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Problem Statement: This knowledgebase solution documents how to install Microsoft SQL Express 2012. | Solution: Step 1.
To begin, launch the install program and choose the top option to install a new stand-alone installation.
Step 2.
Read and accept the license agreement and click Next. At this point you can choose the features that you want to install. You can also change the install folder if you do not want to install to the default location.
Click Next to continue.
Step 3.
Now you can configure the SQL instance. If this is the first instance of SQL Server on your computer, you probably want to change this setting to Default instance. If you already have another instance of SQL Server, you will want to use Named Instance and give it a name.
Click Next to continue.
Step 4.
The next step is server configuration. From here you can change the Windows services associated with this instance of SQL Server. You can keep the defaults here unless you want to specify different user accounts for the services. You can also change the default collation settings if you are not in the United States.
Click Next to continue.
Step 5.
Now we come to the Database Engine configuration. On the Server Configuration tab you can select whether SQL Server will only authenticate using Windows accounts or you can choose Mixed Mode which will allow Windows accounts and SQL accounts. I usually set this to mixed mode and set a password for the “sa” account. You can also add or remove accounts that will be SQL administrators.
Step 6.
On the Data Directories tab you can change the locations of various files that SQL will use. Depending on your server configuration and the load that will be put on SQL, you may want to put the database and log folders on separate drives. For most people, you can leave the default values.
Click Next to continue.
Step 7.
The next step configures Reporting Services. Set this to Install Only if you don’t need reporting services or may need them in the future. You can always go back and configure it later.
Click Next to continue.
Step 8.
On the Error Reporting step, you can choose whether or not you would like to send error reports to Microsoft to help them improve future releases of SQL server.
Click Next to continue.
At this point, SQL Server will install on your computer. This could take a while to complete depending on the computer you are using.
Once the installation has completed, you will receive a screen showing the details of what was completed and if there were any problems.
KeyWords
RDBMS
SLM
Keywords: None
References: None |
Problem Statement: Is it normal for both streams in a Heat Exchanger to be decreasing their temperature? | Solution: The expected behavior on a Heat Exchanger is for the cold stream to increase its temperature and the hot stream to decrease its temperature. However, it is possible to encounter scenarios where the cold stream can also be decreasing its temperature.
Thermodynamically speaking, when you are in the V+L region of a system, any pressure drop will cause an automatic temperature drop as well.
This is better represented in a PH envelope:
Lets neglect pressure effects for now (P=constant). Outside the V+L region, changes in enthalpy will cause a significant/notorious effect on temperature. If enthalpy increases, so does temperature (and vice versa).
On the other hand (still neglecting pressure effects), inside the V+L region, enthalpy changes have a small effect on temperature (non existing for pure components - no temperature change).
Now, for the case of a cold stream (for which temperature is expected to increase), inside the V+L region, enthalpy increments could barely increase its temperature. However, the effect of pressure drop (caused by friction for example) could cause a temperature decrease, so the overall effect is a lower temperature at the end of the exchanger.
Hence, even if the expected behaviour of the stream was to increase its temperature up, it actually cooled down as well.
If you are encountering these issues and you want your Heat Exchanger Cold Outlet Temperature to increase, you should specify the dP of either tube side or shell side (depending on the cold stream location) as zero.
Keywords: Cooling, Heat, Exchanger, Stream
References: None |
Problem Statement: Is it possible to customize a BLOWDOWN flowsheet to attach the depressurization line to the liquid outlet of the vessel? | Solution: Blowdown performed from the vessel bottom allows the most rapid decrease of liquid level with time, hence the interest on modeling this configuration in BLOWDOWN.
In Aspen HYSYS, the default Single Vessel template will not allow any re-location of the depressurization (Blowdown) line, this default template will only allow the user to attach the blowdown line to the vapor outlet, the vessel or to the inlet lines.
In order to simulate a system with the blowdown line attached to the liquid outlet of the vessel, the user should download and install the Bottom BLOWDOWN™ Template (*.BLO). This template file, along with instructions about how it can be installed in Aspen HYSYS can be found here.
Keywords: Liquid, Bottom, BLOWDOWN, Flowsheet, Pipe, Pipeline.
References: None |
Problem Statement: Why do I have a zero value in the Olefins content in the feed stream of the HBED? | Solution: When you use the HBED reactor, the required component list is HCR.cml with the HCRSRK package. Given a stream with these settings to be used as feed stream of the HBED reactor, you can notice the Olefins content is always zero.
If the composition of the HBED is not manually defined, you usually get it with a cutter. This one allows to do the transition between other component list and fluid package (for example, an assay defined from Petroleum Assays and Peng Robinson as property package) to the HSRSRK package with its corresponding component list.
Currently there is no way to get the olefin composition from the stream going to the HBED. Even if the olefin components were non-zero (before a cutter transition), it would map them back to the non-olefin species and then remap back to the olefin components based on what was entered for the olefins or the bromine number.
The reason for this is we typically don't expect to have accurate olefin information beyond the naphtha region (not to mention that many of the unsaturated double bonds may be attached to aromatic or naphthenes which wouldn't be captured by the olefin property as those take precedence over olefins).
As a workaround, the user can either enter a bromine number or olefin content directly on the HBED. If they have a stream before transition that they think has a good olefin content, they could use that to specify the value (either through a spreadsheet or perhaps a set block).
Keywords: Olefins, Bromine Number, Stream, Properties, HBED, Feed.
References: None |
Problem Statement: Is it possible to report the same stream property with two or more units in the Aspen HYSYS Workbook? | Solution: Currently all the properties reported in the Aspen HYSYS workbook will always use the same units that are specified in the selected unit set, this means that if the user adds multiple times the same stream property, all the duplicates will always use the same unit.
There are two issues to solve in this situation, first that the HYSYS workbook currently has no way of allowing the user to change the reported unit for each variable, and second, since the workbook can report the information of all the streams in the simulation, we need to implement a change that is applied to all the streams of the model in a fast and easy way.
The best solution is to create a simple user variable, that will only simply report any property of interest in a specific unit. An example showing how these variables are defined from scratch can be found on article 028815
One thing to consider while building the user variable is that the user can control the units in which this variable will be reported, this is specified from the variable setup:
The user can freely choose any unit applicable to the variable, but it’s important to not delete the quotation marks (“”) and to enter the variable with the exact same spelling that HYSYS uses, respecting lower and upper caps (i.e. kPag). This unit is completely independent from that specified on the global unit set.
It is recommended for the user to set the variable to be Calculate only, choose the “User” units to display decimal digits and set Automatic activation so the variable is reported in all streams. Entering a useful Tag for the variable is also important, this tag will be displayed in the workbook.
Once the variable has been successfully created it can now be reported on the workbook.
Note: Values for the user variables will always be displayed as <empty> the first time the variable is added to a stream or each time it is edited. To fix this simply force the stream to solve again by changing any spec on the stream and then switch back to the original inputs.
To add the variables to the workbook simply click on the Setup button and click on Add, all the variables will be organized under the User Variable category. Click Done after adding all the necessary variables.
The user variables will now be reported on the HYSYS workbook and their units will be different from those reported for the normal variables:
You can find attached a simple example with two user variables to report Pressure and Temperature. The user variable file (*huv) is included as well. The file was created in HYSYS V10, an XML version is included for older versions.
Keywords: Workbook, User Variables, Stream, Units, Single, Double, Example.
References: None |
Problem Statement: Can I track the temperature profile of a Tail Pipe across its length in a BLOWDOWN scenario? | Solution: Tail Pipes in BLOWDOWN record a full temperature profile, not only for each time evaluation, but they also report the temperature profile across the pipe length. It is important to notice that even though all the pipes in a BLOWDOWN flowsheet record and report the temperature for each time step, only the tail pipes (downstream of the orifice) can report a profile across the pipe length.
To view the two temperature profiles, locate the tail pipe of interest on the BLOWDOWN flowsheet, double click on it to open the pipe summary
Switch to the Results page, this will display two tables, the top one shows data obtained for each time step, while the bottom one will display the length data at a specific time.
To view the length temperature profile, the user must first select a row on the top table that corresponds to the time of interest. Once a row is clicked, the bottom table will update automatically. A label between both tables will indicate the time of evaluation of the data on the second table.
If the user selects a different row on the first table, this allows the user to review how the profile changed as the blowdown analysis progressed with time.
Keywords: Profile, Length, Temperature, Tail pipe, Piping, Blowdown, Orifice.
References: None |
Problem Statement: Is there a minimum limit for the time step on the BLOWDOWN run controls? | Solution: The specified time step in BLOWDOWN run controls allow the user to report the conditions during the depressurization at different paces. Though there is no limit on the number of points that can be reported for long time specifications, there is a limit for the minimum time step that can be entered.
The minimum time step is 0.0001 seconds, upon entering a value lower than this the following warning will appear.
To avoid seeing this warning, make sure that the time step entered on the Run Controls form is higher than 0.0001.
Keywords: Run Controls, Blowdown, Halt, Minimum, Limit.
References: None |
Problem Statement: Data Reconciliation: differences between running a model with and without measurements | Solution: The Data Reconciliation run mode is used to minimize mismatch between measurements and model by adjusting model parameters and offsets and tries to obtain the best value by doing so. It distributes mismatch to among the measurements. It is a non-square case, meaning there are many degrees of freedom (specified as variables). These variables behave in a way in which they have a certain freedom.
The very first step in setting the Data Reconciliation problem is to Define the Sum of Squares objective function. This function minimizes the Weighted Sum of Square Errors; this minimize is subject to satisfying model equations and feasibility constraints.
In a simple Data Reconciliation problem, you do not necessarily have to add Measurement Blocks to the model. The data available from the Plant can be added on the Setup tab of the Objective function under EO Configuration.
In this example, we are not using a Measurement block, so we enter the Plant variable values as the Mean and the Model values as the variable; then apply Standard Deviation for the Mean in the form.
So, in this first Reconciliation (without Measurement blocks) we are merely minimizing the difference between the Plant and the Model with the Sum of Squares objective function (similar to the Data Rec in SM mode, where it will estimate the offset from the model results vs the data you provide).
An important concept is the mean. The Mean, as the name states, is the mean or average value of the variable configured in the Data Rec form. In other words, if the Variable in the Sum of Squares function is the Model value, the Mean would be the Average Model value (Plant value); if the Variable is the Offset, the Mean is the Average Offset, etc.
Without Measurements, the Bias in the results can be seen as the Mean (input specified value) in the Objective Function Results | Term Results:
On the other case (where we do have Measurement blocks), the Sum of Squares function remains the same; however, both the Variable and the Mean values change. The Variable is now defined as the Offset and the Mean is defined as ZERO, hence, we are now minimizing the offset (once the Measurement blocks are entered, they have Offset as available variable for selection):
If the values and the variables were introduced the same way, the results should be identical between one mode and the other.
Keywords: EO, Reconciliation, Data, Measurement
References: None |
Problem Statement: How to set the stream composition via a feeder block in steady state and dynamic mode without do the normalization every time? | Solution: Each feed stream has a Feeder Block, which is a holder for composition and conditions of the stream. This is used to make sure the stream composition and conditions are recovered after a case of flow reversal, where the stream acts as a product stream and gets its conditions and composition from the downstream operation. The feeder block compositions can be found in the Specs sections of Dynamics Tab of the stream and clicking on the feeder block button.
The feeder block can be used in steady state and dynamic state to change the composition. As mentioned, in the Article Setting stream composition via a spreadsheet, the user can set the composition of the stream via spreadsheet. However, this option does not work in a dynamics simulation.
To use the feeder block in the Spreadsheet, instead of add the Master Comp Mole Fracc as an exported variable in the Spreadsheet, select the Feeder Block and the desire composition.
In the attached file "Composition Set via Spreadsheet.hsc", the user can see the differences of the two methods.
Keywords: Spreadsheet, Feeder Block, Compostions
References: None |
Problem Statement: Can I access the variables of an Aspen Hydraulics flowsheet through VBA? | Solution: The objects inside an Aspen Hydraulics subflowsheet are not directly incorporated in the VBA libraries of Aspen HYSYS, so these objects cannot be exposed through automation as any normal object in Aspen HYSYS.
If the user wishes to access these objects using VBA, the only workaround currently available is to access them as a backdoor variable.
For more information and applied examples on backdoor variables, we recommend reviewing article 031157.
Keywords: VBA, Automation, Hydraulics, Backdoor, Pipe, Flowsheet.
References: None |
Problem Statement: Is the user coding automatically read by AFR or do I have to specifically invoke it? | Solution: The five different subroutines are invoked by AFR at different times. The user does not have to invoke them separately as this is an automated process.
Simulation_Start / SimStart - Invoked once per simulation. All object properties and conditions are initialized according to the designed states.
Lifecycle_Start / TimeZero - Invoked once at the beginning of every life cycle. All object properties and conditions are initialized according to the designed states.
Lifecycle_Event / SimEvent- Invoked once for every event that occurs during a lifecycle. There are six events:
An event activates
An event deactivates
A tank becomes full
A tank becomes empty
A tank reaches its set point
Spare replenishment
Lifecycle_End / EndofTime- Invoked once at the end of every life cycle.
Simulation_End / SimEnd- Invoked once per simulation.
Key words
user coding, SimEvent
Keywords: None
References: None |
Problem Statement: Is it possible to use the Aspen HYSYS Simple Solid Separator in Dynamics mode? | Solution: The simple solid separator equipment has a Dynamics tab but when you access to it, you will read the message "Unable to run Dynamically at this time".
This is because currently the solid operation in Dynamics are not supported.
Keywords: Dynamics, Mode, Solid Separator.
References: None |
Problem Statement: How are the nozzle Parameters for a Heat Exchanger in Dynamics defined? | Solution: For a Dynamics Heat exchanger user can enter the nozzle parameters under Rating | Nozzles. The inputs that can be entered are described as follows:
Base Elevation Relative to Ground Level is the distance between the base of HX and the ground level. Elevation (Base) is the distance difference between the nozzle elevation and elevation of HX base. Elevation (Ground) is the difference between nozzle elevation and ground level.
To calculate the last number, we need HX height. HX height is equal shell diameter if HX is horizontal and height is equal to tube length if HX is vertical. Elevation (% of height) can now be calculated,
Elevation (% of height) = Elevation (Base) / HX height (shell diam in this case) * 100%
You will notice that the Elevetion (% of Height) limits the input from 0-100%, this is because the nozzle elevation with respect to HX height should be between 0% (bottom) and 100% (top). This number relates back HX height. This means that practically user should not input any value for Elevation (Base) that is larger than the height of HX.
Keywords: Dynamics, Heat Exchanger, Parameters, Nozzles.
References: None |
Problem Statement: Why the Column Internals Holdups are different from the Rate-based Holdups? | Solution: For a rate-based packed column, the result reported for the Column Internals Liquid Holdups (Column Internals | Sections | CS-1 | Results | By Stage | Hydraulic Results) might be different from the values reported on the Rate-based Liquid Holdups (Rate-Based Modeling | Interface Profiles | Holdups)
The Column Internals Holdups are used to calculate the pressure drop based on vendor correlations, while the Rate-Based Holdups are used to calculate the reaction rates based on the holdup correlation specified by the user (Rate-Based Modeling | Rate-based Setup | Holdups). Therefore, the calculated holdup results could be different.
Note: AspenTech is not authorized to disclose vendor correlations, so it’s not possible to know the specific correlation Aspen Plus is using to calculate the Column Internals Liquid Holdup.
Keywords: Column Internals, Rate-base modeling, Liquid Holdup, Holdup correlation.
References: None |
Problem Statement: How do I change the default file path when clicking on Open Case in Aspen HYSYS? | Solution: When clicking on File | Open | Open Case button, Aspen HYSYS opens the default Samples folder. To change this folder, go to File | Options | Simulation | Default File Paths and change the Cases path to the desired one.
To change the path in Aspen Plus, please refer to the following article: How do I set the default file path when opening a case in Aspen Plus
Keywords: Path, HYSYS, Location, Cases.
References: None |
Problem Statement: This knowledgebase solution documents how to install Microsoft SQL Express 2012. | Solution: Step 1.
To begin, launch the install program and choose the top option to install a new stand-alone installation.
Step 2.
Read and accept the license agreement and click Next. At this point you can choose the features that you want to install. You can also change the install folder if you do not want to install to the default location.
Click Next to continue.
Step 3.
Now you can configure the SQL instance. If this is the first instance of SQL Server on your computer, you probably want to change this setting to Default instance. If you already have another instance of SQL Server, you will want to use Named Instance and give it a name.
Click Next to continue.
Step 4.
The next step is server configuration. From here you can change the Windows services associated with this instance of SQL Server. You can keep the defaults here unless you want to specify different user accounts for the services. You can also change the default collation settings if you are not in the United States.
Click Next to continue.
Step 5.
Now we come to the Database Engine configuration. On the Server Configuration tab you can select whether SQL Server will only authenticate using Windows accounts or you can choose Mixed Mode which will allow Windows accounts and SQL accounts. I usually set this to mixed mode and set a password for the “sa” account. You can also add or remove accounts that will be SQL administrators.
Step 6.
On the Data Directories tab you can change the locations of various files that SQL will use. Depending on your server configuration and the load that will be put on SQL, you may want to put the database and log folders on separate drives. For most people, you can leave the default values.
Click Next to continue.
Step 7.
The next step configures Reporting Services. Set this to Install Only if you don’t need reporting services or may need them in the future. You can always go back and configure it later.
Click Next to continue.
Step 8.
On the Error Reporting step, you can choose whether or not you would like to send error reports to Microsoft to help them improve future releases of SQL server.
Click Next to continue.
At this point, SQL Server will install on your computer. This could take a while to complete depending on the computer you are using.
Once the installation has completed, you will receive a screen showing the details of what was completed and if there were any problems.
KeyWords
RDBMS
SLM
Keywords: None
References: None |
Problem Statement: Is it normal for both streams in a Heat Exchanger to be decreasing their temperature? | Solution: The expected behavior on a Heat Exchanger is for the cold stream to increase its temperature and the hot stream to decrease its temperature. However, it is possible to encounter scenarios where the cold stream can also be decreasing its temperature.
Thermodynamically speaking, when you are in the V+L region of a system, any pressure drop will cause an automatic temperature drop as well.
This is better represented in a PH envelope:
Lets neglect pressure effects for now (P=constant). Outside the V+L region, changes in enthalpy will cause a significant/notorious effect on temperature. If enthalpy increases, so does temperature (and vice versa).
On the other hand (still neglecting pressure effects), inside the V+L region, enthalpy changes have a small effect on temperature (non existing for pure components - no temperature change).
Now, for the case of a cold stream (for which temperature is expected to increase), inside the V+L region, enthalpy increments could barely increase its temperature. However, the effect of pressure drop (caused by friction for example) could cause a temperature decrease, so the overall effect is a lower temperature at the end of the exchanger.
Hence, even if the expected behaviour of the stream was to increase its temperature up, it actually cooled down as well.
If you are encountering these issues and you want your Heat Exchanger Cold Outlet Temperature to increase, you should specify the dP of either tube side or shell side (depending on the cold stream location) as zero.
Keywords: Cooling, Heat, Exchanger, Stream
References: None |
Problem Statement: How to add the Aspen HYSYS’ Adjust ‘Reset’ button into Aspen Simulation Workbook (ASW)? | Solution: By design, the Adjust ‘Reset’ button is not available through the ASW Organizer. However, you can use a SendMessage action via macro to access to it:
Open an ASW workbook linked to a case that includes an Adjust block (for this example, let's call it “Adj-1”)
Place a button control onto the Excel worksheet and link it to a VBA macro. The macro should contain the following code:
Sub DoReset()
AspenSimulationWorkbook.ASWHysysSendMessage “Top.appModel.Blocks.Adj-1”, “Reset”
End Sub
Click the button. The macro will then invoke the SendMessage action which in the HYSYS adapter results in the “Reset” message being sent to the block Adj-1.
Keywords: ASW, Adjust reset button, VBA macro, SendMessage.
References: None |
Problem Statement: While building the model, I want to be able to check what happens if a certain equipment goes down and how that affects the rest of the model. Is there a feature that can be used for the same? | Solution: The easiest way to achieve this is using the View Active Status button with the Validate feature.
Clicking the View Active Status button opens the Operational Status window. The window lists each unit in a closeable folder containing all events associated with the unit. You can use the checkbox to change the active status of events and units. Clicking the unit-level checkbox overrides the active status of events in the unit. (for example, deactivating Unit3 deactivates Event8, Event9, and Event10). To create a mixed state for a unit, you must manually change the active status of events in the unit (for example, Unit2).
The unit checkbox has four possible displays:
Gray with inactive check if the unit contains no events.
Blue with white check if the unit contains events and all events are active.
White with no check if the unit contains events and all events are inactive.
White with blue square if the unit contains more than one event and the unit is in a mixed state.
The event checkbox has two possible displays:
Blue with white check if the event is active.
White with no check if the event is inactive
The wrench icon appears whenever the event is inactive regardless of the method used to change its status.
Note that Specifying an event's active status in the graphical user interface is used only for validation purposes. To manipulate an event's active status during a simulation, specify the condition in VSTA.
After deactivating the concerned Events/Units, you can click on the Validate button to see the effect on the model.
Key words
View Active Status, Validation
Keywords: None
References: None |
Problem Statement: Why can I not run the FAST add-in in AFR V10 with Office 2010? | Solution: When using Office 2010 with AFR V10 you will need to download VSTO (Visual Studio Tools for Office) from the Microsoft website. The link is given below:
https://www.microsoft.com/en-us/download/details.aspx?id=48217
You will need to restart Excel after installing VSTO.
Keywords: Office 2010, VSTO
References: None |
Problem Statement: Can I include fittings in the pipelines of my BLOWDOWN model? | Solution: In Aspen HYSYS BLOWDOWN, not all the piping items perform pressure drop calculation. Depending on the BLOWDOWN template that the user choses to load in HYSYS, some types of pipes will be able to perform this calculation.
In the normal Single Vessel template, only the “Tail Pipe” pipes can perform this calculation:
Because pressure drop is only calculated on this type of item, this is the only section where fittings will have an effect and should be considered. The rest of the pipes should not have any changes due to fittings.
The Pipe Geometry form in BLOWDOWN does not have any direct option to allow the users to choose and add fittings. Thus, the effect of fittings should be manually calculated and entered as a total equivalent lenght in the Tail Pipe(s). By entering the total equivalent lenght in these piping items, the system will correctly use it to calculate the pressure drop.
Note: AspenTech has developed another version of the Single Vessel template which allows pressure drop calculations on the Blowdown Pipe items (Upstream of the orifice). Entering equivalent length inputs in these type of itemsb are also effective when using this template.
The template can be downloaded here:
(Template name: Single Vessel: Pressure drop considered upstream and downstream of the blowdown orifice)
Keywords: Fittings, Pressure Drop, BLOWDOWN, Equivalent Length.
References: None |
Problem Statement: Why does Aspen Flare System Analyzer is not using the given constraints for the Tailpipes and Headers | Solution: In Aspen Flare System Analyzer, a pipe can be treated as a Tailpipe or a Header and user has the option to define different constraints for each type by clicking Scenarios | Edit and select the Constraints Tab.
If the user wants to treat a pipe as a tailpipe, the Yes option must be selected in the Tailpipe drop down menu of the Pipe editor.
If Yes is selected and the "Rated Flow for Tailpipes" calculation option is selected under Calculation Settings | General, the pressure drop for this pipe will be calculated using the rated flow in place of the relieving flow rate.
If No is selected the pressure drop for this pipe will be calculated using the relieving flow rate instead of the rated flow.
Keywords: Constraint, Mach number, Tailpipe, Header, Aspen Flare System Analyzer
References: None |
Problem Statement: How can I rearrange the columns in the Flare Analyzer Pressure/Flow Summary? | Solution: You can left-mouse-click a column header, then (holding down the left mouse button) drag the column to a different location (example screenshots below):
Before:
After:
Keywords: None
References: None |
Problem Statement: Why the heat transfer area calculated by the Activated Energy Analysis is different from the one reported on Aspen HYSYS and Aspen Plus? | Solution: The total heat transferred (Heat Exchanger duty) can be defined in terms of the overall heat transfer coefficient, the area available for heat exchange, and the log mean temperature difference:
Where:
Q = total duty of the heat exchanger
U = overall heat transfer coefficient
A = heat transfer area of the heat exchanger
ΔLM = log mean temperature difference (LMTD)
FT = LMTD correction factor
Both Aspen HYSYS and Aspen Plus allows you to either specify or calculate the U (in Aspen Plus) or the UA (in Aspen HYSYS) for the exchanger models.
However, the Activated Energy Analyzer calculates the overall heat transfer coefficient U from process stream film coefficients, and this could lead to a different calculated heat transfer area.
Still, the user can change the U method to ‘Simulation’ on the Energy Analysis Environment | Project | Saving Potentials | Heat Exchanger details, to retrieve and use the same overall heat transfer coefficient used by Aspen Plus or Aspen HYSYS.
Note: Changing the “U” from Default to Simulation does not affect the total duty, but the existing area for that Heat Exchanger will be re-calculated, and hence your existing network total area changes. The Area Target for the HEN remains the same, but the “% of Target” for Total Area will be also affected.
For more information about the heat transfer coefficient calculations, refer to the article Where can I find the equations used to calculate HTC?
Keywords: Heat Transfer Area, Energy Analysis, Heat Exchanger, Heat Transfer Coefficient.
References: None |
Problem Statement: Is it possible to open my HYSIM files in Aspen HYSYS V8.6 and upwards? | Solution: Since V7.3 the option to open .sim cases was removed therefore you don't have the option to open these files in newer versions of HYSYS. The only alternative is to open the HYSIM case in older versions (for example V7.2) and save the case as .hsc. However, older versions are no longer supported and there's no guarantee to have working cases because compatibility issues. The newest versions have been modified and improved to offer better solutions.
Keywords: HYSIM Cases
References: None |
Problem Statement: When running the Activated Exchanger Design and Rating (EDR) tool within Aspen Plus, the simulation stops converging and the user gets the following message on the Control Panel:
ERROR WHILE GENERATING RESULTS FOR UNIT OPERATION BLOCK: “xxx” (MODEL: “HEATX”)
FAILED TO ACCESS SECURITY LICENSE FOR SHELL&TUBE
BLOCK BYPASSED
How can we overcome the error message? | Solution: This license error message may appear due to various reasons:
The user does not have enough tokens to run both Aspen Plus and Aspen EDR at the same time
The Aspen EDR license key is not available on the license server
The license server is not reachable or not running
Detailed steps on how to resolve the license issue are contained in the following articles:
How do I troubleshoot the error message "All licenses are currently in use"?
What is the SLM License Profiler and how do you use it?
If the steps mentioned on the articles listed above do not solve the issue, as a workaround, the user can import the transport properties and phase equilibrium data from Aspen Plus to Aspen EDR standalone:
Import Heat Exchanger Data to Aspen EDR for Preliminary Design
Keywords: Activated Exchanger Design and Rating, FAILED TO ACCESS SECURITY LICENSE FOR SHELL&TUBE
References: None |
Problem Statement: Why do I get the message "Error whist checking out license, this may be due to a time-restriction on the license"? | Solution: The error you are getting means your license has expired. To verify if your license has expired please follow the simple steps mentioned below:
Step 1: Locate a copy of your license file.
Step 2: Open your license file in a text editor like Notepad.
Step 3: Check the date of expiration in the file. Example shown below:
If your license has expired please submit a new license key: Place a License Key Request
Keywords: Code: -939519987, This may be due to a time-restriction on the license, Error while checking out license HYSYS_Process, Error while checking out license AspenPlus, License, SLM, expire.
References: None |
Problem Statement: How to get error messages from DMCplus Collect logged in Valid.err. | Solution: In DMCplus Collect, if the data collection has an error due to tag validation then it is possible to record this error in valid.err file. The following steps show how to enable this feature -
1) Click on My Computer/Properties
2) Navigate to Environment Variables - Add system variable name as ACOD_HOME
3) Variable value - C:\ProgramData\Aspentech\APC\Online
4) Reboot the system.
5) The error messages in collect file are now collected in valid.err file.
Keywords: Collect
Valid.err
References: None |
Problem Statement: In Aspen Plus, why doesn’t liquid heat capacity change with temperature when utilizing the NRTL property method? Plotting liquid heat capacity vs. temperature in the Properties environment does not reflect temperature dependence. | Solution: The NRTL property method does not, by default, utilize liquid heat capacity parameters (this can be deduced by examining the Route Details for the HLMX liquid mixture enthalpy property):
By default, the NRTL method indirectly back-calculates liquid heat capacity, from liquid enthalpy. If the user wants the NRTL method to utilize liquid heat capacity parameters, they can create a new NRTL method (e.g. NRTL-CP), and specify it to use liquid reference state enthalpy:
Keywords: None
References: None |
Problem Statement: When “Use Multi-Processing” option is turned on while running a model with PIMS AO Multi-Start, it is observed that sometime the OBJFN could be different in each run. Why is this happening? | Solution: This is by designed. If you are running model with multi-processing turned ON, and if you have # trial points (# starting points) >= # processors, the run is non-deterministic, i.e., the results may change with each run.
The fact is that when we use “Use Multi-Processing” to run Multi-Start, the input solution for next solve is determined from the feedback (solution) of previous solve, and hence the results can be different depending on the order of the solve (which could be different at every individual run) and the feedback from that previous solve.
Here is the detailed step of how multi-start works with “Use Multi-Processing” turned on, the key point to note is step 4 and 9 which explains why is there a difference in the results.
1. RUN 1: The base problem is solved and a solution is generated.
2. The solution is used to generate a large set of candidate input solutions. Proprietary methods are used to generate these candidates, but they are designed to cover the entire solution space of all the variables being randomized.
3. When “Use Multi-Processing” option is turned ON, we start a number of different parallel solves, depending on how many solves you want and how many processors you selected to use. Let say we want 20 solves (starting points) and we have selected 4 processors. The initial 4 solves each get an input solution selected from the candidate set, again using proprietary methods to choose which input solutions are "best".
4. One of the solves completes and comes back, let's say the one from processor 1 using input solution 1. The information from this solve including the objective function value and the variable values is used in a proprietary algorithm to select another input solution from the candidate set to send to the processor to do another solve (say the 5th solve).
5. This happens each time for the remaining solves, each time an input solution is selected from the candidate set using feedback from the previous solves.
6. The solve completes and reports the best found solution from the base solve and the 20 Multi-Start solves.
7. RUN 2: Now we run the same model with Multi-start again (on the same machine or on a different machine). Again the base solve is done and this will be the same as the previous run.
8. The same set of candidate solutions is created. The same 4 input solutions are selected and sent to the 4 processors. Those 4 solves will be the same.
9. This time, from those 4 solves, a different one completes first, eg. the one on processor 2 with input solution 2. The objective function and variable values from this solve are different than the one in step 4. The next selected input solution sent to the 5th solve from the candidate set can and will most likely will be different than the one selected in step 4. Then the 6th selected input solution from the candidate set will be different and so on. This can result in different solutions being found from the 20 solves and possibly a different solution (OBJFN) being reported back at the end as the optimal.
Therefore, due to the behavior of how “Use Multi-Processing” works (as above), the results could be different in each run.
Keywords: Use Multi-Processing, Multi-Start, PIMS AO, OBJFN, number of processor, starting points, global optima, local optima
References: None |
Problem Statement: When starting to use any feature from Plant Data, nothing happens for a while, and then any of these messages appears:
No connection could be made because the target machine actively refused it
An existing connection was forcibly closed by the remote host | Solution: The Aspen OnLine service is not running. Use this procedure to start the service and set it for automatic start:
Using an account with administrative privileges, open the Control Panel. Search for Services and run it.
In the Name column, locate and click Aspen OnLineVX.X.
In the Status column in this row, the word Started will appear if it is started. On the left side of the window click Start to start the service if it is not started, or Restart if it’s already running.
In the Startup Type column, the word Automatic should appear. If it does not, double click it and select Automatic in the Startup type field in the dialog box that appears.
If this problem keeps happening each time the computer is rebooted, it may be caused by the service taking too long to start at boot. To fix this, repeat the above procedure but select Automatic (Delayed Start) as the Startup type.
Keywords: Plant Data, Aspen OnLine, No connection could be made because the target machine actively refused it, An existing connection was forcibly closed by the remote host
References: None |
Problem Statement: In the Safety Analysis environment, is it possible to change the actual standards used by HYSYS to calculate a Rupture Disk area? | Solution: Aspen HYSYS uses the Coefficient of Discharge (Kd) Method Calculation based on the API 520 and Fike Form No. TB8102-3. Aspen HYSYS uses these standards because they are the most common ones used.
Unfortunately, it is not possible to change these standards in Aspen HYSYS. Users could use a spreadsheet and add the equations for the Rupture Disk based on the new standard.
Keywords: MNFA, Fike Standards, TB8104-15, TB8102-3, Rupture Disk, API 520
References: None |
Problem Statement: When sizing a shell and tube exchanger, you might see a warning message showing that "Operation Warning 1346: The shell side liquid-only outlet nozzle is not self venting". What does this warning message mean? How to eliminate this warning? Are there any resources that help explain "self-venting" system?
Root Cause
When liquid flows by gravity out of a vessel or down a pipe, a possible operating problem of gas entrainment may occur unless sufficient care has been given to the design of the offtake pipe and the plant arrangement. Entrained gas should be avoided because it not only raises the pressure drop, but also reduces the static head available to overcome the pressure drop, and thus drastically reduces the capacity of the pipe. Similar problem exists when liquid reaches its boiling point temperature, or contains dissolved gases.
One typical solution to avoid gas entrainment problem is to design a "self-venting" liquid outlet system. In this kind of self-venting system, liquid exit velocity should keep sufficiently low so that it allows entrained gas escaping out of liquid. As for liquid-only outlet nozzle design in exchanger, self-venting criteria are used to guarantee the single liquid phase exit.
In a summary, EDR reports operating warning 1346 to give a concern of gas entrainment at high liquid velocity in the heat exchanger liquid outlet nozzle. The root cause of the warning is that liquid outlet nozzle size is smaller than what the program expects. | Solution: You can try to increase the shell side liquid-only outlet nozzle size to get rid of this warning message. Please go to Exchanger Geometry > Nozzles > Shell Side Nozzles and modify the liquid outlet nozzle diameter (screen shot is showed below).
Note 1: Please review these two papers FP3: Gravity Flow and FM8: Design of Gravity Flow Systems posted in aspenONE Exchange (also attached) for more detailed explanation on "self-venting" flow system. In order to avoid entrainment of gas by liquid in vertical pipeline, low superficial velocity of liquid is necessary and the recommended criterion (cited from FM8: Design of Gravity Flow Systems equation 6) is showed below:
Note 2: Since V8.8, Aspen Process Manual and HTFS Research Network Report have been available in aspenONE Exchange, where you can find detailed design methods, equations and calculation examples. Please refer to two videos mentioned in KB 000040029 and learn how to use aspenONE Exchange.
Keywords: Aspen EDR, Shell and Tube Exchanger, Self venting, Nozzle, Pipeline, HTFS Research Network Report
References: None |
Problem Statement: When I change the decimal digits for Mass Flow in the Variable Formats Dialog, the Mass Flow label on the flowsheet still shows only one decimal digit. Why? | Solution: Since Aspen Flare System Analyzer V9.0, the Mass Flow label is limited to show only once decimal digit regardless of the changes made on the Variable Formats Dialog (File | Preferences | Formatting | Edit Variable Formats | Result | Mass Flow).
However, even though the Mass Flow label on the flowsheet will show only one decimal digit, the changes made on the Variable Formats Dialog are visible on both the pipe summary and the Pressure/Flow Summary.
The following images illustrate an example for which the decimal digits for the Mass Flow label are changed to 5. The Mass Flow label on the flowsheet still shows one decimal digit (200,000.0 kg/hr), but both the pipe summary of 'Header1' and the Pressure/Flow Summary show the mass flow value with 5 significant digits (200,000.00000 kg/hr).
Keywords: Decimal Digits, Variable Format, Mass Flow, Label.
References: None |
Problem Statement: Differences with solids-handling in Aspen Batch Modeler V10 | Solution: In V10, there are differences on how Aspen Batch Modeler performs physical properties calculations when there are solids involded, compared to previous versions.
These modifications can cause that older files opened in V10, behave in a different way and provide different results.
This is a list of the existing modifications:
In pre-V10 versions, non-volatile components, even liquids, were excluded from the composition vector, hence, they were not being considered for liquid-phase enthalpy and density calculations.
In V10, only components explicitly defined as “Solids”, will be excluded from the composition vector for liquid-phase enthalpy and density calculations.
This can cause that non-volatile components that were supposed to be solids were excluded from liquid-phase calculations in pre-V10, but not in V10 (generating different results).
When components originally defined as non-volatile “Conventional” type are changed to “Solid” type, parameters previously defined won't be transferred to the solid forms, so they will have to be populated manually by the user.
For solids to be considered in energy and volume calculations, Valid Phases selection must be Vapor-Liquid-Solid (Configuration form), otherwise, they will be excluded from these calculations too.
Keep in mind Vapor-Liquid-Solid option is only available when configuration is set as Pot-Only.
Keywords: Batch modeler, solids, non volatile, V10
References: None |
Problem Statement: How do I know if my Aspen HYSYS simulation is in Steady State or Dynamics? | Solution: A straightforward way to identify the type of simulation you have is reviewing the Dynamics tab on the HYSYS ribbon. When you have a Dynamics simulation, the Dynamics Mode button must be highlighted and the Run controls will show active.
If the Dynamics Mode is inactive, you have a Steady State simulation.
Keywords: Dynamics, Steady State, Mode.
References: None |
Problem Statement: This knowledge base article describes on how to display time in dd:hh:mm format in SCM. | Solution: Consider time = 114.7488 hrs , the logic below Rule RTEMP displays it as 4:01:02 (dd:hh:mm)
RULE
Trace of RTEMP
The below trace explains the step by step execution of RTEMP by SCM to display 114.7488 hrs as 4:01:02 .
>RTEMP1
==> Rule started >RTEMP1
RTEMP TRUE IF: ?DAY = 4.781200 = [?DECTIME=]114.7488 / 24
RTEMP TRUE IF: ?DAY = 4 = INT [?DAY=]4
RTEMP TRUE IF: ?DAY24 = 96 = [?DAY=]4 * 24
RTEMP TRUE IF: ?NX = 18.74880 = [?DECTIME=]114.7488 - [?DAY24=]96
RPARSE0 TRUE IF: [?DELIM=]. NE
RPARSE0 TRUE IF: ?NDELIM = . = [?DELIM=].
RPARSE0 TRUE IF: APPENDIF FMTVARR DELIM
RPARSE0 TRUE IF: FMTVAR(@,1,8) = [?NDELIM=].
RPARSE0 TRUE IF: APPENDIF FMTVARR INTERNAL_STRING
RPARSE0 TRUE IF: FMTVAR(@,1,64) = [?INPSTR=]18.74880
RPARSE0 TRUE IF: FMTDATA ONE RUTILSTR(PARSE)
RPARSE0 TRUE THEN: PARSE [?INPSTR=]18.74880 DELIMITED_BY [?DELIM=].
RTEMP TRUE IF: PARSE [?NX=]18.74880 DELIMITED_BY .
RTEMP TRUE IF: ?HH = 1 = CODEOF PARSEWK(0)
RTEMP TRUE IF: ?HH = 01 = STRFMT([?HH=]01,I02)
RTEMP TRUE IF: ?MM = 2 = CODEOF PARSEWK(1)
RTEMP TRUE IF: ?MM = 02 = STRFMT([?MM=]02,I02)
RTEMP TRUE IF: ?TIME = 4:01:02 = '[?DAY:KOLON?HH:KOLON?MM=]****'
RTEMP TRUE THEN: RTEMP_CONVERT_DECIMAL_TIME [?DECTIME=]114.7488 [?TIME=]4:01:02
RTEMP1 TRUE IF: RTEMP_CONVERT_DECIMAL_TIME 114.7488 [?TIME=]4:01:02
RTEMP1 TRUE IF: STATMSG [?TIME=]4:01:02
RTEMP1 TRUE THEN: RTEMP_RUN
==> Rule >RTEMP1 total time: 0.00 sec
Note : Trace log can be generated from Developer tab
Keywords: None
References: None |
Problem Statement: Which property method is recommended to model dehydration process using glycols (MEG, DEG, TEG)? | Solution: We recommend users to use the improved Cubic- Plus- Association (CPA) package to model MEG, DEG and TEG dehydration processes starting V10.0. The Aspen HYSYS V10.0 CPA package includes updated validated parameters that cover a broader range of components and operating conditions. You can continue to use the Glycol property package for legacy TEG dehydration cases or for situations where faster performance is required. However, Glycol property package cannot model MEG and DEG due to the lack of parameters.
For more information, please review the dehydration example: https://esupport.aspentech.com/S_Article?id=000045430
Keywords: Dehydration, TEG, MEG, DEG, CPA package
References: None |
Problem Statement: Does an expansion in a pipe segment can affect the Mach number calculation in Aspen Flare System Analyzer? | Solution: In Aspen Flare System Analyzer (AFSA), as mentioned in the Article ID 000032070 the mach number is defined as the fluid velocity between the sonic velocity or:
If the customer add a drastic expansion between two pipes, this expansion will generate a considerable change in the pressure and the density (Pressure depending) generating an increase in the Mach number.
For example, if the customer has a pipe with diameter of 16 in and connect a pipe with 42 in diameter with the following data.
The Mach number will be:
Upstream: 0.39637
Downstream: 0.99170
The customer can notice that the Mach Number increases 2.5 times when the fluid go through the expansion between the two pipes.
Keywords: Mach number, Density, Pressure Drop, Pipe, Velocity, diameter, change
References: None |
Problem Statement: Is possible to use the Antoine Parameters for the simple Antoine Equation within Aspen Plus?
P = Pressure
T= Temperature
A,B,C = Simple Antoine Parameters | Solution: The Aspen Physical Property System uses the Extended Antoine Equation:
P = Pressure
T= Temperature
Cn = Extended Antoine Parameters
Although it’s not possible to apply the Simple Antoine Equation, we can adjust its parameters to be used on the Extended model with the following considerations:
Since the common logarithm log10 from the simple model should be exchanged by the natural logarithm Ln of the extended equation, multiply the A and B parameters by ln(10) = 2.302585.
C1 = A*Ln(10)
C2 = -B*Ln(10)
C3 = C
Consider C4=C5=C6=C7=0
Example:
The Ethanol NIST Antoine Equation Parameters are the following, for P=bar and T=K:
A B C
4.92531 1432.526 -61.819
Which becomes:
C1 C2 C3
11.34095 -3298.513 -61.819
Finally, these values can be an input in the Extended Antoine vapor pressure equation model (PLXANT) within Aspen Plus.
Note: Do not forget to change the Temperature and Property units to correctly match the model units
Keywords: Antoine Parameters, Vapor Pressure, PLXANT.
References: None |
Problem Statement: How can you select the reaction set required for the acid gas absorber in Advanced Modelling option? | Solution: For the Acid Gas examples in Aspen HYSYS 3 sets of reactions are created automatically by the Acid Gas fluid package.
If the calculation type is changed to Advanced Modelling, then you need to select the reaction set to use.
The recommendation to select the reaction is:
Set-1: Used for Absorber or Liquid-Liquid Exchanger conditions (moderate temperatures)
Set-2: Used for Stripper/Regenerator (high temperatures)
Set-3: Corresponds to the chemistry (all reactions assumed to be at equilibrium)
This applies to all Acid Gas mixtures.
Keywords: sets of reactions, Acid Gas
References: None |
Problem Statement: Every time I close the VSTA window there is a significant time lag before I can resume working on the AFR model. Can I save changes to the VSTA code/ AFR model without closing the VSTA window every time? | Solution: The time lag after closing VSTA is caused on the VSTA side and isn't really an AFR issue. As an alternative it is recommended to keep the VSTA window open while working on the AFR model. Ensure that you save any changes before running the model. Remember, if you click on the save button on the AFR window it also saves any changes to the associated VSTA code.
Key words
VSTA, save changes
Keywords: None
References: None |
Problem Statement: Can I access column tray be tray physical and transport properties using Automation? | Solution: The attached Excel spreadsheet illustrates how to do this (try using the sample case “Atmospheric Crude Tower.hsc” sample case located under C:\Program Files (x86)\AspenTech\Aspen HYSYS VX.X\Samples to test the spreadsheet).
It obtains the following tray by tray properties for a selected column:
Actual and estimated Temperature
Pressure
Vapour Mole flow, Density, Viscosity and Molecular Weight
Liquid Mole flow, Density, Viscosity and Surface Tension
Note: Viscosity and Surface Tension must be obtained via a FluidPhase object (obtained from the stage vapour or liquid) since they cannot be obtained from the Fluid object associated with the Vapour or Liquid properties of the SeparationStage object.
Keywords: OLE, Excel, Column, Fluidphase, Fluid, Viscosity, Surface Tension
References: None |
Problem Statement: Are the quality lines on the phase envelope on a molar or volumetric basis? | Solution: Like vapour fraction, the quality lines on the phase envelope are on a molar basis. The property table could be used to determine these values on a volumetric basis.
Keywords: Phase Envelope, Quality Lines, Molar Basis.
References: None |
Problem Statement: How do I change the format (font, font style, size and colour) of all the PFD Tables in an Aspen HYSYS model? | Solution: You can modify the default format of the PDF Tables by changing the default Preferences.
To change the tables colour, go to File | Options | Resources Options | Colour Options. Search the PFD Table option and click on Select Custom Colour as shown below.
To change the font, scroll down in the same location to see the Font Options section. Again, search the PFD Table option, then click on Select Custom Font as shown below.
Finally, click OK to apply the changes.
Once you modify the format, any new table added to your flowsheet will keep the same selection. You can always customize a specific PFD table format by selecting the table and using the Format tab on the ribbon.
Note: If you want to apply the default preferences, just go to to File | Options | Resources Options | Colour Options and/or Font Options and press the Reset All Fonts button.
Keywords: PFD Table, Format, Options, Preferences, Font.
References: None |
Problem Statement: What is the PSV Kb factor and when to use it in Aspen Flare System Analyzer? | Solution: In Aspen Flare System Analyzer (AFSA), the user can define the back pressure correction factor (Kb) in the Methods tab of the PSV.
The back pressure is defined as a pressure existing at PSV’s outlet. It impacts to opening pressure, reduction capacity, instability or may combination of all. Kb is required for correction of reducing capacity.
For the low back pressure system that the impact is not significant, conventional type can be used. And for the excessive back pressure service, pilot type PSV is required to overcome it.
If empty, this value is calculated from the valve type and back pressure. This value should only be specified in exceptional cases.
1.The backpressure capacity correction factor Kb is equal to 1 for conventional valves and pilot operated valves; for balanced-bellow valve types, this value is calculated in accordance with API 520 or obtained from the valve manufacturer. This is applicable to Vapor, Steam, Mixed A/B/C, and Direct models.
2. When using the Unwetted Fire calculation method, to remain consistent with API 521 Section 4.4.13.2.4.3, make sure that the Vapor orifice sizing method with Kc and Kb set is equal to 1. API 521 6e Section 4.4.13.2.4.3 derives the required relief load equation for unwetted pool fire from the vapor orifice sizing equation in API 520 7e Section 3.6 Equation (3.2) and (3.5). In this derivation, Kb, Kc, and Z were assumed to be 1.
Note: Rated flow for steam pressure relief valves may change. Prior to V9, the rated flow used Kw for backpressure correction instead of Kb. In V9, affected PRVs may be identified by a calculation method of API Steam.
Keywords: Kb, PSV, Back pressure, Correction factor, API 520, API 521
References: None |
Problem Statement: What are the equations involved in the tube bundle used in dynamic mode? | Solution: Vessel Liquid U, Vessel Vapor U, Tube Liquid U, Tube Vapor U are values specified by the user.
Once user provides these values, we calculate Shell (Vessel) U, Tube U, and overall UA using equations below (the 4 variables above are highlited bold in the equations):
BundleHeight% = BundleHeight / VesselHeight * 100
BundleBottomHeight% = BundleBottomHeight / VesselHeight * 100
h = BundleHeight% - BundleBottomHeight%
LiquidCover = (VesselPercentLevel% - BundleBottomHeight%)/h (LiquidCover value is bounded [0,1])
ShellU = VesselLiquidU * LiquidCover + VesselVaporU * (1 - LiquidCover)
TubeU = (TubeLiquidU * TubeLevel + TubeVaporU * (100 - TubeLevel))/100
U = 1/(1/ShellU + 1/TubeU)
myUA = U * HeatTransArea
Keywords: Tube Bundle, Dynamic, Separator, U value, Parameters.
References: None |
Problem Statement: What is the Catalyst Inventory value that must be included in the FCC Catalyst Activity? | Solution: The Catalyst Inventory value can be entered in the FCC simulation environment under Reactor Section tab | Catalyst Activity.
The same value can be found in the calibration environment under Catalyst tab | Activity.
You should enter the total catalyst inventory that would include both, the regenerator and the reactor catalyst.
In the calibration environment there is also a Catalyst Inventory value under Operation tab | Regenerator. This one corresponds to the Catalyst inventory in the regenerator dense bed.
Keywords: FCC, Catalyst, Regenerator, Inventory.
References: None |
Problem Statement: The Activated Economics Evaluation is not supported in V10 while working with the DBR Amines property package, using it could lead to a crash/freeze. | Solution: Update the DBR Amines package to the new Acid Gas package to use the Activated Economics Evaluation.
Keywords: Activated Economics, DBR Amines, Crash, Freeze.
References: None |
Problem Statement: What are the different components of the license files? | Solution: To find out what are the different components that a license file contains, right click on the license file and select Open with Notepad. The different components will be displayed on Notepad, it might be confusing to extract information out of it, but once the components are broken down, it will be much easier to understand. The following screenshot explains in details the different license file components.
License file birth date – This is the date the license file was actually generated.
License file name – This is an example of what the name of the license file looks like. Note 080_2ca87 will be printed on one side of the dongle.
080 – represents a dongle locked license.
010 – represents a dongle-free license locked to the Ethernet address.
100 – represents a network license (standalone) locked to the preferred network.
Key serial number or dongle id: Represents the ID number printed on one side of the dongle.
System name: Unique ID number issued by Aspen Technology.
Start date/expiration date: The actual dates the key is valid.
License type: Standalone or network.
Application name: The name of the licensed application requested in a license file.
Keywords: License file
Components
References: None |
Problem Statement:
The user installed AFR V10, then updated with the latest patches. The user then installed Visual Studio 2015. However, when the user tried to open the VSTA IDE from within AFR V10 (via the Write Key Routines ribbon button) then IDE would not open. No error message was given, AFR V10 would not do anything. | Solution:
You will first need to check if you have VSTA 2015 runtime binaries installed. Open “Program and Features” window and look for “Microsoft Visual Studio Tools for Applications 2015”. If it is not listed then you'll have to manually install it as described in the steps below. In case you have it installed, please contact Aspen Tech support for further assistance.
You need to manually download “Microsoft Visual Studio Tools for Applications 2015” directly from Microsoft website link (provided below). Once the file is downloaded, you will have to ensure that all AFR V10 instances are closed. Then install “Microsoft Visual Studio Tools for Applications 2015” (will require admin rights by the user). After the installation is complete, open AFR V10 and try to open the VSTA IDE via the ribbon button. The IDE was able to be successfully opened.
Microsoft Link: https://www.microsoft.com/en-US/download/details.aspx?id=49031
Key Words:
Visual Studio, Write Key Routines
Keywords: None
References: None |
Problem Statement: How can I enter the orifice area of the second vapour relief valve in the depressuring utility? | Solution: To know the workflow of specifying two vapour PRD’s in the depressuring utility, please consult KB Article 030716 ‘How can I specify two vapour relief valves in the depressuring utility?’.
To enter the orifice area for the second vapour relief valve, use the 'General' flow equation for the liquid valve to specify the discharge coefficient and orifice.
The calculated final pressure for both valves will be always the same.
Attached to this KB Solution is an example file that may serve as a guide for setting up this type of depressuring cases. In the example file, a mixture comprised of hydrocarbons (mostly n-Butane) at 183.7 F and 665 psig is used as the reference stream for the depressuring utility, which will relief during 2 hours and has been set up with two pressure relief valves with the same orifice area, 0.1960 in2.
Due to the fact that the depressuring utility is run in dynamic mode and because of the improvements on the dynamics solver in the latest versions (V9.0 and V10), this example file has been created in V9.0, so that it can be run in both V9.0 and V10.
Keywords: Depressuring Utility, Pressure Relief Valve, Vapour, Orifice, Area
References: None |
Problem Statement: Can Aspen HYSYS predict weeping in tray sections? | Solution: Yes, Aspen HYSYS predicts weeping as soon as the dry hole pressure drop through the tray becomes too small.
For further details please review the Article 30780.
Since V9.0, you could also use the Column Internals Analysis tool to predict weeping. Please refer to Article ID 44581.
Keywords: Weeping, Tray Section, Column Internals.
References: None |
Problem Statement: Does Aspen HYSYS include Kinetic Hydrate Inhibitors in the Hydrate Formation Analysis? | Solution: The Kinetic Hydrate Inhibitors are polymers and/or copolymers that are not supported at the moment in Aspen HYSYS.
In V10.0 the inhibitors that are supported in the Hydrate Formation Analysis are:
Methanol
Ethylene glycol
Diethylene glycol
Triethylene glycol
AspenTech is currently investigating the feasibility of supporting this type of inhibitors.
Keywords: Inhibitor, Hydrate Formation, Kinetic Inhibitor, Polymers
References: None |
Problem Statement: Why is the Real Time factor significantly affected by the Pressure Flow Model selected in the Relief Valve? | Solution: In a Dynamics simulation, the Real Time factor is calculated by dividing a time interval for a case by the actual time required time required by HYSYS to simulate that time interval. This factor depends on the computer’s processing speed and the complexity of the simulation case. This factor is displayed on the General tab of the Integrator.
You could notice a significant difference in Real Time factor when using different Pressure Flow Models in the Relief Valve. This operation offers two different models: Cp/Cv and HEM. For further details about the models, please refer to What is the difference between the Pressure Flow Model methods for a Relief Valve in Aspen HYSYS V9.0?
In the following images, you can see the difference you could see in the Real Time factor using different methods in the Relief Valve.
The reason behind this is that HEM method is computationally very intensive because several PH Flashes are needed to converge to a correct solution, whereas Cp/Cv is a simple function evaluation.
HEM model will not be ever as fast as Cp/Cv.
Keywords: HEM, Cp/Cv, Relief Valve, Real Time, Factor, Integrator, Pressure Flow, Dynamics.
References: None |
Problem Statement: Estimation of the Twu alpha function parameters (L, M and N) in Aspen Plus.
Using the Twu alpha function improves the accuracy of the vapor-prediction from an equation of state. The alpha function is a function of the acentric factor at a constant reduced temperature. It is recognised as the best alpha function available. The parameters L, M and N must be determined from regression of pure-component vapor pressure data or other data such as liquid heat capacity. | Solution: To estimate the twu alpha function parameters, some input information is needed in terms of the specific equation of state used. For this case, the Soave-Redlich-Kwong (SRK) is used
1.In Methods|Specifications, select SRK and in the free water method, select STEAMNBS.
2. In Methods|Selected Methods|SRK|Models select/highlight the complete table and hit edit to change the model name to ESRKS. Go to option codes, and change the first code to 8.
3. Add a new regression case in Regression|New. Make sure you have previously created a pure component data set in the data folder. In Regression/Parameters add the parameters RKSTWUP 1, 2 and 3 which correspond to L, M and N, respectively. Specify the component and give initial values and bounds if desired.
4. If the regression doesn’t converge. Increase the number of iterations in Regression|Input|Algorithm| increase from 50 to 100.
5. The regressed parameters, residual and sum of squares are available in the folder Regression|Results.
Keywords: None
References: None |
Problem Statement: This knowledge base article describes on how to launch URL from Aspen ONE SCM | Solution: SYS CMD /C start "" <url>
This will open the site, but a windows command prompt will open for a split second
Write batch file with this:
Start "" %1
call SYS C:\BatchFile.BAT <url>
Keywords: None
References: None |
Problem Statement: Why is the initial pressure in my batch tank near vacuum when it should be higher? | Solution: When providing specifications for a dynamic simulation (batch operations run in dynamic mode), we need to be very careful with the initial conditions.
When it comes to pressure, we need to make sure there is some vapor/gas inside the tank at time t=0, otherwise initial pressure will be near vacuum. When only liquid phase is being fed or already present at the beginning of the batch, there are a few things we can specify to avoid near vacuum conditions:
Specify there is an inert gas already present in the tank
Specify a small but higher than 0 vapor fraction for the feed stream to acount for some vapor inside the tank.
Add an additional feed stream to the tank with vapor in it.
Please consider the following things:
For option 1, you usually only need to specify at which pressure the inert gas is.
For options 2 and 3, you will need to specify the amount of vapor to be entered into the tank, which will determine the pressure of the vessel. Keep in mind that for these options, pressure at t=0 will still be near vacuum, but it will start rising as the vapor enters the vessel.
Keywords: Batch, pressure, vacuum, initial condition
References: None |
Problem Statement: When extracting logs files from the event viewer, depending on the amount of time one is collecting the files may come out too big, making difficult to transfer them and even search for the information needed. | Solution: To extract application and system logs with an specific time frame do the following:
Go to Windows Start Menu and Look for Events Viewer
On the left tree Extend Windows Logs and select Application or System depending on the type of log you need.
Select events from the list around the time the issue occurred, and click on save selected events.
Save the file, a window will pop up asking for Display information language, select Display Information for English language.
Keywords: Event Viewer, evtx, Windows.
References: None |
Problem Statement: I have several pipes in my model. Is there a way to automatically give logical names to pipes in the model? | Solution: Since most models have multiple pipes it becomes cumbersome to name each pipe. To reduce user effort, there is a 'Auto-name' option available in the RAM Data section. Navigate to the RAM Data environment and click on the Pipes folder. Select the pipes you want to auto name as shown in the screenshot (Auto name pipe select). Click on the Auto-name button and the selected pipes will be named based on the Units that they are connecting to, as shown in the screenshot (Auto name pipe result).
Key words
Auto-name, pipe
Keywords: None
References: None |
Problem Statement: What are the additional files need to be embedded to run modeler cases into OTS? | Solution: Aspen modeler products require aspen properties file and/or any .dll files containing subroutines. These files can be included in OTS by clicking the Additional Files button. This shows a list of any files already added and lets you add or remove items from this list. These files will be stored in the .aots file when you save the case.
Note that .appdf and .aprpdf files only work with the aspenONE version in which they were generated. If you want to run your Aspen OTS Framework case using a newer version of Aspen Modeler, you must remove the .appdf/.aprpdf file from the case, and replace it with one generated from the same newer version of Aspen Plus or Aspen Properties.
Key Words
Modeler, Properties, subroutines
Keywords: None
References: None |
Problem Statement: This knowledge base article describes on System tuning for transferring data to/from SQL server. | Solution: To set Max server memory on the server if it is a virtual machine, do the following in the Virtual Machine Setting dialog box:
Specify the appropriate amount of memory.
Clear Enable Dynamic Memory.
Next, change the Power Plan from Balanced to High Performance. Refer to the following link for details:
https://support.microsoft.com/en-us/kb/2207548
Open the Control Panel.
Select Power Options, and then select High Performance.
Move the Data, Log, and tempdb files to different drives.
Configure Traceflag 4199.
Refer to the following link for details:
https://support.microsoft.com/en-us/help/974006/sql-server-query-optimizer-hotfix-trace-flag-4199-servicing-model
Move Data, Log, and tempdb files to different drives by doing the following:
Create folders named DATA and Log in other drives than the one in which SQL Server is installed.
Modify the startup parameters, as in step 9. below.
Go to SQL Server Configuration Manager and click SQL Server Services and go to SQL Server().
Open its Properties, then modify its Startup Parameters, as seen below:
Apply the updates.
Restart SQL Server and SQL Server Agent.
Configure MAXDOP on the server. Refer to the following link for details:https://support.microsoft.com/en-in/help/2806535/recommendations-and-guidelines-for-the-max-degree-of-parallelism-confi
In the Virtual Machine Setting dialog box, under Hardware, set the Processor to the largest Number, as seen below:
When creating New Database, in the New Database Setting dialog box, specify the value for the Max DOP setting, as seen in the following example:
Note: The value you enter for the Max DOP setting is determined by your computer.
Keywords: None
References: None |
Problem Statement: Using cas2dat and dat2cas utilities in SCM V10.0 | Solution: Cas2dat and dat2cas utilities are not supported with configured Applications(CAPS) . These utilities would work only for old legacy MIMI cases.
Keywords: None
References: None |
Problem Statement: How to connect a workstation to use the Aspen Properties Enterprise Database (APED) V9 or V10 on another computer | Solution: On the client computer, go to Start | Programs | Aspen Properties | Database Manager – Aspen Properties
Databases must be registered before they can be used by programs on your computer such as Aspen Plus or Aspen HYSYS., first remove existing databases by right clicking each and selecting Delete Database Registration
To add the central SQL properties databases, Right-click Aspen Physical Properties Databases under console root and select Register Database
1. Database Type - Only SQL Server is supported.
2. Server - If your administrator has set up a database server to be shared over the network, select the name of the server from the list. To connect to SQL Server Express, you must add "\SQLEXPRESS" after the computer name.
3. Login Name -apeduser2
4. Password -Aproperty88#
5. Database: Select the Database listed in the list of Database Example: APEOSV90, APV90, NISTV90 and FACTV90.
6. Click Ok
7. Repeat step 1 – 7 for all APEOSV90, APV90, NISTV90 and FACTV90 databases.
8. Exit Aspen Properties Database Manager.
Keywords: Aspen Properties Enterprise Database, APED, remote server, SQL Express, SQL Express configuration
References: None |
Problem Statement: How can a flowsheet be optimized using sequential modular mode? | Solution: Attached is an example of how to optimize the operating margin for a simple flowsheet.
See file Optimiz2-V73.bkp. This file will run in V7.3 and higher.
The value of a process is calculated as the value of the product and the byproduct, minus the cost of the raw material, and minus the cost of steam for the reactor. The Fortran sheet is used to calculate the cost function:
C CPROD = PRICE OF PRODUCT, $/LB
CPROD = 1.30
C
C CBYPR = PRINCE OF BYPRODUCT, $/LB
CBYPR = 0.11
C
C CFEED = PRICE OF FEED, $/LB
CFEED = .20
C
C CSTEAM = COST OF STEAM, $/MMBTU
CSTEAM = 4.00
C
C COST FUNCTION
CFUNC = CPROD * P + CBYPR * G - CFEED * A - CSTEAM * Q /1D6
There are two constraints: one specifying the maximum duty for the reactor and the other specifying the minimum product purity. Optimization is used to find the reaction temperature and the feed flow rate that maximizes the cost function.
The molar flow rate of P and of G in stream PROD, the molar flow rate of A in stream FEED and the reactor duty are the sample variables for the optimization. These variables are called P, G, A, and Q, respectively.
The optimization problem is converged when CFUNC is at a maximum.
There are two manipulated variables; the reactor temperature and the flow rate for the reactant A in the feed. The optimization convergence block finds the combination of values that makes CFUNC a maximum subject to the constraints.
The Fortran sheet is used to calculate the cost function CFUNC.
The manipulated variables are specified in the blocks just as if there were no optimization. The specified value is the initial estimate used by the optimization convergence block.
You do not have to specify convergence of the design specification. ASPEN PLUS automatically generates a convergence block to converge the specification.
There are two constraints associated with the optimization problem. They are called DUTY and PURITY.
The constraint DUTY is satisfied when the reactor duty is less than or equal to 3 MMbtu/hr.
The constraint PURITY is satisfied when mole fraction of P in the stream PROD is greater or equal to than 0.9.
For more information see the Aspen Plus Help topic Simulation and Analysis Tools -> Sequential Modular Flowsheeting Tools -> Optimization.
Keywords: None
References: None |
Problem Statement: I am getting an Input Error in AFR V10. Is there any way AFR can display the cause of the error? | Solution: In AFR V10 CP3 (Cumulative Patch 3), we introduced a new feature in the Message Panel to list the Errors, Warnings and Model Status updates as shown in attached screenshot. Navigate to to the View ribbon tab and click on Message Panel to see the results. The Message Panel will list the Unit ID and the cause of the error. If you have V10 and cannot see the Message Panel details, ensure that you have CP3 installed on top of V10. CP3 is available for download on the support site.
Key words
Message Panel, Input Error
Keywords: None
References: None |
Problem Statement:
Can I access HYSYS Reactions using OLE? | Solution: The following Excel VBA code illustrates how to:
· Access / Add Reactions
· Manipulate Reactions (eg. conversion)
· Access / Add Reaction Sets
· Manipulate Reaction sets - setting which reactions are active etc.
· It is designed to work with the "C-4.hsc" HYSYS sample case.
Public Sub AccessReactionManager()
'
'Description: Demonstration of how to manipulate the reaction manager with OLE ' Illustrates accessing reactions, adding reactions, accessing reaction sets ' Adding reactions to reaction sets, changing which reactions are active in the set
'
'Declare Variables
Keywords: None
References: None |
Problem Statement: When entering a constant temperature or pressure for Pure Component or Mixture Data on the Data | Setup sheet used for data regression, what standard deviation is used? | Solution: For user specified constant temperature or pressure data on the Data form, the default standard deviation (std-dev) of 0.1 for Temperature (T) and 0.1% for Pressure (P) is used. The standard deviation of these data is NOT zero; therefore it is indeed part of the objective function for a regression case.
Keywords: None
References: None |
Problem Statement: When you have an Aspen HYSYS Oil Manager Assay and would like to convert it to Petroleum Assay Manager, the below message may appear: | Solution: As the message states, the Petroleum Assays require distillation data in either TBP, D86, D2887 or D116 format to be imported from the Oil Manager Environment.
In these cases, the user must check that the Assay Data Type used on the Oil Manager is on the formats mentioned above. The Equilibrium Flash Vaporization (EFV) and Chromatographic analysis are not supported for the assay conversion.
For detailed steps on how to convert an Oil Manager Assay to a Petroleum assay, refer to the KB article How to convert the Oil Manager input assay to Petroleum Assays in V8?
Keywords: Oil Manager, Petroleum Assay, Convert, Distillation data.
References: None |
Problem Statement:
The user installs Visual Studio after installing AFR V10. When this installation order occurs, AFR V10 will not be able to open the IDE. The “Write Key Routines” ribbon button will be disabled. | Solution:
When the “Write Key Routines” ribbon button is disabled, it is a clear indication that the above installation order has been followed. This is due to the fact that when Visual Studio is installed, “Microsoft Visual Studio Tools for Applications 2015” (installed by the AFR V10 installer) is not aware of this installation. Thus, does not recognize that Visual Studio is installed. Therefore AFR V10 disables the “Write Key Routines” ribbon button.
Have the user repair the “Microsoft Visual Studio Tools for Applications 2015” installation. This is a standard requirement for any software that depends on a different installed software. “Microsoft Visual Studio Tools for Applications 2015” needs to be made aware that Visual Studio is installed.
1) Open the “Programs and Features” window.
2) Select the “Microsoft Visual Studio Tools for Applications 2015” application
3) Either
a. Click the “Change” button or
b. Right click and select “Change”
4) A Visual Studio installation widow will open. Click the “Repair” button. Follow the instructions on the Visual Studio installation window.
5) After the repair installation is complete, open AFR V10 and test if the “Write Key Routines” ribbon button is enabled and that the IDE can be opened.
Key Words:
Key Routines disabled
Keywords: None
References: None |
Problem Statement: This knowledge base article describes on how to import a .txt file into SCM table. | Solution: To import a .txt file into SCM follow the below steps.
Step 1: Add the name of the table as entry to the set IMPITEMS.
Step 2: Enter description in USENGLISH and UKENGLISH columns in the set IMPLNG.
Step 3: Specify a group name in IMPGRPS.
Step 4: Enter 1 in the ALL column and the group column in IMPMAP.
Step 5: Enter the name in IMPITEM, IMPFLAG to Y, and IMPMETHOD to ASCIID in the set IMPCTL.
Step 6: Enter the file name and the corresponding fields (columns in the txt file) in the file in IMPASCID.
Step 7: In FMTFDEF table, enter IMPORT2 ; IMPORT2 specifies the path where the Delimited ASCII file (.txt file) is stored.
Step 8: Run >RDVCONV
Step 9:
CSTPOVRR = NULL
CSTPOVRR = CSTPCUSR
CSTPOVER = CSTPCUST
Step 10: Run VMACTION CGLOBAL: GLOBAL! REFRESH
Go to Run Step menu from the Data tab of the Planning Board ribbon and Import Data.
Keywords: None
References: None |
Problem Statement: What are the types of files saved inside a single OTS case? | Solution: The following are the types of files generally saved inside single OTS case (.aots extension):
One or Multiple dynamic simulation cases (HYSYS Dynamics/Aspen Plus Dynamics)
A configuration file which stores simulation case names, streams, control signal connections and tags.
Any saved snapshots
Key Words
OTS, Dynamic, Tags
Keywords: None
References: None |
Problem Statement: How to change the correlations used in properties estimation for Hypothetical components | Solution: When create a hypothetical component, and estimate certain properties, some correlations are used by default. However, you have the option to change the methods as desired.
To see the correlations used and change them if needed, please go to the Home tab in the Properties Environment and select the Hypotheticals Manager button. Move to the Settings tab. You will found all the available properties with a drop-down menu for each one to define the method you want to apply.
KeyWords
Hypothetical, Property, Method, Estimation.
Keywords: None
References: None |
Problem Statement: What is the Purpose of “” option in Blend Optimization Dialog Box in MBO ? | Solution: Running Gauge Comp Tanks , feature is used to account additional VOLUME of Components generated [or] VOLUME of Component being received during the Blend operation and that VOLUME will be accounted for Blend Optimization process.
In Detail,
Consider a situation, where REF1 ( REFORMATE ) coming from Unit and stored in the COMP TANK TREF, before used for Blending.
In the Begging Time of the Blend EVENT ( 08:00 AM ) the Available component Volume in TREF is 5,000 M3. The Blend Duration is 10 hrs, thus the End time will be 18:00 hrs.
During the Blending duration, the tank TREF is continuously receives rundown from the unit and this additional material VOLUME is say approximately 500 m3.
Enabling “Running Gauge Comp Tank” option account for ,
a). Initial VOLUME 5,000 m3 and
b). the amount of additional component generated during the Blending Process, in this case it is 500 m3.
So in Total 5,500 m3 will be used for Component availability calculation.
Usually this feature should be enabled for the component tanks, which continuously receives streams from the Process units, during Blending Process.
This Difference in Quantity will be noticed when you hit MAX VOL in the Blend Event Dialog box.
Keywords: Running Gauge Tanks
Blending
MBO
References: None |
Problem Statement: How to change Aspen Modeler controller set point from OTS? | Solution: If the controller set point is “Auto” or “Manual”, then it cannot be changed during simulation run from Aspen OTS Framework or the OPC client. Please make sure PID controller is set to "Cascade" mode shown below:
Key Words
OTS, PID, OPC, Cascade
Keywords: None
References: None |
Problem Statement: What is the definition for the TEMA Sheet Tube Number in Aspen Exchange and Design Rating (EDR)? | Solution: In Aspen EDR, for a U-tube exchanger, the number of tubes is defined as the total number of holes in the tube sheet i.e. twice the number of actual U-tubes. In other words, a U-tube is counted as two-tubes, so the tube count still gives the total number of holes in the tubesheet.
The number of U-tubes on the TEMA sheet is based on number of tubes specified by on the Geometry summary (Input | Exchanger Geometry) inputs.
For TEMA type units, the TEMA sheet value = Tube Number/2
For units not covered by an official TEMA designation, like a Multi-tube hairpin (M-shell) exchanger, the TEMA sheet value = Tube Number
Keywords: U-tubes, Tube Number, Tube Count, TEMA Sheet.
References: None |
Problem Statement: This knowledge base article describes about List Scheduler in Aspen Plant Scheduler. | Solution: List Scheduler is an alternative for Gantt chart in tabular format located under the Format tab of Aspen Plant Scheduler V10.0.
Colors of activities in List Scheduler match the Planning Board coloring scheme. List Scheduler can be docked next to the Planning Board and can be made in synch with the Planning Board.
Users can bring up the Supply Demand Balance Report from Reports Tab and can select the time range to view the activities. Users can turn on/off the Date Slider.
What can I do with List Scheduler?
Resequence activities using Step Size and up/down arrows on selected row(s).
Drag and drop activities by dragging and dropping the rows of report.
Open the activity editor by double clicking on a row.
Open the activity editor by selecting a row and then click on pencil icon.
Delete an activity by selecting a row and clicking on red X icon.
Delete an activity using Shift – Delete by selecting a row in Planning Board synchronous mode.
Keywords: None
References: None |
Problem Statement: ERROR: "[Microsoft][ODBC Driver Manager] The specified DSN contains an architecture mismatch between the Driver and Application" | Solution: To resolve the error , select a DSN that is created using a 32-bit ODBC driver in the 32-bit Administrator.
A 32-bit ODBC DSN can be created on Windows 64-bit as follows:
Go to Start > Run.
Type C:\windows\syswow64\odbcad32.exe
Click OK.
Click Add
Select the ODBC driver from the list.
Configure the DSN.
Keywords: None
References: None |
Problem Statement: What network security settings are required to access AspenTech web content or receive email from AspenTech? | Solution: AspenTech content like the AspenTech website, software or patch downloads, or email may be blocked by your company's network security policies and may require changes in firewall and email configuration to allow you access.
To access AspenTech web content, your IT group may need to grant access to the following:
*.aspentech.com
*.core.windows.net
To receive AspenTech email, your IT group should whitelist the following domains:
[email protected]
*@aspentech.com
Remember to check your Junk or Spam folders for AspenTech email.
If you continue to have issues accessing AspenTech web content or receiving AspenTech email, then please work with your IT group to help you troubleshoot the issue.
Keywords: Support website access
Receiving emails
Unable to get emails
References: None |
Problem Statement:
The user attempts to open the VSTA IDE via the “Write Key Routines” ribbon button. This will usually crash AFR V10 without writing anything to the log file (more common with files that are not new). If the user tries to create a new file, a system exception error is thrown and then crashes AFR V10. | Solution:
Following are the steps for troubleshooting:
1) Check that Visual Studio is installed
2) Check that Microsoft Visual Studio Tools for Applications is installed
3) Open Visual Studio (not from within AFR V10) and make that it is licensed properly.
The above always occurs if the user did not fully license their Visual Studio instance after installing. The user will need to launch Visual Studio (independent from AFR V10) and input their license key. Once Visual Studio is licensed, then launch AFR V10 and try to open the IDE. If problems still persists, then repair the Microsoft Visual Studio Tools for Application or contact Aspen Tech Support.
Key Words:
VSTA IDE, Visual Studio license
Keywords: None
References: None |
Problem Statement: How to increase the significant digits shown in Aspen Flare System Analyzer for phase properties results. | Solution: In Aspen Flare System Analyzer, you can edit and show less or more digits for any calculated property in the results forms. This solution shows how to control the digits in the Results | Physical Properties section. These properties include Viscosity, Density, Thermal conductivity, Surface tension and some others.
Go to File | Preferences and select the formatting tab, then click on the Edit Variable Formats button.
A new window will appear, where you can find all the objects where AFSA displays results. Select the Phase option to display the physical properties reported by AFSA. Highlight the property whose digits you want to modify and click on Format.
In the appearing window simply select the number of decimal digits you want to display. If desired, you can also change the format to Exponential.
Keywords: Phase, Results, Physical, Properties, Digits, Format, Decimal.
References: None |
Problem Statement: The DLL Mtell.Sensor.Common is missing from the following folders:
C:\Program Files\AspenTech\Aspen Mtell\Mtell Agent Service
C:\Program Files\AspenTech\Aspen Mtell\Training Service
C:\Program Files\AspenTech\Aspen Mtell\Suite\Watch Dog Service
C:\Program Files\AspenTech\Aspen Mtell\Suite\Retry Service
C:\Program Files\AspenTech\Aspen Mtell\Suite\ Reporting Service
C:\Program Files\AspenTech\Aspen Mtell\Suite\API Service
C:\Program Files\AspenTech\Aspen Mtell\Suite\MDM
C:\Program Files\AspenTech\Aspen Mtell\Suite\Tools\Agent Builder
C:\Program Files\AspenTech\Aspen Mtell\Suite\Tools\Mimosa Explorer
C:\Program Files\AspenTech\Aspen Mtell\Mtell\Mtell Gateway Server
C:\inetpub\wwwroot\AspenTech\AspenMtell\MtellView\bin
C:\inetpub\wwwroot\AspenTech\AspenMtell\InteropServer\MIMOSA\bin
C:\inetpub\wwwroot\AspenTech\AspenMtell\APM\bin
Please note that the folder paths listed above are the default locations that Mtell is installed to. If a non-standard install path has been selected, please adjust the folder paths accordingly. | Solution: 1. Stop the Mtell Windows services first. You can do this either using the Task Manager or the Service Console. The Mtell Windows services include the following:
Aspen Mtell Agent Service
Aspen Mtell API Service
Aspen Mtell Asset Sync
Aspen Mtell Message Retry Service
Aspen Mtell Reporting Service
Aspen Mtell Training Service
Aspen Mtell Watch Dog Service
Aspen Mtell Work Sync
2. Copy Mtell.Sensor.Common.dll from the System Manager folder to all the folders listed above. The System Manager folder path is typically “C:\Program Files\AspenTech\Aspen Mtell\Suite\Tools\System Manager” for a standard install.
3. Re-start the Windows services again. You can do this either using the Task Manager or the Service Console.
Keywords: Mtell.Sensor.Common.DLL
References: None |
Problem Statement: How can I delete a Personal Workspace in Aspen Basic Engineering V10? | Solution: 1. Close out of any application that is connected to the workspace.
2. Navigate to C:\AspenZyqadServer\Basic Engineering19.1\Workspaces and locate the folder name corresponding to the workspace and delete it.
3. Open Workspaces.lst (located in the same folder) with a text editor such as Notepad. Erase the line corresponding to the workspace you wish to delete, then save the file.
4. Open Windows Services and locate the AZ191Broker service. Right-click and select Restart.
The workspace should no longer appear in your list of workspaces.
Keywords: Workspace
References: None |
Problem Statement: How Heat Exchangers costs are calculated in Aspen Shell & Tube Heat Exchanger (EDR) program? | Solution: The three elements of the Exchanger Cost are:
Material Cost
The material costs are determined component by component using the material prices from the material database and the rough dimensions calculated as part of the mechanical design. The material prices can be changed to suit the local market conditions.
Labor Cost
The labor costs are determined from the labor rate (hourly rate) and the labor hours required to fabricate each component and assembly within the shell and tube heat exchanger. The labor hours come from correlations that have been developed from several hundred labor estimates for a wide variety of exchanger types and design conditions. These correlations are a function of design pressure, shell diameter, weight, tube length, and material. The hours required for every shop activity and for the fabrication of every component can be changed by modifying the Labor Efficiency Factors. These are denominator quantities. If the program calculates 10 hours for activity "A", that means that the program calculates 5 hours for activity "A" divided by the default efficiency factor of 0.5 to yield 10 hours.
Mark-ups on Material and Labor
The mark-ups are a quick way of customizing the answers as these can be used to increase of decrease the calculated exchanger cost.
Keywords: cost, edr, labor, material, mark-up cost
References: None |
Problem Statement: Why if I run a design case in Aspen Shell & Tube Exchanger V10 I get different geometry results than if I run it in previous versions? | Solution: In versions prior to V10, the final design is selected based on the Optimization Algorithm you have selected, which could be for minimum cost or minimum area.
In V10 there is a new improved design algorithm to find the cheapest exchanger with no operational issues concerning:
Vibration
Thermosiphon Instability
TEMA Unsupported tube length
TEMA nozzle rho-V-squared limits
In Results Summary | Optimization Path, the status for operational issues is available:
Getting a different geometry design using different EDR versions is expected. V10 is working with an enhanced design algorithm.
Keywords: Vibration, Operation Warning, selected design, Optimization path
References: None |
Problem Statement: Where do I map the materials and components imported from SP3D to ACCE? | Solution: Since V9 of Aspen Capital Cost Estimator a new workflow has been added to let users modify the mapping codes or add new codes used in the SP3D Import feature.
The workflow uses an Excel file which behaves in a similar way to the existing customer external library files. By default, it contains the table of component code mappings between SP3D and ACCE. You can add and modify the code mappings as you please and save the file to finalize your changes.
Once the library file is added to the project, the project references the newly defined 3D code mappings when an import from SP3D is done.
You must have all projects closed to access this file.
To modify it go to Libraries | Customer External Files | SP3DImport | Default.
Duplicate the default file to create a copy and modify it. Double click on the duplicated file and a spreadsheet will be opened, allowing you to modify the mapping.
The 3D Attribute Value column will be the link between SP3D and ACCE.
Keep in mind that if the spreadsheet you are importing from SP3D has an attribute value that is not listed in this file, the import will throw errors.
Once modified, you can save this library file and use it to update your project.
To load the file into your current project you must go to Project Basis View | Customer External Files | SP3DImport. Right click on SP3DImport and select the desired external file.
Keywords: SP3D, mapping, external, file
References: None |
Problem Statement: This knowledge base article provides a sample XML for PropertiesGrid Configuration | Solution: <?xml version="1.0" encoding="utf-8"?>
<CONFIG>
<START
Header="Model Parameters"
ViewModelID=":START_VM">
<PrimaryView
Type="PropertiesGrid">
<PropertyGroups>
<Group1>
<Properties>
<Item
Caption="ModelParameters"
Property="DATA1"/>
<Item
Caption= "ModelParametersGroups"
Property= "DATA2"/>
</Properties>
</Group1>
</PropertyGroups>
</PrimaryView>
</START>
<START_VM BeforeSubstitute=">_RSTRBEF">
<States>
<STATE1 Setup="">
<Properties>
<DATA1
Type="Enum"
ValueSource="_SCHCH"/>
<DATA2
Type="Enum"
ValueSource="_DEMSPLO"/>
</Properties>
</STATE1>
</States>
</START_VM>
</CONFIG>
Keywords: None
References: None |
Problem Statement: How to solve an Enthalpy Consistency Error in a Component Splitter? | Solution: The component Splitter separates a feed stream into two material streams based on the parameters and split fractions that you specify. Once the composition, vapor fraction, and pressure of the outlet streams are known, a P-VF flash is performed to obtain the temperatures and heat flows.
Under certain circumstances, the product streams flash specifications could lead to an energy imbalance on the unit. To avoid this type of errors, is necessary to add an energy stream, to comply with the energy balance:
Where:
hE = enthalpy of energy stream
hF = enthalpy of feed stream
hO = enthalpy of overhead stream
hB = enthalpy of bottoms stream
Keywords: Component Splitter, Consistency Error, Energy Balance.
References: None |
Problem Statement: What are the requirements to use a Black Oil PIPESIM case with a PIPESIM Net block? | Solution: To use a Black Oil PIPESIM case, you must select a Neotec Black Oil COMThermo fluid package first. This package will require a Neotec Black Oil license, which is provided by Schlumberger.
This is not required when working with a compositional PIPESIM case.
Keywords: .bpn, extension
References: None |
Problem Statement: How can I delete a Personal Workspace in Aspen Basic Engineering V10? | Solution: 1. Close out of any application that is connected to the workspace.
2. Navigate to C:\AspenZyqadServer\Basic Engineering19.1\Workspaces and locate the folder name corresponding to the workspace and delete it.
3. Open Workspaces.lst (located in the same folder) with a text editor such as Notepad. Erase the line corresponding to the workspace you wish to delete, then save the file.
4. Open Windows Services and locate the AZ191Broker service. Right-click and select Restart.
The workspace should no longer appear in your list of workspaces.
Keywords: Workspace
References: None |
Problem Statement: This knowledge base article describes on how to call a stored procedure in Informatica. | Solution: Edit the map using Designer and add the transformation.
Menu item Transformation> Create Transformation> Stored Procedure
Import the definition from the database using the database connection or skip. If you skip it comes in empty.
Give it a name SP_NAME_PROD_RATE_HIST.
Double click on transformation > select properties tab. Populate similar to example below:
Use help to determine the “Stored Procedure Type”.
Save changes.
Open Workflow Manager and edit related Session (attached to modified map).
In the session properties, Mapping tab, select the new procedure transformation and update database connection information.
If there is no map. Then you will have to create a new dummy map. Easiest map would be one that read from a file and writes to a file then drop in your unconnected transformation into this map. Create a new session for the new map and link the session execution to a workflow.
Keywords: None
References: None |
Problem Statement: When the system is in supercritical region, depressuring calculation may fail. The system is supercritical, and various property packages struggle with supercritical fluids. Hysys property packages do not handle supercritical fluids well. For depressurization calculation to occur, there must be "vapor" in the system. However, above the critical point there is no distinction between liquid and vapor, yet various property packages will still yield a "vapor fraction." Above the supercritical region, the fluid vapor fraction often flips between 0 and 1 (since it is neither vapor nor liquid). Due to this reason, HYSYS predicts no vapor at the initial condition; therefore the depressuring cannot be initiated. | Solution: 1) Set the stream temperature to -20 F -- the ambient temperature represents the lowest possible temperature at which depressuring could begin. Also it is a potentially reasonable assumption in the event that the pipeline is depressured after some amount of time and the inventory has had time to equilibrate with the atmosphere
2) Set the Heat Loss model to "None." This is also a reasonable assumption since the pipe is at ambient temperature. However, it is important to note that this method will result in quite conservative temperature results from the utility, because potential heat losses to the environment is not taken into account.
Keywords: Depressuring utility, Supercritical fluid
References: None |
Problem Statement: How do I create a strip chart for a variable for all the streams in the simulation? | Solution: In the newer Aspen HYSYS versions (from V8.2) the user can add a variable to a strip chart directly from the stream or for all the streams in the simulation from the Workbook.
For a stream, the user can select the variable, apply right mouse click and then send the variable to strip chart. If the strip chart does not exist then this also offers to create a new chart.
If the user wishes to create a strip chart for a variable for all the streams in the simulation then this can be achieved from the workbook. Please follow the steps below:
Open the workbook from the Navigation Pane on the left.
You can uncheck the Horizontal Matrix option to display stream in the column view.
Highlight a column for the variable to be added in the strip chart.
Apply right mouse click to any value in the column.
Then select Send to Strip Chart. You can create a new chart or send to an existing chart.
Keywords: Strip Chart, Stream Variable
References: None |
Problem Statement: Can I password protect my APEA project? | Solution: No, this functionality has been only implemented for Aspen Capital Cost Estimator.
Users will not be able to set, change, or remove a project password in APEA. However, APEA will prompt the user for the password if a user opens a password protected ACCE project in either APEA.
Keywords: Password, APEA, Project
References: None |
Problem Statement: This knowledge base article shows a sample configuration for Layout Grid in XML. | Solution: <?xml version="1.0" encoding="utf-8"?>
<CONFIG>
<START
Header="Model Parameters"
ViewModelID=":START_VM">
<View
Type="LayoutGrid"
Rows="auto,auto"
Columns="auto,auto">
<Views>
<LABEL1
Row="0"
Column="0"
Type="PropertyView"
Editor="Label"
HorizontalAlignment="Right"
DataSource="LABEL1"/>
<DATA1
Row="0"
Column="1"
Type="PropertyView"
HorizontalAlignment="Left"
DataSource="DATA1"/>
<LABEL2
Row="1"
Column="0"
Type="PropertyView"
Editor="Label"
HorizontalAlignment="Right"
DataSource="LABEL2"/>
<DATA2
Row="1"
Column="1"
Type="PropertyView"
HorizontalAlignment="Left"
DataSource="DATA2"/>
</Views>
</View>
</START>
<START_VM BeforeSubstitute=">_Rtemp">
<States>
<STATE1 Setup="">
<Properties>
<LABEL1
Type="String"
Value="Caption1"/>
<DATA1
Type="Enum"
ValueSource="SET1"/>
</Properties>
</STATE1>
<STATE2 Setup="">
<Properties>
<LABEL2
Type="String"
Value="Caption2">
</LABEL2>
<DATA2
Type="Enum"
ValueSource="SET2">
</DATA2>
</Properties>
</STATE2>
</States>
</START_VM>
</CONFIG>
Keywords: None
References: None |
Problem Statement: What is the reference used for the thermal conductivity values in the pipe segment? | Solution: In the pipe segment operation in Aspen HYSYS, there are a couple of default values for thermal conductivity used with the Estimate HTC heat transfer method for different insulation types.
These thermal conductivity values are based on:
Gregory, G. A., "Estimation of overall heat transfer coefficient for the calculation of pipeline heat loss/gain", Technical Note No. 3, Neotechnology Consultants Ltd., 1991.
These values are also available in Table 19.7 in the book "Subsea pipelines and risers" by Bai, Y. and Bai , Q. (2005).
Keywords: Pipe Segment, Thermal Conductivity, Insulation, Estimate HTC, Heat Transfer.
References: None |
Problem Statement: This knowledge base article describes on User Management and Role Permissions in SCM | Solution: User Management and Role Permissions are found under Security Section in the Navigation Pane.
The user management screen allows the user to add, modify roles for, or delete users. Users are set up with a primary role, and potentially with additional valid roles. When a user opens the model, the model will be loaded with the primary role for the user. The user can switch to any valid role by clicking on the Switch Role button on the View tab of the ribbon. Current users and role assignments can be viewed on the User Management screen, and additions, modifications, and deletions can be done on the Properties panel as follows:
To add a new user
Enter the Userid and Description for the Userid (generally the name of the user) in the Add User section of the panel
Select a Primary Role from the drop down list
Click the Add button at the bottom of the Add User section of the panel
To modify a user
Select the user in the drop down list in the Modify User Role section
To add a valid role for the user
Select the role in the Additional Roles list in the Add User Role section of the panel
Click the Add button at the bottom of the Add User Role section
To remove a valid role for the user
Select the role in the Roles list in the Modify User Role section of the panel
Click the Remove button
To change the primary role for a user
If the desired role is not already a valid role for the user, add the role as described in 2b
Select the role in the Roles list
Click the Set as Primary button
To delete a user
Select the user in the drop down list in the Delete User section of the panel
Click the Delete button
Role Permissions
This screen allows the user to add or delete roles in the model, and also to view and modify which screens, actions, and action steps are valid for each role. The screen contains a table of check boxes for each combination of a screen, action, or action step and a role. A check mark in a box indicates that the screen, action, or action step is valid for that role. Roles can be added or deleted through the Properties panel.
To modify roles
Update the table as desired to define the available screens
Click the Apply Changes button on the Home tab of the ribbon
To add a role
Type in the name for the new role in the Add Role section of the Properties panel
Click the Add Role button
To delete a role
Select the role in the drop down list in the Delete Role section of the Properties panel
Click the Delete Role button
Keywords: None
References: None |
Problem Statement: Can ACCE V10 and V9.1 coexist on the same machine? | Solution: No. Whenever Aspen Capital Cost Estimator V10 is installed, V9.1 will be deleted.
The same can be said about any in-between version, V8.8.2 and V9 can’t coexist or V8.7.1 and V8.8 This is because the full release version and the in-between are considered complementary, as they share the cost basis.
Keywords: Version, coexist, V10, V9.1
References: None |
Problem Statement: Why is the Vibration & Resonance analysis not performed when D or M shell types are used in Aspen Shell & Tube Exchanger? | Solution: Double-pipe (D-shell) and Multi-tube hairpin (M-shell) are shell and tube type exchangers, but are not covered by an official TEMA designation.
The Shell&Tube Flow-induced vibration analysis is performed only when a TEMA-supported shell type is selected. Multi-tube hairpin is covered in the vibration analysis only if the unit has segmental baffles.
Keywords: Vibration & Resonance analysis, D-shell, M-shell, Non-TEMA
References: None |
Problem Statement: How do I access the Calibration Reports? | Solution: Since Aspen Capital Cost Estimator V10 a new set of Calibration Reports are available for users.
To access them you must first evaluate the project. Once evaluated click on the Capital Costs button to access the Interactive Reports.
In the Interactive Reports, toggle Excel reports, select Other Reports | Calibration.
Run the report according to the level you want to calibrate L1 for Overall code of account (e.g. All pipe components COA 300 to 399), L2 for a specific group of code of accounts (e.g. All Carbon Steel valves) or L3 for individual code of accounts (e.g. Flanged carbon steel valve COA 316).
Keep in mind that to update your index basis using these reports, an Indexing file must be selected on Project Basis View prior to run the Calibration Reports.
Keywords: Indexing, Calibration, Reports
References: None |
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