated as of V8.0 and the suggested approach to bulk load tags from a data acquisition device into Aspen InfoPlus.21 is to use Aspen SQLPlus or to use the Aspen Configuration Tool (an Excel Add-in) that was introduced in V7.3. See, What are the different ways to populate the tags in Aspen Cim-IO Transfer record?
Keywords: Bulk load
Mass population
Configure Database Wizard
OPC Address Scanner
AMS v8
References: None |
Problem Statement: Where are the log or warning messages stored in Aspen HYSYS? | Solution: You may set up Trace and/or Status Logs to track your file constantly.
In the bottom Messages section, right-click on either the left (Status) or right (Trace) section and choose View Properties. On the file name, provide a directory and then either Status.Log or Trace.Log.
For instance:
C:\Users\(user name)\Desktop\Trace.Log
Then the text file will store the messages.
You can set up the default locations for these from File | Options | Simulation | Default File Paths.
Note when you right-click, you also have an option to dump the current messages to a file.
Keywords: None
References: None |
Problem Statement: What’s New in V11: Add Larger Pile Diameter for Drilled and Cast-in-place Concrete Pile | Solution: We have increased the pile diameter (size) of drilled and cast-in-place concrete piles to 48 IN [1200 MM]. The applicable pile types include AUGR - Auger cast piles, FRNK - Franki piles, and POUR - Poured concrete piles. The 48 IN [1200 MM] size has been added to the pile size dialog box available in the project/area level Civil specs. Additionally, the 48 IN [1200 MM] size has been added to the Drilled and cast-in-place concrete piles (SD POURED) component located in Site development, Piling.
Keywords: V11, new, pile diameter, pile drilled, cast-in-place, piles, pile, concrete
References: None |
Problem Statement: I have a sub-cooled liquid stream. When I adjust the stream pressure, the enthalpy stays the same. Why is this happening? | Solution: The enthalpy is not changing because this is a sub-cooled (or compressed) liquid stream and liquid is essentially in-compressible under normal circumstances. In these situations, it is common for pressure to be ignored leaving only temperature having an effect on the enthalpy.
The software is reporting the enthalpy of the saturated liquid at the specified temperature. You may test this by holding temperature constant, deleting the specified pressure and then entering 0 for vapor fraction. This will create a saturated stream at the specified temperature. You may then observe the enthalpy and the calculated pressure at these conditions. Then, delete the 0 vapor fraction and put back in the original pressure (or any pressure above the calculated one, making it sub-cooled) and you will find it keeps the saturated enthalpy.
This is a common practice because the pressure effects on enthalpy are minimized in the subcooled region. This may be observed visually in a Pressure-Enthalpy diagram where the Temperature curves become nearly vertical with respect to Pressure.
Keywords: None
References: None |
Problem Statement: Can I use compressor curves in Aspen HYSYS Dynamics Mode? | Solution: Yes, compressor curves can be used in Aspen HYSYS Dynamics Mode. When running a Dynamics case with characteristic curves, select the Use Characteristic Curves check box to use the curve(s) specified on the Rating tab | Curves page.
If a single curve is specified in a dynamic Compressor, the speed of the Compressor is not automatically set to the speed of the curve. You can specify a different speed, and HYSYS extrapolates values for head and efficiency. When this check box is cleared, HYSYS does not consider the characteristic curves when solving the case.
You should be aware of specifications that may cause complications or singularity in the pressure flow matrix. For instance, the Speed check box should be cleared if the Use Characteristic Curves check box is cleared.
For more details on Dynamic Specifications, please refer to KB14463
Keywords: Compressor, Curves, Speed, Dynamic Spec, Use Characteristic Curves
References: None |
Problem Statement: What’s New in V11: Multiple Item Options for Control Cable in Electrical Bulk Items Form | Solution: Currently the electrical bulk items forms allow adding three different power items. However, only one control item (control cable plus push button station) can be specified for each. In V11, you can specify multiple control items for as many as five different items. (All Programs)
This enhancement will therefore address this by adding the following fields under each item:
Number of pushbuttons
Control cable length
Control cable no. of conductors
Control cable type
Control cable size
Control cable conduit option
The 'Number of pushbuttons' field is required to estimate each of the five control items. If the 'Number of pushbuttons' field is not specified, the control item will not be estimated.
Keywords: V11, new, options, control cable electrical bulk, control, cable, electrical, bulk
References: None |
Problem Statement: What is the purpose of enrich O2 option for on the FCC Reaction Section | Regenerator page and how is the value used? | Solution: To burn the coke in the regenerator, the operator can use air or enrich O2.
The main purpose of using enrich O2 is if you have air blower limits and you need flexibility in processing various feeds to the FCC. Since the enrich O2 is basically pure O2, you need much less of it than you would need air to burn the same amount of coke.
Keywords: None
References: None |
Problem Statement: What’s New in V11: Pile Diameter Size Increase of Drilled and Cast-in-place Concrete Piles | Solution: The pile diameter (size) of drilled and cast-in-place concrete piles is increased to 48 IN [1200 MM]. The applicable pile types include AUGR - Auger cast piles, FRNK - Franki piles, and POUR - Poured concrete piles. The 48 IN [1200 MM] size has been added to the pile size dialog box available in the project/area level Civil specs. Additionally, the 48 IN [1200 MM] size has been added to the Drilled and cast-in-place concrete piles (SD POURED) component located in Site development, Piling.
Keywords: V11, new, pile diameter, pile diameter, drilled, cast-in-place, concrete
References: None |
Problem Statement: What dimensions are reported on the TEMA Sheet headings? | Solution: In the Shell and Tube program, the TEMA Sheet (Results | Result Summary | TEMA Sheet) has some results displayed on the top section (headings), such as the Type of exchanger, effective surface area and size:
The size being displayed in this section is the Nominal Shell ID – Tube Length. Since the Shell ID is the nominal shell ID value (meaning it will be the nominal diameter closest to the actual shell diameter), the reported number can vary from the actual Shell ID being used for the unit.
Regardless of the differences, the Shell ID specified will be the one used for calculations.
Keywords: shell, ID, tema, sheet
References: None |
Problem Statement: How is the “Draft at burners” reported in the API sheet calculated in Aspen Fired Heater? | Solution: The API sheet, on the Combustion section, reports the “Draft at burners”:
This draught result is the combination of all draught losses from the Firebox to the Stack. All the individual contributions are reported under Results | Calculation Details | Draught Details:
In this case for example, adding up the contributions from the Firebox to the Stack, we have:
(-178.6) + 4.1 + 0.2 + 98.5 + 56.2 + (-154.1) = -173.7 Pa
Which is the same value reported in the API sheet.
Keywords: Firebox, burners, Draught, Draft.
References: None |
Problem Statement: How would someone rate an air cooled exchanger for natural convection? | Solution: You should use Simulation calculation - Outlet temperature on both sides, and X-side flow (natural convection), on Input | Problem Definition | Application options | Application Options tab.
If you set the simulation mode to Natural convection, then this will turn the fans off and calculate the flow rate due to the buoyancy forces within the bundle and plenum chamber. Therefore, you might want use the natural convection mode if you want to model a Natural Draft on the Air-Side.
Natural Convection is a simulation calculation, so the X-side mass flowrate will be determined together with the exit temperature of air and the exit temperature of the process stream. Process mass flowrate and inlet temperature are specified so is the X-side inlet temperature. This mode can be used when all fans in an air-cooled heat exchanger are switched off.
Note: On Aspen EDR, the simulation mode for natural convection can be used only when the process stream is the hot side, as the free convection model used is related to a hot surface and cold air.
If you specify the X-side as the hot side, you will get the Error 3510 (Why do I get “Error 3510: There is no buoyancy pressure drop calculated for a no fans case on EDR Air Cooler?)
Keywords: Natural convection, Fans
References: None |
Problem Statement: What’s New in V11: New Detailed Material and Labor Line for Ducts | Solution: Currently for round and square ducts the material and labor line items do not contain the duct diameters. As a result it is not possible to distinguish between two duct line items of the same material but with different duct diameters in the unit rate file. To solve this we have added the duct diameter in the item description.
The material cost line items for duct and fittings will have the duct diameter or dimension (for square duct)
For the duct labor line items (handle and erect duct), the details will be turned on only when user has Create detailed labor line items set to Y in the Design basis --> Piping Specs --> General form.
For the duct insulation material cost line item, the duct dimension and insulation thickness will be added to the line item description.
The duct paint line items will remain unchanged.
After evaluation, the duct material line items will show the duct diameters in the item description. If the Create detailed labor line items field is set to Y in the Design basis --> Piping Specs --> General form, the duct labor line items should also contain duct dimensions.
Keywords: V11, new, ducts, material, labor
References: None |
Problem Statement: What’s New in V11: Add Equipment Fireproofing to Horizontal Vessel Saddles, Heat Exchanger Saddles, and Air Cooler Legs | Solution: Equipment fireproofing has been added to the following equipment models which include heat exchangers, reboilers, and horizontal tanks
DHE FIXED T S
DHE FLOAT HEAD
DHE U TUBE
DHE PRE ENGR
DHE TEMA EXCH
DHT HORIZ DRUM DHT DESALTER
DHT JACKETED
DHT MULTI WALL
DRB KETTLE
DRB THERMOSIPH
DRB U TUBE
Equipment fireproofing has also been added to the DHE AIR COOLER legs when the leg height is specified as greater than 0.
The equipment fireproofing for the equipment models above will be added to the estimated equipment material and labor costs when equipment fireproofing is specified at the project/area levels. When equipment fireproofing has been specified, users will see higher material and labor costs for these equipment models due to this change.
Keywords: V11, new, equipment fireproofing, fireproofing, horizontal vessels, heat exchanger saddles, air cooler legs
References: None |
Problem Statement: How do you display small values (less than 1e-20) in the sensitivity results form? They are reported as zero by default. | Solution: Unfortunately, there's no option presently to display the variables with small values. However, as a work-around, you can use an expression to scale up the value:
This will display the value multiplied by 1e20.
Keywords: sensitivity results
References: None |
Problem Statement: Example of an extracted steam turbine | Solution: Extracted steam turbines are used when a constant pressure steam flow must be extracted for process purposes. In these types of turbines, the power generated can be maintained at a steady level despite variation in the process steam demands.
Part of the steam is extracted from the turbine stage to heat feed water or for some other process. This steam is known as extraction steam.
The following description and the attached example illustrate how to model a process for extraction steam across three turbine stages.
Specifications:
Components: Water
Property method: STEAMNBS (any steam table)
Blocks:
*Note the Stage 3 compressor’s Valid Phases have to be specified as Vapor-Liquid since the turbine’s outlet is below dew point.
Feed stream: “1”; P = 5 bar; T = 200 C, Flow = 5000 kg/hr; Composition = 1 (Water only)
Description:
3 Compressor blocks specified as turbines are added to the process, with each stage depressurizing the process stream to a lower pressure. On each stage outlet, a simple splitter is added, which separates a portion of the steam (these streams are the actual extracted steam). The remaining stream is then fed onto the next turbine.
The values are used for example purposes only. If a particular demand of extracted steam is desired, the split fraction can be changed until the extracted steam meets process requirements.
Keywords: extract, turbine, steam, compressor
References: None |
Problem Statement: What’s New in V11: Specification of Unions, Couplings and Bushings in Conduit Plant Bulk Form | Solution: The system estimates conduit elbows, fittings, unions, seals, couplings and bushings for all conduit runs in a project. Currently, the number of elbows, fittings and seals can be specified for electrical and instrument conduit plant bulk items. However, the number of unions, couplings and bushings are only system generated. Users would like the option to specify these as well.
To address this, additional fields for the number of unions, number of couplings and number of bushings will be added to the Electrical and Instrument conduit plant bulk forms.
If these fields are left blank, quantities will be system calculated as follows:
Number of couplings - Default of 1 coupling per two 30 FT [9 M] lengths of conduit.
Number of unions - Default of 2 unions per elbow (1 elbow is estimated by default per 100 FT [30.48 M])
Number of bushings - Default of 2 per conduit run. (Only estimated for above ground conduit)
If you specify quantities in these fields, the user specified quantities override the system defaults.
Keywords: V11, new, Unions, couplings, bushings, conduit, plant bulk, bulk, plant
References: None |
Problem Statement: How to define custom instrument for Incoming and outgoing flow rate in AtOMS? | Solution: ThisSolution provides an idea as to how to define custom instruments for an AtOMS model for Flow rate.
Using the AtOMS Admin Tool , you can define custom instrument naming FLOW_R (For Receiving rate) & FLOW_D (For Dispatching Rate) or any other name that you prefer.
You can then map these instruments to IP.21 Tags to get the exact readings.
Refer recommended steps that you can try first in your Test Server:
Here’s how you can open the AtOMS Admin tool, either from atOMS Client.exe > Refer screenshot or from Windows start > AtOMS Admin
Go to View and click on Oil Movement explorer and once done you will have the list of options available
On the left navigation pane, Right click on Instrument Type > CREATE New instrument and once done, go to Node Instrument to map this instrument with IP.21 Tag Name
Also mapping to each tank needs to be done using this tool and mapping these tanks under field named ‘NODE’
Make sure to Check the Flag for Movement Monitor & Tank Monitor.
Once done, Right click and refresh & reload on the node instrument from navigation pane
After completion, restart the Tank & Movement Monitor Services one time.
You should now be able to see these instruments in your AtOMS Tank Summary Page and their respective values
This will allow you to have two instruments through which incoming flow and outgoing flow rate can be tracked in AtOMS.
Keywords: None
References: None |
Problem Statement: How to model “Combining Redistribution” in Aspen Plate Fin exchanger (EDR)? | Solution: During “Combining Redistribution”, a stream present in a set of layers changes its conditions (Temperature, Pressure, flow, composition, physical properties) at a specific point along the exchanger core. It is called ‘combining redistribution’ because this change is usually caused by mixing the stream present in the layers with another stream, although this is not the only possible cause. Some examples of ‘combining redistribution’ are:
- An external stream (from outside the core) enters the exchanger and mixes with a stream already present in a set of layers.
- A fraction of an internal stream (already present in a different set of layers within the core) mixes with another stream within the exchanger
- A stream exits the core to be reconditioned (change in T and/or P) and then re-enters the core.
In none of these cases however, EDR can model the mixing (or reconditioning) of the stream on its own. Nevertheless, by integrating EDR with Aspen HYSYS, it would be possible to model such applications, in which case all the mixing/reconditioning would take place on the HYSYS side, while EDR would only take care of the heat transfer/hydraulic calculations. The iterative process would also be handled by HYSYS.
In the attached example we have 3 main streams:
- Stream 1: Hot stream. This stream will be subjected to mixing/reconditioning
- Stream 2: Hot stream. This stream will leave the core at some intermediate location.
- Stream 3: Cold stream. This is the only cold stream in the system.
In reality, a fraction of Stream 1 will remain in Layer A, while the rest will mix with an external stream and will enter Layer B (previously occupied by Stream 2).
In the HYSYS/EDR simulation we will model this by using 5 streams, Streams 1-3 to represent the main streams, Stream 4 to represent the fraction of the stream 1 that remains in Layer A, and Stream 5 to represent the other fraction of the stream 1 that mixes with the external stream and enters Layer B.
Keywords: Combining, redistribution, plate fin, EDR
References: None |
Problem Statement: How can I use automation to modify and save as a new event in APS? | Solution: The following automation can be used to get an existing event, make changes in the event and save the event as a new event.
==================================================
Sub copyevent()
Dim evntcoll As New orion.EventsColl
Dim originalevnt As orion.EventItem
Set originalevnt = evntcoll.ItemByEventSeq(255)
Dim newevnt As orion.EventItem
Set newevnt = originalevnt
newevnt.Start = DateAdd(d, 1, originalevnt.Start)
newevnt.Stop = DateAdd(d, 1, originalevnt.Stop)
newevnt.Color = RED
newevnt.Label = New event
newevnt.StartLink = 0
Dim seq As Integer
seq = evntcoll.Add(newevnt)
Set evntcoll = Nothing
End Sub
==================================================
Keywords: None
References: None |
Problem Statement: Why the Reid VP at 37.8C stream property is showing a negative value? | Solution: Reid VP at 37.8 C sometimes seems to be negative when the unit set is set to measure pressure as gauge pressure (psig, for example). If this is changed to measure pressure as absolute pressure (psia, in this case) the Reid VP at 37.8C value will be a positive number.
Additional information can be found on the articles below:
How is Reid Vapor Pressure [RVP] calculated in Aspen HYSYS?
Definition of TVP and RVP
In the attachments you will find a simple example of the RVP being measured in absolute pressure and in gauge pressure.
Keywords: Reid Vapor Pressure, Reid VP, RVP.
References: None |
Problem Statement: When rating an air cooled exchanger, EDR cannot generate a tube layout with my input of number of tubes per bundle.
It also generates an error message 3008: | Solution: With a Bundle type of Staggered-even rows to left, 4 tube rows, the number of tubes shall be multiple of 4. Otherwise, EDR will not be able to run the model. The exchanger layout in the current datasheet is not fully supported.
For more details, you could check the knowledge article below:
How to prevent Results Error 3008 “An inconsistency has been found when setting up a non-symmetrical bundle arrangement”?
A workaround is to change the number of tubes per bundle to 244 or 248 instead of 246, then it would solve. It would still give you accurate simulation result.
Key Words
Air cooler exchanger
Number of tubes
Error 3008
Keywords: None
References: None |
Problem Statement: RadFrac with Column Analysis now supports custom trays for rating calculations. | Solution: Starting in V11, now RadFrac with Column Analysis supports custom trays for rating calculations only.
You can use custom trays to model innovative or unusual tray designs not covered by the specific tray types available in Column Analysis. For these trays, you specify key parameters such as the fraction of active area, fraction of hole area, fraction of downcomer area, and the diameter.
Aspen Plus will calculate the results as for other trays; only average or total downcomer properties are available since details about individual downcomers are not specified.
Keywords: RadFrac, Column Analysis, Custom Trays, Rating.
References: None |
Problem Statement: Aspen CimIO for OPC fails to connect to an OPC DA Server with a “Class Not Registered” error. | Solution: The error indicates the OPC DA Server in not registered correctly. Therefore the entries in the registry for this OPC DA
Server should be verified and changes made if needed.
Locate the COM application in DCOM Config.
R-Click on the application and select Properties.
Copy the Application ID.
Open the system registry and search for the Application ID.
Review all the registry entries for the application to verify everything is correct.
Example;
Verify “LocalServer32” contains the correct path for the OPC Da Server exe.
Verify “ProgID” contains the expected OPC DA Server program name.
Make sure to stop the OPC Server and CimIO for OPC before making any changes in the registry.
Keywords: Asyncdlgp
DCOM
References: None |
Problem Statement: What’s New in V11: Add Saddle Height Field to Horizontal Vessels and Heat Exchangers | Solution: A saddle height field has been added to the following equipment models, which include heat exchangers, reboilers, and horizontal tanks:
DHE FIXED T S
DHE FLOAT HEAD
DHE U TUBE
DHE PRE ENGR
DHE TEMA EXCH
DHT HORIZ DRUM DHT DESALTER
DHT JACKETED
DHT MULTI WALL
DRB KETTLE
DRB THERMOSIPH
DRB U TUBE
The default saddle height has been specified as 10 inches [254 mm] to keep existing saddle weights the same [Moss Book]
Minimum saddle height is 6 inches [150 mm]
Maximum saddle height is 96 inches [2400 mm]
Previously the saddle material cost and shop labor wasn't included in the equipment cost. Users will now see higher equipment costs due to this change.
Keywords: V11, new, saddle height, saddle, height, horizontal vessels, heat exchangers
References: None |
Problem Statement: What are some key terms used in Aspen Utilities Planner? | Solution: Demand blocks
Used to specify a demand for a certain utility. Demand blocks are available for water/steam, fuel, power, and air.
Efficiency curves
Used to show how the efficiency of a unit operation (e.g., boiler) varies with load.
Equipment design constraints
Used to specify physical limitations of the equipment (e.g., maximum steam generation).
Feed blocks
Used to specify the supply of a certain utility. Feed blocks are available for water/steam, fuel, power, and air
Hot standby requirements
The amount of spare generation capacity that must be available during operations. For example, the hot standby capacity of a boiler will be the difference between the maximum generation capacity and current load. You can specify and enforce hot standby requirements through the Optimization settings.
Multi-period optimization
Optimization carried out over two or more time periods. Multi-period optimization allows the user to take into account constraints that span periods, for example start-up and shutdown time and some elements within utility contracts.
Tier
Some utility contracts are split into separate subcontracts or tiers. For example, a natural gas contract may provide part of the gas supply at a low variable cost, but with a fixed cost element and the remainder of the gas at a higher variable cost and no fixed price elements. This would be modeled as a single contract with two tiers.
Keywords: Tier, Demand blocks
References: None |
Problem Statement: What’s New in V11: Improvements to Cable Tray Fittings and Supports | Solution: Cable tray systems are widely used to provide orderly paths to house and support cabling both overhead and beneath the ground. Currently, ACCE estimates cable tray runs with only the option to specify generic '90 degree bends' in the electrical and instrumentation plant bulk items and no option to specify supports to the cable tray runs estimated in the project.
Plant Bulk Cable Tray Fittings:
With this enhancement, the option to specify a number of cable tray fittings will be added to the electrical and instrumentation cable tray plant bulk items only:
Horizontal bends - 90°, 45°, 60° and 30° options
Vertical bends - 90°, 45°, 60° and 30° options
Tees - Horizontal and Vertical
Crosses
Reducers
Splice plates
Tray covers
The current field for 'Number of 90 degree bends' is renamed 'Number of horizontal bends' and any data in the 'Number of 90 degree bends' field from existing projects will be migrated into the 'Number of horizontal bends' field.
Plant Bulk Cable Tray Type:
The cable tray types for electrical and instrumentation cable tray plant bulk will be updated as follows:
L| Ladder tray
T| Ventilated trough tray
B| Solid bottom trough tray
This is because there is now a separate field to either include or exclude the tray cover.
If the C option is specified in previous versions, this entry will be migrated as the 'T' tray type AND the 'S' option in the tray cover field in V11.
If the B option is specified in previous versions, this entry will be migrated as the 'B' tray type AND the 'S' option in the tray cover field in V11.
Project/Area Cable Tray Type:
The cable tray type descriptions in the project and area level specs forms will be updated as follows:
L| Ladder tray
T| Ventilated trough tray
C| Ventilated trough tray with cover
B| Solid bottom trough tray with cover
A new option will be added as follows:
S| Solid bottom trough tray
Cable Tray Supports:
There are no specific requirements for cable tray supports in the NEC, the support span length (distance between supports) depends on the type of tray and the weight of the cables in the tray. However, the industry standard strongly recommends that only one cable tray splice be placed between support spans.
This enhancement will give users the option to include cable tray supports for all above ground cable tray systems in the project (in the case of project level specification), or include cable tray supports for all above ground cable tray systems in the area (in the case of area level specification) or include cable tray supports for the electrical and instrumentation cable tray plant bulk items. Users will be able to specify the distance between supports.
Keywords: V11, new, cable tray fittings, supports, cable tray, tray, fittings
References: None |
Problem Statement: What’s New in V11: 2018 Cost Basis Update - Pricing Changes | Solution: The pricing basis for this release has been updated to the First Quarter 2018. The table below summarizes an approximation of material pricing changes from the V10.1 EP2 version of Aspen Economic Evaluation (i.e. 2017 pricing basis). These results were obtained by running a general benchmark project containing a representative mix of equipment found in a gas processing plant. In addition to pricing changes, model enhancements and defect corrections have affected overall percentage differences. Note: this may include quantity or design differences as various models and methods have been updated or fine-tuned based on client feedback and defect reSolution (see information provided in this document regarding defect corrections which may cause pricing and/or installation scope changes in the V11 What’s Fixed section of Economic Evaluation release notes for further information).Your results will differ based on the overall mix of equipment, bulk items, and specified materials of construction contained in your project.
Keywords: V11, new, 2018, Cost Basis Update, pricing
References: None |
Problem Statement: What’s New in V11: Tube Wall Thickness | Solution: An initial tube wall thickness value is needed for sizing in order to estimate the global heat transfer coefficient and therefore needed to calculate the heat exchanger area. The value is either read from simulator data or set to a default value. In V11 the value used for sizing is no longer written back to the project component, allowing the tube wall thickness to be calculated from the ASME design code when the component is evaluated.
Keywords: V11, new, tube wall thickness, tube, wall, thickness
References: None |
Problem Statement: How is the “Draft at arch” reported in the API sheet calculated in Aspen Fired Heater? | Solution: The API sheet, on the Combustion section, reports the “Draft at arch”:
This draught result is the combination of all draught losses from the Firebox arch to the Stack. All the individual contributions are reported under Results | Calculation Details | Draught Details:
In this case for example, adding up the contributions from the Firebox arch to the Stack, we have:
4.1 + 0.2 + 98.5 + 56.2 + (-154.1) = 4.9 Pa
Which is the same value reported in the API sheet.
Keywords: Firebox, arch, draught, draft
References: None |
Problem Statement: Is it possible to calculate partial molar properties in Aspen Custom Modeler (ACM)? | Solution: Although there are no out-of-the-box property procedures for the calculation of partial molar properties available in neither Aspen Properties nor ACM, it is absolutely possible to calculate these thermodynamic properties in ACM.
The custom model shown down below is just an example of the calculation of the partial molar enthalpy for each component in a ternary mixture (water, methanol and benzene).
Model PartialMolarEnthalpy
x(ComponentList) as molefraction (spec:Fixed, 1/3);
dx as hidden molefraction(Fixed, 1e-3, Description:Mole fraction perturbation);
x_pert(Componentlist, ComponentList) as hidden molefraction;
T as Temperature(Fixed, 25);
P as Pressure(Fixed, 1);
H as enth_mol_liq;
H_pert(componentlist) as hidden enth_mol_liq(Description:Calculated enthalpy at perturbed composition);
H_partial(componentlist) as enth_mol_liq(Description:Partial molar enthalpy);
//Calculate base molar enthalpy
call (H) = pEnth_mol_liq(T, P, x);
for c in componentlist do
x_pert(c,c) = x(c) + dx;
for c1 in componentlist - c do
x_pert(c,c1)=x(c1);
endfor
//Calculate enthalpy at perturbed mole fraction of component c
call (H_pert(c)) = pEnth_mol_liq(T,P,x_pert(c,componentlist));
//Calculate partial molar enthalpy for component c
H_partial(c) = (H_pert(c) - H)/dx;
endfor
End
Note: The *.acmf, *.aprbkp and *.bkp files attached to this article were built in V9.0 and are upward compatible.
Keywords: Partial Molar Properties, Partial Molar Enthalpy.
References: None |
Problem Statement: What’s New in V11: Add Civil to HE Spiral Plate | Solution: We are now including a factored estimate for Civil in the EHE SPIRAL PLT heat exchanger component estimated costs. An 'OTHER EQUIPMENT CONCRETE' line item will now be estimated for this item in the details in the CCP report.
Keywords: V11, new, civil, HE spiral plate, spiral, plate
References: None |
Problem Statement: What’s New in V11: Add Pipe Schedule/thickness and Flange Class for Lined Pipe and Fittings | Solution: In ACCE, lined pipe and fittings (e.g. pipe, elbow, reducer, tee, strainer) are always estimated as flanged items. The cost is estimated by adding the cost of the two end flanges to the cost of the pipe/fitting. Therefore the cost of a fitting or pipe segment of a given diameter and lined material depends on:
The pipe diameter
The pipe material
The pipe schedule or thickness
The flange class of the pipe
Currently Icarus reports only the diameter and the schedule. As a result, two lined pipe/fitting items with the same diameter, lined material and schedule but with different flange classes may get different unit material costs. This makes it difficult to reconcile the unit material costs of these items in the unit rate input file. To remedy this we are including the flange class in the item description
Keywords: V11, new, pipe schedule, flange class, fittings
References: None |
Problem Statement: Where does one go to find reliable contractors for the measurement of physical property data (pure and mixture)? | Solution: A number of contractors can be found in both the United States, Europe and Africa.
Physical Properties Contractors in the United States
1. Wiltec Research Company, Inc.
Types of experimental data equipped to measure:
Thermophysical Properties: vapor pressure; liquid densities; vapor PVT; critical properties; heat of vaporization; heat of mixing; vapor, liquid, and solid heat capacities; surface tension; and liquid and vapor viscosities.
Phase Equilibria: vapor-liquid equilibria (VLE), liquid-liquid equilibria (LLE), simultaneous vapor-liquid and liquid-liquid equilibria, solid-vapor or solid-liquid equilibria, infinite dilution activity coefficients, gas solubilities, and distillations.
Chemical Equilibrium: reaction equilibria, reaction kinetics, heats of reaction, and simultaneous chemical and phase equilibrium.
Data are normally held confidential for five years. The confidentiality period can be extended to 20 years with a 25% surcharge. Only the measurement data is published; any information concerning business or processes is permanently and strictly held as confidential by Wiltec.
2. Prof. Amyn S. Teja, Chemical Engineering Department, Georgia Institute of Technology
Pure Component Properties: critical temperature; vapor pressure; liquid and vapor densities; liquid heat capacities; liquid viscosity; liquid thermal conductivity; and PVT data for electrolyte and non-electrolyte systems.
Mixture Properties: PVT data; excess volume; solubilities in supercritical gases; heat capacity; thermal conductivity; viscosity; and PTxy VLE data.
Confidentiality period: 1 year.
3. National Institute of Standards and Technology (NIST)
Available equipment for:
VLE up to 5000 psia mole fractions from 10D-4 to 0.9999
Gas solubilities up to 5000 psia of gases in liquids
Solubilities in supercritical fluids
Vapor pressure measurements from 10D-8 Torr up (solids, heavies possible)
Cp and Cv measurements, speed of sound (for Cp and Cv of gases)
Enthalpies ofSolution (mixing) and adsorption
Viscosities and Thermal conductivities of fluids from cryogenic up to
Diffusion coefficients in supercritical fluids
Polymer-solvent equilibria
Surface tensions (high pressure, non-ideal systems)
Electric conductivity
Physical Properties Contractors in Europe
1. Laboratory for Thermophysical Properties (LTP)
The Laboratory for Thermophysical Properties was founded as an independent research organization in 1999 by Prof. Dr. Juergen Gmehling and Dr. Kai Fischer. The priority of LTP GmbH is the experimental determination of thermophysical properties of pure compounds and mixtures, as they are required for the design, simulation and optimization of industrial separation and conversion processes.
The experimental facilities comprise a variety of equipment for the determination of
pure component properties (vapor pressures, liquid densities, heat capacities, heats of fusion,etc.)
phase equilibria (VLE, azeotropic data, activity coefficients at infinite dilution, LLE, SLE, gas solubilities, Henry coefficients,etc.)
excess properties (heats of mixing, excess volumes)
kinetic data.
More than 20 thermophysical properties for gases, liquids and solids can be measured.
2. Processium, France
Processium measures and models physical properties for process design. Thanks to our experimental facilities, we measure:
Vapor pressures, vapor-liquid and liquid-liquid equilibria between -50 and 300 C, and between 0.0001 pa and 200 bar
Azeotropes, distribution coefficients, critical points
Activity coefficients, Henry's law constants
Melting points, sublimation pressures
Distillation
3. Sergey P. Verevkin, Department of Physical Chemistry, University of Rostock
Equipment available:
Vapor-liquid equilibrium, including gaschromatographic determination of vapor solubilities
Vapor pressure, including measurements of thermally unstable compounds
Heats of combustion and vaporization
4. Additional Sources in Europe
Kikic at Trieste in Italy for infinite dilution activity coefficients (including supercritical solvents)
Grolier in France for Heat Capacity and Heat of mixing
Richon in France for VLE and viscosity at high pressures
de Swan Arons in the Netherlands for high pressure VLE, LLE
Maurer in Germany for electrolyte and reactive
Physical Properties Contractors in Africa
1. Thermodynamic Research Unit (TRU), South Africa
Prof. Deresh Ramjugernath ([email protected]) +27.031.260.3218; +27.082.336.3925
Prof. Paramespri (Prathieka) Naidoo ([email protected]) +27.031.260.3177; +27.082.478.2440
The experimental facilities comprise a variety of equipment, including:
Computer-controlled isothermal/isobaric dynamic/recirculating stills with an operating temperature range from ambient to approximately 450 K and an operating pressure range from close to absolute vacuum to 500 kPa. The equipment is capable of VLE and VLLE measurements, vapour pressure measurement, and boiling point measurements.
Static equipment for high pressure measurements with an operating temperature range of approximately 240 K to 520 K and an operating pressure range from 0 to 35 MPa, using variable volume or static cells.
Equipment for liquid-liquid equilibrium measurements at both atmospheric pressures and pressures up to 20 MPa. The operating temperatures ranges are from approximately 240 K to 470 K.
Equipment for solid-liquid equilibrium measurements at atmospheric pressure for temperatures ranging from approximately 200 K to 360 K.
Equipment for the measurement of absorption and desorption isotherms which make use of volumetric and gravimetric techniques.
Equipment for the measurement of infinite dilution activity coefficients using differential ebulliometry, gas-liquid chromatographic, and inert gas stripping techniques.
Equipment for the measurement of partition coefficients, e.g. octanol/water and water/air.
Equipment for the measurements of thermophysical properties (density (up to 600 bar), refractive index, excess properties, viscosity, heat capacity, electrical conductivity, speed of sound).
Pilot plant facilities include distillation columns with a spinning band column and both packed and trayed columns for batch distillation trials. Continuous distillation studies can also be undertaken using Normschlift columns with Sulzer packing and tray sieve-plate columns.
Keywords: property data
References: None |
Problem Statement: Why is the tubeside pressure drop calculated differently between Aspen TASC and Aspen Exchanger Design and Rating (EDR)? | Solution: In Aspen TASC (sunsetted on 2008), the friction factor used to determine the pressure drop is based upon commercial tubes.
Starting with Aspen TASC+ (released on 2006), and subsequently renamed Aspen Shell & Tube Exchanger (EDR), the default value for the tube surface relative roughness is Smooth, which is what is normally appropriate to heat exchanger tubes for process industry applications, and has been recommended following consultations with the HTFS Tubular Exchangers Review Panel. Commercial pipe will normally give an overprediction of what is found in heat exchangers and should not be used unless you have a reason to believe your tubes are exceptionally rough.
On Aspen EDR, you can choose between Smooth or Commercial, and even specify an explicit tube wall roughness* from Input | Tubes | Tube | Tube surface
*Using specified roughness should be done with caution. Neither the smooth tube nor commercial pipe curves match up with any fixed roughness value.
Typical roughnesses are sometimes published for various types of tube. Two random examples are:
0.025mm, for new steel tubes (from The Heat Exchanger Design Handbook)
0.15mm, for steel tubes cleaned after long use (from the Wärmeatlas)
When specifying a roughness, make sure you have appropriate units selected. The units conversion utility might give poor conversion accuracy with very low lengths.
Keywords: Friction Factor, Roughness, Tube surface, Pressure drop, Smooth, Commercial pipes.
References: None |
Problem Statement: A shell and tube exchanger consists of a bundle of tubes located inside a cylindrical shell. The arrangement allows heat transfer between a fluid flowing through the tubes and a fluid flowing over the tubes. The latter flow is usually directed by a series of traverse baffles in cross flow over the tube bundle as shown below for a two pass AEL shell.
The heat transfer coefficient between the fluid and the tube inside wall is referred to as the tubeside coefficient.
The heat transfer coefficient on the outside of the tube bundle is referred to as the shellside coefficient. The traverse baffles as shown above (being of the single segmental type) have two purposes; to give high rates of heat transfer on the outside of the tubes due to crossflow and to support the tube bundle to minimize vibration. The flow direction on the shellside, due to the flow around the baffles is not pure crossflow but a combination of crossflow and longitudinal flow, where the departure from pure crossflow depends upon the baffle spacing and baffle cut. The flow in addition is further complicated by manufacture tolerances for assembly, which causes clearances between the tubes to baffle or baffle to shell for example. | Solution: Due to the by-pass that occurs due to the constructional gaps for assembly, only a portion of the total shellside flow passes over the bundle in crossflow. The flow on the shellside of a baffled exchanger is complex and is shown in the figure below:
The various flow streams are shown where sometimes they have different terminology as below:
Crossflow: B - Crossflow
Window: W - Window flow
Baffle hole - tube OD: A - Tube/baffle leakage
Baffle OD - shell ID: E - Shell/baffle leakage
Shell ID - bundle OTL: C - Bypass
Pass lanes: F - Inline pass partition
Crossflow: The fraction of the total shellside flow which flows across the baffle space, nominally in crossflow. In poorly designed exchangers this value may be low, where below a value of 0.3, the Shell and Tube program issues an Operation Warning 1336 to re-evaluate the design.
Window: The flow inside the window region (the area due to the cut away of the baffle).
Baffle hole - tube OD: The tube/baffle leakage flow is due to tube-to-baffle clearance which is required for assembly of the bundle.
Baffle OD - shell ID: The baffle/shell leakage flow is due to the baffle-shell clearance which is required to allow the bundle into the shell.
Shell ID - bundle OTL: Bypass flow due to the bundle-shell clearance and is determined by the type of construction. For example a greater clearance is needed for a removable bundle heat exchanger because of the space required for the floating head flange than in a fixed tube sheet unit.
Pass lanes: Bypass flow arises from gaps in the bundle itself due to the presence of pass partitions if multiple tube passes are used.
In the Aspen Shell & Tube, the shellside flow fractions are shown in Results | Thermal/Hydraulic Summary | Flow Analysis | Flow Analysis tab. The flow fractions are shown for 3 locations;
· Inlet; where the shellside flow enters the exchanger
· Middle; in the baffled portion of the exchanger
· Outlet; where the shellside flow leaves the exchanger
Using the stream letter and letting F denote a fraction of the total flow rate in the heat exchanger then a mass balance will give;
To achieve good heat transfer, the crossflow fraction should be high as possible.
It might be thought that decreasing the baffle spacing will increase the cross flow velocity and hence improve the heat transfer. However, in practice, decreasing the baffle pitch will increase the pressure drop in the exchanger and increase the leakage flows (A, E, C & F), which decreases the cross flow (B). As a general rule, decreasing the baffle spacing to 20% of the shell diameter or below may cause deterioration in the duty due to the cross flow fraction decreasing.
Another way to improve the crossflow fraction is to insert sealing strips that divert some of the Shell ID to bundle OTL (bypass) flow back into the bundle improving the heat transfer but increasing the shellside pressure drop.
Keywords: Flow fraction splits; Flow fraction, Operation warning 1336, Low Crossflow, Sealing strips.
References: None |
Problem Statement: When using the h21chgpaths.exe utility to alter the history fileset paths to reflect a new location, the result is simply to list the usage. No changes appear to be made:
eg.
h21chgpaths.exe C:\Program Files\AspenTech\InfoPlus.21\c21\h21\ E:\Archive\
Results in:
Usage: h21chgpaths old_string new_string
Changes all pathnames in the current config.dat file
replacing old_string with new_string.
This is puzzling because you are certain the old_string is correct and you have used double quotes to surround it to take account of the spaces in the path. What could explain the failure to search and replace? | Solution: The problem is caused by the fact that the backslash character (\) is acting as an escape character when it precedes extended characters like the double quote symbol.
You should replace the trailing two character combination (\) with just the double quote symbol (). Eg. For the example above, change it to read:
h21chgpaths.exe C:\Program Files\AspenTech\InfoPlus.21\c21\h21 E:\Archive
To demonstrate that backslash really is acting as an escape character, you could also achieve success by escaping all the backslash characters that precede the double quote symbols in order to stop the double quotes being included in the search/replace strings. Eg:
h21chgpaths.exe C:\Program Files\AspenTech\InfoPlus.21\c21\h21\\ E:\Archive\\
This double backslash approach would explicitly identify a folder called h21. This would have been required if there had been multiple sub-folders in c21 folder, all starting with h21.
Keywords: not working
nothing happens
repository
folder
search
config.dat
References: None |
Problem Statement: How to create a user variable in ACM products? | Solution: For many instances, we may need to create a dummy variable for ACM, Aspen Plus Dynamic or in Aspen Adsorption. For an example, if we need to create a new variable for Energy demand which does not exist in any units in the flowsheet. In that case, we can go to Flowsheet > Constraint and declare the variable as real parameter.
Now this variable will be listed in the “Local Variable” form and its value can be modified if needed. The user should be able to use this variable from “Task” window.
Key Words
User Variable, Constraint, Local
Keywords: None
References: None |
Problem Statement: Error message “Stream Feed1: Dynamic flash not possible with current (insufficient?) specifications” when running the depressuring tool at some time in Aspen HYSYS? | Solution: To get rid of the error message, what you would need to do will be:
1. When the feeder block pops up, select the temperature radio button. Then, press the Export Conditions to Stream button.
2. Close the feeder block window.
3. Run the depressuring utility again - it should run fine now.
Keywords: Aspen HYSYS, Depressuring, Error Message
References: None |
Problem Statement: What is the recommended best practice for using data integration tools in APS? | Solution: Assuming you're looking at the staging tables for importing data (tank baselines, events, assay, etc.), in theory, both EIU and any customized interfaces will write data into these tagging tables, and functions the same way. The benefit of using EIU is, it comes with APS software and users do not have to maintain it except for working on the Excel data templates. For customized interfaces, users will have to maintain it by themselves and this is a huge IT burden. So from best practice standpoint, using EIU is a better choice, unless there are other interfaces passing the data to APS but the function does not exist in EIU currently (i.e. PIMS target passing...etc.).
If you are writing to the CORE Events table rather than the ORION_MGR_EVENT_IMPORT table, it is not recommended to do so. The recommended approach is either using EIU or custom interface to write into ORION_MGR_EVENT_IMPORT table.
Keywords: None
References: None |
Problem Statement: Under Convergence/ Options/ Methods/ Wegstein, how does the Wait parameter work? | Solution: Wegstein method uses the q parameter to accelerate the convergence:
xk+1 = q xk + (1 - q) F(xk)
Where s is Secant approximation of derivative:
However, for the first iteration, k = 1. We do not have an xk-1. Therefore, q and s cannot be calculated, and we have to use the Direct Substitution method instead:
x2 = F ( x1 )
where x1 is the initial value of x. This initial value could be the result of the previous run, or user’s initial estimate, or the system default (usually 0).
The “Wait” parameter here controls the number of direct substitution iterations before the first Wegstein acceleration iteration. In Newton method and Broyden method there is a similar Wait parameter. In Wegstein method, this parameter should be set to at least 1. Otherwise you will see an error message:
Key Words
Wait parameter
Wegstein method
Direct substitution
Keywords: None
References: None |
Problem Statement: This knowledge base article provides steps to resolve the error
[AspenTech][SQLplus] SQLplus Access Denied - No read access
which can appear in the Aspen SQLplus Query Writer, the Aspen Tag Browser or from a custom program which uses an ODBC connection to connect to the Aspen InfoPlus.21 database. | Solution: This error indicates that the Aspen Framework (AFW) or Aspen Local Security (ALS) role the affected user is in does not have read permission to the Aspen InfoPlus.21 database.
Please try the following (recreating the AFW cache files) to resolve this error:
1. On the Aspen InfoPlus.21 server:
Stop the AFW Security Client service.
Ensure the AFW Security Client service is set to start under a domain account which has privileges to read group information from the Active Directory.
2. Stop the Aspen InfoPlus.21 Task Service.
3. Delete the four cache files. See Knowledge Base for the location of these files: How do I change the location where the Aspen Security cache files are stored?
4. Delete the IP21AFWCACHE.DAT file from the Group200 folder:
ProgramData\AspenTech\InfoPlus.21\db21\Group200
5. Restart the AFW Security Client service and the Aspen InfoPlus.21 Task Service. This will recreate the cache files that were just deleted.
Important: If the AspenTech Calculator Engine service was automatically stopped during this procedure as a consequence of stopping a dependent service then start the AspenTech Calculator Engine service.
If recreating the AFW cache files does not resolve the problem then the next step is to ensure that there are no problems with the AFW/ALS client/server components or individual user accounts. AFW Diagnostics can be used to check whether or not the AFW/ALS client or server components experience any problems. AFW Diagnostics will also perform ADSI tests to determine whether or not an individual user account has sufficient permissions to query the network for group membership information. Run AFW Diagnostics on the Aspen InfoPlus.21 server using the account which starts the AFW Security Client service then check the results for any failed tests.
If AFW Diagnostics does not detect any problems with the client or server security components the next step is to see which roles are detected for the user accounts which experience the problem. The user should be in a role which at least has read access to the Aspen InfoPlus.21 server. This can be done using the AFW Security Client Tool.
Once the AFW Security Client Tool has been started, you can access the test by selecting Advanced Options... then Test Security Functions. Choose Out of Process and then click button Refresh Cache. After refreshing the cache, you can test the client's access to the security configuration. Using this tool, ensure that the correct AFW roles are returned for your users when the 'Get Roles' option is tested.
If the correct roles are returned using the AFW Security Client Tool then open the Aspen InfoPlus.21 Manager, go to
Actions | User Roles...
Ensure that the correct roles are shown here. The role list shown by the Aspen InfoPlus.21 Manager is read from the IP21AFWCACHE.DAT file. If this role list is incorrect, this file will need to be deleted then recreated following steps 1-5 above.
Finally, restart the following tasks in Aspen InfoPlus.21 Manager: TSK_SQLR, TSK_SQL_SERVER, TSK_IQ*
If none of these suggestions resolves your problem then you can likely get a quick work-around if you add '-n' to the command line parameters of TSK_SQL_SERVER then restart the task. This will bypass Aspen SQLplus security but should not be considered as a long term fix.
Keywords: Access
Deny
Permission
TB
ATB
SQL+
References: None |
Problem Statement: How can I change the Control Mode (Off / Auto / Man) of a controller with either the Event Scheduler or a Spreadheet? | Solution: The Control Mode of a controller can be directly changed in its Parameters | Configuration form or with an external object, such as the Event Scheduler or a Spreadheet.
To do so, you will need to access the controller’s ‘Control Mode’ variable and set a numerical value for it from the options below, thus setting the controller operating mode:
0 – Off
1 – Man
2 - Auto
Keywords: Controller, Control Mode, Off, Man, Auto.
References: None |
Problem Statement: What is does the option Update Properties on the Home Ribbon / Components Group of the Properties Environment do? | Solution: The Update Properties button can be used to refresh the parameters for components within your case, replacing the previous values with values from the built-in database. When users open a case created in a previous version, the parameters from previous versions are generally used by default. If improvements have been made in a particular area, click Update Properties to take advantage of the latest component parameters.
Please note that not all components in the HYSYS database contain a full set of parameters. For example, Gibbs Free Coefficient values are not stored in database for all components. In this instance, the values that appear on the Component view are obtained through estimation. If you update the library properties for such a component, the empty value from the database will overwrite the estimated value on the Component view.
Keywords: Update Properties, Properties Environment.
References: None |
Problem Statement: How can I make sure that physical properties in ACM get calculated in the exact same way they are in Aspen Properties? | Solution: In ACM, you can use property callable procedures to compute physical / transport / caloric properties for pure components and mixtures using the property settings of the Aspen Properties file being used by the ACM model. Moreover, you can also use ACM commands to look at the pure component and binary (scalar and temperature-dependent) parameters being used in the ACM model.
In this article, an Aspen Properties model (find it in the attachments section) has been set up to include methanol, benzene and water in the Component List. The thermodynamic model was set to NRTL – SRK and the liquid mixture dynamic viscosity mixing rule was set to MULMX14 (Aspen model), which is a linear mixing role (mole average).
This Aspen Properties model also has a PURE analysis set up to calculate the (liquid phase) absolute viscosity of the three components (methanol, benzene and water) as pure components at 40 deg C and 1 bar.
The ACM model (also included in the attachments section), is using the Aspen Properties file mentioned above. This model contains a custom model named as ‘LiqViscosity’. This model uses the following command to retrieve the pure component temperature dependent parameters of the MULDIP correlation:
MULDIP (componentlist,[1:7]) as realvariable;
call(MULDIP) = pParamT(MULDIP,1); (these commands are asking ACM to retrieve the 7 pure component parameters (from element 1 to element 7) of all components defined in the component list and also defines them as real variables in the model)
This example custom model uses the following liquid mixture dynamic viscosity callable property procedure:
call(viscl) = pvisc_Liq(T,P,x); (which makes the liquid mixture absolute viscosity into a function of temperature, pressure and liquid phase composition)
The above is the reason why the liquid mixture dynamic viscosity mixing rule was set to a linear mixing rule (although users can use different logical statements to replace this line in the example custom model).
After successfully compiling the ‘LiqViscosity’ model and running-stopping the model in dynamic mode, the following results are computed for the liquid viscosity of methanol, benzene and water at 40 deg C and 1 bar:
So, the conclusion is that ACM will make use of the physical / transport / caloric property correlations that were set up in Aspen Properties if the model was using an Aspen Properties file. Results will be consistent between products.
Note: The *.acmf, *.aprbkp and *.apropz files attached to this article were built in V9.0 and are upward compatible.
Keywords: Physical Properties, Transport Properties, Caloric Properties, Aspen Properties, Callable Property Procedure, Custom Model.
References: None |
Problem Statement: What’s New in V11: Add Electrical Conduit Type Override at Area Level | Solution: The 'Above ground conduit type' field at the project level allows specification of the electrical and instrumentation conduit material in the project, while the 'Below ground conduit type' assigns material type to the underground electrical conduit only since instrumentation cables are usually installed above ground only. In V11 you can specify the instrument and electrical conduit material at area level.
To enable this, fields have been added to the area level electrical specifications form to allow override of the project level conduit type values for a particular area.
Keywords: V11, new, electrical conduit, override, conduit
References: None |
Problem Statement: How to add information to an input data table without manually creating the rows | Solution: When the user enter information to an input data table (i.e distillation curve, performance curves, etc), the user can directly copy-and-paste it from Excel and Aspen HYSYS will recognize automatically the data and will add the required rows to match with the Excel data.
Note: Just keep in mind to have the data in the same order of the table in Aspen HYSYS.
Keywords: Input Data Table, Copy, Paste, Excel, Manual
References: None |
Problem Statement: What’s New in V11: Calculate Leg Height for Cone Bottom Vessel Based on Dimensions | Solution: The default calculated leg height for the cone bottom vessel (DVT CONE BTM), has been updated based on the dimensions provided for the vessel. Specifically, the default calculated value is based on the cone height (determined from the vessel diameter and a 60 degree cone angle) and a 2 foot clearance below the cone. A user specified leg height will override the default calculated value.
Keywords: V11, new, calculate, leg height, leg, height, cone bottom vessel, cone, vessel, dimensions
References: None |
Problem Statement: Why cant I select 'Actuator Failed' variable in Aspen HYSYS V11.0? | Solution: The reason users cant select Actuator Failed because in V11 this variable is OP Signal Failed.
In V10.0 (and earlier), as shown in screenshot below, the option available was 'Actuator has Failed'. If users import this variable, it was available as 'Actuator Failed'.
In V11.0, as shown in screenshot below, the option available is 'OP Signal has Failed'. If users import this variable now, it is available as 'OP Signal Failed'.
Keywords: Actuator, Actuator Failed, OP Signal Failed, Dynamics, Valve
References: None |
Problem Statement: After installing Aspen Batch Interfaces and/or Production Record Manager Server, you can see the Aspen Production Record Manager Extractor Server in the services.msc but cannot find the Batch Extractor Administrator GUI. Where is it? | Solution: In order to install the Batch Extractor Administrator, select Aspen Administration Tools product group within the branch of the tree headed aspenONE Manufacturing Execution Systems:
No file shortcut to the Batch Extractor Administrator GUI is automatically created; locate the file using File Explorer and create a short cut for this yourself (or Pin to Start).
By default, the file is located here:
C:\Program Files (x86)\AspenTech\Batch.21\Client\ExtractorAdministrator.exe
Note, recent versions of the installer no longer create file shortcuts for a number of other Production Record Manager related programs including the Batch Detail Display, Alias Browser and Characteristics Browser. This is not an indication of imminent deprecation of any of these programs and more as an attempt not to overwhelm the Windows Start menu.
Keywords: setup.exe
APRM
BXE
References: None |
Problem Statement: What’s New in V11: Automated Risk Analysis Model and Reports | Solution: Estimators frequently need to use estimate and engineering data to assemble a stochastic-based risk analysis model and use third party tools to perform risk analysis. The new Risk Analysis feature allows estimators to conduct cost risk analysis within ACCE using a Monte Carlo Simulation approach.
The results of the analysis are
a table of contingency values and percentages for various confidence intervals
Total cost histogram and S-curve for total project cost and total direct cost
Sensitivity chart for all the elements of the cost estimate that are included in the risk analysis.
Before you run the analysis, the ACCE project must have the required scope (process equipment, piping, plant bulks, design basis, contract structure etc.) defined. The New Reporter option must be selected in the ACCE Preferences. Ideally the project should not have a contingency amount or percentage defined.
To use the risk analysis feature,
Click Run > Risk Analysis > Create Input File. The project must be evaluated before creating the input file
In the Input file, User Input - Ranges worksheet, specify the min and max values for each of the cost elements included in the risk analysis. The default min/max % values in the input file are -10% and 10%.
Set the number of risk analysis iterations. The default number of iterations is 10000. The minimum is 5,000, the maximum is 50,000.
In the Input file, User Input - Correlations worksheet, specify the correlation coefficients between the cost elements included in risk analysis. The input file has default correlation coefficient values specified.
Save and close the file and then click the Run > Risk Analysis > Run Analysis menu item.
The results worksheet contains the table of contingency amounts and percentages for the total project cost for various confidence intervals, and the histogram and sensitivity charts (tornado charts) for the total project and total direct costs.
Keywords: V11, new, risk analysis, risk, analysis, tornado
References: None |
Problem Statement: How to resolve the “.NET Framework” error while trying to new Layer on existing gas bed? | Solution: Please follow these steps to create a new Layer set range to get rid of this error:
Go to Variable Find
Type “LayerSet” and hit “Find”.
Right click on the bed name and select “Properties”
Modify the range of Layer as needed. Hit Apply and OK.
This will now enable to add more Layers without the .NET error.
Key Words
Layerset, .NET, Gas Bed
Keywords: None
References: None |
Problem Statement: Why a window which says ‘Clipboard copy is not implemented’ frequently pops up in Aspen Energy Analyzer? | Solution: It is found that the problem is caused by on-line dictionary programs like Bing Dictionary. As the dictionary program uses clipboard frequently when it is activated, there are conflicts with these two programs. The problem will disappear if you close the dictionary programs.
Keywords: AEA Clipboard
References: None |
Problem Statement: How can I define the color and style of the material streams in my Aspen Plus model? | Solution: There are two very easy ways to change both color and style of material streams in the flowsheet:
1) Right-click on any material stream in the flowsheet and select the ‘Color and Style…’ option.
The ‘Color and Style’ window will appear and you will be able to set the outline color, weight (width) and style of the selected material stream. Finally, click on the ‘OK’ button.
2) Expand the ‘Stream Groups’ folder (which is located under ‘Setup’ folder) and select the default stream group (feeds, products, initial, tears) that your target stream(s) belong to.
You will be redirected to a format form which the exact same options from the ‘Color and Style’ window of the optioned described above. Finally, click on the ‘Stream-Groups’ folder and make sure that the checkbox located under the ‘Format Active’ column is ticked.
Keywords: Color, Style, Material Stream, Stream Groups, Format Active.
References: None |
Problem Statement: How can I find the breakdown of the functional groups used by Aspen Plus when doing an estimation calculation based on molecular structure? | Solution: It is possible to get information on the functional groups and the number of occurrences that Aspen Plus uses when trying to do an Estimation. To obtain such values follow the instructions below:
Increase the Diagnostic Message Level to at least 6 for Physical Properties (SetUp | Specifications | Diagnostics)
Run the Estimation
Click on the History report button on the Home tab.
The generated file will be a text report, with the breakdown values available there:
3 UNIFAC
NO. OF COMPS = 2
J NSEQ NO OF GROUPS
1 1 3
2 2 4
NO. OF GROUPS = 7
J GROUP NO NO OF OCCUR
1 1015 4
2 1010 3
3 1005 2
4 1065 1
5 1055 1
6 1015 1
7 1010 1
For the example above, the History file is reporting:
Estimation method – UNIFAC
Number of components – 2
The first component is using 3 functional groups
The second component is using 4 functional groups
Number of Occurrences for each functional group
You can review what is the functional group that corresponds to each GROUP NO by going to Components | Molecular Structure | (select a compound) | Functional Group tab
Note: using V11, the Structure sheet is now integrated into the left side of the Functional Groups sheet, allowing you to reference this picture when specifying functional groups.
In this window you can select the estimation method and select a Group number from a dropdown list. During the selection you can see what is the functional group that corresponds to each GROUP NO.
For additional information, refer to the article Perform Component Properties Estimation using Aspen Properties and Aspen Plus
Keywords: Molecular Structure, Functional Groups, Estimation, UNIFAC, Joback, UNIQUAC.
References: None |
Problem Statement: How can I access pure component temperature dependent parameters in Aspen Custom Modeler? | Solution: Pure component property parameters can be retrieved using physical property procedure calls. For temperature dependent parameters, you need to use the procedure pParamT.
This example attempts to do the following:
1. Retrieve the PLXANT parameters (T-dependent) for two components.
2. Use the retrieved parameters in ACM to calculate vapor pressure of each component.
Description:
- The model uses Aspen Properties.There are only two components in the component list: N2 and O2:
- A custom model named “VapPres” was created to achieve the two goals described above using the following code:
- The retrieved parameters, along with the results, are shown in the “AllVariables” table of the custom model:
- Example file is attached
Keywords: ACM, parameters, pparamt, temperature dependent
References: None |
Problem Statement: What is the exact modification of mass-transfer coefficients in rate-based simulations for structured and random packings when applying the RateFrac model? | Solution:
Keywords: RateFrac, Tsai, mass-transfer coefficients, dimensionless
References: s
R. E. Tsai, F. Seibert, B. Eldridge and G. T. Rochelle, A Dimensionless Model for Predicting the Mass-Transfer Area of Structured Packing, AIChE J., 57, p. 1173, 2011.
Private communication, Raschig GmbH, November 29, 2011. |
Problem Statement: Why do I get “Error 3510: There is no buoyancy pressure drop calculated for a no fans case on EDR Air Cooler? | Solution: In an Aspen Exchanger Design and Rating (EDR) Air Cooler model, you can specify the Fan configuration for the type of draft in the process.
In processes that use natural convection, it is common to have Induced draft (Air Cooler with fans, induced air is sucked through the bundles) or a No Fans configuration (Air Cooler does not have fans, only the tube bundle).
However, if you run an air cooler model in Simulation mode using the option to calculate Outlet temperatures on both sides, and X-side flow (natural convection), the No Fans configuration will not work:
No Fans does not work for this configuration. You need to specify Forced or Induced type of fan even though fans are not included in the natural convection calculations.
This is because the air side flow calculations cannot be performed, since there is no actual form of knowing how the air is behaving if the unit only consists of the tube bundle, so it is necessary to change the fan configuration to either Forced or Induced.
Note: On Aspen EDR, the simulation mode for natural convection can be used only when the process stream is the hot side, as the free convection model used is related to a hot surface and cold air.
Keywords: Error 3510, Natural convection, no fans, Buoyancy, Pressure drop
References: None |
Problem Statement: How can a vent with a reducer at the Flare Tip be modeled in Aspen Flare System Analyzer? | Solution: This system can be set up by modeling the flare stack as a pipe with a reducer at the end and then another pipe with zero length, used to define the reducer dimensions.
Do not forget to add a flare tip at the end of the network so that the flowsheet gets fully defined. Please refer to the attached example file (the example file was built in V9.0, but its XML is also attached to be used in older versions).
Keywords: Vent, Reducer, Flare Tip, Flare Stack, Pipe, Zero Length, Dimensions
References: None |
Problem Statement: Can composition data be copied and pasted onto a source composition form? | Solution: If the user copies all the composition values of a source in Aspen Flare System Analyzer (AFSA), it will be absolutely possible to paste them all at once on the composition form of another source, even in a different AFSA model. In other words, users can copy over the composition values for all components at once among AFSA models.
However, if the user attempts to copy the composition information from an Aspen HYSYS / Aspen Plus material stream to further paste it onto an AFSA source composition form, the following warning message will pop up indicating that it is not possible to handle the copied data:
Composition data from an Aspen HYSYS / Aspen Plus material stream can only be copied over to an AFSA source for each component in the component list, one at a time. Just make sure to double-click on a composition field (it will be highlighted in blue) to paste the copied composition data.
Keywords: Composition, Copy, Paste, Source, Material Stream.
References: None |
Problem Statement: How to fix recipes in multiple blend events? | Solution: In Aspen Refinery Multi-blend Optimizer (MBO), to fix recipes in multiple blend events at the same time, you can first select blend events you would like to change, right-click and select Fix Recipe to fix the recipe for multiple events.
Keywords: None
References: None |
Problem Statement: Can Aspen Plus optimize on integer variables, such as feed stage to column? | Solution: The Aspen Plus Optimizer is designed to work with real continuous variables only; however, nothing prevents the user from setting up a problem that varies an integer variable. The algorithm assumes that the manipulated variable is a real variable, but when the value is passed to the block, it is truncated to form an integer. Since this truncation most likely leads to an incorrect calculation of the Jacobian and Hessian matrices, the optimizer probably would not converge to the trueSolution.
Depending on the initial guess and the number of manipulated parameters, we can have these outcomes:
The SQP and Complex algorithms may appear to work correctly for several iterations, driving towards theSolution, until they finally fail, noted by a line search failure message
The BOBYQA method could to completely converge, but if the user changes the initial input values, the Optimizer will reach a different result.
As workaround, the user has two options:
For a simple optimization, is more practical to determine the optimum value of an integer variable by varying the integer value in a Sensitivity block and graphically determining the optimum.
For a more complex problem, a multivariable optimization, you can approximate the optimization treating the integer number as a continuous variable. See example below.
For additional information, refer to the next articles:
How are SM optimization problems solved in Aspen Plus?
How to vary the feed stage location and the total number of stages in RadFrac
Example: Minimize Column Energy Requirements by changing the feed location
On the attached model, is possible to approximate the feed optimization with a real number by using a calculator and a feed stream splitter. The idea is to define a global parameter that can be manipulated by the optimizer and turned into an integer by the calculator block, which then sets the feed stage location.
The main considerations are described below:
FEED stream is splitted into FTOP and FBOT (in block FSPLIT), which are fed into different stages of the column
The Calculator C-STAGE is set up with the following variables:
RSTAGE is PARAMETER 1 with initial value 80.1
NSTAGET is the feed stage for stream FTOP
NSTAGEB is the feed stage for stream FBOT
FRAC is the flow fraction of FBot (from stream FEED)
The C-STAGE block take RSTAGE as input and other variables as output with the following code:
NSTAGET = INT(RSTAGE)
NSTAGEB = NSTAGET + 1
FRAC = RSTAGE – NSTAGET
For the optimization problem, one should use PARAMETER 1 as the optimization variable.
For the optimized initial RSTAGE = 93.492, we get:
NSTAGET = 93
NSTAGEB = 94
FRAC = 0.49221
Note: If you have two different feeds, you will need two calculator/splitter.
Keywords: Optimization, Integer, SQP, Complex, BOBYQA, Sensitivity, Stages.
References: None |
Problem Statement: How to run a Sensitivity Analysis to tabulate Phase Equilibrium results? | Solution: Tabulating K-values (V-L equilibrium constant) for a mixture can be useful when we evaluate the performance/results of a thermodynamic model. A FLASH2 block calculates K-values for each component, but this variable is not accessible through a Sensitivity Analysis, so it wouldn’t be possible to evaluate K’s at different conditions other than doing it manually.
Nevertheless, there is a Property Set, KVL, that flashes a stream at the specified conditions and calculates the K of the desired components.
The following description and the attached example illustrates how to run a Sensitivity Analysis using this approach to generate phase equilibrium results.
Specifications:
Components: Ethylene, butane
Property method: SRK
Blocks: “SEP” (FLASH2); P=0 bar, Q=0 cal/sec
Feed stream: “IN”; P=1 bar; VF=1e-5 (bubble point), Flow=100 kmol/hr; Composition=50/50 mole fractions
Property Sets: “K1” – KVL – Qualifiers | Component | Ethylene; “K2” – KVL – Qualifiers | Component | Butane
Sensitivity Analysis: “S-1” – Vary pressure of stream “IN” – Define 3 variables, temperature of stream “IN”, Property Set “K1” for stream “IN”, Property Set “K2” for stream “IN” – Tabulate the same 3 variables
Description:
2 Property Sets are created using the property KVL, to calculate the K-value of each component. The KVL property set flashes the stream at the stream conditions and calculates the correspondent K-value.
Then, we use a Sensitivity Analysis to vary the stream pressure and tabulate the results for the K-values at the bubble temperature (VF~0) and the calculated bubble temperature as well.
The SEP block is used for validation purposes only. The calculated K’s in the SEP block (Results | Phase Equilibrium) should match the results of the first case of the Sensitivity Analysis.
Keywords: K, phase equilibrium, sensitivity analysis
References: None |
Problem Statement: What’s New in V11: Option to Estimate Push Buttons with Motor Operated Valves | Solution: If a Motor Operated Valve is specified in an instrument loop (installation bulks), ACCE currently do not automatically create a pushbutton station for the electric actuator. Users would like an option to include pushbutton stations for the motor operated valves estimated in the project.
To enable this capability, a field, 'Motor operated CV pushbuttons' will be added to the General Instrumentation Specs form with the following options:
Exclude pushbuttons from motor operated valves (default option)
Provide pushbuttons with motor operated valves
By default, the field will have the 'N' option. If this option is specified, there will be no pushbutton station estimated for the motor operated valves and nothing should change from the previous version.
If user specifies the 'Y' option, a pushbutton station (with 2 pushbuttons and pilot lights) and a control cable (from the pushbutton station to the control center) will be estimated for each MOV estimated in the project.
The length of the control cable estimated will be calculated as follows:
((Distance equipment to MCC + Distance MCC to CC) + 10ft.[3 m.]) * 4 (Number of conductors)
Distance equipment to MCC - specified in area electrical specs form
Distance MCC to CC - specified in CC form
Keywords: V11, new, push button, push, button, motor operated valves, motor, valves
References: None |
Problem Statement: What are the PSC products and how they are licensed? | Solution: PSC products are comprised of the following products:
Licensing:
Baseload Products – Charge by per site.
Aspen PIMS (50)
Aspen Supply Planner (55)
Aspen Petroleum Supply Chain Planner (35)
Aspen Inventory Management and Operations Scheduling (20)
Aspen Fleet Optimizer (30)
Tokens are consumed permanently and not returned when application is closed
Please refer to below KB article to find out the exact function of each product.
https://esupport.aspentech.com/S_Article?id=000048390
Keywords: PSC
PSC Licensing
References: None |
Problem Statement: How can I estimate the overall amount of vapor emissions generated by a batch process? | Solution: The best way to do this is to send all the final streams for each Vapor Emission Paths to an Inventory Location - Vapor. The Excel report Composite Vapor Emission Streams will then report the overall amount of vapor emissions sent to that inventory location.
The attached example uses this approach to calculate the total amount of emissions going to an inventory location. The specifications include the following:
- Two Emission Control Devices in the Amberglass facility: Condenser VC-01 (Outlet temperature = 10C) and Condenser VC-02 (Outlet temperature = 20C):
- Two Emission Control Paths in the Amberglass facility: Amberglass Emission Pathway, consisting of Condenser VC-01, and Amberglass Emission Pathway 2, consisting of Condenser VC-02:
- For each path, the final stream is sent to the 'Inventory Location - Vapor' from the Amberglass facility named Atmosphere.
- Each Emission Control Path is connected to a particular operation under File | Preferences | Vapor Emissions | Emission Control Paths:
- Make sure that the option 'Enable Air Emission Calculation' has been turned on before running the simulation under Tools | Options | Simulation Batch.
- After running the model, review the Excel Report named “Composite Vapor Emission Streams”, where the overall amount of vapor emissions will be displayed.
- Check Excel Report named “Vapor Emission Stream Table” for additional details.
Keywords: Vapor emissions, emission control device, emission control path, inventory location
References: None |
Problem Statement: Is there any example file user can refer for modeling the column with overhead heat pump? | Solution: There is an Aspen Plus V9 example and an Aspen HYSYS V9 example uploaded in Attachments section for reference.
If you already have Process Flowsheet Diagram (PFD), mass balance and energy balance information, it is easy to build model in Aspen HYSYS or Aspen Plus.
If you are trying to build this kind of process model start from concept design, it is much harder and need principle knowledge from literature to support design idea. Fortunately, aspenONE Exchange function imbedded in Aspen Plus, HYSYS, EDR provided the literature search and review service on this demand. You can search ‘heat pump’ as keyword in aspenONE Exchange to find whether there is any suitable literature or document can refer to. ‘aspenONE Exchange heat pump reference.png’ (figure 1) screenshot with steps is uploaded in Attachments section for reference.
Figure 1. Use aspenONE Exchange to search heat pump related literature
Keywords: Aspen Plus, Aspen HYSYS, aspenONE Exchange, Column, Heat Pump
References: None |
Problem Statement: How can I export an Economic Evaluation project scenario and then import it back in a new project? | Solution: If a project is partially corrupted, it can be useful to export its project specs as a SPECS (*.ic2) project file and then import it back on a new project.
Open the Economic Evaluation software and select the desired project
Go to File | Export to SPECS File
Browse to the desired location and create a new folder. Rename the file SPECS.IC2 by removing the .IC2 extension, and leaving the file name as 'SPECS'. Once you save the file, you will note the SPECS.IC2 on the new folder, but also other files as CURRENCY.DAT, dispid.DAT, STREAM.DAT, USER.DAT. All these files are necessary to recover the project information.
Create a New Project by selecting File | New. A window will pop up. Enter in a new project name and scenario name.
Click on the Import option and browse for the folder where the SPECS.IC2 is located
Wait until the project is loaded.
Keywords: SPECS, *.IC2, Corrupted, Recover, Export, Import.
References: None |
Problem Statement: A problem arises when you have more than one hot and/or cold utility. You must determine the optimum usage levels of the available utilities which will minimize operating costs, and satisfy the overall utility target requirements. How to allocate utilities load using GCC (Grand Composite Curve) based method? | Solution: The GCC Based Method uses the Grand Composite Curve to allocate utilities (Linnhoff et. al. 1982, Parker 1989). The general heuristic is to maximize the use of the cheapest utilities. This is based on the assumption that the least expensive utilities are the hottest cold utilities and the coldest hot utilities.
In this program, a utility is considered cheaper not based on cost but based on temperature. A hot utility at a lower temperature is cheaper than a hot utility at a higher temperature.
The following methodology is used to allocate utilities using the GCC Based Method:
1. Generate the Grand Composite Curve associated with the hot and cold process streams.
2. Since the Grand Composite Curve is plotted in terms of shifted temperatures, you are required to shift the utility temperatures. The hot utility temperatures must be decreased by ∆Tmin/2 and the cold utility temperatures must be increased by ∆Tmin/2.
3. Isolate all pockets in the GCC. It is assumed that pockets are self-sufficient in energy.
Note: For point utilities, see steps #4 to #7. For non-point utilities, see steps #8 to #10.
4. It is assumed that the utilities closest to the pinch are the least expensive. For hot utility streams, use the utility with the lowest outlet temperature first. For cold utility streams, use the utility with the highest outlet temperature first.
5. Draw the first (least expensive) utility line from the temperature axis to the Grand Composite curve. Do not extend the utility line beyond the entrance of any pockets in the GCC.
6. Draw a vertical line from the outlet temperature of the first utility line to the inlet temperature of the next (second least expensive) utility.
7. Continue using utility streams in this manner until you satisfy the minimum required utility load (target utility load).
8. Plot the inlet utility temperature vertically above the end vertex of the Grand Composite Curve.
9. Depending on the outlet utility temperature, pinch temperature, and the shape of the GCC, there are three possibilities.
9.1. If the outlet utility temperature is below the pinch temperature, draw a line from the inlet utility temperature to the pinch point. Extend this line to the outlet utility temperature. The load and losses can be determined graphically as shown below.
9.2. If the outlet utility temperature is greater than the pinch temperature, draw a line from the inlet utility temperature to the outlet utility temperature on the temperature axis.
9.3. If a large pocket exists in the GCC and is situated between the inlet and outlet utility temperatures, draw a line from the outlet pinch temperature to the inlet temperature such that it touches the GCC only at one point. The load and losses can be determined graphically as shown below.
10. Continue using other utility streams in this manner if the minimum required utility load (target utility load) is not satisfied.
Key Words
Grand Composite Curve
GCC
Utility load allocation
Pinch analysis
Keywords: None
References: None |
Problem Statement: How are the semi-dynamic flash calculations carried out in the Fire Scenario of the Safety Analysis Environment? | Solution: The semi-dynamic method first carries out an initialization as follows:
1. Flash the reference stream at operating conditions to get the liquid and vapor
2. Re-mix according to the relative masses of liquid and vapor based on the stated liquid level
3. Apply constant density flash at relieving pressure
4. Calculate wetted area based on revised liquid density, taking into account of vaporization
Then based on these initial values the maximum relief flow is calculated as follows:
1. Flash liquid contents to next temperature
2. Note amount vaporized
3. Based on wetted area from the previous iteration, calculate heat input.
4. Based on enthalpy difference, calculate time elapsed
5. Calculate relieving flow from amount vaporized and time elapsed
6. Update wetted area based on remaining liquid
The steps are repeated until the stated maximum iteration temperature is reached. The maximum volumetric flow is then selected for relief calculation.
Keywords: Safety Analysis Environment, Fire Scenario, Semi Dynamic Flash
References: None |
Problem Statement: How to add several sets of physical property parameters to accurately representing physical properties in different operating conditions? | Solution: Most parameters used in property models can have more than one set of values for a given component or pair of components. To enter several sets of values for a parameter, you must use a separate Parameters form (with a unique ID) for each set of data.
For example, you can use this feature when you use one set of the UNIQUAC parameters (Data set=1) for vapor-liquid equilibrium calculations and another set (Data set=2) for liquid-liquid equilibrium calculations. To do this, you must create or define two property methods using the Methods | Selected Methods | Models sheet, as follows:
1. Define one property method to use the UNIQUAC model (GMUQUAC) to calculate activity coefficients (Liquid gamma) with data set number 1.
2. Define another property method to use the UNIQUAC model. Check the “Modify” box, and enter a new property method name (for example, UNIQUAC2). Change the data set for GMUQUAC to 2.
3. Use the Methods | Parameters | Binary Interaction | UNIQ-1 form to enter the vapor-liquid parameters (Data set=1), and the UNIQ-2 form to enter liquid-liquid parameters (Data set=2).
4. Go to Simulation Environment, in Block Options | Properties, you could select UNIQUAC (which uses UNIQ-1 binary interaction parameters) or UNIQUAC2 (which uses UNIQ-2 binary interaction parameters) for different blocks depending on their operating conditions.
Key Words
Physical property parameters
Data set
Property method
Keywords: None
References: None |
Problem Statement: What’s New in V11: Reporter Economic Evaluator (EE) Functionality and Usability Upgrade | Solution: The EE reporter has undergone significant changes to upgrade its functionality and usability.
The reporter database new features include:
“Crystal reports” items are replaced with SQL Server Reporting Services (SSRS) also known as Report Definition Language (RDL) generated reports.
A new SQL Server database is added (support for Local Database only) to support the SQL Server Reporting Services. It will run concurrently with the legacy Access DatabaseSolution. (Support for Access will continue for an undetermined time.)
All current ‘standard’ reports are presented in a .pdf format. MS Word and HTML format reports are discontinued. (.pdf can be displayed in a browser if needed)
Queries for Access database reports will be migrated to SQL Server database and queries for Crystal Reports will be migrated to RDL reports.
The Icarus reporter user interface update includes:
Basic usability improvements in existing forms
Update of file creation/browse and loading forms to modern conventions
Keywords: V11, new, new reporter, reporter, SQL, upgrade
References: None |
Problem Statement: Why the Microsoft Access databases no more work in Aspen Utilities Planner V11? | Solution: Starting from V11, all databases used for Optimization need to be configured in SQL server databases.
All existing Microsoft Access Databases must be converted to SQL databases (.mdb) before running Optimization in V11. A conversion tool is supplied with the V11 installation media. This tool can be found in:
C:\Program Files\AspenTech\Aspen Utilities Planner V11.0\bin\ATUDatabaseConverter.exe
Key Words
Optimization, SQL Database, Conversion
Keywords: None
References: None |
Problem Statement: When performing distillation synthesis, in the azeotrope search report there are three classifications for pure components and azeotropes: stable node, unstable node and saddle. What are their differences? | Solution: Pure components and azeotropic points are called nodes. Three different types are possible:
Stable node: This is the pure component or the azeotropic point with the highest boiling temperature and lowest vapor pressure in a distillation region. All residue curves end at stable nodes.
Unstable node: This is the pure component or the azeotropic point with the lowest boiling temperature and highest vapor pressure in a distillation region. Residue curve never reach an unstable node.
Saddle: These are pure components or azeotropic points with an intermediate boiling temperature and vapor pressure in a distillation region. Residue curves move toward and then away from saddles but saddles are never end points. Only border lines start or end at saddles.
For example, in the ternary map below, the three vertexes for pure MEOH (methanol), ETAC (ethyl acetate) and ETBE (Ethyl tert-butyl ether) are stable nodes. The azeotropes of 62.28 degree C and 71.84 degree C are saddles. The azeotrope of 57.19 degree C is an unstable node.
Key Words
Stable node
Unstable node
Saddle
Azeotrope search
Distillation synthesis
Keywords: None
References: None |
Problem Statement: This | Solution: frames to select what user can access to specific APC applications.
Solution
In this case I have two users: student with admin privileges and instructor with operation privileges, and two applications named: testcol and acol.
The target here is to make only testcol and acol available for the user instructor and take away the rest of the application from this user view:
1.- On the administrator page (in this case student) go to the configuration tab and then to security. The first thing to set here is to add a role (optional) and a new user. In this case I have already add the role Webtest and the user instructor.
2.- Go back to permissions and you will have to add the application that will be displayed for that user. to do this and after selected the host server (in this case APC), click on add (next to the application drop down list) and manually enter the applications that will be the target, in this case acol and testcol.
3.- I will select first the acol application and just give the correct permits for this application. in this case i will allow the same permits for student and instructor, and the same thing for testcol:
Then click on apply (this may take a couple of minutes).
4.- Verify that for the rest of the applications from the drop down list the specific user does not contain any other specific permit, otherwise these applications will appear on the display of the user which you want to restrict the access. Take special care with the default option from the drop down list and remove all the permits that you have for the specific role, if not the rest of the application will display and click on apply.
5.-Finally you should see just the application restricted for every user. if you do not notice the changes probably you will need to do an IIS reset for the changes take place specially for the new roles and users add.
Keywords: PCWS, User and Roles, Security
References: None |
Problem Statement: Flare KO drum내 조성(composition) 기입은 왜 필요한가요? | Solution: KO drum 의 용도는 Flash통해 발생된 liquid product성분을 분리하기위함입니다.
만약 KO drum의 outlet product가 순수100% liquid일 경우, vapor outlet은 발생하지 않을 것이며, 이로 인해 전체 flarenet software 수렴에 문제를 야기 할 수 있습니다.
따라서 이러한 수렴오류 방지를 위해, flarenet제품은 KO drum내 가장 light gas성분의 조성(<0.001% by default)을 vapor outlet조성으로 사용합니다. 물론 user가 이러한 값을 직접 입력도 가능합니다. 즉, outlet product가 100% liquid일 경우, KO drum내에 입력된 미량의 vapor 성분이 자동으로 적용 및 수렴되도록 flare 제품은 디자인되어 있습니다. 참고로 outlet product에 vapor가 존재할 경우, default (or user입력한) vapor 조성 반영되지 않습니다.
Keywords: KO Drum, Composition, Light Gas
References: None |
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