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Problem Statement: Guidelines to choose controller tuning parameters. | Solution: The output of PID controller equation is defined as:
A screenshot for the PID controller view in HYSYS is given below.
Generally, the proportional control is considered the principal component in the controller equation. The integral and derivative actions are used to trim the proportional response. Therefore, the controller gain should be tuned first with the integral and derivative set to a minimum. While the integral term in PID control reduces the noise, it also adds lag to the response compared to proportional control. The derivative action shortens the controller response. However, if a controller has a noisy input the use of the derivative action can amplifies the error and makes the controller less stable. Most oil and gas processes generally give noisy process measurement and as a result the derivative action is not normally considered in the PID controller.
The following is a guideline for choosing controller tuning parameters.
Flow Control
The flow is typically a fast responding process input, where the lead time and capacity is small. The recommended for Kc is in the range of 0.2 to 0.5 and Ti in the range of 0.05 to 0.25. If the controller gets unstable then the gain should be reduced. Since the flow measurement is naturally noisy, the derivative action is not recommended.
Level Control
The level is generally slow process, the response time increases with the size of the vessel. There is some noise associated with the measurement of level in liquid control. If this noise can be practically minimized, then derivative action can be applied to the controller. For PI only control, the liquid level controller is typically set to have a gain (Kc) between 2 and 10 and the integral time between 1 and 5 minutes.
Pressure Control
Liquid pressure - Like the flow control, the liquid pressure is typically fast. The controller gain (Kc) should be set between 0.5 and 2 and the integral time (Ti) should be set between 0.1 and 0.25 minutes.
Gas pressure - Gas pressure control is similar to liquid level control. Because of the capacitive nature of most vessels, the gas pressure process usually has a small process gain and a slow response. Consequently, a high controller gain can be implemented with little chance of instability. The pressure loop can easily be tuned for PI control. The controller gain (Kc) should be set between 2 and 10 and the integral time (Ti) should be set between 2 and 10 minutes.
Temperature Control
Temperature dynamic responses are generally slow, so PID control is used. Typically, the controller gain (Kc) should be set between 2 and 10, the integral time (Ti) should set between 2 and 10 minutes, and the derivative time (Td) should be set between 0 and 5 minutes.
Keywords: PID Controller, Tuning Parameters
References: None |
Problem Statement: PCSPUT failure and WFAILM | Solution: WFAILM is the option flag for handling PCSPUT errors, i.e., write errors. These can occur if a controller mode is changed from CASC to non-CASC or the MV limits are changed between the read and write phase of the controller cycle. If the point in the Process Control System has been deleted and re-built, PCSPUT errors can occur because the point address is incorrect. WFAILM=0 says kill the controller process on any PCSPUT failure. WFAILM=1 says turn the controller off on first failure, then kill the process on the next failure. WFAILM=2 says turn the controller off and is a good choice during commissioning when you may have addressing issues. WFAILM=3 says ignore PCSPUT failures and is a good choice after the database is stable and the controller has been excercised a good bit. The watchdog timer logic at the DCS level should flunk the controller and set regulatory loops to normal mode when the timer expires due to communications link failure.
It is necessary to stop, unload, load and start the controller to get the new value for WFAILM into the controller. A re-load will not change the value. If you want to save recent tuning changes in the online controller, you should do a manage save before stopping and unloading the controller. Please confirm that you have followed these steps to ensure activation of the WFAILM change.
KeyWords
PCSput, failure, WFAILM, DMCplus, DCS
Keywords: None
References: None |
Problem Statement: How do I change the conversion/interconversion method in Petroleum Assays for D86/TBP and D2887/TBP? | Solution: In order to change the conversion/interconversion methods, follow the steps shown below:
- Go to Home tab in the Properties environment and locate the "Options" button under Oil section.
- The Assay Options window is displayed. Here you will see the Conversion Methods section available. Select the desired method.
The D86-TBP Interconversion methods available are:
- API 1974
- API 1987
- API1994
- Edmister-Okamoto 1959
- Aspen Edmister
- Aspen API 1992
- Aspen PML
While the D2887-TBP Conversion methods are:
- API 1987
- API 1994 Indirect
- API 1994 Direct
Keywords: Conversion, Interconversion, Method, TBP, D86, D2887.
References: None |
Problem Statement: How to model radial heat transfer in cylindrical geometry. | Solution: For axisymmetric configuration, the temperature depends only on a single coordinate, r, and the heat transfer equation can be written as follows:
Due to the formulation of the equation, we will need a distribution for the temperature and another one for the r(dT/dr).
T as Distribution1D(XDomain is x) of temperature;
rdTdr as Distribution1D (XDomain is x, HighestOrderXDerivative: 1) of realvariable;
and the heat transfer model can be coded as follows:
$T(x.interior) = alpha/x*rdTdr.ddx + q/cp;
Keywords: Cylindrical geometry, distribution
References: None |
Problem Statement: Error message shows "Invalid SS cost for CVs" when adding a rank 9999 for some CVs.
This occurs because a CV which has a steady state cost specified cannot be ignored by the engine completely and a Rank 9999 is not allowed for such CVs. | Solution: CVs added to a controller application only for economics optimization purposes, cannot be ignored from feasibility check. However, they could be given the least important rank in the feasibility list, essentially allowing the controller to ignore the CV limits in preference to the more important process limits. This can be done by specifying the following configuration for the economic CV.
1. Large unimportant ranks can be specified like Rank 999
2. Broad operator limits
3. Large ECE values (1E6)
For a DMC3 controller deployed with SmartTune based tuning, CV costs based tuning is not implemented because SmartTune builds an objective function based on MV priority and CV ranking preference to calculate a cost for its optimization. If a DMCplus based application which has CV costs enabled in it has been converted into a DMC3 application with SmartTune based tuning then the DMC3 controller will reject the CV costs and only consider the costs developed by SmartTune.
It is recommended that the user needs to manually remove the CV cost from DMCplus application before the conversion to DMC3 because ignoring the CV could result in an error "Invalid SS cost for CVs" when the application in deployed. This error occurs because the application still has CV costs (even though it is not used) and ignoring the CV (like adding a rank of 9999) is not allowed if it has CV costs associated to it.
Keywords: CV costs
Ranks
Feasibility & Economics
SmartTune
References: None |
Problem Statement: What does "zapped large volume error" signify? | Solution: When the “Truncate large volume integration errors” in the Integrator is checked, the system will try to rectify any errors in volume of the holdup calculations.
If the volume of the holdup doesn't match the physical volume of the vessel and this option is checked, the vessel of volume is slightly modified in order to reduce the error.
The "zapped large volume error" is shown in message panel when the system tries to do so and indicates there are severe changes occurring. To avoid this issue, user must provide accurate dimensions of the vessels.
Key Words
Compressor, Singularity, Speed, Pressure
Keywords: None
References: None |
Problem Statement: How to use #LP in your units' worksheet | Solution: To use linear optimization in your units worksheet, use the keyword #LP to specify the LP matrix to be optimized. This keyword can be used in the following worksheet types:
- INIT
- PREP
- POST
- UNITS
To optimize in the schedule enter the keyword #LP (or #LPX for XPRESS LP solver) in column A. A sample LP matrix is as below:
The following information is returned
- The entry in column B of the #LP row determines whether or not to execute the LP Solver. If the cell has a 0 (zero) or is left blank, the Solver will be executed. If the cell has a non-zero value, the LP will not be executed
- Columns for the matrix are defined starting in column D and continuing until the entry TYPE is found on the #LP row
- The first two rows following the #LP row define the column minimums (MIN) and maximums (MAX), respectively
- The next row is the column activity (ACT) that is calculated by the optimizer
- The next row is the column incremental (INCR) value (shadow price) calculated by the optimizer
- The next row is the objective function. The objective function (PROFIT) is always maximized
- Following the first five rows are rows of the matrix as desired, until the keyword #END is encountered in column A.
- The status of the LP solution is returned by the optimizer and entered into the Profit row in the INCR column as one of the following values:
o 0 - Optimal
o -1 - Infeasible
o -2 - Unbounded
Attached to this KB is an example for the #LP which is optimizing blend components of a single blend (regular gasoline), from given blend component properties and compositions taken from a blend event (event id: 243). Open the model from \Demo #LP\Access\Demo.mdb with username “ADMIN”, model start date is 06/02/2011, model length is at default for 1 day. Use the attached units file and the SMC folder.
In the Units.xls file, go to the “POST” worksheet to find the #LP example. While making changes, be sure to reload the simulator and then run the simulation again. Note that, the solution holds good at the end of the simulation period.
The optimization solution provides the optimum activities of blend components for the specific single blend, subject to volume balance and property constraints.
Keywords: #LP, Units worksheet, Linear Programming, Optimization
References: None |
Problem Statement: How are the Lower/Higher Heating Values (LHV/HHV) calculated for hypothetical components? | Solution: Details about how the LHV and HHV heating values are calculated in Aspen HYSYS are provided in Knowledge Base Solution 116935. For hypothetical components where the user has specified a heat of combustion in the Properties environment, HYSYS will report the same values for both the LHV[std] and HHV[std]. To specify the heat of combustion for hypothetical components, navigate to the Properties environments|Components list and select the user defined hypothetical component. In the Point tab, the user will be able to enter the Heat of Comb (25C) for the hypothetical component.
The relationship that should hold between the LHV[std] and HHV[std] is as follows:
(1) HHV = LHV + sum(x[i] * Heat_of_Vaporization_of_H2O * #Hatoms[i]/2)
As HYSYS is unable to predict the hydrogen atoms within the hypothetical component it neglects the heat of vaporization term in equation 1. It reports identical values as HYSYS is unable to predict the number of hydrogen atoms associated with the hypothetical component.
To calculate HHV[gas] and LHV[gas] HYSYS uses a route through ISO 6976:1995(E) to evaluate the heating values. It matches hypothetical component molecular weights with data of hydrocarbons which are within the HYSYS database. If the molecular weight of the hypothetical component is greater than Decane, then the data found for Decane in the HYSYS databank is assumed.
Keywords: Hypothetical Components, LHV, HHV
References: None |
Problem Statement: I am using the Activated Economics feature inside Aspen HYSYS. On my Aspen HYSYS simulation, some of the utilities required are represented by material streams. When I do the cost evaluation, the operating costs related with those utilities does not show on the results. How can I include those costs? | Solution: The user needs to designate such material streams with a utility type. To do so just open up the material stream on HYSYS that is representing the utility and tag it with an utility type:
The utilities available in the drop down list are included in a database inside HYSYS, but the user can add their own to the list by going to the Process Utility Manager inside HYSYS (Economics ribbon > Process Utilities).
Once you tag the stream in HYSYS, when you load the case into APEA the system will identify that stream as an utility and during the loading you will get windows like the following:
Â
Here the user can assign a cost to the utility stream. This cost will be multiplied by the flowrate to get a final operating cost related with that utility usage.
Keywords: Steam, Cooling water, HP refrigerant
References: None |
Problem Statement: When having a Fire Scenario for a PSV in the Safety Analysis environment, how is the Latent heat estimated with the Wetted method? | Solution: The Wetted calculation method estimates the latent heat of vaporization based on the duty required to vaporize a specified portion of the holdup liquid in the vessel on a molar or mass basis. The sensible heat can be or not included, depending on the selection.
An example is attached based on the Pressure Relief example available in HYSYS. The file has been modified to have the right conditions for the Wetted method (a vessel with liquid is required to use this method). A train of heaters and separators was created to simulate the vaporization according to the specifications in the Wetted method fields.
The spreadsheet in the Flowsheet contains the imported values that are used in the estimation and the obtained value can be compared with the Fire Scenario results.
Notes were added to the flowsheet to allow a better comprehension of the calculation.
NOTE: The results might show a small difference of ±0.1 for latent heat due to the numerical calculation performed by each environment.
Keywords: PSV, wetted method, API, Fire Scenario, HYSYS
References: None |
Problem Statement: (Japanese) 仮想成分を作るのに最低限必要な情報は何ですか? | Solution: 添付PDFファイルを参照ください。
Keywords: Hypo
JP-
References: None |
Problem Statement: The sulfur recovery process involves many energy-intensive steps, where process streams must be heated and cooled to achieve conversion and sulfur removal. A bottlenecked sulfur recovery system can prevent processing of high sulfur feedstock leading to significant opportunity loss. | Solution: Sulsim technology, the leading sulfur recovery process simulator developed by Sulphur Experts, has been fully integrated in V9 of Aspen HYSYS, allowing users to optimize the entire gas plant in one simulator. Additionally, Sulsim Sulfur Recovery in Aspen HYSYS V9 includes new functionality, models and unit operations, enabling prediction of a much wider range of operating conditions and process configurations at high fidelity.
This jump start guide will elaborate on the benefits of using Sulsim Sulfur Recovery in Aspen HYSYS to optimize your Sulfur Recovery Unit (SRU) design and operational performance.
Keywords: Sulfur Recovery, Claus Process, Sulsim, Sulphur Recovery, SRU
References: None |
Problem Statement: When a user would like to change the composition of a stream using the case study tool, the stream will try to normalize the composition with each state, which might require some user interaction. How can we change the composition of a stream as independent variable to monitor properties as dependant variables? | Solution: The solution is to use the spreadsheet. The composition could be entered in the spreadsheet and exported to the stream.
Then, the user can add the input composition from the spreadsheet to the case study as an independent variable. Each case study state will change the composition in the spreadsheet and Aspen HYSYS will normalize the composition in the stream automatically.
Keywords: composition, normalization, case study, spreadsheet
References: None |
Problem Statement: Can Aspen HYSYS calculate the oil shrinkage factor? | Solution: The oil shrinkage factor is a measure of how much oil shrinks as the light components are blended into a common crude oil stream.
In the industry, this is usually calculated with API's publication 2509C or with the more recent equations in Chapter 12, Section 3 of the 1996 Manual of Petroleum Measurement Standards.
Even though the oil shrinkage factor as calculated by the standards mentioned above is not directly reported by HYSYS, the effects of mixing the lighter and heavier petroleum components are considered in the rigorous calculation of the mixture's density.
By comparing in a mixer the difference between inlet and outlet volumes, the oil shrinkage factor will be the percentage of the real mixture volume of the total mixture ideal volume. Liq Vol Flow @ Std Cond and Std Ideal Liq Vol Flow can be compared, for example.
The shrinkage factor in these correlations depends on the concentration of the lighter component in the mixture and the gravity difference in degrees API. If you want to report the oil shrinkage factor as calculated by these standards in HYSYS, you can use a Spreadsheet operation or create a user variable.
It is important to mention that the correlations from API 2509C and MPMS Chapter 12.3 were developed by using empirical data and as a result, have a limited range of applicability. The shrinkage calculated by HYSYS however, is the result of rigourous calculations and will be more accurate even outside of these limits.
Keywords: shrinking, correlation
References: None |
Problem Statement: How do I model Insulated Vessel blowdown under Fire scenario? | Solution: Use the Stephan Boltzman Fire equation or fix an external heat flux using Fire (just set C1 to a value and the remaining constants to zero). Add the insulation by using the 'detailed' heat loss model. Make sure you have checked the "Apply duty stream to outside wall" checkbox, which will ensure the fire duty is applied on the outer most wall ie the external surface of the insulation.
'Detailed' Heat loss model is not recommended with API 521 Fire method in HYSYS. This is because API 521 Fire model does not take into account the vessel mass and conductivity.
Keywords: Blowdown, Fire scenario, Stephan Boltzman Fire equation, Insulation, API 521 Fire method
References: None |
Problem Statement: Is there a standard way to determine relief conditions for blocked outlet scenarios? Will AspenTech implement one in the near future? | Solution: Many customers have requested that AspenTech provide an automated blocked outlet relief load calculation.
At AspenTech we work continuously to make your work easier and faster, however we will not pretend to offer a solution where significant engineering judgement is required; this is the case of blocked outlet scenarios.
Tube rupture, control valve failure, pool fire – these are all scenarios where there is a well-published and understood reference that conservatively assesses the relief load (e.g. Crane’s TP-410, published papers, API 521 guidance). Additionally, since these documents are widely available, engineers can easily understand the assumptions and limitations in the automated methodologies.
For blocked outlet scenario, the analysis changes significantly depending on your system and the specific company guidelines. There is no one right way to always analyze blocked outlet scenarios.
Some of the things to be considered are:
1. What does a blocked outlet mean to you?
2. Blocked vapor outlet
· Will the full inlet feed flow be relieved? At what conditions?
· Will just the vapor flow be relieved? Will an adiabatic flash be used to simulate going from normal to relief conditions? Is it the right assumption taking only the vapor to saturated conditions at the relief pressure?
· Is there steam injection? Or any other source of heat input that could cause additional vaporization of the inventory during a blocked outlet?
3. Blocked liquid outlet
· Do you need to calculate the time to overfill so you can take some credit for operator intervention based on the level alarm configuration?
· Do you size the device for full liquid flow regardless of system conditions?
· Do you size the device for full feed flow regardless of system conditions?
Within the simulator, you have all the tools necessary to use your engineering judgement in order to determine the relief load and relief conditions.
As a reference guide, attached to this document is a HYSYS file that shows how to leverage the simulator to answer some of the questions above.
If your company follows a standard practice when analyzing blocked outlet scenarios, you could implement a subflowsheet with the appropriate type of flashes and calculations to determine the relief load. See the attached HYSYS files for examples. These sub-flowsheets can be saved as template files or be copy-pasted across HYSYS cases. This allows you to save time and effort, while also ensuring that you fully understand the steps in the analysis.
Keywords: Relief Valve sizing, Blocked outlet scenario, PSV, HYSYS, Safety Analysis Environment
References: None |
Problem Statement: I have noticed a difference between the heat capacities (Cp) of my aqueous phase in a hydrocarbon / MEG fluid between Aspen HYSYS V7.1 and V7.3. The Cp tables for water / MEG mixtures agree with the values obtained from V7.3. | Solution: In Aspen HYSYS V7.1 or earlier versions, the Lee-Kesler enthalpy method calculates enthalpy, entropy, and heat capacity (Cp and Cv) of a mixture that contains water by calculating the contribution from the non-water components (dry basis) using the Lee-Kesler equation of state model and the contribution from water using the Steam Table. The two contributions are then combined using mole-fraction average to obtain the property of the mixture. This approach leads to incorrect enthalpy or heat capacity values.
In Aspen HYSYS V7.2, the Lee-Kesler enthalpy method was modified to always make the calculation on the wet basis. That is the model is used to calculate enthalpy, entropy and heat capacity of the entire mixture, not just the water-free portion. This change resolves all above problems that were present in Aspen HYSYS V7.1. But because Lee-Kesler method is not good for pure water the results of property are not good when stream is pure water or like pure water.
In V7.3, the Lee-Kesler enthalpy method was improved to make property calculations changing Lee-Kesler method (wet basis) to Steam Table smoothly by using nonlinear extrapolation for the like-pure-water or pure water stream.
If you run a case that was created in V7.2 without hotfix or earlier versions using V7.3, you can expect different results for enthalpy, entropy, Cp, and Cv. This is the reason you see different entropy values, if you check properly, you will also see differences between enthalpy and Cp values. However, the results from V7.3 are more accurate.
Keywords: Heat Capacity, Aqueous Phase
References: None |
Problem Statement: I have created a stream inside my subflowsheet that I wish to use as a feed stream in the main flowsheet. If I look on the Connections page of the subflowsheet view, however, the stream is displayed as an inlet connection to the subflowsheet. Is there a way to specify this stream as an outlet connection to the subflowsheet? | Solution: By default, Aspen HYSYS will assume that an unconnected stream inside a subflowsheet is an inlet connection to that subflowsheet. To alter this behavior, create a new unit operation inside the subflowsheet and connect the stream as a product to this newly created operation. If you now exit the subflowsheet environment and view the Connections pagetab of the subflowsheet operation, you will note that this stream is shown as a outlet connection to the subflowsheet (once you have established the desired external connection to the subflowsheet stream, you can delete the "dummy" operation that was created inside the subflowsheet).
Alternatively, you could create the desired stream in the main flowsheet first (i.e. do not create the "outlet" stream in the subflowsheet as your initial step). Once this process stream has been created, you can connect it as an external outlet connection to the subflowsheet (via the Connections pagetab of the subflowsheet operation). After the connection to the subflowsheet has been made, the target process stream will also appear inside the subflowsheet.
Keywords: outlet, product, connection, feed, inlet, flowsheet, subflowsheet
References: None |
Problem Statement: How to use the Dynamic Depressuring Utility to depressurize at constant flow rate? | Solution: The Dynamic Depressuring Utility in Aspen HYSYS can be setup to give a constant flowrate following the steps given below.
1. Add a new Depressuring Utility to the stream that you want to analyze.
2. Define the geometry of the vessel appropriately via the Connections page.
3. Open the Valve Parameters page, set the Vapor Flow Equation to "Use Spreadsheet" and press the "View Spreadsheet button".
4. Set the mass flow rate that you want in cell B7.
5. Close the Spreadsheet and return to the Depressuring Utility.
6. Set the Vapor Flow Equation to Fisher and enter a reasonable value for Cv and Valve Opening. This is required as we need to initialize the utility with the Fisher model before we can run with a constant flowrate.
7. Run the utility.
8. After the Utility has run, change the Vapor Flow Equation back to "Use Spreadsheet". Press the View Spreadsheet button again, and enter a value of 1 on cell C7.
9. Close the Spreadsheet and run the utility.
You should see that the mass flow rate is constant and equal to the value that you set in step 4.
Note: Caution should be applied when using the utility in this manner as the utility will start to give errors once the pressure in the vessel falls below the back pressure of the valve.
An example that shows a utility with a constant flowrate is attached.
Keywords: Dynamic Depressuring, Constant Flow
References: None |
Problem Statement: What could cause Aspen Capital Cost Estimator to stop evaluating the project after clicking the "Evaluate" command? | Solution: If you get an empty evaluation progress bar such as this:
"Percent Completed: 0%"
And if you try to evaluate an individual component you get an error message:
"Capital cost report not found, may need to evaluate item."
There is a chance that your ACCE Engine is damage, the reason for this can be multiple but some other software might have corrupt or damage the FORTRAN libraries. To verify first go to the path: C:\Program Files (x86)\AspenTech\Economic Evaluation V#.#\Program\Sys\ and look for the file iccost.exe and try to execute the program.
If you get a run type library error, is very likely that the engine is damaged:
"The program can't start because libifcoremd.dll is missing from your computer. Try reinstalling the program to fix this problem."
To solve the problem, you need to ask your IT department to help you with a re-installation of ACCE and the patches.
Keywords: Capital cost report not found, may need to evaluate item, The program can't start because libifcoremd.dll is missing, ACCE stop evaluating
References: None |
Problem Statement: Can I specify different maximum shop fabrication diameters for different areas? | Solution: Since V7.2, user is allowed to specify different maximum shop fabrication diameters for different areas by changing the shop fabrication maximum diameter field that is added in the area level equipment specifications form.
Keywords: Area equipment spec, maximum diameter
References: None |
Problem Statement: What do I need to do to get the "Air cooler, free-standing or rack-mounted" component hung on my steel structure? | Solution: If you set the height (leg height) to 0 it will be rack mounted.
Keywords: Air cooler, free-standing, rack-mounted, leg, height, rack, steel, structure
References: None |
Problem Statement: I unlinked some of the areas from control centers and unit sub-stations. When evaluating the project I received such error message as ?Aspen Icarus Cost Engine Application has encountered a problem and needs to close?. | Solution: When a new area is created by user, it automatically gets linked to a control center and unit sub-station. If for some reason, user unlinked some areas and did not link them back to any of the control panels and sub-stations, the aforementioned error will appear. Making sure all areas are linked to control centers and unit-substation will clear that error.
Keywords: Area, control center, unit-substation
References: None |
Problem Statement: Can I modify my wage rates in Excel and then use that in Aspen Capital Cost Estimator? | Solution: Yes. You can copy the wage rates from Aspen Capital Cost Estimator into Excel and make your modifications. When you are through, then use the Paste Selection feature to copy them back to Aspen Capital Cost Estimator.
Keywords: None
References: None |
Problem Statement: What version of Primavera (P3) will work with Aspen Kbase and Aspen Icarus Project Scheduler? | Solution: For Aspen Kbase versions 2006.0.4 (Aspen Kbase v2006 with Cumulative Patch 4) and higher, Primavera v5.0 is the only supported version.
This means that version 6.0 if Primavera is not supported at this time.
Keywords: primavera, p3, version, compatible, 5.0, 3.1, 3.0, P3, P3ec, P3e
References: None |
Problem Statement: How do I enter new rental equipment? | Solution: Aspen Capital Cost Estimator provides empty slots in every equipment class for user-entered equipment items. Any that you enter are added to those that Aspen Capital Cost Estimator develops based on your project work items. To enter a new rental item:
1. In the Basis for Capital Costs folder, right-click Equipment Rental; then click Edit on the pop-up menu. Aspen Capital Cost Estimator displays the equipment rental specifications form in the Main Window. A column for the first rental item, labeled Item 1, is provided. If you need to add a column, click Add.
2. Enter an item description. The first 20 characters will appear in the Description column on the Equipment Rental Summary report. The next 16 characters will appear in the size column on the Equipment Rental Summary report.
3. Enter an equipment number. Numbers 1-20 are for the equipment class AUTOMOTIVE. All other numbers will share the equipment class of the equipment number before it. For example, an item assigned equipment number 79 would be classified EARTHMOVING because that is the equipment class of equipment number 78. Each equipment class includes unused numbers for user-entries. Refer to Icarus
Keywords: Rental equipment
References: ,Chapter 32, for a complete list of construction equipment and associated equipment numbers.
4. Click Add as the Rental Action Code.
5. Enter the Rental Days Required.
6. Enter the Monthly Rate.
7. Click OK to save the specifications and close the specifications form. |
Problem Statement: When installing the new aspenONE v2006.5 software, I get an error message stating:
"Error 1303. The installer has insufficient privileges to access this directory: 'C:\Documents and Settings\user_login\My Documents\AspenTech\Aspen Icarus 2006.5 Files'. The installation cannot continue. Log on as an administrator or contact your system administrator"
or the error could read:
"Error 1303. The installer has insufficient privileges to access this directory: 'C:\Documents and Settings\All Users\Documents\AspenTech\Shared Aspen Icarus 2006.5 Files'. The installation cannot continue. Log on as an administrator or contact your system administrator." | Solution: There are 3 possible reasons that we know of at the moment that can cause this problem:
Reason 1
An important finding is a documented fact regarding the Windows Installer and Folder Encryption. One should be familiar with this, as it will enlighten you to the hardships that using File Encryption can cause:
http://blog.colinmackay.net/archive/2007/06/21/36.aspx
Reason 2
The use of File Encryption for the user's My Documents folder or the 'C:\Documents and Settings\All Users' folder. Please be sure to turn File Encryption off prior to installation of the Aspen Icarus software.
New folder directories are being used for v2006.5. Please see solution document 121905 for this new directory structure.
Reason 3
Permissions are incorrect for one or more of the following:
1. The person installing the software does not have Administrator privileges. Installation of the software requires the installer to have Administrator rights.
2. The Local Group 'Users' does not have the user's domain login (ex: CORPDOMAIN\username) added.
3. The SYSTEM account or The Everyone group does not have Full Control privileges.
Items to Check
1. Open Windows Explorer and change directories to the ?C:\Documents and Settings\All Users\Documents\AspenTech\Shared Aspen Icarus 2006.5 Files? folder, to see if it can be accessed or if it is created.
If you receive this message:
"You do not have privileges to access this directory: C:\Documents and Settings\user_login_name\My Documents\AspenTech\My Aspen Icarus 2006.5 Files."
Check the Properties permissions to the C:\Documents and Settings\user_login_name\My Documents\AspenTech\My Aspen Icarus 2006.5 Files folder.
The 2 groups that have permissions to access this folder are: SYSTEM and Users.
2. Check to make sure that the domain login of the user (ex: CORPDOMAIN\username) is part of the local PC or laptop ?Users? group. If it is not, then the software will not run (or possibly not be installed) because of the Error 1303 or if the Aspentech 'Configuration Dialog box' keeps appearing time after time, but still does not allow the software to be run.
Group permissions for the following folders is as follows:
C:\Documents and Settings\All Users\Documents\AspenTech: Everyone.
For the 'C:\Documents and Settings\All Users\Documents\AspenTech\Shared Aspen Icarus 2006.5 Files'
folder, the group permissions are: SYSTEM and Users.
Conclusion:
In general, the more secure a computer is, the more inconvenient it is to operate it.
For example, compare Windows Vista with Windows XP. Vista is securer than XP. This means that one has to adapt to User Account Control (UAC) in Windows Vista. Some software can not run correctly in Vista system up to now. So if one needs the additional security, one has to accept the inconvenience caused by a higher level of security. So we pass the information on to the customer to decide on what would work best for their needs??it?s a matter of balancing an increased level of security and convenience.
AspenTech's developers and programmers agrees that the installation of our software is only eligible for common environments. Unfortunately, AspenTech can not consider all the special software environments of every customer?.(i.e. systems with Encryption File System enabled).
If you are still unable to install or run your AspenTech software product, please send an e-mail with screen shots to [email protected].
Keywords: 1303, error 1303, insufficient, privileges, access, installer
References: None |
Problem Statement: Are there any supports given for conduit with piping, or do I have to library an item? | Solution: At this time, the economic evaluation software does not provide conduit supports. You will have to account for the conduit support either through a quoted item or by adjusting your material/man-hours for that item.
KeyWords
conduit
support
supports
Keywords: None
References: None |
Problem Statement: According to the Association for the Advancement of Cost Engineering (AACE) International, what will be the Estimation Class that Aspen Capital Cost Estimator (ACCE) will give me? | Solution: ACCE cost is applied for the Conceptual estimate phase, which has a typical accuracy between +/-20% and +/-10%. In terms of class, it is equal to a CLASS 3 Estimate, according to the AACE International.
Find the attached file with the explanation.
Keywords: Accuracy, AACE, Class 3
References: None |
Problem Statement: Ho can I solve the following error:
FATAL> 'T - 2' CURRENCY INPUT USED, ALL INPUT FIELDS MUST BE SPECIFIED | Solution: This error refers to the General Project Data form, specifically the lines defining project base currency:
Please note that the conversion factor in the screenshot above is in light blue, which means is a default value, however in some circumstances the value might not be correctly picked up by the calculation engine and the error is generated. This can be misleading. In order to solve the problem just renter the conversion factor, so it shows a black font.
Keywords: ACCE, fatal error, T-2
References: None |
Problem Statement: A situation might occur where a user who views their AACM secondary, primary and overflow queues, notices that they are not decreasing in a timely manner. The messages in the AACM log file indicate the following:
Output - AACM server log file.
IP21Admin (1130308) 04/18/2005 16:39:15.586 AtQueue::Get - QueueGet: The system cannot find the path specified.
IP21Admin (1130304) 04/18/2005 16:39:15.821 AtQueue::Get - QueueGet: The system cannot find the path specified.
The problem is that the AACM secondary, primary and overflow queues are full of unhandled events. These files cannot be processed in this state. The exe file that is attached to this solution systematically processes the files into a state that allows the files to be processed. | Solution: The GUI has three edit boxes where each of the queue file names are entered. The entire file path needs to be entered and convert to text button is pressed. Each queue file will be converted into a set of text files that are 10MB each that the user can view in an edit and change the events (malformed etc). Use the administrator process file option on the server node after stopping queue processing to have the AACM server process the file and insert the events it contains into the database. After each process file completes a dialog and text file is written indicating the number of events that succeeded and failed (malformed).
KeyWords
unhandledevent file
AuditAndComplianceUnhandled.txt
alarm and event
AA&CM
A&E
Keywords: None
References: None |
Problem Statement: What is the frequency or slug frequency Slug Tool? | Solution: The Slug frequency is defined as
v = c / (Lslug + Lbubble)
where c is wave speed.
The slug and bubble lengths tend to infinity as the slug frequency tends to zero.
Keywords: Frequency, Slug Frequency, Slug Tool
References: None |
Problem Statement: How to display or print the workbook table on PFD with desired streams and formatting, and export to Excel. | Solution: 1. When you get the workbook window, you should find workbook menu as the following:
2. Click the setup in workbook menu:
3. You will get the following window:
4. You will build a stream tab by choosing material stream and click ok:
5. You can change to different tab name and add or delete the variables:
6. For example, I set the name to "Report Flowrate" 7. Then you go back to PFD and right click empty space. Choose Add Workbook table:
8. Select Report Flowrate in window:
9. To show the desired streams, you will need go back to workbook and the tab you created. Select the streams you do not want to show. Then you can right click your mouse.
You choose Hide Object. You will see those streams will not show on your PFD table.
10. If you want the number display in non-scientific view, you will need to go to Tools -> Preferences:
11. In the Preference, select the Variables tab:
12. Choose Formats. Select the variables you desire to change and click Format:
13. You can change the format in her:
For example, I change format as following:
You can see those changes.
To print the results:
1. Go to workbook and the tab you created. You could put your mouse cursor over the blue bar of workbook and right click:
2. In the "Select Datablocks" view as the following, you uncheck other tabs.
You will then be able to print the results.
To export the results to Excel:
3. You will need go to the workbook menu and choose Export.
4. Choose option: To Excel.
Keywords: Results, workbook, print, format.
References: None |
Problem Statement: In the Menu Bar, why don?t I have the option for ?WorkBook? | Solution: The options for WorkBook and PFD only appear in the Menu Bar when that particular item is open on the DeskTop and has focus. So to get the WorkBook option in the Menu Bar, the WorkBook must be open and have focus.
Keywords: :
References: None |
Problem Statement: How can I add another Property Package when working with Amines just for a few unit operations? | Solution: Sometimes, you need to work with amines, but not for the whole simulation, because it might cause some problems (You can check the next solution which shows that Peng Robinson is not good in simulating Amines 109782).
That's why it's recommended to choose to use the Amine Pkg or the DBAmine Pkg for the specific Unit Operation that handles amines and after that choose another Property Package for the rest of the simulation.
Now, how to add different Property Packages in one Simulation.
1. Add your components.
In the case of choosing DGAmine, if you choose Peng Robinson, Hysys will warn you that if you use PR the results may not be the best ones, but you will click on ''Keep Components'' because after this you will add another property package to model amines.
The screen will look like this:
2. Then go to the Simulation Basis Environment> Fluid Pkgs Tab> Click Add> Choose Amine Pkg as you can see in the following screenshot:
Now you will have two Property Packages in your simulation.
3. Then go back to the Simulation Basis Manager and in the right part you will see the Fluid Package Association. In here you can select for a specific Unit Operation, in this case your column, a specific Property Package. There is an example of how your screen would be like at this moment:
At this time you can work with Amine Property Package in your Amine Column and in the rest of your simulation with Peng Robinson.
Keywords: Amines, Peng Robinson, different property packages
References: None |
Problem Statement: What are the main differences between HYSYS Oil Manager and Petroleum Assay Manager? | Solution: HYSYS Oil Manager
Petroleum (RefSys) Assay Manager
Each petroleum assay blend has its own set of component lists. If you have 10 blends, each contains 30 hypo-components, you will have 300 hypo-components in the component list.
Multiple assays / blends share the same component list. The number of hypo-components is independent of number of assays / blends.
Property values can be less accurate as each assay blend has its own component list.
Property values are more accurate as all assays share the same component list.
Deals with a very few petroleum properties.
Deals with all petroleum properties.
Use simplified options to characterize a petroleum assay.
Use advanced options to characterize a petroleum assay.
Keywords: Petroleum assay, oil manager, difference
References: None |
Problem Statement: How di I override the default emulsion viscosity method in pipe segment for an Oil/Water mixture? | Solution: For an Oil/Water mixture, Aspen HYSYS uses the following mixing rule to calculate mixture viscosity (see Solution 108998)
A? For V(oil) > 0.5, Mu(m) = Mu(oil) * e^[3.6*(1-V(oil)]
A? For V(oil) < 0.33, Mu(m) = [1 + 2.5 V(oil) ((Mu(oil) + 0.4 Mu(water))/(Mu(oil) + (Mu(water))] Mu(water)
A? For 0.33 < V(oil) < 0.5, the viscosity is calculated by a weighted average between the equation for V(oil) > 0.5 and for V(oil) < 0.33:
Mu(overall) = Mu(V(oil)>0.5)*(V(oil)-0.33)/(0.5-0.33) + Mu(V(oil)<0.33)*[1-(V (oil)-0.33)/(0.5-0.33)]
where:
Mu(m) = apparent viscosity of the mixture
Mu(oil) = viscosity of hydrocarbon phase
Mu(water) = viscosity of aqueous phase
V(oil) = volume fraction of the hydrocarbon phase in the blended mixture
Different from ordinary mixing rule, this mixing rule takes account of emulsion formed in the blended oil-water mixture. Consequently, a high mixture viscosity is predicted.
Viscosity is important for pressure drop calculations in the pipe. If the pipe gives unrealistic pressure drop calculations with the default mixing rule in particular when emulsion is predicted it is advisable to use an appropriate viscosity method as made available in the pipe segment from HYSYS V7.3 with the latest patches installed.
In the Design tab of pipe segment, user can override the viscosity method in the Emulsion page. Use F1 for details of available methods.
Keywords: Emulsion Method, Pipe Segment, Oil/Water Mixture
References: None |
Problem Statement: How do I configure the variable (step-wise) fire load in depressurizing utility? | Solution: The fire load can be applied as constant or variable based on vessel wetted area in the depressurizing utility. A constant fire load of different size during depressurizing can be configured in the spreadsheet available under the Operating Mode in the Heat Flux page. See screen-shot below.
To implement different fire load at different time, the integrator time needs to be included in the spreadsheet. The screen-shot below shows as an example how three fire loads of 150,120 and 100 kW can be applied at 0, 600 and 1800 seconds in the depressurizing stages.
Keywords: Variable Fire Load, Depressurizing Utility.
References: None |
Problem Statement: How to get a collections of utilities of a certain type in Aspen HYSYS through VBA Automation. | Solution: The property "UtilityObjects" from HYSYS.SimulationCase can be used to retrieve the collection of all utilities in a simulation case, however this property doesn't take an indexer to narrow by type the elements like "HYSYS.Flowsheet.Operations" does (see solution 144577).
This simple piece code illustrates how to create an array of utilities filtered by type:
Dim hyApp As HYSYS.Application
Dim hyCase As HYSYS.SimulationCase
Dim hyUtil As Object
Dim utilCol() As Object
Set hyApp = CreateObject("HYSYS.Application")
Set hyCase = hyApp.ActiveDocument
Dim count As Integer: count = 0
For Each hyUtil In hyCase.UtilityObjects
   If hyUtil.TypeName = "htfsplusdesignutil" Then
       ReDim Preserve utilCol(count)
       Set utilCol(count) = hyUtil
       count = count + 1
   End If
Next
'utilCol contains all the shell&tube sizing utilities
Â
Keywords: VBA, HYSYS, Utilities
References: None |
Problem Statement: In the Oil Manager, I have created an Assay and a Blend from that Assay, but I cannot install the Blend. I can give the blend a stream name but cannot select a flowsheet for the installation. | Solution: This happens because the Oil Manager does not have the correct Fluid Package associated with it, or the Fluid Package that is associated with the Oil Manager is not associated with any of the flowsheets or subflowsheets in the simulation.
You will need to leave the Oil Manager and return to the Simulation Basis Manager. Go to the Oil Manager tab and ensure that the "Associated Fluid Package" selected is the same as the Fluid Package which is being used by the Flowsheet that you wish to install the oil into.
Please refer to the attached image as an example of what your Oil Manager Fluid Package Association should look like.
Keywords: oil, blend, assay, install, flowsheet, manager, stream
References: None |
Problem Statement: Getting Non-compatable Fortran DLL compiler error after applying the patch for PIPESIM 2010.1 in V7.3 | Solution: After applying the patch for PIPESIM 2010.1 in V7.3,A you may get the error as the below when you solve the PIPESIM.
"Warning during libifport.dll initialization: Non-compatible version of Fortran libifcore DLL was loaded to process address space."
In the case, if you copy the newer versions of the two files libifcoremd.dll and libmmd.dll from the PIPESIM directory into C:\Windows\system32 the problem goes away.
Keywords: Pipesim 2010.1, Hysys, patch.
References: None |
Problem Statement: How can I use mass fraction or volume fraction when importing assay from a csv file? | Solution: In the csv file, the Heading COMPOSITION (MASS) or COMPOSITION (VOLUME) should be specified in the table.
Make sure that you add the type of fraction in brackets.
KeyWords
Import, csv, volume fraction
Keywords: None
References: None |
Problem Statement: How do I calculate gas property correlations (HHV, LHV and Wobbe Index)? | Solution: The HHV (vol basis) and Wobbe Index gas correlations are calculated based on "ISO 6976:1995", and are identical to equations 8.2.1 to 8.2.6 in the "GasProps User Guide.doc" attached here with the solution.
The value of Z is calculated from equation 8.2.1 (not calculated from HYSYS via Z = pV/RT). The HHV (molar basis) was added in HYSYS V7.2 and was based on the following equation:
HHV (molar basis) = HHV (vol basis) / (p/ZRT), where Z was calculated from equation 8.2.1 in the "GasProps User Guide.doc"
Note Z is a function of the square root of B parameters for given components. The B parameter (actually square root of B) @ 15C, 101.325kPa can be found in Table 2 in the ISO 6976:1995 report. The user need to get access to this report on their own.
The source component LHV and HHV values are in units of MJ/m3, so if other units are selected the internal values calculated are converted using:
kJ/m3
Multiply by 1000
kcal/m3
Multiply by 238.846
Btu/ft3
Multiply by 26.8392
At the same time HHV (molar basis) was added, a new unit BTU/SCF was added as well and the following conversion was used:
1 kJ/kmole = 0.001132992 BTU/SCF
Keywords: HHV, LHV and Wobbe Index
References: None |
Problem Statement: What conditions should the gas or liquid be referenced when adjusting a reservoir composition to suit the Gas-Oil (or Gas-Condensate) Ratio | Solution: Depending on the referenced condition, the user will obtain different values i.e at stock tank conditions, reservoir saturation conditions or the first flash.
The GOR or GCR calculations should be done in the way the GOR or GCR measurement was done. The difficulty here is finding out how it was carried out. In most cases, users tend to do a single flash at standard conditions.
There is an extension that models a well head, relating flow to pressure, using entered data that can be downloaded from the support site KB 130427
Keywords: GOR, GCR, Extension
References: None |
Problem Statement: What are the formulae used for calculating Surface Area, Metal Volume and Fluid volume as displayed in Performance\Summary of the Plate Fin (LNG) Exchanger? | Solution: The calculation of Fluid Volume, Surface Area and Metal Volume for an LNG exchanger has been illustrated in the attached example HYSYS file.
The LNG exchanger ' LNG HX' attached with this solution consists of one hot stream ( A) and two cold streams (B and C). In order to calculate fluid volume, surface area and metal volume it is necessary to know the zone geometry and the fin properties.In the simulation these parameters can be found on the LNG exchanger unit operation /performance/Summary page.
For LNG Unit operation three zones have been defined on the Rating/Sizing page of the exchanger. Plate and fin properties are added and the heat transfer data has also been specified.Having known the above mentioned data and when used in the below formulae produce the same results as calculated by Aspen Hysys ( refer to the attached Excel spreadsheet).
The HYSYS calculated values for Zone (0), Layer 0A for fluid volume, surface area and metal volume are 0.1794 m3, 607.2 m2 and 9.961e -4 m3 respectively. The corresponding hand calculated values are shown in the spreadsheet. This shows that the values match with the HYSYS results. The formulae used to derive these results are given below:
1) Fin Area = (2 * pitch * (height-thickness) * width * length * (100 - Perforation)) *100
2) Plate Area = 2 * (1-pitch*thickness) * width * length
3) A1 =( Fin Area + Plate Area) / 2
4) A2 = A1/ 1 where the numerical 1 refers to the number of sides and is always assumed to be unity in Aspen Hysys.
5) A3 = A2 * Repeated sets.
6) Surface Area = A3 *2
7) Total volume = height * width * length
8) Metal horizontal volume (m3) = thickness * width * length
9) Metal vertical volume(m3) = (height-thickness) * thickness* pitch *length * width
10) Metal Volume = Metal horizontal volume + Metal vertical volume.
11) Actual holdup volume = (Total volume ? Metal volume) * repeated sets.
Keywords: LNG, Fluid volume, surface area, Plate Fin exchanger
References: None |
Problem Statement: How can I use MS Excel to retrieve the heating and cooling curve of a heat exchanger in user specified units? | Solution: In HYSYS, you can find the data on the Performance tab | Tables page of Heat Exchanger property view. For either tube side or shell side, HYSYS provides temperature, pressure, enthalpy, heat flow and vapor fraction along the curves.
From Excel, the heating and cooling curves can be retrieved using VBA macros. To use this example,
1. Download the attached files, both HYSYS case and Excel workbook, to a local directory
2. Open HYSYS and load case 'heat exchanger.hsc' (make sure there is only one instance of HYSYS open)
3. Open Excel and load workbook 'get HX curves.xls'.
4. Click on the 'Get Available Curves' button to get the names of tube side and shell side curves for the heat exchanger named in cell D6 (the list of curves is shown in cell D9). HYSYS use a inlet_stream-outlet_stream naming convention to represent the curves.
5. Select a curve from cell D9 and then click 'Get Curve Data' button to view the data of the selected curve. The units for the data are specified in cells B16, C16, D16 and E16. If desired, the user can change the units to any HYSYS recognized units, then click the 'Get Curve Data' button again to update the data values.
Users can make changes to the worksheet or the macros for their modeling needs. To access the VBA macros, select Tools | Macro | Visual Basic Editor from the workbook. Inside the Visual Basic Editor, check Tools |
Keywords: heating, cooling, curve, temperature, enthalpy, heat exchanger
References: s to ensure the HYSYS Type Library is referenced.
The macros have been tested for both End Point and Weighted heat exchanger models. |
Problem Statement: Under specific circumstances, when inserting a Tag in the Legend Area of an Aspen Process Explorer plot, users might encounter the following message:
Note: This message is for informational purposes only. Upon clicking the Close button, Aspen Process Explorer will continue to work. In other words, it does not affect functionality. | Solution: Starting in version 2006.5, Aspen Process Explorer performs two different run-time license check routines:
1. It verifies and checks out an Aspen Process Explorer license.
2. When connecting to a specific InfoPlus.21 (version 2006.5 and above) to retrieve tag data, it verifies whether or not the InfoPlus.21 Server is running in licensed mode.
The message described in this Knowledge Base article occurs during the second routine, and it means that the Aspen Infoplus.21 Server is running unlicensed mode. To examine and troubleshoot issues related to Aspen InfoPlus.21 licensing, please refer to KB 123811:
http://support.aspentech.com/webteamcgi/SolutionDisplay_view.cgi?key=123811
Keywords: Unable to acquire InfoPlus21 License
Process Explorer License
References: None |
Problem Statement: The optimizer has stopped and is giving me the message ?Cost convergence?, ?step convergence? or ?globally infeasible?, or ?Flat?. What does this status mean? | Solution: For the HYSYS.RTO+ optimizer, the user can enter tolerances for cost convergence and step convergence.
Cost convergence - the optimizer has found the optimum, and converged to a point where the improvement attainable by taking a subsequent optimization step will improve the objective function by less than the user specified cost convergence value.
Step convergence - the optimizer has reached a point where it is trying to improve the objective function. It decreases the size of the step taken due to mismatch between the projected results using the first order derivative matrix and those observed by the model. In some cases, this can be related to the required step size for the optimizer being smaller than the perturbations used in gradient calculation. If this is the case, one option which could be investigated would be to decrease the perturbation factor at the given operating point.
Globally infeasible - the optimizer is unable to locate a feasible operating point given current operating point and the gradient information calculated at that point. This often can be alleviated by adjusting the optimizer tuning parameters (including those affecting perturbation sizes and scales on constraints).
Flat - the change in the objective function is zero between optimization steps. Ensure that the objective function is not showing up as empty, and that there is a non-zero price associated with the objective function variables in question.
Keywords: Optimizer, results, step convergence, cost convergence, flat, globally infeasible
References: None |
Problem Statement: I am getting this error message:
"No calculation warnings encountered. PIPESYS extension not converged. Invalid data in an object of type class CPressureDiff Value = 147909". What does it mean? | Solution: The problem deals with the pressure drop or difference being more than the allowed value. The best way to resolve this problem is to click the "Force Enthalpy Convergence" box on the tolerances tab. This tightens-up the tolerances and solves the problem.
Keywords: pipesys, error, pressure
References: None |
Problem Statement: What criteria does the Pipe Segment use when checking for Choked Flow ? | Solution: In order to make the Pipe Segment check for choked flow, tick the "Check Choked Flow" checkbox on the Design ... Calculation page.
[The default setting is for this option to be switched off. This option was introduced with Aspen HYSYS 2.4.1]
If this is switched on then as it solves the pipe checks whether
V^2/c^2 > 1
Where V is the fluid velocity in the pipe and c is the speed of sound in the fluid.
c^2 is calculated from the standard partial differential relationship:
c^2 = dP / d rho at constant S
Where P is pressure, rho is mass density and S is entropy
In Aspen HYSYS, dP/drho is calculated by a finite difference method. Two flashes are carried out at slightly different pressures but such that the entropy is constant and the gradient is then calculated.
Because of the extra flashes involved this slows down the pipe calculations.
Why is this important ?
The correlations used by the Pipe Segment are not valid for use with choked flow.
The Compressible Gas Pipe Operation or the separate Aspen Flarenet program are suitable for compressible flow systems.
Keywords: Pipe Segment, Choked Flow, Speed of Sound
References: None |
Problem Statement: </b></u>
How can I make Valve Actuator Opening and Closing rates different?
<b><u> | Solution: </b></u>
The Valve unit uperation only allows one Actuator rate to be specified (Dynamics ... Actuator page). However using a Transfer function operation and a Spreadsheet it is possible to make the Actuator rate vary depending on the whether the valve is opening or closing. The attached HYSYS 2.4.1 (Build 3870) case illustrates this.
The Transfer Function operation is used to get the valve position at a set delay time (in this case 5 seconds previously). The Spreadsheet then compares the current valve opening with the opening from 5 seconds ago and hence decides whether the valve is opening or closing. An Actuator opening rate is then exported to the valve accordingly. A similar method could be used to set the First Order time constant.
<b><u>KeyWords</b></u>
Valve Actuator; Dynamics; Controls
Keywords: None
References: None |
Problem Statement: How do I add the Process Data COM add-in after previously removing it? | Solution: Add the following entries to
HKEY_CURRENT_USER\Software\Microsoft\Office\Excel\Addins\AspenTech.PME.ExcelAddin.ProcessData
Â
After adding the registry key, the Process Data tab will appear in Excel.
Keywords: COM add-in
Process Data add-in
registry
regedit
References: None |
Problem Statement: How do I obtain phase 'Standard' properties using OLE Automation? | Solution: Retrieving standard properties ('Liq Vol Flow @ Std Cond', 'Std. Gas Flow', 'Liq Mass Density (Std Cond)') for Fluid or FluidPhase objects is not as straightforward as for the majority of properties. Since these properties are not yet available within the HYSYS type library, it is necessary to use a 'Backdoor' method. This uses the internal variable name (or 'Moniker') to directly access the value.
The code below will retrieve the light liquid phase 'Liq Vol Flow @ Std Cond' property. It does not include any error checking; in practice you should check whether there is a light liquid phase in the stream before trying to access it.
It is not possible to directly retrieve the standard liquid density of a Fluid or FluidPhase object; the way to get this is to calculate it from the mass flow and the standard liquid volume flow.
The attached Excel spreadsheet includes example code which retrieves all the standard properties for all the phases (overall, vapour, light and heavy liquid) in a specified stream. It includes better error checking and also determines which units HYSYS is currently using for these properties.
For troubleshooting advice on common HYSYS / OLE Automation errors see Solution #112361.
To use the code below: open up Aspen HYSYS with any case, paste the code into the VBA editor in Excel, modify the code to link to a particular stream, make a reference to the HYSYS type library (Tools ...
Keywords: None
References: s menu option in the VBA editor), and run the procedure.
Private Sub GetPhaseStdLiqVolFlow()
Dim hyApp As HYSYS.Application 'HYSYS Application
Dim hyCase As HYSYS.SimulationCase 'HYSYS Case
Dim hyStream As HYSYS.ProcessStream 'HYSYS stream
Dim hyFluid As HYSYS.Fluid 'HYSYS Fluid
Dim hyPhase As HYSYS.FluidPhase
Dim hyBD As HYSYS.BackDoor
'Must be declared as a BackDoor object type - hence need a type library declaration
Dim hyStdFlowVar As HYSYS.RealVariable
Dim dblFlowVal As Double
'Link to App, Case and Stream
Set hyApp = GetObject(, "HYSYS.Application") 'Only works if HYSYS is open
Set hyCase = hyApp.ActiveDocument
Set hyStream = hyCase.Flowsheet.MaterialStreams.Item("StreamName")
'Get stream as a fluid
Set hyFluid = hyStream.DuplicateFluid
'and link to a particular phase
Set hyPhase = hyFluid.LightLiquidPhase
'Obtain a Backdoor variable for the Phase
Set hyBD = hyPhase
'Here could equally do - to put the overall fluid into the backdoor
'Set hyBD = hyFluid
'Use a backdoor variable to retrieve the value
Set hyStdFlowVar = hyBD.BackDoorVariable(":StdLiqVolFlow.501.0").Variable
'The moniker for Standard Gas flow is: ":StdGasFlow.501.0"
dblFlowVal = hyStdFlowVar.GetValue("m3/h")
MsgBox dblFlowVal & " m3/h"
End Sub
KeyWords
OLE Automation, phase, standard conditions, Current units, backdoor |
Problem Statement: How does PIMS use API and SPG values? What is the relation between the two of them? | Solution: If API is provided, but not SPG, SPG will be calculated from API. If SPG is provided,
but not API, API is not available for that stream in the matrix. If both API and SPG
are provided (and not correctly related), then PIMS uses SPG for calculations and
keeps the API value as an independent property.
Keywords: API
SPG
Properties
Property
References: None |
Problem Statement: Under specific circumstances, when inserting a Tag in the Legend Area of an Aspen Process Explorer plot, users might encounter the following message:
Note: This message is for informational purposes only. Upon clicking the Close button, Aspen Process Explorer will continue to work. In other words, it does not affect functionality. | Solution: Starting in version 2006.5, Aspen Process Explorer performs two different run-time license check routines:
1. It verifies and checks out an Aspen Process Explorer license.
2. When connecting to a specific InfoPlus.21 (version 2006.5 and above) to retrieve tag data, it verifies whether or not the InfoPlus.21 Server is running in licensed mode.
The message described in this Knowledge Base article occurs during the second routine, and it means that the Aspen Infoplus.21 Server is running unlicensed mode. To examine and troubleshoot issues related to Aspen InfoPlus.21 licensing, please refer to KB 123811:
http://support.aspentech.com/webteamcgi/SolutionDisplay_view.cgi?key=123811
Keywords: Unable to acquire InfoPlus21 License
Process Explorer License
References: None |
Problem Statement: Aspen InfoPlus.21 can expose some of his records as OPC DA items to be read by any OPC DA client like Matrikon OPC Explorer or OPC Expert. In the case of custom records definitions, to expose his values trough the IP.21 OPC DA server they need to have timestamp and quality status fields properly associated. This solution provides examples on how to properly create custom records definition which values is exposed by IP.21 OPC DA server. | Solution: Start by creating a new definition with a Value, Quality and Timestamp fields on the normal area of the records as follow:
In this case cst_value hold a Real single precision value formatted by a format record, cst_time is a normal time stamp value also formatted by a format record and cst_quiality is a signed 16-bit integer with format provided by quality-states selector.
To make the this record to be read as valid OPC record you need to specify a time stamp field and a quality field. For the time stamp field use Special / Timestamp field / Add/Modify option:
For the quiality status use the Special / Quality status option:
Verify that a quality status field and Timestamp field appears on the properties for the value field:
Try creating a tag for this definition and read it using any OPC DA client:
Keywords: Custom definition records, OPC DA, IP21 OPC DA
References: None |
Problem Statement: AspenWatch Maker configures the AspenWatch database to collect and historize data from almost all of the known variables (entries) that will be in a .ccf. What about the "user defined entries" | Solution: User defined entries can be historized into Miscellaneous tags. If there are user defined entries in the .ccf, there is a file that is created by AspenWatch Maker when a controller is loaded, called "UserEntryTags.txt", and placed in the ...\AspenWatch\app\<controllername> directory, which contains the user defined entries in a format suitable to be imported into Miscellaneous tags.
The information (comments) at the top of this file is as follows:
# The following tags are the user defined entries in CCF:
# C:\Program Files\AspenTech\Aspen Watch\App\C2RX\c2rx.ccf
# Import this file in Maker to create Miscellaneous Tags for each
# user defined entry in the CCF. Be aware that Maker does not
# clean up these tags if they are changed or removed from the CCF.
Note that the names used are "best guess" based on the names of the entries in the .ccf. It is possible you may want to edit them, and change them if you want more informative names. Just keep in mind the need for all tag names to be unique in the IP.21/AspenWatch database. As indicated, once you put them in, Aspen Watch forgets about them, and you will have to perform any "bookkeeping" tasks that end up being required.
Keywords: watch, tags, misc, excel, import
References: None |
Problem Statement: Collection tasks in AspenWatch Maker are not collecting | Solution: The most common reason for the AspenWatch collection tasks not collecting, is because the DMCplus Context server is not running on the DMCplus Online machine.
To correct:
Go to the Aspen DMCplus Online machine and check for a process cimio_dmcp_dlgp in the process window of the task manager.
If the process is running, stop it. This can be done by either stopping the process in the process window of the task manager or by going to the Services Panel and stopping it. You would then want to check the task manager to confirm that it is no longer visible in the task list.
Go to the Services panel in control panel.
Start the DMCplus Context Server Service.
Check the process window of the task manager and confirm that the DMCplus Context Server has started by confirming the process cimio_dmcp_dlgp is present. If this is the same process window that was opened to see if the process was running, you may need to refresh to see the new process.
If the process is running, return to the AspenWatch machine and check the collection tasks, they should now be collecting.
KeyWords
collections, aspenwatch, task
Keywords: None
References: None |
Problem Statement: Aspen Watch Maker is unable to start the collection from a controller with a Run Status of “Not Licensed”. On a further inspection the time from the last scan (Watch) does not correspond to the time showed on the server: | Solution: Aspen Watch Maker is linked to the current time from the IP.21 Database. To confirm if this time is the same as the one showed on the server open IP.21 Administrator and then right click on the server name. Hit properties and then go to the “Time Parameters” tab.
Then confirm if you have the correct UTC Time zone in the time options from Windows. Options like Amerca/Chicago or America/Los Angeles will show the above behavior.
Keywords: Time Zone
IP.21
AW Maker
References: None |
Problem Statement: 在Aspen InfoPlus.21 Definition Editor中把自定义纪录（custom definition record）转换成可应用（usable）的时候,出现如下错误。 | Solution: 此问题是因为删除字段（field）的时候没有把 references 先删除。它通常出现在历史重复区（history repeat area）被修改了的时候。此问题可以通过如下步骤来重现：
1. 在 Aspen InfoPlus.21 Definition Editor 中复制 （duplicate） IP_AnalogDef。
2. Duplicate Definition Record 中输入名称。
3. 分别右击历史重复区 IP_#_OF_TREND_VALUES 中的 IP_TREND_TIME, IP_TREND_QLEVEL, IP_TREND_QSTATUS 和 IP_TREND_VALUE 字段，并从右键菜单中选择删除 (Delete)。
4. 右击 IP_#_OF_TREND_VALUES 并从右键菜单中选择删除 (Delete)。
5. 点击 Record | Save 来保存自定义纪录。
6. 选择 Definition Records | Make Usable 来把自定义纪录转换成可应用。
这种情况下，为了解决此问题，需要重新用rld文件重载 (reload) 此自定义纪录，或者复制现有的可用纪录。
1. 重新用rld文件重载此自定义纪录，或者复制现有的可用纪录。
2. 右击历史重复区字段 (例如：IP_#_OF_TREND_VALUES)。
3. 从右键菜单中选择修改 (Modify)。
4. 在 Details 部分选择 Normal。
5. 单击"确定"按钮。
6. 在 IP_#_OF_TREND_VALUES 的重复区中分别右击各自字段后，从右键菜单中选择删除。
7. 删除重复区 (repeat area) (例如： IP_#_OF_TREND_VALUES)。
8. 选择 Record | Save 来保存修改的自定义纪录。
9. 选择 Definition Records | Make Usable 来把自定义纪录转换成可应用。
如果不能删除重复区的所有字段，可以通过如下方法来解决。
1. 重新用rld文件重载此自定义纪录，或者复制现有的可用纪录。
2. 展开历史重复区的字段 (例如： IP_#_OF_TREND_VALUES)。
3. 右击要删除的字段 (例如： IP_TREND_VALUE)。
4. 从右键中选择 Special | History Source。
5. 在 History 的下拉列表中选择 <None>。
6. 单击"确定"按钮。
7. 右击字段 (例如： IP_TREND_VALUE)。
8. 从右键菜单中选择删除。
9. 选择 Record | Save 保存修改的自定义纪录。
10. 选择 Definition Records | Make Usable 来把自定义纪录转换成可应用。
Keywords: Definition Editor
<Defintion_name> is referenced by <Defintion_name>and can not be made unusable.
CN-
References: None |
Problem Statement: Historian log files generated by archive tools like h21summary.exe or h21arcck.exe contain PointIDs or TagIDs mentioned as references to history events. What is a history point ID, and how do you translate it to an Aspen InfoPlus.21 record ID? | Solution: A history Point ID embeds both the Aspen InfoPlus.21 record ID of the tag and the field pointer of the history repeat area count field and can be calculated with the following formula:
PointID = ( 1024 * IP21RecID) + Field_Pointer of the Repeat-area count field
Where:
? Every record in the Aspen InfoPlus.21 database has a unique Record ID (IP21RecID) and
? The calculation of Field Pointer is illustrated in the following example:
Records defined by IP_AnalogDef have a history repeat area count field named IP_#_OF_TREND_VALUES.
The record IP_#_OF_TREND_VALUES defined by FieldLongNameDef has a data field named FIELD_NUMBER(hex) with a value of 241B as shown below:
The Field_Pointer is derived from the 10 least significant bits of the FIELD_NUMBER (0000011011). So the field pointer is 27 (decimal) for IP_#_OF_TREND_VALUES.
Suppose a record defined by IP_AnalogDef has a record ID of 1829. History events generated for this tag will have a history PointID of 1872923 or (1024 * 1829 + 27).
To convert a history point ID to a record ID, divide the point ID by 1024 and ignore the remainder.
For example, the history point ID 1872923 corresponds to record ID 1829 because 1872923/1024 = 1829 using integer arithmetic.
Keywords: Archive, History, Fileset, Repository, History point ID, Record ID
References: None |
Problem Statement: 有些时候，可能会想运用脚本语言来联系 Aspen InfoPlus.21 Database API 因为不需如 C 语言需要编译。这解决方案目的在于举例如何应用 Python 和 Aspen InfoPlus.21 Database API 做连接。 | Solution: 以下有几点要注意。
1. 必须要晓得 Python 语言。
2. 附加的脚本需应用于 Python 2.6.6，因为已对这个版本测试过了。
3. 由于Python 3.x 上的变化， 脚本可能无法正常运作。
所提供的 Python 附加脚本只是提供为参考，AspenTech Support 并不支持。
Keywords: Python
API
CN-
References: None |
Problem Statement: Why does Aspen Production Control Web Server (PWCS) block the installation of the plotting components AtWebControls.cab?
The PCWS History Plot shows a??Windows has blocked the installation because it cannot verify the AtWebControls.cab publishera?? | Solution: The following message appears: a??Windows has blocked the installation because it cannot verify the AtWebControls.cab publishera?? when the PCWS History Plot is selected.
NOTE: It applies to V7.3 with AtWebControls.cab dated 3/3/2011
Solution 134591 (Aspen InfoPlus.21 Process Browser ECR20120619 (v7.3.0.3)) addresses the same issue a??Windows has blocked the installation because it cannot verify the AtWebControls.cab publishera?? Ita??s for IP21 Process Browser but the two failing files are the same used by PCWS AtWebAddinControls.cab and AtWebControls.cab
Ita??s suggested to rename the current AtWebAddinControls.cab and AtWebControls.cab files as AtWebAddinControlsOLD.cab and AtWebControlsOLD.cab, before applying the patch.
The instructions are almost the same.
Installation
1. Stop IIS on the IP.21 Process Browser PCWS server and stop InfoPlus.21 on the InfoPlus.21 server.
2. Unzip WB120619A.zip to a temporary location
3. Copy AtWebAddinControls.cab and AtWebControls.cab files to AspenCUI folder (for example, C:\Inetpub\wwwroot\AspenTech\AspenCUI), replacing the existing one.
4. Start IIS and InfoPlus.21.
Note: In Windows 2008 verify that both files are not blocked (Unblock button).
Post Installation
It may be necessary to clear your PCWS client's cache in order for the changes to be applied there.
To clear the cache in Internet Explorer 8 and Internet Explorer 9:
1. In your web browser, click Tools > Internet Options.
2. Under Browsing History, click Delete...
3. Under Temporary Internet Files, click Delete files... and click Yes.
4. Under Cookies, click Delete files... and click Yes.
Verification
To verify installation of the patch, check the modified date of the AspenCUI/ AtWebControls.cab file. This should be 4/20/2012.
After the patch is applied, the Publisher changed from a??Unknowna?? to a??Aspen Technologya??
Ita??s suggested to review the following solution 134267 "How do I manually download and register when permissions prevent download of plotting components?" if the plotting is still not working.
Keywords: PCWS, History Plot, AtWebControls.cab, Verify Publisher
References: None |
Problem Statement: If you want to remove a significant number of tags from a transfer record, it can be time-consuming to accomplish this using the InfoPlus.21 Administrator. | Solution: Using SQLplus, you can purge the tags from the transfer record and repopulate it with only the desired tags.
ALWAYS REMEMBER BEFORE RUNNING ANY SQLPLUS SCRIPTS THAT MODIFIES YOUR INFOPLUS.21 DATABASE TO FIRST BACK UP A COPY OF YOUR DATABASE USING THE SAVE SNAPSHOT FEATURE.
The script below contains this safety feature in code. However, before you run the script for the first time, please back up the snapshot manually just in case the script runs into any problems executing the automated snapshot backup code contained in the first few lines.
Here is an example script:
-- This program will clean up the list of tags which you want to delete from an iogetdef record
-- Requirement: Specify a cleanup file which is a text file containing a list of tag to be
-- deleted from a ioget record.
LOCAL snapshot_SavePath CHARACTER(255);
MACRO GetRecName = 'AspenChem_Get'; -- name of IOget/IOGetHistDef record
MACRO filterList = 'd:\list.txt'; -- text file containing a list of unwanted IO Tags
snapshot_SavePath = 'd:\infoplus21_bkup'; -- name of your snapshot file you want to save (DO NOT include .snp
snapshot_SavePath = snapshot_SavePath || CAST(current_timestamp AS CHAR FORMAT 'DDMMYY') || '.snp'
-- Save snapshot before performing cleanup
SYSTEM '""%SETCIMCODE%\dbsave"" ' || snapshot_SavePath;
-- Turn off the IOget Record
UPDATE "&GetRecName" SET IO_RECORD_PROCESSING = 'off';
-- Clear the iotagname for unwanted tags
FOR (SELECT LINE AS recName FROM '&filterList') DO
END
UPDATE "&GetRecName"
SET IO_TAGNAME = ' ' WHERE IO_TAGNAME = recName;
WRITE
'Unwanted list =' || (select count(line) from 'd:\list.txt');
-- Output filtered occurrences to file
SET OUTPUT 'd:\ioget.txt';
SET COLUMN_HEADERS 0;
SELECT
IO_TAGNAME , ',' ,
IO_DATA_PROCESSING , ',' ,
IO_DATA_TYPE , ',' ,
"IO_VALUE_RECORD&&FLD" , ',' ,
IO_DATA_CONVERSION , ',' ,
IO_DATA_DEADBAND , ',' ,
IO_DATA_STATUS , ',' ,
IO_DATA_STATUS_DESC , ',' ,
IO_MAX_COUNTS , ',' ,
IO_MIN_COUNTS , ',' ,
IO_RANGE_HI , ',' ,
IO_RANGE_LO , ',' ,
IO_DEADBAND_TYPE , ',' ,
IO_DEADBAND_VALUE
FROM "&GetRecName".1 WHERE CHARACTER_LENGTH(TRIM(IO_TagName)) > 0;
SET COLUMN_HEADERS 1;
SET OUTPUT DEFAULT;
WRITE 'Filtered IOGET =' || (select count(line) from 'd:\ioget.txt');
-- Remove all occurrences
UPDATE "&GetRecName"
SET "IO_#TAGS" = 0;
-- Import filtered occurrence from file
SET EXPAND_REPEAT = 1;
INSERT INTO "&GetRecName"
(IO_TAGNAME,
IO_DATA_PROCESSING,
IO_DATA_TYPE,
"IO_VALUE_RECORD&&FLD",
IO_DATA_CONVERSION,
IO_DATA_DEADBAND,
IO_DATA_STATUS,
IO_DATA_STATUS_DESC)
SELECT
SUBSTRING(1 OF LINE BETWEEN ','),
SUBSTRING(2 OF LINE BETWEEN ','),
SUBSTRING(3 OF LINE BETWEEN ','),
SUBSTRING(4 OF LINE BETWEEN ','),
SUBSTRING(5 OF LINE BETWEEN ','),
SUBSTRING(6 OF LINE BETWEEN ','),
SUBSTRING(7 OF LINE BETWEEN ','),
SUBSTRING(8 OF LINE BETWEEN ',')
FROM 'd:\ioget.txt';
UPDATE "&GetRecName"
SET IO_RECORD_PROCESSING = 'ON';
UPDATE "&GetRecName"
SET "IO_ACTIVATE?" = 'YES';
KeyWords:
cimio Get
IoGetDef
Ioget
iogethist
sqlplus
occurrence
Keywords: None
References: None |
Problem Statement: It is possible to import the contents of IoGetDef and IoPutDef Records into Microsoft Excel without the use of Aspen SQLplus Scripts. This solution steps you through how to bring these records into Microsoft Excel using an ODBC connection. | Solution: The steps to accomplishing is subdivided into three component parts. On a Windows platform, follow the steps below to call Microsoft ODBC.
Part One
? Start ----.> Settings --------> Control Panel
? Double click on Administrative Tools
? Double click on Data Sources (ODBC)
? Choose System DSN (Second Pull down Tab)
? Choose Add... (Another Screen Appears.)
? .Select AspenTech SQL Plus
? Select Finish
A new screen appears: SQLplus ODBC Setup
? In the ODBC Data Source Name Field, type in anything such as for example, MYIPDATA1
? For Description Field, type anything or leave BLANK
? For Data Source Field, pull down on arrow and find your Database
? Choose OK and exit Control Panel
Part Two
BRINGING YOUR DATA INTO Microsoft Query Database
? Open Microsoft Office Excel.
? Pull down on the "Tools" menu and select "Add-Ins".
? Check the box Aspen "Process Data Add-In" and click OK
? Pull down on "Data" menu and choose "Import External Data".
? Choose "New Database Query..."
? Under Databases, find the ODBC Name you created : MYIPDATA1
? Click OK, and the Add Tables box comes up. (You are still in MS Query data base)
? Scroll down to IoGetDef_1, choose this by highlighting it and clicking on "Add". Close this box and you will see the IoGetDef_1 table populated at the top left hand corner of the Query spread sheet.
? Your screen is split into upper and lower screen. Maximize the upper screen and drag the IoGetDef_1 window at the bottom and right hand edges to make it slightly large so that you can see the contents.
? Select the following fields one at a time and watch them populate in the lower window: Name, IO_TAGNAME, IO_DATA_PROCESSING, IO_DATA_TYPE. Stop at this point even though you have not selected your last field which is IO_VALUE_RECORD&FLD.
? Scroll down to IO_VALUE_RECORD&FLD and highlight it. (Do not double click)
? Click on the SQL button under the Format drop down menu and an SQL statement box opens up.
? After the word NAME, insert "OCCNUM", and after IO_DATA_TYPE, insert
"IO_VALUE_RECORD&&FLD" Note: the two inserted words must be in double quotes. Also note the extra amper-sign shown, this is very important. Execute by choosing OK.
This inserts all your fields. Maximize your lower window.
Part Three:
Remember, you are still in the Query database. Now, go to the Pull down on the FILE menu and select ... "Return (Import) Data to Microsoft Office Excel". This will bring your data from Microsoft Query into Microsoft Office Excel.
FINISHED.
Now, save your data in Microsoft Office Excel.
Keywords: None
References: None |
Problem Statement: PIMS can report PI values in the Full solution, Process Submodel Summary for feed and yield streams.
The PI value for the stream is also called "Incremental value" which represents optimal price of the stream.
How to configure the table to report the PI value? | Solution: Add optional column "PI" in table SUBMODS and enter non-zero value (e.g. 1) to report PI value for the submodels.
Please refer to the following example.
Full Solution Report:
Keywords: SUBMODS
Full
References: None |
Problem Statement: After a fresh installation, Aspen APC Web data provider and AFW Client Security services crashed when accessing PCWS. The error shows on the browser included the comwebserver.connect() phrase. | Solution: The installation was not successful. When task manager is pulled up on the server, it is showing an MsInstall.exe running and the Event Viewer is showing Msinstall failure under the System Event.
At that time, the Aspen APC Web Server package needed to to uninstall using AspenOne Uninstaller. Reboot after the uninstall and then re-install the package using the Aspen media.
Keywords: comwebserver.connect(); PCWS
References: None |
Problem Statement: Creating and Using Custom Reports | Solution: The attached presentation covers the following topics in the creation and use of custom reports in the Economic Evaluation products:
· General reporting overview
· Custom user attributes
· Creating customer reports
· Step-by-Step Report Creation for Excel Reports
· Version Upgrades
Keywords: custom reports, custom, reports, excel
References: None |
Problem Statement: There may be a situation in which you want to use a scripting language instead of C language to call on the Aspen InfoPlus.21 Database API as it does not involve compilation. This solution aims to provide an example of how Python can be used to interface with Aspen InfoPlus.21 Database API. | Solution: There are a few points to note.
1. Knowledge of Python language is a MUST.
2. Usage of Python 2.6.6 as the attached script has been tested against this version of Python.
3. Python 3.x may or may not work with the script due to the inherent change make in 3.x.
The attached Python script is provided AS IS to provide a sample and will not be supported by AspenTech Support.
Keywords: Python
API
References: None |
Problem Statement: Assume that you specified a value of 15.9999 in cell A1 of the spreadsheet in the attached HYSYS file. Instead of displaying the exact value you specified, HYSYS shows a value of 16.00. How can you get the value of 15.9999 displayed? | Solution: What you need to do is to modify the default format setting in the HYSYS Preference file. Here are the steps to follow:
1. From the HYSYS top menu bar, select "Tools" and then "Preferences..."
2. Go to the "Formats" page on the "Variables" tab page.
3. Scroll down the list to find the variable called "CellValue". Its default format is "4 significant figures".
4. Highlight the format cell beside the "CellValue" variable and press the "Format" button on the right-hand side.
5. Replace the default setting of 4 significant figures to 6 or a larger number and press OK to close the view.
6. If you want to keep such setting, you can save this change to your HYSYS Preference file. Simply press the button "Save Preference Set..." at the left-bottom corner of the Preference view and confirm your decision to save it.
Keywords: Preference file, format, unitless, CellValue, display, spreadsheet
References: None |
Problem Statement: Steady state calculation of the effect of heating / cooling a closed system.
A typical application of this would be to calculate the final conditions after heating a vessel or shut in section of pipe work. | Solution: In steady state operation HYSYS can only model flowing systems; so instead of modelling a fixed volume it is necessary to create a flowing system and ensure that the volume flow stays fixed. A good way to do this is to use a heater / cooler and have an Adjust operation to vary the outlet conditions until there is no change in density and hence volume flow.
For example, in the attached case the aim is to calculate the final pressure when heating a closed volume of Nitrogen from a known starting temperature and pressure to a given final temperature.
To work out the energy required to do the heating of a particular volume it is necessary to set the flow rate appropriately. For a volume of X m3, set the flow rate such that the stream has an Actual volume flow of X m3/h (this can also be done using an Adjust) and then read the energy required from the heater as Y J/h.
A similar approach can obviously be used to calculate the final temperature and pressure when a known amount of energy is applied to a closed system. To do this set the energy flow into the heater as above, leave the outlet temperature to be calculated and use an Adjust to vary the pressure so that the density remains constant.
KeyWords
Heating, Cooling, Fixed, Closed, Volume
Keywords: None
References: None |
Problem Statement: In an Aspen HYSYS or Aspen Plus simulation with Activated Economics results, how can I create a case study by varying an inlet variable and reviewing the impact on Activated Economics reports? | Solution: The Case Study tool cannot be used to perform this calculation. The workaround is to send the variables to the Aspen Simulation Workbook add-in for Excel.
· Be sure that the simulation is running and Activated Economics is generating results with no warnings or errors (the steps below are for Aspen HYSYS, but they are the same for Aspen Plus)
· Open Economic Equipment Data Summary.
· Click on Send to Excel/ASW button
· Select the tables you want to import, table locations, and click on Export tables to Excel
· Open the file in Excel and be sure that Aspen ASW Tab is available in Excel.
· Copy and paste the values you want to keep under this conditions.
· Vary the conditions in Aspen HYSYS file.
Activated Economics results will be recalculated in Aspen HYSYS and, and the new result is linked to ASW. Copy and paste the values you want to keep under this conditions and compare with the last results.
Keywords: ASW, Case Study.
References: None |
Problem Statement: How to show mass and energy balance around a column stage? | Solution: A user can check mass and energy balances around a column stage using the flowsheet shown in the attached simulation case.
HYSYS column offers a check box for splitting an external feed. If this this box is checked, the vapor potion of the feed goes to the stage above directly. If this box is not checked as default, the feed with be combined with all other incoming streams to the feed stage. Essentially the calculation of a column stage is a PH flash of all incoming streams to determine the vapor and liquid conditions leaving the stage. An energy stream can be considered as an enthalpy input to the PH flash.
The flowsheet accomplish three things:
1. Determine any possible split of external feed if Split is checked
2. Mix all incoming streams, including external material and energy feeds and internal streams coming to the stage under investigation
3. Perform a PH flash at the stage pressure.
The feeds with Split checked go through a flash. The vapor portion goes to stage above, while the liquid portion will mix with other incoming streams to the stage. The feeds with Split unchecked, and energy feeds go to the mixer directly. At the outlet of the mixer, we have compositions and molar enthalpy matching those of the holdup on the stage. These data are transferred to the inlet of the PH flash. We pass the pressure of the stage directly from the column through a spreadsheet. This arrangement will avoid possible pressure value below that of the stage under investigations. This is likely because some external feeds and the liquid from stage above may have lower pressure. As a result, the pressure on the outlet of the mixer will be lower than the actual value.
In the simulation case, we use the sample case R-1available under your HYSYS installation directory, typically Program Files\Aspentech\Aspen HYSYS 2004.2\Samples.
We show balances around stage 28. There are one external material feed with Split unchecked and one external energy feed to the stage 28, along with vapor from stage below (stage 29) and and liquid from stage above (stage 27).
On the PFD, Feed w Split Off is identical to Atm Feed, and Feed w Split On is not used (zero flowrate). Energy to Stage n is identical to Q-Trim. L n-1 is identical to L from 27, and V n+1 is identical to V from 29. A Balance unit is used to transfer compositions, total flowrate and enthalpy to HoldUp On Stage n, and a Spreadsheet unit is used to read the pressure on stage 28 and write to stream HoldUp On Stage n.
Keywords: Mass balance, energy balance, column, stage, tray
References: None |
Problem Statement: What are the equations used in the separator for the calculation of the convection heat transfer coefficients when pressing the "Estimate Coefficients Using Current Conditions" button? | Solution: The correlations used for estimating the heat transfer coefficients (HTCs) in the separator are the same as those used in the Dynamic Depressuring utility by the Detailed heat loss model (these can be viewed in the Dynamic Depressuring utility by selecting the Correlation Constants radio button and clicking on the Correlation Help button).
They are as follows:
Outside heat transfer coefficient for air: h = C-(delta_Temperature / length)^m
All other correlations: Nu = C-(Gr-Pr)^m
where Nu = Nusselt number, Gr = Grashof number, Pr = Prandtl number
The coefficients C and m are calculated based on Tables 7.1 and 7.2 in JP Holman's "Heat Transfer" textbook (McGraw-Hill, Inc.).
Additional information regarding the Heat Loss model in HYSYS can be found in sections 1.3.4 and 1.6.1 of the HYSYS Dynamic Modeling guide.
KeyWords
Heat transfer coefficient, heat loss model, correlations
Keywords: None
References: None |
Problem Statement: Which property package should I use for modeling a liquid sulfur system? | Solution: There are three compounds in HYSYS database representing liquid sulfur. They are S_Liq_150, S_Liq_190 and S_Liq_280. This is mainly due to the abnormal behavior of the viscosity of liquid. It is not possible to reproduce such behaviour using a generalized correlation. Therefore, HYSYS uses three components to represent the liquid sulfur in different temperature ranges. You should pay attention to the following temperature ranges in your simulation: using S_Liq_150 < for temperature < 170 degree C; S_Liq_190 for the range of T= 170 to 190 degree C; and S_Liq_280 for T > 190 degree C.
While choosing the property package suitable for a liquid sulfur system, you are encouraged to gather data from open literature and take advantage of the HYSYS Tabular feature, because it is not realistic to expect a generalized thermodynamic model to be able to accurately present the thermodynamic and physical behavior of liquid sulfur.
Presented in the attached Excel file are some validation results where literature data were used to validate the results generated in HYSYS. This is also meant o illustrate what HYSYS Tabular can achieve. The reference data used in this document were taken from "The Sulphur Data Book". What the Tabular did was to generate the Viscosity-T, Density-T and Cp-T relationships using the provided data to overwrite the corresponding values for these properties calculated by the defined HYSYS property package. As you can see, the Tabular results match the experimental data almost perfectly for most of the properties calculated, while the traditional PR model didn't perform even close to such accuracy. Please refer to the attached files for details.
Keywords: liquid sulfur, liquid sulphur, property package, thermodynamic properties, transport properties, viscosity, density, Cp, heat capacity
References: None |
Problem Statement: Which Property Package should I use for Sour Water systems? | Solution: The PR Sour or SRK Sour models are specialized in representing sour water systems. They use Wilson's model to account for the ionization of H2S, CO2, and NH3 in the aqueous phase and therefore provide a better prediction of the solubility of these components in the water phase. They may be applied to sour water strippers, hydrotreater loops, crude columns, or any process containing hydrocarbons, acid gases and H2O. If no water phase exists the Sour model will be reduced to the ordinary PR or SRK model.
You can find more information on selecting the appropriate Property Package for a HYSYS simulation in Solution 109012 or in Appendix A of the Simulation Basis Manual (see Technical Library, Documentation).
KeyWords
sour, water, gas, H2S, CO2, NH3, ammonia, carbon dioxide, property package, method, EOS, select, selection, model.
Keywords: None
References: None |
Problem Statement: In this application example, users will learn how to:
· Solve a common sulfur recovery problem using HYSYS: Use simulation tools built into HYSYS to create value in the plant
· Leverage the power of Aspen HYSYS integrated simulation models: Optimize operations across the acid gas treating and sulfur recovery processes
· Use the new Case Study Utility features for smart decision making: Reduce product quality giveaway and save on solvent costs
· Configure & use a new data model in the HYSYS Optimizer: Maximize sulfur recovery efficiency given operating variables & constraints
In the base case simulation in this example, measured sales gas H2S composition and HHV are well within product specification. Opportunity may exist to reduce product quality giveaway and save on OPEX costs. We suspect current SRU operations are not optimized for maximum sulfur recovery. SRU operations may need to be re-optimized after changes to amine unit operations. The user will need to evaluate furnace inlet air flow rates and re-heater temperatures.
The questions the user will try to answer using HYSYS are:
· Can we use the HYSYS Case Study Utility to determine the limiting sales gas specification?
· Can we reduce sales gas quality giveaway to reduce solvent costs?
· Can we use the HYSYS Optimizer to determine the ideal furnace air rate and re-heater temperatures for this operation? | Solution: The Aspen HYSYS Optimizer is a multi-variable steady state optimization tool that finds optimal operating conditions given specified variables, constraints, and objective functions. The HYSYS Optimizer provides many data models, including the new DMO, LSSQP, and BOBYQA options in V9. DMO and LSSQP use successive quadratic programming (SQP), which are fitting to solve large-scale optimization problems.
Acid Gas Cleaning in Aspen HYSYS is a rate-based solution that accounts for both mass-transfer and kinetic effects in the absorber and regenerator columns. Acid Gas Cleaning property packages support a range of amines and amine blends, heavy hydrocarbons, mercaptans, acid gas components, and other key components. Reaction chemistries are automatically generated and “Efficiency” and “Advanced Modeling” modes are supported for increased accuracy or performance.
Sulsim Sulfur Recovery in Aspen HYSYS is the industry’s most accurate tool for modeling the modified-Claus process for sulfur removal. Sulsim Sulfur Recovery utilizes empirical models validated over hundreds of commercial configurations to accurately predict thermal, catalytic and tail gas stages using 33 unit operations, specific sulfur properties, and validated conversion models.
At the end of this example, the user will discover they can decrease solvent rate by 11 USGPM to the minimum HHV sales gas spec, saving on OPEX through reducing product quality giveaway. The user will also use the LSSQP data model in the HYSYS Optimizer to increase the SRU recovery efficiency by 6.7%.
Keywords: HYSYS, Acid Gas Cleaning, Column Hydraulics, Column Analysis, rate-based modeling, absorber, regenerator, amines, amine blend, MDEA, efficiency mode, advanced modeling mode, heat stable salts, amine treating, acid gas treating, gas plant, gas processing, tail gas treating, hydraulics, flooding, weeping, base case, max rating, turndown, example, air demand, incinerator, flare, modified-Claus, Claus, SRU
References: None |
Problem Statement: The Aspen Plus Getting Started Using Equation Oriented Modeling Manual states the following:
"Aspen Plus is not able to solve all SM problems with the EO approach. Certain features that have been implemented for SM have not been implemented in EO. Refer to Features Not Supported in Equation-Oriented Models in online help for a detailed list of which SM features are not supported by EO."
Which are the features not supported by EO and where can this information be found? | Solution: Certain blocks do not have equation-oriented formulations. However, the capabilities are still available for the EO Solution Method via the Perturbation Layer, except for RBatch, which is not available because it is a dynamic model which will not work with the steady-state EO formulation in Aspen Plus.
Some other blocks with EO formulations do not support certain model features in their EO formulations. These vary by block and are listed separately for each block.
The features listed below are not supported in EO, even via the Perturbation Layer.
A? Conventional solid substreams with particle size distribution (CIPSD)
A? Non-conventional solid substreams (NC and NCPSD)
A? Polymers (polymer, segment, and oligomer components; polymer-related component attributes; and reaction sets other than power law, LHHW, and general)
A? Mass-balance-only simulations
A? Solids-handling unit operation models, besides ClChng
A? Polymers
A? Balance Blocks
A? Data-Fit
A? Optimization (use EO Optimization run mode instead)
A? Constraint (specify variable bounds instead)
A? Water solubility option (this applies to all calculations of the fugacity of water in sequential-modular calculations, even if free-water is not specified, but only applies to the free-water phase in equation-oriented calculations)
This information is part of the Aspen Plus Help Contents and can be found under Aspen Plus
Keywords: EO, Equation-Oriented Modeling, Features not supported
References: | Equation Oriented Modeling Reference Manual | Unit Operation Model in EO | Features Not Supported in Equation-Oriented Models. |
Problem Statement: The incompatible error message occurred when exporting a file from Aspen Custom Modeler to Aspen Plus because the Microsoft Visual Studio 2013 is not supported. The error message is
"A compatible version of Visual Studio 2008 was not detected on the system. This update is designed for only the Microsoft Visual Studio 2008 (ENU) product family, and is not compatible with any Express editions." | Solution: A new compiler.cfg is needed to support Microsoft Visual Studio 2013 as a compatible version. The new compiler.cfg that supports MS Visual Studio 2013 can be download from KB 131011.
Keywords: Microsoft Visual Studio 2013, Compiler.cfg, Aspen Plus, and Compatibility
References: None |
Problem Statement: How do I display a physical property such as viscosity on the Stream Summary? | Solution: Any prop-set property can be added to a stream report. Follow the instructions below to display stream viscosity in the stream report. You can also use this procedure to display other physical properties in the stream report.
1. Create a new property set.
2. Use the search button and type the name of physical property you want to display such as viscosity. You can also add multiple physical properties by clicking on Add button. Click Ok if the final selection of properties has been made. You can also specify the unit of the property.
3. Go to the Qualifier tab and specify the phase such as liquid. You can also specify multiple phases as well as limit the subset of component.
4. Now go to the simulation tab and then, go to Setup | Report Options | Stream | Property Sets. Here using the arrow, we can select the properties out of the available properties we want to display.
Keywords: Physical property, viscosity
References: None |
Problem Statement: How to fix graphics format lost when copying / importing a simulation into a hierarchy. | Solution: Please follow the steps below as a work around to fix this problem:
1. Open your file and add a Hierarchy in the main flowsheet.
2. In the main flowsheet right-click on the hierarchy you have just added and select “Import�.
           Import one bkp file from Aspentech examples knowledge base, Cogeneration.bkp for instance.
3. In the window “Import Options� just press “Continue�.
4. After imported the file, delete from your flowsheet the Hierarchy you have just created.
Now add a new Hierarchy to your main flowsheet and from now on you should be able to copy simulations into the Hierarchy without losing the graphics.
Keywords: Hierarchy, Graphics Format, Copy, Import
References: None |
Problem Statement: I have a HeatX block inside my Aspen Plus simulation. Why is the the option "Detailed" in the Model fidelity section of Setup | Specifications sheet greyed out? | Solution: Starting from version 8.8, the Detailed option is no longer available. The Detailed radio button still appears in the User Interface for compatibility with older files. If you open a file created in an earlier version of Aspen Plus in version 8.8, the option can still be used. However, files created in this version will have this option greyed out.
To consider geometry in the heat exchanger calculations, you can use the Rigorous method, which will use the Aspen Exchanger Design & Rating family of products to rigorously model the heat exchanger.
Keywords: geometry, heat exchanger, EDR
References: None |
Problem Statement: How is the NPSH calculated? | Solution: The Net Positive Suction Head (NPSH) available for a pump is defined as:
NPSHA = Pin - Pvapor + Hv + Hs
Where:
NPSHA = Net Positive Suction Head Available
Pin = Inlet pressure
Pvapor = Vapor pressure of the liquid at inlet conditions
Hv = Velocity head
(= u^2/2g where u is the velocity and g is gravitation constant)
Hs = Hydraulic static head corrected to the pump centerline
The NPSH available has to be greater than the NPSH required (NPSHR) to avoid cavitation. NPSH required is a function of pump design. The Net Positive Suction Head (NPSH) required can be considered the suction pressure required by the pump for safe, reliable operation. The NPSHR can be specified using the performance curves on the PerformanceCurves NPSHR sheet, or calculated from the following empirical equation by specifying suction specific speed (Nss) on the Setup CalculationOptions sheet.
NPSHR = ( N Q^0.5 / Nss )^4/3
Where:
NPSHR = Net Positive Suction Head Required
N = Pump shaft speed (rpm)
Q = Volumetric flow rate at the suction conditions
Nss = Suction specific speed
The units for Q and NPSHR are:
US: Q in gal/min and NPSHR in feet
Metric: Q in cum/hr and NPSHR in meters
KeyWords
Hydraulic Static head
Keywords: None
References: None |
Problem Statement: In addition to Aspen Production record Manager 32-bit ODBC Driver, described in Aspen KB articles 129704 and 129611, there now exists Aspen Production Record Manager 64-bit ODBC Driver.
In order to install this driver you must choose the 64-bit install, as shown below.
Once installed, the APRM 64-bit ODBC driver can be used with 64-bit applications, such as MS SharePoint 2010 and PowerPivot for the 64-bit version of MS Excel. We do not support Aspen APRM Add-in V8.0 with 64-bit Excel.
This Knowledge Base article answers the following question:
What is the token usage of the Aspen Production record Manager 64-bit ODBC Driver? | Solution: When the Aspen Production Record Manager 64-bit ODBC Driver is used by an application like PowerPivot, it will consume 5 tokens for 24 hours. There is no impact to customers that currently use the Aspen Production Record Manager 32-bit ODBC driver.
Keywords: licensing, 64bit, 64 bit
Excel Addin doesn't work in Sharepoint 2010: Invalid URI The hostname could not be parsed
References: None |
Problem Statement: Error "Unexpected result in SelectServerForDA_DA" occurs while trending a tag in Aspen Process Explorer. | Solution: This problem could be caused by an issue during the installation process. SelectServerForDA_DA refers to a function within IP21DAManager.dll. If this library was not registered during installation process Aspen Process Explorer can also show "IP.21 is not accessible from 'NodeName' or is not currently running on 'NodeName'".
To resolve this problem it is necessary to re-register this library as follow:
1. Open a DOS command window and go to C:\Program Files (x86)\AspenTech\ProcessData
2. Un-register the library using the following command: regsvr32 /u IP21DAManager.dll
3. Re-register it using the command: regsvr32 IP21DAManager.dll
If the register has been successful you should see next message:
The machine need to be rebooted to commit the change. Aspen Process Explorer should work as expected after reboot.
Keywords: Process Explorer
IP21DAManager.dll
Unexpected result in SelectServerForDA_DA
SelectServerForDA_DA
References: None |
Problem Statement: This knowledge base article explains what is meant by the error message:
"H/21 Queuing Error" | Solution: When the Aspen InfoPlus.21 historian returns an H/21 Queuing Error this means that the disk where the archive files are stored is full.
Keywords: space
history
file set
arc.dat
References: None |
Problem Statement: When attempting to start Aspen InfoPlus.21, the user may encounter the following error: "Users access permission does not allow the operation". | Solution: This problem may be caused by logging into the Aspen InfoPlus.21 server with a non-Administrator account, an error during the installation, or by a number of other reasons. As such, there are different ways to solve this problem. Just follow the checklist below:
First, make sure that the login account is a member of the Administrator group. If not, go to Computer Management and add the account to the Administrator group. Next, check if restarting the Aspen InfoPlus.21 Task Service resolves the problem (see Solution 106204).
Also, check the DCOM configuration (Start | Run | dcomcnfg.exe) and under the Default Security tab, ensure that the Administrator account or group is added to the Default Access Permissions list and the Default Launch Permissions list. See Solution 104243. In the Default Properties tab, check that the Default Impersonation Level is set to Identify.
Refer to Solution 104284 if this problem occurred after copying the .ipg group configuration (Aspen InfoPlus.21 Manager task configuration) file from another Aspen InfoPlus.21 system.
Next, check the c:\addgroup.log file. There may be the error "failed to add new group" or "failed to create group" (indicating an error during installation). If so, follow the steps below to resolve the problem:
If there's already a group200 you'll have to back everything up first, and then:
1. Remove the folder \Program Files\AspenTech\InfoPlus.21\db21\group200 if it exists.
2. Using Regedit, remove the key: HKEY_LOCAL_MACHINE\Software\AspenTech\InfoPlus.21\<version>\group200
3. Using Regedit, remove the key under HKEY_LOCAL_MACHINE\Software\AspenTech\Security\Registry Security Server.
4. Run the following commands:
cd %SETCIMCODE%
addgroup domain\user password
where domain, user and password are for the account that you want to use to start Aspen InfoPlus.21.
If all of the above methods do not work, as a last resort, you may have to uninstall and reinstall Aspen InfoPlus.21 and Aspen Local Security.
KeyWords:
users access permission
addgroup
Keywords: None
References: None |
Problem Statement: When defining the size of a fileset, and therefore defining when a fileset shift should take place, an administrator decides two parameters - a maximum delta time, and a maximum file size. For example you may input values of 14 days, and 500MB. So the Fileset Shift will occur when the filesize reaches 500MB, or 14 days have elapsed, whichever happens first.
So how does the fileset disk allocation increase, as the fileset size increases, during the 14-day timespan, or to the 500MB limit? | Solution: The good news is that, in the above example, the software will not just automatically allocate 500MB of disk space. There was however a change made with version 4.0 in the way disk allocation for a fileset was and is performed.
Prior to version 4.0, the archiver allocated 256 Kbyte chunks of disk each time it needed more space. For large filesets, this caused disk fragmentation.
With version 4.0 a change was made to the file allocation scheme so that the archiver allocates fewer and bigger chunks of disk space. Now the archiver takes the total size of the archive (500MB in the above example), divides it by 100, and allocates that much disk space (5 Mbytes in this example) at a time.
Therefore with version 4.0 and above, using the example of 500Mbytes, every fileset will be sized at a multiple of 5Mbytes with a maximum unused overhead of 4.99Mbytes, but an average unused overhead of 2.5Mbytes.
KeyWords:
Fileset
Disk
Allocation
Keywords: None
References: None |
Problem Statement: How much disk space do I need for my Aspen InfoPlus.21 historian? | Solution: The amount of disk space needed for history depends on the number of data records, the scan frequency, and the desired data compression. Use the attached Excel spreadsheet to estimate disk space needed for Aspen InfoPlus.21 historical repositories.
KeyWords:
Historian
History
Repository
Size
Keywords: None
References: None |
Problem Statement: Dynamic User Variable - Record the time that an event occured | Solution: The user variable code below is designed to be attached to a spreadsheet. In Dynamics mode whenever the value of the user variable is changed (either by the user, or by an event in the event scheduler) the value in cell B1 is updated to show the Integrator time.
Sub VariableChanged()
On Error Resume Next
ActiveObject.Cell("B1").CellValue=ActiveCase.Solver.Integrator.CurrentTimeValue
End Sub
Attached is an example case that illustrates this (saved in HYSYS 3.1 format). This case is based on the Flow Integrator user variable example case in solution #109857. An Event has been set up in the Event Scheduler to increment the user variable value when the integrated mass flow exceeds 100 kg.
Also attached is an huv file that will allow this user variable to be imported into any other case. (See Solution #109210 for details on how to import the huv file)
Note
The Knowledge Base examples are provided for academic purposes only and as such are not subject to the quality and support procedures of officially released heritage-Hyprotech products. Users are strongly encouraged to check performance and results carefully and, by downloading, agree to assume all risk related to the use of these examples. We invite any feedback through the normal support channel at [email protected].
KeyWords
User Variable, Record Event Time
Keywords: None
References: None |
Problem Statement: Frequently Asked Questions about HYSYS Extensions. | Solution: Please find attached a FAQ document regarding HYSYS Extensions.
KeyWords
HYSYS, Extensions, FAQ, questions
Keywords: None
References: None |
Problem Statement: What is the basis for the HYSIM Inside-Out Column Solver, which is the default algorithm used to solve the Column in Aspen HYSYS? | Solution: The numerical method used for the default Column algorithm in Aspen HYSYS (the HYSIM Inside-Out solver) follows the enclosed paper published by:
Russell, Richard A., A flexible and reliable method solves single-tower and crude-distillation-column problems, Chemical Engineering, October 17 1983, p. 53-59.
The method follows two specific papers developed by Joe Boston:
Boston, J. F., A New Class of Quasi-Newton Solution Methods for Multicomponent, Multistage Separation Processes, Ph. D. Thesis, Tulane University, 1970.
Boston, J. F., and Sullivan, S. L. Jr., A New Class of Solution Methods for Multicomponent, Multistage Separation Processes, Can. J. Chem. Eng., Feb. 1974, p. 52.
The "Modified HYSIM Inside-Out" solver in Aspen HYSYS has been internally modified (with confidential material) by Hyprotech (now owned by AspenTech).
KeyWords
Column, Solver, Algorithm, Solution, Method, Numerical, Iterations,
Keywords: None
References: , Paper, Basis, HYSIM Inside-Out, Modified, I-O, I/O. |
Problem Statement: I am modeling the Free-Radical polymerization of a defined monomer. I want to obtain the results for the z-average molecular weight (MWZ), the polymer weight average molecular weight (MWW) and the polymer number average molecular weight (MWN).
Results show that the value of MWZ is lower than the value of MWW and MWN. Typically the average values are related to each other as follows MWN < MWW < MWZ. Where is the error? | Solution: The attribute MWZ is a class 0 attribute used to specify the polymer z-average molecular weight. MWZ is calculated as the average segment molecular weight (MWSEG) multiplied by z-average degree of polymerization (DPZ).
The degree of polymerization is a class 0 attribute used to specify the polymer weight average degree of polymerization. During convergence DPZ is calculated from class 2 attributes using:
The default built-in attribute group for the free radical selection is shown below:
As it can be seen in the screenshot above, MWZ is not in the default list. To report the MWZ results, the following attributes must be included: MWZ and also DPZ, TMOM, SMOM. .
The same applies if you want to track the live composite, site-based, live site-based and associated polymer average molecular weights. The following table summarizes the attributes that need to be added to the default list in these cases.
Attribute to be reported
Needs to add the following attributes to the built in list.
Composite
MWZ
MWZ, DPZ, TMOM, SMOM
Live composite
LMWN
LMWN, LDPN, LZMOM, LFMOM
LMWW
LMWW, LDPW, LFMOM, LSMOM
Site-based
SMWN
SMWN, SSFLOW, SSFRAC, SDPN, SZMOM, SFMOM
SMWW
SMWW, SSFLOW, SSFRAC, SDPW, SFMOM, SSMOM
SMWZ
SMWZ, SSFLOW, SSFRAC, SDPZ, STMOM, SSMOM.
Live site-based
LSMWN
LSMWN, LSSFLOW, LSSFRAC, LSDPN, LSZMOM, LSFMOM
LSMWW
LSMWW, LSSFLOW, LSSFRAC, LSDPW, LSFMOM, LSSMOM
Associated polymer
AMWN
AMWN, ASFLOW, ASFRAC, ADPN, AZMOM, AFMOM
AMWW
AMWW, ASFLOW, ASFRAC, ADPW, AFMOM, ASMOM
After including all the attributes required for the calculations, the distribution of average molecular weight should be as MWN < MWW < MWZ.
Keywords: Polymer average molecular weight, moment of chain length distribution, live composite, site-based, live site-based, associated polymer
References: None |
Problem Statement: Can Aspen Polymer calculate shear-rate dependent viscosity of a Non-Newtonian fluid? | Solution: Aspen Polymer does not calculate the shear-rate dependent viscosity of a Non-Newtonian fluid in the simulation. It is advisable that any blocks in the simulation do not use viscosity in the calculation. Then, only viscosity calculation will be wrong. To reflect the shear-rate dependency, user can calculate viscosity separately by using calculator with excel which is available under Flowsheeting Options. First, zero-rate viscosity of the stream must be imported into calculator block and then calculation is performed by combining zero-rate viscosity with contribution from shear-rate and result is reported as shear-rate dependent viscosity in the worksheet.
An example is attached in the solution to show the integration of excel in Aspen Polymer. The system in the example file is a polystyrene/styrene system. The zero-rate viscosity mixture model is Aspen Polymer Mixture model, which is the default model in Aspen Polymer.
The calculator with Excel will reproduce Figure 11 in the paper published by Aspen Polymer team. The paper and bkp files are attached together as zip file.
Users can modify the example file to implement their own shear-rate dependent model.
Keywords: Shear-rate, viscosity, Non-Newtonian
References: None |
Problem Statement: Why is Aspen Rate Based Distillation (RateSep) better than using equilibrium stages with efficiencies? There seem to be a lot of fudge factors in rate-based distillation also? | Solution: Equilibrium stage efficiencies are a function of all column conditions (flow, temperature, pressure). This means that they generally do not extrapolate well to other conditions. A rate-based distillation model has more basis in reality using mass- and heat transfer correlations based on transfer properties and tray/packing geometry to predict column performance, without the need of efficiency factors and the fudge factors have more physical meaning. Once the column is calibrated to one set of conditions, it does generally extrapolate to other conditions. We have customers who have had success using RateSep and being able to predict new scenarios after tuning the column to an initial set of conditions. This added degree of rigor is especially critical for modeling gas scrubbers, sour water strippers, azeotropic systems, reactive distillations, nitric acid absorption columns, narrow-boiling separations, and other highly non-ideal separation processes.
The rate-based modeling approach has many advantages over the equilibrium-stage modeling approach. The rate-based models represent a higher fidelity, more realistic modeling approach and the simulation results are more accurate than those attainable from the equilibrium-stage models. The rate-based modeling approach can reduce the risk of inadequate designs or off-spec operation because the rate-based models explicitly account for the actual column configuration which affects column performance.
Designed to model reactive multistage separation problems rigorously and accurately, Aspen RateSep balances gas and liquid phase separately and considers mass and heat transfer resistances according to the film theory by explicit calculation of interfacial fluxes and film discretization. The film model equations are combined with relevant diffusion and reaction kinetics and include the specific features of electrolyte solution chemistry, electrolyte thermodynamics, and electroneutrality where appropriate. The hydrodynamics of the column is accounted for via correlations for interfacial area, hold-up, pressure drop, and mass transfer coefficients.
Fast reactions for processes such as CO2 removal with MEA do need to use the discretization film model available in the current rate-based distillation model not available previously in the older RateFrac.
RateSep uses a rate-based modeling approach, which is much more rigorous than the equilibrium stage modeling approach employed by the original RadFrac module. The rate-based model assumes that the separation is caused by mass transfer between the contacting phases, and uses the Maxwell-Stefan theory to calculate the mass transfer rates[1]. The equilibrium modeling approach assumes that the contacting phases are in equilibrium with each other, which is inherently flawed because the contacting phases are never in equilibrium in a real column.
The rate-based (or nonequilibrium) modeling approach has a lot of advantages over the equilibrium modeling approach, and is becoming more and more popular in both the academia and the industry. The rate-based model is more reliable and accurate than the equilibrium model, and therefore can reduce the risk of inadequate designs or off-spec operation. The rate-based model gives more realistic simulation results than the equilibrium model, because the column configuration is included in the rate-based model and will affect the simulation results as it should. Engineers can use the rate-based model to do more realistic what-if studies and improve the operations of existing columns. The rate-based model can also predicts the behavior of a column more accurately, and can help the process control engineers develop better control strategies.
It is generally accepted in the literature that the rate-based model is more accurate than the equilibrium model. In some cases the rate-based model gives accurate results while the equilibrium model gives wrong results.
Taylor et al. [2] reviewed the modeling of distillation and concluded that the rate-based simulations "are not only feasible, but in some circumstances they should be regarded as mandatory". For a bubble cap distillation column used to separate water, ethanol and acetone, the composition trajectory predicted by the rate-based model agrees with the experimental data very well, while the equilibrium model gives very different results. The rate-based model also accurately predicts that the distillation boundary is crossed, while the equilibrium model wrongly predicts that the distillation boundary can never be crossed. Taylor et al.[2] also used experimental data from Springer et al.[3] for the water-cyclohexane-ethanol system to demonstrate that the rate-based model can predict the composition trajectory accurately, while the equilibrium model cannot.
Kucka et al.[4] used the rate-based model to simulate the sour gas absorption by aqueous amine solutions. They compared the simulation results with experimental data from a pilot plant column and an industrial scale column and found that the rate-based model can accurately predict the temperature and composition profiles.
Springer et al.[5] used the rate-based model to simulate ternary azeotropic distillation and compare the simulation results with experimental data from a bubble cap distillation column with the water-ethanol-methylacetate system. They found that the rate-based model ?is in excellent agreement with a series of experiments carried out in different composition regions. In sharp contrast, an equilibrium (EQ) stage model fails even at the qualitative level to model the experiments.? They concluded that "for reliable simulation of distillation of azeotropic systems exhibiting a distillation boundary, we must adopt a rigorous NEQ (or rate-based) stage model."
Eckert and Vanek[6] studied three-phase distillation columns with the rate-based modeling approach. Extensive experimental work for the ethanol-water-cyclohexane system[7-9] was used to compare the rate-based approach and the equilibrium approach. They found that the rate-based model can predict the composition profiles much better than the equilibrium model, especially in the middle of the column. The rate-based model also predicts the disappearance and reappearance of the second liquid phase very well.
Kreul et al.[10] studied the modeling of reactive separation processes in packed columns and found that the concentration profiles calculated by the rate-based and equilibrium models can be very different, and the rate-based model should be preferred for reactive separation processes.
Kenig et al.[11] studied reactive absorption using models with different complexities. Both the steady state and dynamic models were used. They found that for a H2S scrubber, the rate-based modeling approach can predict the concentration profiles very well, while the equilibrium model may yield results completely inconsistent with the experimental studies.
Sundmacher and Hoffmann[12] used a rate-based model to simulate reactive distillation of the MTBE system in a packed column. The simulation results were validated with experimental data from a laboratory scale column with excellent agreement.
Frey and Stichlmair[13] mentioned in their review paper on reactive distillation that rate-based model has been used to accurately predict the performance of commercial reactive distillation processes in Germany and Texas, and that the model has been validated for the design of TAME, ETBE and TAEE units with data from semi-commercial operations.
Pinjala et al.[14] used a rate-based model for reactive distillation of the MTBE and TAME processes in columns filled with Koch Katamax? packing. The simulation results were compared to some pilot-plant data with good agreement.
Most recently, Kloker et al.[15] compared the rate-based model with the equilibrium model for two reactive separation processes, the synthesis of ethyl acetate from ethanol and acetic acid via reactive distillation and the synthesis of octyle hexanoate from octanol and hexanoic acid via reactive stripping. They found that the rate-based model with a fine discretization is able to match the column temperature profile and the bottom concentration better than the equilibrium stage model.
The rate-based modeling approach has been used successfully to model many industrial separation processes. It has been adopted by many researchers to model reactive distillation of MTBE[12, 14, 16], TAME[13, 14], ETBE[13], TAEE[13], ethyl acetate[15], propylene glycol[17], ethylene glycol[17], propyl acetate[18], diacetone alcohol[19, 20] etc. It is also used to model other reactive separation processes such as reactive absorption[4, 11, 15, 21] and reactive stripping[15]. The rate-based model has also found successful application in azeotropic distillation[5] and three-phase distillation[6, 22, 23].
The rate-based model is especially preferred over the equilibrium model in the following situations:
(1) Packed columns. The rate-based model does not need the HETP (Height Equivalent to a Theoretical Plate) of the packing, while the equilibrium model does. The HETP can vary widely from component to component and from packing to packing, and cannot be estimated accurately in most cases.
(2) Absorption and desorption. The absorption and desorption processes are normally operated in conditions far away from phase equilibrium, and are mass transfer and heat transfer limited. The tray efficiency for a absorption/desorption column can be as low as 5%[2]. Therefore, the rate-based model is more appropriate than the equilibrium model.
(3) Reactive separation such as reactive distillation and reactive absorption. The rate-based model can model reaction rates much more accurately than the equilibrium model. The efficiencies are not meaningful for reactive separation processes.
(4) Strongly nonideal systems. The efficiencies are highly uncertain and can vary widely from tray to tray and component to component. It is very difficult to determine the efficiencies for the equilibrium model. Therefore, the rate-based model should be preferred.
(5) Columns with a complicated configuration (pump-around, side streams). It is very difficult to determine the theoretical stage locations for pump-around and side streams, which are necessary for the equilibrium model. The rate-based model does not need any information about theoretical stages, and should be preferred.
(6) Columns with mixed trays and packing. It is very difficult to determine the number of theoretical stages for each tray/packing section. The rate-based model does not need any information about theoretical stages, and should be preferred.
The major drawback of the rate-based model is that it is much more complicated than the equilibrium model. Previously, the rate-based model was considered as impractical due to its complexity. Right now, the rate-based model can be solved readily on any mainstream PC, thanks to the ever-increasing computing power.
There are some special advantages for RateSep:
(1) RateSep is seamlessly embedded in RadFrac. It is very easy to configuration a RateSep simulation for someone who does not know very much about the rate-based model. The complexity of the rate-based model is in the background and not noticeable to the user.
(2) RateSep has many built-in correlations for mass transfer and holdup. There are default correlations for each tray/packing type. The user does not need to worry abut the correlation unless he/she wants to choose other correlations.
(3) RateSep has detailed examples for user subroutines. The user can easily modify the examples to create his/her own user subroutines for mass transfer, heat transfer and holdup.
(4) A continuation method has been implemented in RateSep to improve the convergence for problems that are difficult to converge. The user only needs to choose two continuation parameters to use the continuation method.
(5) Several tuning parameters have been defined to help the advanced users to model a column more accurately. The user also has control on how he/she wants to calculate the fluxes, how to average the diffusivities and mass transfer coefficients.
(6) It is very easy to switch between the equilibrium mode and the rate-based mode. For a large flowsheet, if the block with RateSep fails to converge, the user can easily switch back to the equilibrium mode and make the flowsheet converge. After that, he/she can switch to the rate-based mode and try to make the whole flowsheet converge.
(7) RateSep supports film reactions and film discretization. Therefore, it is capable of solving reactive separation problems accurately.
It is necessary to have accurate properties, kinetic and equilibrium constants if needed, and then tune the factors such as the interfacial area factor and the heat transfer factor for the rate-based column. But, because the model has more physical meaning, it can then be used to model new situations more accurately. A number of our customers have used the Rate Based Distillation model successfully.
Keywords: None
References: s
[1] Taylor, R. and Krishna, R. (1993). Multicomponent mass transfer. New York: Wiley.
[2] Taylor, R. , Krishna, R. and Kooijman, H. (2003). Real-World modeling of distillation. Chemical Engineering Progress, 98(7), 28-39.
[3] Springer, P.A.M., et al. (2002). Crossing of the distillation boundary in homogeneous azeotropic distillation: influence of interphase mass transfer. Industrial and Engineering Chemistry Research, 41, 1621-1631.
[4] Kucka, L. et al. (2003). On the modeling and simulation of sour gas absorption by aqueous amine solutions. Chemical Engineering Science, 58, 3571-3578.
[5] Springer, P.A.M., van der Molen, S. And Krishna, R. (2002). The need for using rigorous rate-based models for simulations of ternary azeotropic distillation. Computers and Chemical Engineering, 26, 1265-1279.
[6] Eckert, E. and Vanek, T. (2001). Some aspects of rate-based modeling and simulation of three-phase distillation columns. Computers and Chemical Engineering, 25, 603-612.
[7] Muller, D. et al. (1997). Experimental validation of an equilibrium stage model for three-phase distillation. IChemE Symposium Series, 142, 149-159.
[8] Klein, W. (1996). Experimental investigation of the stationary and dynamic behavior of heteroazeotropic distillation. Diploma project. RWTH Aachen (in German).
[9] Dux, A. (1996). Verification of an equilibrium model in dynamic simulation of three-phase distillation. Diploma project. RWTH Aachen (in German).
[10] Kreul, L.U., Gorak, A. and Barton, P.I. (1999). Modeling of homogeneous reactive separation processes in packed columns. Chemical Engineering Science, 54, 19-34.
[11] Kenig, E.Y., Schneider, R. and Gorak, A. (2001). Reactive absorption: optimal process design via optimal modeling. Chemical Engineering Science, 56, 343-350.
[12] Sundmacher, K. and Foffmann, U. (1996). Development of a new catalytic distillation process for fuel ethers via a detailed nonequilibrium model. Chemical Engineering Science, 51, 2359-2368.
[13] Frey, T. and Stichlmair, J. (1999). Thermodynamic fundamentals of reactive distillation, Chemical and Engineering Technology, 22, 11-18.
[14] Pinjala, V. et al. (1992) Rate based modeling of reactive distillation operations, AIChE annual meeting, Session 3, Distillation with reaction.
[15] Kloker, M. et al. (2004) Rate-based modeling and simulation of reactive separations in gas/vapor-liquid systems. Chemical Engineering and Processing, to be published.
[16] Pyhalahti, A. and Jakobsson, K. (2003). Rate-based mixed-pool model for a reactive distillation column. Industrial and Engineering Chemistry Research, 42, 6188-6195.
[17] Dhale, A.D. et al. (2004) Propylene glycol and ethylene glycol recovery from aqueous solution via reactive distillation. Chemical Engineering Science, 59, 2881-2890.
[18] Bart, H.-J. and Landschutzer, H. (1996). Heterogene Reaktivdestillation mit axialer Ruckvermischung, Chem. Ing. Tech., 68, 944-946.
[19] Huang, C.C. et al. (1998). A study of mass transfer behavior in a catalytic distillation column. Canadian Journal of Chemical Engineering, 76, 323-330.
[20] Huang, C.C. et al. (1998). Application of catalytic distillation for the aldol condensation of acetone: a rate based model in simulating the catalytic distillation performance under steady state conditions. Chemical Engineering Science, 53, 3489-3499.
[21] Bolhar-Nordenkampf, M. et al. (2004). Modeling selective H2S absorption and desorption in an aqueous MDEA-solution using a rate-based non-equilibrium approach. Chemical Engineering and Processing, 43, 701-715.
[22] Repke, J., Villain, O. and Wozny, G. (2004). A nonequilibrium model for three-phase distillation in a packed column: modeling and experiments. Computers and Chemical Engineering, 28, 775-780.
[23] Higler, A. et al. (2004). Nonequilibrium modeling of three-phase distillation. Computers and Chemical Engineering, 28, 2021-2036. |
Problem Statement: Is there a way to model a biodegradable polyester process in Aspen Polymers Plus using mass transfer? | Solution: Environmental concerns are driving worldwide efforts to develop new biodegradable polymers. These new products include several polyesters such as polylactide (PLA) and polyester 4,4 (poly (1,4) butanediol-succinate), and for PBSL, the copolymer of butanediol, succinic acid, and lactic acid. The purpose of this document is to demonstrate how Aspen Polymers Plus can be used to simulate the polymerization process to manufacture these materials.
See the attached file: "Biodegradable Polyester.doc".
KeyWords
polyester, mass transfer, step-growth
Keywords: None
References: None |
Problem Statement: How can I avoid column flooding and improve performance in a methylamines process? | Solution: Column Analysis in Aspen Plus V9 can accelerate engineering workflows for designing and rating of distillation columns with insights into the hydraulic limitations on column trays or packing. In a methylamines process, this is important to avoid flooding issues and attain flexibility to change the product slates to meet market needs.
This example will cover
· Using Aspen Plus to simulate a methylamines process
· Using the interactive sizing feature in Column Analysis to perform preliminary sizing of distillation towers to evaluate performance and cost tradeoffs between different internal types
· Using the rating mode in Column Analysis to evaluate off-design cases, understand how flexible the chosen internals are, and locate cost-saving opportunities .
Keywords: Column Analysis, Distillation, Sizing, Design, Rating, Methylamine, Methyl, Amine, Hydraulics, Flooding, Weeping
References: None |
Problem Statement: When using "Update SMC Coefficients", should I expect to update PCALC/PCALCB/BLNPROP values? | Solution: "Update SMC Coefficients" utility is designed to update properties.The code in PIMS does write the updated data to the SMC file
From PIMS:
1.- Launch PIMS. Open Volume Sample model. Run BASE case
2.- Click on Submodel Calculator icon in the tool bar menu
3.- Select "SCNP" submodel. Click "OK"
4.- In the "Submodel Calculator view" click on "Resolve" button on the right
5.- Read the row "RRONLCN" value at column "SCNPLC1". Write the value down(i,e,- 93).
6.- Do a File|Save. Save the file as "SCNP.SMC" to Orion SMC directory (to be use in Orion).
7.- Close the Submodel Calculator view
8.- Open the "BLNPROP" table (blnnaph sheet) from PIMS model tree
9.- Modify RONLC1 to 89. Save the sheet and close the table
10.- Run PIMS, Base case
11.- Open the SCNP.SMC file you saved in Step 6
12.- Click on the "Resolve" button in the Submodel Calculator View
You would see that the row RRONLCN value at column SCNPLC1 does not change
This prove that the SMC file did not get updated
13.- Exit PIMS
From Aspen Petroleum Scheduler (APS):
1.- Launch Orion. Open the DEMO model
2.- Do a FlowSheet|Add Object|Unit to invoke Unit Definition dialog
3.- Choose PIMS Submodel in the Type combo drop down
4.- Type SCNP as the identifier. Click OK to exit the Unit Definition dialog. Example:
5.- Do a Model|Update SMC Coefficients to invoke Update SMC Coefficients dialog
6.- Check SCNP.SMC only in the dialog
7.- Point to the PIMS Volume Sample model you ran in step 1 in the PIMS Model Folder text box.
8.- Click Update button
9.- After it is done updating
10.- Launch PIMS again
11.- Open the SCNP.SMC file you saved in step 6
12.- Click on the Resolve button in the Submodel Calculator View
You would see that the row RRONLCN value at column SCNPLC1 change to 89, the new value we set in step 93. This prove that the SMC file did get updated by the SMC update utility.
Keywords:
References: None |
Problem Statement: Internal Calculations: Differences in BAD value handling between DMCplus and APC Builder | Solution: Both, the traditional Aspen DMCplus Build and new Aspen APC Builder platforms allow users to develop/write internal calculations that can be used to perform custom calculations that will supplement the controller engine calculations. The traditional DMCplus platform uses a built-in calculation feature in order to run the calculations online, while the new APC Builder platform utilizes the powerful Aspen Calc engine for this purpose.
The different calculations engines being used in the two platforms results in dissimilarities in how BAD values are handled in each of the platform. When, a BAD value is supplied as an input to a conditional/logical statement (IF) in the traditional DMcplus transform, the calculation engine always defaults to the TRUE result of the IF statement. While,APC Builder does not default to TRUE. It performs the calculations using the supplied BAD value and could result in either a TRUE or a FALSE result. See example below for details-
DMCplus: X = @IF(@GT(B, 10), 5, X)
If B is greater than 10, set X = 5, else keep the current value of X unchanged.
In this example, if the value of B became BAD, i.e. B = -9999, the DMCplus calculation engine will set X = 5.
APC Builder: IF (B > 10) THEN
X = 5
ELSE
X = X
END IF
In this case, if the value of B became BAD, i.e. -9999, the APC Builder (Aspen Calc) engine will notice that B is not greater than 10 and therefore keep the value of X unchanged.
Additional Note
KB4180 discusses an internal calculation procedure that can be used to disable IPE (Accumulated Prediction Error) feedforward in situations where the accumulated prediction error for the CV gets too large. In this example, a situation might arise when the value of the IPE feedforward variable measurement is marked BAD, which causes the calculation to work differently in DMCplus vs APC Builder.
When converting a traditional DMCplus controller to DMC3 controller, it is always recommended to check (and test) the custom calculations and ensure that they are working as expected.
Keywords: DMCplus Calculations
APC Builder Calculations
Accumulated Prediction Error
IPE
References: None |
Problem Statement: After installing the Aspen Simulation Workbook, the ASW toolbar icons do not appear in Excel 2007 and the Aspen menu does not appear in the Excel menu structure. | Solution: When both the toolbar icons and Aspen menu item are missing, the toolbar may be disabled by Excel. To check for this scenario:
1. Open Excel.
2. Click Office button
3. Click on Excel Option button.
4. Select Add-Ins and go down to see to Disabled Application Add-in section; If Aspen Simulation Workbook appears in the list select Disable items on Manage and click Go.
5. On the Disable items Window select Aspen Simulation Workbook and click on Enable button.
If the above procedure fails to resolve the problem:
1. Open Excel.
2. Click Office button.
3. Click on Excel Option button.
4. Select Add-Ins. On manage select Com Add-Ins and click GO
5. Verify that Aspen Simulation Workbook is in the list. Ensure that it is checked (enabled) and its path is ASWXLAddinLoader.dll in the Aspen Simulation Workbook Location.
6. If not, try to add manually (click on add and browse for ASWXLAddinLoader.dll)
Keywords: Aspen Simulation Workbook, Excel, Link, OSE Workbook
References: None |
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