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Problem Statement: How does one report phase density for each tray in my column in Aspen HYSYS?
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Solution: To display the density of the liquid and vapor phases for each tray in a given column, open the column view to the Performance | Plots page and select the Transport Properties option in the Tray by Tray Properties window. Next, select either the View Graph or View Table button to open the corresponding form and view the transport properties (including the liquid and vapor phase density) for each stage. If desired, click the Properties button (found near the bottom left corner of both the graph and table windows) to select the reporting basis for each property.
Keywords: density, properties, tray, stage, section, column, plot, table, graph
References: None
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Problem Statement: The column was able to converge in the column environment, but an inconsistency error occurs due to a variable that is a result of column convergence when I turn on the solver in the parent environment.
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Solution: This could occur when you have previously converged your column, and then entered the column environment to modify the column unit operations.
Ensure that no variable in the product streams of the column has been specified directly. Add such variables as column specifications on the Monitor / Specs page on the Design Tab of the column.
If this is not the problem, then you may have to delete the product streams in the Parent Environment or break their connection to the column. Create a number of new unspecified streams in the parent environment of equal number to your product streams of the column. Then go to the Connections page on the Design tab, and under Outlet Streams, connect the internal streams in the column environment to the external streams you have just created in the parent environment, with a pressure - enthalpy (P-H) transfer basis. Sometimes, you may need to go into the column to re-run and converge the column before connecting the internal and external streams.
Keywords: Modified column, inconsistency error
References: None
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Problem Statement: In a new model, we want to merge the content of subflowsheets from several existing models, while preserving the layout and selected fluid packages originally in the subflowsheet.
What is the recommended procedure for the tasks?
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Solution: The first task we discuss here is to move the content of an existing subflowsheet to a new case. Currently, HYSYS does not have an operation to allow a user to export the content of a subflowsheet into a standalone model. If you no longer have the access to the original template file used to create the subflowsheet, you will need to follow the following recommended steps:
1) Export the fluid package used as the default for the existing subflowsheet,
2) Import the fluid package into a new case as default,
3) Show hidden objects in the subflowsheet (PFD | Show Hidden Objects),
4) Select the content of the existing subflowsheet for copying (Left mouse button pressed to select, right click to Cut/Paste Object | Copy Selected Objects),
5) Paste Objects onto PFD in the new case,
6) Save the new case or convert it to template.
In the first two steps, we establish the default fluid package in the new case identical to that of the existing one. When we paste objects into the new case, the default fluid package will be copied with the flowsheet, seetSolution 125754 for explanation. In step 4), a user can Copy Objects to File (Export), and in step 5), Paste Object From File (Import).
The second task is a continuation of the first. Now we want to merge several subflowsheet into one model. If we want to create Case (Main) from several flowsheet fragments (not embed in Subflowsheet) , we need to determine the default fluid package up front, and start the new case with this default fluid package. After that, repeat step 4) and 5) to bring the flowsheet fragments into the new PFD, connect with streams if needed, and converged the flowsheet in the new case.
In some cases, we want to embed several flowsheet fragments into Subflowsheet as parts of Case (Main). We need to save the flowsheet fragments in individual template file in step 6). Afterwards, create a Subflowsheet in the new case for each of the templates, Read an Existing Template, connect with streams, verify the assignment of fluid package, and converge the flowsheet in the new case.
The above is tested and recommended procedure to avoid confusions when multiple fluid package are involved, and to maintain the current flowsheet layout of streams and unit operation icons.
Keywords: Export subflowsheet, recreate template
References: None
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Problem Statement: How do I create an 'Ignore This Unit Operation During Calculations' checkbox?
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Solution: Use the following procedure:
add a standard check box to the extension view,
double-click on the check box or right click and select Check Box Properties,
double-click the Target Moniker box or click the Ellipsis button directly beside it,
select Object is Ignored in Calculations,
change the text in the Label text box to &Ignore Unit Operation
Keywords: edf, ignore, ignored
References: None
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Problem Statement: Is it possible to export the PFD to be pasted in another application such as Word?
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Solution: Functionality allowing the export of the PFD was incorporated in Hysys with the v. 2.2 release. To export the PFD, object inspect the PFD background and select Copy Pane to Clipboard. This will copy the PFD to the Windows clipboard. It is then available to be pasted into applications such as MS Word or Paint.
In versions prior to 2.2, there is no direct export function, but there are methods which can be used to capture your desktop.
1. Using Paint Shop Pro, you can capture the PFD and save it in a bitmap format. You can then insert it as an object in Word (Insert / Object / Create from File...).
2. In HYSYS, you can type <Alt><Print Screen>, go into Word and type <Ctrl><V>. This will bring the entire screen, however (with toolbars, menus, etc.).
3. In HYSYS, you can type <Alt><Print Screen>, go into an image editor such as Microsoft Paint (MS Paint) and type <Ctrl><V>. You can then edit the image to get rid of the toolbars, menus. etc. After editing the image, you can load it into Word (as per number 1).
Keywords:
References: None
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Problem Statement: Aspen Properties Enterprise Database (APED) is located on a remote server and you cannot access a database on that server from a client PC using the Aspen Properties Database Manager.
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Solution: This problem is caused when the remote server is not configured properly for remote access and/or the Windows Firewall is blocking access.
Follow these steps to configure a SQL Express 2005 server to be used by remote users. All these steps must be performed on the server machine and may be performed through a remote connection.
1. Launch the SQL Server Configuration Manager from Start | Programs | Microsoft SQL Server 2005 | Configuration Tools | SQL Server Configuration Manager.
2. Under SQL Server Configuration Manager (Local) | SQL Server 2005 Network Configuration | Protocols for <instance name such as SQLEXPRESS>, enable the TCP/IP and Named Pipes protocols by right-clicking and selecting Enable on each one.
3. Under SQL Server Configuration Manager (Local) | SQL Native Client Configuration | Client Protocols, enable all protocols other than VIA (VIA may also be enabled if desired).
4. Launch SQL Server Surface Area Configuration from Start | Programs | Microsoft SQL Server 2005 | Configuration Tools | SQL Server Surface Area Configuration.
5. Click the link for Surface Area Configuration for Services and Connections.
6. Under <instance name> | Database Engine | Remote Connections, select Local and remote connections, then select Using both TCP/IP and named pipes.
7. Under <instance name> | Database Engine | Service, click Stop (if enabled), then click Start to restart the database engine service.
8. Under SQL Server Browser | Service, ensure the Startup type is Automatic. Click Apply and OK after changing this setting. Then click Stop (if enabled), then click Start to restart the server browser service.
9. Open the control panel from Start | Settings | Control Panel and double-click Windows Firewall.
10. In the Windows Firewall control panel, click Add Program.
11. Click Browse, and add sqlservr.exe and sqlbrowser.exe to the list of allowed programs. The locations depend on where SQL Server was installed, but typical locations are:
C:\Program Files\Microsoft SQL Server\MSSQL.1\MSSQL\Binn\sqlservr.exe
C:\Program Files\Microsoft SQL Server\90\Shared\sqlbrowser.exe
12. On SQL Server Express, the user interface for configuring the server is not installed by default. If you do not have it, download it from Microsoft and install it: http://www.microsoft.com/downloads/details.aspx?FamilyId=C243A5AE-4BD1-4E3D-94B8-5A0F62BF7796&displaylang=en
13. Run Start | Programs | Microsoft SQL Server 2005 | SQL Server Management. The Connect to Server window appears.
14. Select the server name and Windows Authentication. Click Connect. The Microsoft SQL Server Management Studio Express window appears.
15. In the tree on the left, right-click the name of the server and select Properties. The Server Properties dialog box appears.
16. At the left, click Connections.
17. Verify that Remote Connections is checked. If you change this here, you must restart the server again for it to take effect. You can do so by right-clicking the server name in the Microsoft SQL Server Management Studio Express window and selecting Restart.
Keywords: Aspen Properties Enterprise Database, APED, remote server, SQL Express, SQL Express configuration
References: None
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Problem Statement: Where can I find FAQs on SLM Installation?
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Solution: The SLM is a security system which is used across several products. SLM questions will be found by selecting SLM as a product, rather than under each specific software application product name.
Keywords: SLM
References: None
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Problem Statement: When tiny amount of water is added to a flowsheet using the PC-SAFT property method, the computation time increases dramatically.
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Solution: Adding a tiny amount of water will activate the association term in PC-SAFT. The association term in PC-SAFT is self-contained and has to be solved within each iteration for the density. The increase of the CPU time due to the association is proportional to N^2 where N is the number of components in the stream. Therefore, if there are about 10 components in the mixture and as long as a component has the association, the CPU time is about 100 fold compared to a 10 component mixture without any association.
Keywords: None
References: : CQ00405521
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Problem Statement: After pasting a copied stream, the newly created stream contains no process information. Is there an easy way to transfer all the process information from the original stream?
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Solution: When you create copy a stream (i.e. select Edit | Copy from the main menu, or right click on the stream icon from the PFD and select Cut/Paste Objects...Copy Selected Objects), Aspen HYSYS copies only the user-specified values, including composition. For example, if all values in the original stream are calculated (i.e. all process variables are displayed in black), then no process information will be transferred and the pasted stream will be blank.
To copy a stream that does not have sufficient user-specified information to solve, you will first need to create a duplicate stream using the Define from Other Stream feature (as described inSolution 109277), then create a copy of this duplicate stream.
Keywords: copy, copied, stream, paste, duplicate
References: None
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Problem Statement: After creating a new, in-house databank and adding to the Aspen Properties Enterprise Database (APED), how do I generate a report of the components, properties, and values?
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Solution: This option is available with aspenONE version V7.2 and higher only. AspenONE V7.2 has a new functionality called APRDTS which exports all the compounds and property names from a given databank to a simple text file. APRDTS will not put the actual values in this report.
To do so, right click on any databank, APRDTS option appears, Select APRDTS for obtaining the text file.
Keywords: APED
APRDTS
Report
DataBank
References: None
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Problem Statement: How is wax deposition calculated in the pipe segment using the ProFES wax model?
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Solution: The deposition of the wax from the bulk oil onto the pipe wall is assumed to only be due to mass transfer; shear dispersion is not considered to be a significant factor. The rate of deposition is described by:
m' = k[Cwall - Cbulk] * A * MWwax
m' = deposition rate (kg/s)
k = mass transfer coefficient (mole/m2s)
C = local concentration of wax forming components (mole fraction)
Mwwax = molecular weight of wax (kg/mole)
A = cross-sectional area (m2)
The mass transfer coefficient (k) is calculated using the following correlation:
Sh = k * DH / c * D
where:
Sh = 0.015 * Re0.88 * Sc1/3
and
Re = Vl * rl * DH / ?l
D = diffusivity of wax in oil (m2/s)
?l = liquid viscosity (kg/ms)
rl = liquid density (kg/m2)
k = mass transfer coefficient (mole/m2s)
DH = hydraulic radius (m)
Vl = liquid velocity (m/s)
c = liquid molar density (mole/m3)
The Reynolds number that is used in these calculations is based on the local liquid velocity and liquid hydraulic radius. Physical properties are taken as the single phase liquid values. The viscosity used is based on the fluid temperature and shear rate at the wall. The difference in concentration of wax forming species between the bulk fluid and the wall, which is the driving force for the deposition of wax is obtained from calculating the equilibrium wax quantities at the two relevant temperatures. These calculations provide a wax deposition rate which is integrated over each time step to give the total quantity of wax laid down on the pipe wall.
Keywords: wax, deposition, pipe, segment, ProFES
References: None
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Problem Statement: How does one import or copy composition from Excel to Aspen HYSYS?
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Solution: Select the desired range from MS Excel and click Ctrl+C to copy the values to the Windows clipboard. Switch to Aspen HYSYS and open the target stream to the Worksheet | Composition page. View the composition window by selecting the Edit button then press Ctrl+V to paste the values into the form, ensuring that the appropriate basis (mole, mass or volume fraction) is enabled.
Note that the cursor should be on the first composition element prior to pasting the values, otherwise the target matrix may not be the appropriate size and the paste operation will fail.
Keywords: copy, paste, import, mole, mass, volume, fraction, excel
References: None
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Problem Statement: Sometimes, you or your clients would like to generate PFD tables in different units for different unit operations of the same type. So how do you do it?
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Solution: Currently, all graphic user interface features are using the same unit set. You can only use a different unit set within a spreadsheet unit. To create PFD tables showing the same unit parameters in different units, you can consider two options, 1) using HYSYS spreadsheet unit operation, or 2) using user variables. In both cases, to show the values correctly on the PFD tables, the variables have to be defined as unitless type, i.e., Unitless for Var Type in spreadsheet, and Index for Units in user variable definition.
We use Pipe Segment unit as example to show both approaches. We want to show that the feed and product pressure are in different units. For one pipe segment, we use psig as pressure units. For the other, we use in H2O as pressure unit.
To implemented the first approach, we define two unit sets. We place two spreadsheet units to PFD and select one unit set for each. Next, we import the parameters, and convert them to Unitless. Afterwards, we create PFD tables using the unitless parameters.
To implement the second approach, we need to define four user variables with VB macros. These user variables have type information as Real | Scalar | Index. Inside the macro, the unit operation parameters are retrieved, converted to value in desired units, and passed to the user variable edit box.
Keywords: Data table, table, units
References: None
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Problem Statement: How does one increase the line thickness on a plot within Aspen HYSYS?
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Solution: To increase the line thickness for any plot displayed in Aspen HYSYS, follow the steps below:
1) Right-click on the graph and select Graph Control from the ensuing menu.
2) On the first page tab (i.e. Data) of the Graph Control window and highlight the curve of interest from list on the left hand side.
3) Input a numeric value (from 0-5) to indicate the desired thickness (5 being the thickest), then close the Graph Control window.
Keywords: plots, curves, line, thickness
References: None
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Problem Statement: Is it possible to report Std Gas Flow using a different pressure basis?
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Solution: Std Gas Flow is based on the molar volume of an ideal gas at standard conditions (in Aspen HYSYS, standard conditions are 15 Celsius and 1 atmosphere if SI units are selected and 60 Fahrenheit and 1 atmosphere if Field units are selected). This value is a direct conversion from the stream's molar flow rate based on the following definitions:
An ideal gas at 15?C and 1 atm occupies 23.644 m3/kgmole
An ideal gas at 60?F and 1 atm occupies 379.46 ft3/lbmole
For example, if the stream flow rate is 1000 kgmole/h, then the Std Gas Flow would be reported as 23644 Std_m3/h. To convert the units to MMCSFD, the following internal conversion factor is used in Aspen HYSYS:
1 MMSCFD = 0.32712 Std_m3/s.
If you wish to use a different value when defining atmospheric pressure (Aspen HYSYS uses 14.696 psi) and would like to report Std Gas Flow using this new basis, you will have to report this variable by creating a new user unit.
To do this, calculate the ratio of ideal gas molar volumes at HYSYS standard conditions and at your revised pressure conditions, then go to Tools | Preferences | Variables. Select SI or Field units and click Clone. Next, scroll down the display Units until you reach to Std Gas Flow and then click the Add button. Define a new unit by multiplying the internal unit by the ratio calculated above.
Keywords: Std Gas Flow, basis, standard, conditions
References: None
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Problem Statement: Basic Aspen Solubility Modeler work flow
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Solution: The basic work flow is as follows -
1. The Aspen Solubility Modeler from Windows start menu will open up its installation folder. The bin sub folder contains the help file. The NRTL-SAC holds the actual files.
2. Setup Excel for using Solubility Modeler. Use the file help since it has step by step instructions.
3. Copy the whole folder NRTL-SAC (the default full path is C:\Program Files\AspenTech\Aspen Solubility Modeler V7.2\NRTL-SAC) to a working folder since the original folder is write protected.
4. Double click Regression and Calculate work sheets in the working folder as needed and follow steps seen on the sheets. Make sure to re-point aprbkp file to the one in working folder in step1 on the sheets.
A few other details for attention -
The drug name is a place holder where user can give it any name. So it does not matter it is called Aspirin, Drug or other names.
When the molder is run, the drug will be mapped to DRUG component in the aprbkp file and its precipitation solid will be mapped to SOLID component.
The aprbkp and aprpdf files will be updated by the Regression runs and therefore it is critical for the Calculation phase to use the same aprbkp file in the working folder since it would contain the regressed parameters for the drug in the Regression phase.
The minimum number of solubility data points recommended is the number of parameters being regressed, but user may enter more, up to the limit of the rows in this section of the spreadsheet (30 for pure solvents and 40 for binary solvents). user can enter the standard deviation for each data point as well as indicate whether to include it in the regression or not. The XYZ parameters and the Ksp parameters have to be regressed together, if they are to be regressed.
Keywords: Work flow, minimum, map, drug
References: None
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Problem Statement: The RESET button on the column view does not appear to remove all the estimates. Why is that?
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Solution: The column RESET button clears the currentSolution as well as any estimates generated by column. If you have manually entered some estimates on the Parameters | Profiles pagetab or the Parameters | Estimates pagetab, then clicking the RESET button will not remove those estimates.
In order to remove any estimates that have been entered by the user, you will need to press the Clear All Trays button on both the on the Parameters | Profiles pagetab and the Parameters | Estimates pagetab.
Keywords: reset, clear, trays, estimates, composition
References: None
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Problem Statement: What flash types are available in Aspen Properties Toolkit and what are the KODE, SPEC1 and SPEC2 arguments for FLSH_PFLASH?
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Solution: To be able to use the Aspen Properties general flash utility for flash calculations, FLSH_PFLASH, you must specify one of the following combinations of information for two and three-phase flash calculations:
? Temperature and pressure (TP flash)
Pressure and molar vapor fraction (PV flash)
Temperature and molar vapor fraction (TV flash)
Temperature and enthalpy (TH flash)
Pressure and enthalpy (PH flash)
Pressure and entropy (PS flash)
Pressure and internal energy (PU flash)
FLSH_PFLASH calculates all unspecified state variables, phase splits, phase compositions, and phase thermodynamic properties. Phase transport properties can be calculated by calling transport property monitors immediately following FLSH_PFLASH.
In the calling sequence for FLSH_PFLASH, the flash option code is specified with the argument KODE, which will have the following values:
1 - PH (SPEC1 = P, SPEC2 = H)
2 - TP (SPEC1 = T, SPEC2 = P)
3 - PV (SPEC1 = P, SPEC2 = V)
4 - TH (SPEC1 = T, SPEC2 = H)
5 - TV (SPEC1 = T, SPEC2 = V)
6 - PS (SPEC1 = P, SPEC2 = S)
7 - PU (SPEC1 = P, SPEC2 = U)
The specification must be 1 or 2 if NPHASE = 1 or 11, where 1 is Single-phase calculation, phase specified by KPHASE and 11 is Liquid-water, two-phase, free-water calculation.
The documentation from version 7.1 onwards includes this information.
Keywords: KODE, flash option, FLSH_PFLASH, toolkit
References: None
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Problem Statement: How do I get started using Aspen Properties Mobile on an iPhone, iPod or iPad?
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Solution: Here is a Step by Step Tutorial for Aspen Properties Mobile.
Once connected to the Aspen Properties interface, you will see the message ?Creating a new case will clear the current case?. Select Clear to proceed. Then select ?Create new case? to start a new case.
Components can be added under the ?Components? tab. Add the components by tapping on the ?+? sign.
Type in the name of the component, for example water. Tap the desired component from the list and tap Done.
Keep adding components by tapping on ?+? sign.
User can tap on ?i? beside the component name to see detail information of that component.
Once all components have been selected, go to ?Calculation? tab. You will see the following screen:
Select the Method by taping on ?>? under Method field.
A selection of physical property is available. Tick the ?property? to be analyzed. For example, Density.
The Phase and Basis can be changed accordingly. Specify the fluid's pressure and provide the temperature limit.
The units can be changed by tapping on ?Global Units?.
After all specifications have been input, go to Results tab and see the results - ?Density? of the components at fixed pressure and a range of temperatures as specified.
Tap on Plot to plot the property as a function of temperature.
User can drag the x-axis line to report the result of a particular temperature.
Results can be saved by tapping on ?Save? button. Results can also be emailed as .csv (excel) file provided outlook or other email account has been set up properly.
Keywords: physical properties, mobile
References: None
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Problem Statement: After run, when opening 'Results Window', the transport map does not show correctly.
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Solution: The reason is that the path to the geo sets need to be fixed. Those files are all in the relative path. The followinsg are the procedures to fix it,
1. Right click 'Maps' on the model tree, select 'Set Folder for MapX Files...', select the Maps folder which gets installed in the sample model directory, or if the user saved their geo sets in a different directory, select that one.
2. Right click the .gst file on the model tree, select Fix Internal GST Paths.
3. Open 'Results Window'
Keywords: Results Window
transport
geo
path
map
References: None
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Problem Statement: Stream Cutter does not solve. What do I do?
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Solution: 1. Make sure you have a transfer basis. Double click on the cutter || Transition tab || choose a Transfer basis (usually T-P flash). If no radio button is chosen then bottom of this window will show Transitions Not Ready. The following picture shows the interface.
2. If the Transfer basis is ready but the cutter is not solved: You probably don't have the cutter active. Please check the box to make it Active.
3. If you have number 1 and 2 checked and still the cutter is not solved, you may not have even one common component between the inlet and outlet of the cutter with greater than zero flow. If you have common components between the two streams, then check the flowrates/compositions. At least one common component must be present with a nonzero flowrate.
Keywords: Stream Cutter, does not solve, Transitions not ready
References: None
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Problem Statement: Can Aspen HYSYS predict the composition of combustion gases?
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Solution: By using the Gibbs reactor, Aspen HYSYS can predict the composition of exhaust gases resulting from the combustion of fuel gas. For this, it is required to define the composition of the fuel gas, as well as the expected combustion products, like CO, CO2, NOX, etc.
The Gibbs reactor calculates the outlet composition such that the phase and chemical equilibrium of the outlet streams are attained. At equilibrium, Gibbs free energy of the reacting system is at a minimum and is used to calculate the product mixture composition.
The Gibbs reactor in Aspen HYSYS is based on the chemical equilibrium theory that can be found in: Smith, J.M., H.C. Van Ness and M.M. Abbot, Introduction to Chemical Engineering Thermodynamics, 5th edition, McGraw-Hill, 1996. Chapter 12. Chemical Reactions.
For example, 1000 kg/h of fuel gas having the following composition:
CH4 = 80 mole%
C2H6 = 15 mole%
C3H8 = 5 mole%
With a 15% of excess air for combustion and keeping the reaction at 900oC, Aspen HYSYS predicts the following composition:
Component
Composition (mole %)
CH4
0.0
C2H6
0.0
C3H8
0.0
O2
2.52
N2
72.71
CO
0.0000003
CO2
8.85
NO
0.00583
NO2
0.000054
H2O
15.92
Enclosed to thisSolution there are two simulation examples, built in Aspen HYSYS 3.2 (S118546_32.hsc) and Aspen HYSYS 2004.2 (S118546_20042.hsc).
Keywords: Combustion, Gibbs reactor, Reaction
References: None
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Problem Statement: How do you view and compare static properties in Aspen Properties Mobile?
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Solution: Tap the information button () next to any component to view more details, including the chemical formula, CAS number, list of synonyms, and a list of static properties (molecular weight, critical constants, and other values which are independent of temperature and pressure).
Use the Compare button on the Components screen to view the static properties of the selected components side-by-side in a table.
Tap any property name to view the full name in a dialog box.
Keywords: None
References: None
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Problem Statement: When using the Hayden-O''Connell model at elevated temperatures and pressures, you might encounter a discontinuity in the predicted PVT-behavior and related properties, such as vapor phase densities, fugacity coefficients etc.
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Solution: The discontinuity is caused by an automatic constraint mechanism which steps in any time you are trying to use the Hayden-O''Connell model beyond the range of its applicability. This constraint mechanism will recalculate the vapor phase molar volume. Hence, the effect on density and other derived properties.
Applicability and limitations of the Hayden-O''Connell model
The model is a second order virial equation-of-state which is valid up to densities of about one half the critical density. In terms of pressure, the range of validity is approximately:
PRES <= T/2 * PCMIX/TCMIX
where
PRES : upper pressure limit
T : system temperature
PCMIX: pseudo critical pressure for a mixture calculated using a mole fraction average of the pure component critical pressures TCMIX: pseudo critical temperature for a mixture calculated using a mole fraction average of the pure component critical temperatures
What the constraint mechanism does
If the system pressure (P) is higher than the threshold value (PRES), the vapor phase molar volume will be calculated using PRES instead of P:
VCALC = R*T/PRES + B
where
VCALC: calculated molar volume
R : gas constant
B : second virial coefficient
PRES : calculated pressure (= T/2 * PCMIX/TCMIX)
A message will be printed to the Control Panel, informing you about the activation of the constraint mechanism:
WARNING IN PHYSICAL PROPERTY SYSTEM WHILE GENERATING PROP-TABLE: RHO
EQUATION OF STATE MODEL ESHOC
SPECIFIED PRESSURE OF 0.59918E+07 IS TOO HIGH
TEMPERATURE = 507.15, VOLUME CONSTRAINED TO 0.541
Please note that because the Hayden-O''Connell model can only be used in conjunction with an activity coefficient model in Aspen Plus or Aspen Properties, limitations of that activity coefficient model with respect to the valid presssure/temperature and composition range also apply.
Keywords: Hayden-O?Connell
volume
constrained
References: None
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Problem Statement: Why does my column not converge if I turn the solver on inside Column Environment, but if I do the same in the main PFD it converges?
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Solution: When you turn the solver on in the column environment you are running the column solver only.. In this scenario, you can run into two situations; one in which the column will converge, and a second in which it will not.
Scenario 1 - No product streams interact with any feed streams outside the column environment:
In this scenario, the column solver has no problem converging the column independently. The attached simulation solvescase.hsc is an example of this scenario. The file does not have any feed-product heat exchangers or any other external interaction. If you go to column environment and turn the solver on, the column will converge.
Scenario 2 - Product and feed streams are interdependent outside the column environment:
One example of this might be when one of the product streams from the column exchanges heat with one of the feed streams. In this scenario, the product stream's conditions must be available in the main PFD to solve the heat exchanger. The feed stream is then re-calculated and returned to the column environment to re-solve the column. Since you are running only column solver (and main solver is on hold) the column feed does not have enough information to solve and the column becomes un-converged. The attached simulation unsolvedcase.hsc is an example of this scenario. This file has one product stream preheating one feed stream. If you go to the column environment and turn the solver on, the column will not converge.
Keywords: column, environment, solver, converge, green, red, light, solve
References: None
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Problem Statement: How to access the Aspen Properties functions in MS Excel 2007?
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Solution: In order to get the Aspen Properties function in MS Excel 2007, you need to add the Aspen Properties Excel 'Add-in' following the steps given below.
1. Click on MS Office button (colored button upper left hand corner of the Excel file, next to save button) II Excel options II Add-ins II Manage 'Excel add-ins' II Click on 'GO'
2. Browse for Aspen Properties.xla file (path example - C:\Program Files\AspenTech\Aspen Properties V7.1\ Engine\ xeq\ AspenProperties.xla) and click OK.
This should add the Aspen Properties Excel Calculator in the Excel file and the Aspen Properties functions will be available. User can test this by clicking on any cell in the Excel worksheet II Click on 'Insert function' fx icon from Formulas tab II Insert Function, here user can see 'Aspen Properties' in 'select a category' drag down option.
Keywords: Aspen Properties Excel Calculator, Excel 2007
References: None
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Problem Statement: Why can't I close my case using Ctrl+Z? This used to work in previous versions of Aspen HYSYS.
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Solution: New in Aspen HYSYS 2006.5, Ctrl+J was added as a shortcut key to close simulation cases. The old shortcut key used for this purpose (Ctrl+Z) is currently used for for the ?Undo? feature, in accordance with Microsoft standards.
Keywords: shortcut, short, cut, hotkey, hot, key, close, case
References: None
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Problem Statement: What's new in version 2006 for Expander Simulation?
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Solution: In versions of HYSYS prior to HYSYS 2006, Performance curves for expanders could only be specified in terms of Volume Flow vs Head
Entering data in this form required the user to convert from the data format typically provided by expander vendors as Mass Flow vs Shaft Power. The need to perform this conversion is obviously inconvenient and prone to introducing errors, so in Aspen HYSYS 2006, an option to enter the expander curve data in Mass Flow vs Shaft Power has been added.
When creating a new expander operation, prior to entering the curves for the expander, the Basis for Flow (Volume or Mass) and Performance (Head or Power) can be selected. You can make these selections on the Rating tab page of the Expander Property View. Once a curve is created, the Performance and Flow basis can no longer be changed as conversion between bases is not supported.
Attached file contains a recorded demo. It shows exactly what mentioned above. Please note that this file is over 13MB in size. If you are interested in download and play it, you are advised to check with your system administrator first to see if such a large file is allowed for your system.
Keywords: what's new, v2006, expander
References: None
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Problem Statement: How do I model a batch process in Aspen HYSYS?
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Solution: A batch process can be modeled with Aspen HYSYS by leveraging specific features and capabilities available in Aspen HYSYS Dynamics. For example, the Event Scheduler can be used to trigger the start-up and shutdown sequences related to your batch process. For more details on the capabilities and features of Aspen HYSYS Dynamics, please consult the Dynamic Modeling guide available via the Documentation link on the support website. Chapter 2 in the Dynamic Modeling guide (Dynamic Tools) contains an excellent example on how to set up the Event Scheduler.
Keywords: batch, dynamic, dynamics, event, schedule, scheduler
References: None
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Problem Statement: How do I subcool a stream?
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Solution: Add the attached user variable 'subcool.huv' to a stream.
The 'subcool.huv' user variable will set the temperature of a stream such that it is subcooled by the amount you specify in the user variable 'Worksheet | Uservariables | Subcooling'. For a pure water stream at atmospheric pressure where you set it to 5?C you would get 95?C as a stream temperature.
Keywords: Subcool, user variable, Ole, Automation
References: None
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Problem Statement: Which versions of Aspen FCC are compatible with Windows 2000?
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Solution: Aspen FCC 10.2 DOES NOT WORK WITH WINDOWS 2000 OR OFFICE 2000. It is based on the old RT-Opt 10 software which never ran on 2000.
Aspen FCC 11.1 will support NT and 2000. Please note that we support Office 97 on NT and Office 2000 on Windows 2000. There will be no mixing and matching of Office versions with OS versions.
Keywords:
References: None
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Problem Statement: What are the advantages and disadvantages of installing the Aspen Properties Enterprise Databanks (APED) on a central SQL server and not installing the databanks on each workstation in an organization?
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Solution: Accessing data from the central server will be slower than the local database, plus the added cost of administering it centrally. The benefits lie in the fact that company-specific databases can be centrally created, controlled and deployed thus ensuring that all users and applications that need them have access to the same up-to-date data.
The administrator of the central database server can setup users and privileges to control access of their users as they see fit (e.g., read-only or read/write). Keeping all data centrally can also reduce the cost of supporting databases on each individual PC.
One has to consider the needs. If you do not have in-house or company-specific database, there is not a compelling reason to install the databases on a central server. The standard installation of Aspen Plus, installs everything that you need to run/use the database and there is not much to gain from putting the databases on a central server, except to save some disc space.
To install the database on the SQL server in version 2006, you have to install the entire Aspen Plus product, even though you really only need the database files. In Aspen Plus version 2006.5 there is an option to allow you to install only the database files.
Keywords: APED, Aspen Properties Enterprise Databanks, SQL, central server
References: None
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Problem Statement: How do I add the Energy Stream and Composition tabs to my workbook so that they are always present when I open a new case?
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Solution: You can add a composition tab to the workbook by going the workbook menu at the top of your program (only available with the workbook open) and choosing Setup. This will bring up a window with the heading Workbook Tabs on the left. Press the Add button. A window displaying all the default workbook tabs is shown. Select Material Streams and press OK. This will create a tab called Material Streams 2. You can change the name to Compositions. Go to the Variable section on the Setup window and highlight all the variables and press Delete (you don't want these variables). Then, press Add under variables. Choose Component MoleFrac and the radio button All. Compositions for all components will now be shown for all streams. For energy streams, follow the same procedure to add a workbook tab but instead of choosing Material Streams, choose Energy Streams instead.
The file that controls what the default workbook looks like is called hysys.wrk and it can be found in the HYSYS root directory. To ensure that all cases have all four tabs in the workbook, export the workbook file that you make by following the above procedure. Move the existing hysys.wrk to another directory and put your new .wrk file in the root directory instead. Rename your new one as HYSYS.wrk. HYSYS will always use the hysys.wrk file in a new case.
Keywords: workbook, energy stream, hysys.wrk, compositions, new case
References: None
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Problem Statement: Why I am getting an error that says Unable to Load Extension Server?
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Solution: The error message is shown in the following image:
This error message refers to the fact that the simulation case has been opened uses an Aspen HYSYS extension that is not registered on the current machine. Aspen HYSYS extensions are external pieces of code (in the form of a DLL) that must be registered locally in order to be used within Aspen HYSYS.
To resolve this problem, you will need to identify the missing extension(s), and register the corresponding *.dll and *.edf files. If the extension has been supplied by Aspen Technology, they requisite files can be down loaded from our support web site at http://support.aspentech.com. After you have registered the correct extension(s), the error message(s) should no longer appear (you will only have to register an extension once, as this results in a permanent change to your registry). Note that after registering the missing extension(s), you may need to restart Aspen HYSYS.
Please refer toSolution 120871 for a more detailed description of how to register an extension.
Keywords: error, unable, extension, server, load
References: None
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Problem Statement: How can a user customize the appearance of sets and tables in SCM?
|
Solution: Sets and tables appearance may be customized, including the Information Table (INFO) and the Error Messages Table (ERROR).
To perform this action, open SCM and select OPTIONS / SYSTEM from the toolbar. Then, click on the tab EDITORS.
The EDITORS window contains various features that can be modified in order to change the appearance of sets and tables. To change the fonts or colors of sets and tables for example, click on the list box button and select what part of the tables or sets has to be modified (i.e. Cell Foreground, Cell Background, Header,?). Then, click on the 3 dots (...) button located to the right of the list box button to open the color or font list.
Please note that any modification performed by a user will be applied to all sets and tables for all case files.
Additional information about the features of sets and tables that can be modified is available in the SCM Online Help (Description of Editor Window Display Settings).
Keywords: None
References: None
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Problem Statement: The table for the UNIFPS parameter used in the PSRK Equation of State requests Aij, Aji,Bij,Bji, Cij,and Cji; however, there is no documentation regarding the temperature dependency.
|
Solution: The UNIFPS parameter has the following dependence:
tau = exp -(UNIFPS(1)/T + UNIFPS(2) + UNIFPS(3)*T)
This parameter is used in a special UNIFAC model (model name = GMUFPSRK) which is used in the PSRK property method. This property method uses the PSRK equation of state, which uses a mixing rule that incorporates activity coefficient model. By default the GMUFPSRK activity coefficient model is used. The user can change it to use other model, such as NRTL.
The GMUFPSRK model is similar to the standard UNIFAC (vapor-liquid) model, except that the group binary interaction parameters (UNIFPS) are temperature dependent and there are special groups (3800-3870) defined for light gases such as CO2, H2, NH3, N2, O2, CO, H2S, and Argon. This model shares a large number of interaction parameters with the standard UNIFAC model.
Keywords: None
References: : CQ00302674
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Problem Statement: What is Aspen Solubility Modeler?
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Solution: Aspen Solubility Modeler is a new part of Aspen Properties introduced in V7.0 as part of the Process Development module. It consists of a series of Excel workbooks which were developed using Aspen Properties Excel Add-In and Aspen Properties. Each workbook is associated with an Aspen Properties backup file.
The following features are provided:
Simplified NRTLSAC package of Aspen Solubility Modeler?
NRTLSAC package of Aspen Solubility Modeler?
NRTLSAC package (including residue curve calculation) of Aspen Solubility Modeler?
Excipient NRTLSAC package of Aspen Solubility Modeler?
eNRTLSAC Pure Solvent package of Aspen Solubility Modeler?
eNRTLSAC Binary Solvents package of Aspen Solubility Modeler?
pH Profiling package of Aspen Solubility Modeler?
A package here means a set of Excel files and an Aspen Properties file that can be used together to get the NRTLSAC/eNRTLSAC parameters of a drug through regression of experimental data and to predict the drug solubility based on the regressed NRTLSAC/eNRTLSAC parameters.
The following files will be delivered and installed when Aspen Properties is installed
\\Program Files\AspenTech\Aspen Solubility Modeler V7.0
No Start menu shortcut will be created when these files are installed.
When the Process Development module is installed and the Solubility Modeler option is selected, then the Start menu short cut will be created for
Start | Programs | AspenTech | Process Development V7.0 | Aspen Solubility Modeler
Instruction to open an Excel workbook with Aspen Solubility Modeler
A package is distributed as a subfolder under Aspen Solubility Modeler; it usually contains one workbook for performing parameter data regression and one or two workbooks for solubility calculations.
Before opening any workbook with Aspen Solubility Modeler, follow the steps below to add Aspen Properties V7.0 Excel Add-In to Microsoft Excel:
1) Open an empty excel, go to Tools->Add-Ins?
2) From Add-Ins?dialog, click on ?Browse?? to locate AspenProperties.xla delivered with Aspen Properties V7.0 at \\Program Files\AspenTech\Aspen Properties V7.0\Engine\xeq. Click on ?OK? to add Aspen Properties to Add-Ins? dialog:
3) Click on OK to quit the dialog.Aspen will be created on the menu bar:
4) Quit Excel.
5) Now go to Aspen Solubility Modeler V7.0, then to a subfolder for a package. Let?s use Simplified NRTLSAC package as an example; it has a workbook for parameter data regression called Drug_NRTLSAC.xls and another workbook for solubility calculations called Drug_Calculations_130_Solvents.xls.
6) For the purpose of demonstration, double click on Drug_Calculations_130_Solvents.xls and Security Warning will be pop up. To continue, Enable Macros button must be clicked to insure the license check-out:
7) Another warning from Microsoft Excel may be pop up. Since this warning is not related to Aspen Solubility Modeler, Don't Update button should be clicked:
8) Some of workbooks for solubility calculations adopt ActiveX controls to perform special calculations such as property analysis and phase diagram; it will have the following warning and Yes button should be clicked:
9) When the network or local computer is slow, it may take as long as a few minutes to checkout the license or initialize ActiveX controls; the following warning may pop up several times before the workbook is completely open:
Keywords: None
References: None
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Problem Statement: When entering PROP-DATA for asymmetric binary parameter such as HENRY for a legacy databank using DFMS, do you need to enter both the ij and ji values if one set is meaningless?
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Solution: For asymmetric parameters where only one of the two parameters is available or meaningful, use a value of missing (1e35) or an asterisk (*) in place of the missing value. For example, for Henry constants only one compound in many pairs is plausibly the solvent, so one of the two values is meaningless. In this case, you would have a value and an asterisk for each pair.
For example, there are 7 elements for HENRY for each pair of components (i,j), the 8th element is for the reverse (j,i) pair. Since this set is meaningless, a value of missing (1e35) should be entered. The value of 1e35 is a flag for MISSING and should be entered as exactly this value.
Â
Using a simulation with components CO2 and H2O and exporting a .dfm file to create a file for an Aspen Properties Enterprise Database (APED), generates the following input (notice the value of the eighth element is 0.100000E+36):
PROP-LISTÂ Â Â Â Â Â Â Â Â Â Â Â Â Â HENRYÂ Â Â Â 1
  BPVAL 'CO2        ' 'H2O        '  171.378     -8741.55     -21.6690   Â
                                       0.110259E-02  273.000      353.000   Â
                                        0.00000   Â
                                       0.100000E+36  0.00000      0.00000   Â
                                        0.00000      273.000      353.000   Â
                                        0.00000   Â
 Â
NEW-PROP
          HENRY    7
Keywords: APED
References: None
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Problem Statement: How do you configure and view calculations in Aspen Properties Mobile?
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Solution: The current version (V7.2.1) of Aspen Properties Mobile is designed to calculate and report pure component properties for one or more species. Thermophysical and transport properties can be calculated for the liquid, vapor, or solid phases.
Aspen Properties Mobile offers a number of calculation methods including equations of state such as the ideal gas law, Peng-Robinson, and Redlich-Kwong-Soave. Aspen Properties Mobile also includes highly accurate methods for specific systems, including the IAPWS 1995 steam tables, GERG 2008 model for natural gas systems, and the NIST
Keywords: None
References: Fluid (Refprop) method for common heat transfer fluids.
Temperature-dependent properties are displayed in tables. They can also be viewed in interactive charts.
Select the property calculation method at the top of the screen. Tap on the method name to see a list of all available methods. You can tap on the information button on the Method screen to view the full name and a short description of the property method.
Use the middle section of the Calculation screen to select the property, units, phase, and basis. Tap the name of the property to view a list of all property types. Tap the desired property to select it.
Enter the pressure, temperature limits, and number of points at the bottom of the Calculation screen.
After configuring the property calculation options, tap the Results icon on the Navigation Bar at the lower right side of the screen. There will be a short delay while the client application sends data to the server and retrieves calculation results. The delay depends on the speed of your wireless internet connection - the calculations on the server are extremely rapid.
You can use the Property, Phase, and Units buttons to change the calculation parameters.
Use the Plot button to create an interactive chart. You can rotate your iPhone or iPod Touch to change the aspect ratio of the plot.
The interactive chart can be zoomed using standard pinching motions, or panned using a dragging motion.
You can tap on the temperature field to enter a specific temperature using the on-screen keyboard. Alternately, drag the slider control to change the selected temperature. The property values are displayed numerically at the top of the chart. These correspond to the selected temperature. If you change the temperature slider there will be a short delay while the application requests calculations from the server. Use pinch motions to zoom in/out Use drag motions to pan
Use the Email button to mail the results as a comma separated value (CSV) file.
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Problem Statement: How does one delete references to extension unit operations in a case where the extension units themselves are not registered?
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Solution: The situation arises when a simulation file is copied from one machine to another but the latter machine does not have the same extensions registered as the first machine.Typically users would register the required extensions on the second machine as well, however; occasionally it may be advantageous to get the model running without using those extensions. In this case, the references to those extensions need to be deleted. However, since those extensions do not show up on the PFD (or the Unit Ops page of the workbook), the user simply does not have a readily available method to delete them. In order to accomplish this, following these steps:
1. Create a work book page of object type Extension Unit Operation via the Workbook | Setup menu.
2. All extension operations should now be listed on a separate Workbook page.
3. Click on the delete key to remove them one by one via the Workbook page.
4. Save the case.
Keywords: extensions, extension operation, workbook
References: None
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Problem Statement: What is the difference between between the DBR Amine Package and the Amine Pkg available in Aspen HYSYS?
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Solution: Both property packages are based on AMSIM, which is an amine simulator developed by DBR & Associates. The DBR Amine Package, which was introduced in Aspen HYSYS 2004, uses the latest version of AMSIM (currently v7.3) whereas the Amine Pkg uses an earlier version of AMSIM (v7.0). Although the Amine Pkg has not been updated to use the most current version of AMSIM, it is maintained within Aspen HYSYS in order to achieve consistency and compatibility with previous releases.
As a result of using the latest version of AMSIM as its basis, the DBR Amines Package contains both physical solvent (i.e. DEPG) and chemical solvent (i.e. MEA, DEA, MDEA, DIPA, DGA and TEA) models, whereas the Amine Pkg can only represent chemical solvents. As well, the DBR Amine Package has the option of using a variety of flash routines (including the AMSIM flash), while the Amine Pkg uses the deafult HYSYS flash method.
Internally, the primary difference between the Amine Pkg and the DBR Amine Package is the fact that the latter is a COMThermo property package. COMThermo is a thermodynamic calculation framework which makes it possible to develop independent, extensible, customizable and encapsulated thermodynamic calculation modules. COMThermo property packages give you more flexibility over standard packages because you can select specific methods to be used in the calculation of certain properties (i.e. you can select which thermodynamic model is used to calculate viscosity regardless of the VLE model selected.
Keywords: amine, package, DBR, pkg, difference, AMSIM
References: None
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Problem Statement: NRTLSAC spreadsheets don't work with new AspenProperties.xla when using Aspen Solubility Modeler.
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Solution: V7.0 will deliver a new product called Aspen Solubility Modeler. The product consists of a set of Microsoft Excel spreadsheets and Aspen Properties files configured to allow customers to quickly and easily calculate the solubility information using the power of the Aspen Properties engine. When a spreadsheet is executed, it will consume two (2) licenses: the Solubility_Modeler license and the Aspen_Properties license.
However, these spreadsheets have been developed since 2006 release and have been distributed to customers without charge on individual request. For those customers who've already had some (if not all) of the spreadsheets from 2006 or 2006.5, they can still run these spreadsheets with V7.0 without consuming the solubility modeler license only if they keep 2006 or 2006.5 release when they install V7.0. Otherwise, those spreadsheets from 2006 or 2006.5 may not work with V7.0 alone due to some references that may not be transferred properly from 2006 or 2006.5 to V7.0. For example, pfsplotv210.ocx is the ocx controlused to draw the ternary diagram in the calculation spreadsheets in 2006.5. V7.0 will deliver pfsplotv220.ocx. This reference cannot be transferred automatically from 2006.5 to V7.0.
Keywords: None
References: None
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Problem Statement: Why can I not see the current data in my strip chart? The integrator is running, but the plot does not appear to be updating properly.
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Solution: Depending upon the state of the simulation, it is possible that the low bounds for the plot may have been set such that no current data can be plotted on the chart. To rectify this, right click on the plot and select Graph Control. Next, click on the Time Axis pagetab, and change the Low Time and High Time accordingly. Alternatively, you can simply left click on the Low Time Axis Control (i.e. the small red triangle near the bottom left corner of the plot) and the time axis will be automatically scaled. In the figure below, the low time for the strip chart has been set for approximately -180 hours (with an interval of roughly 184 hours), so very little of the real time information is being plotted.
Note that you may also want to increase the number of data points that are maintained by the stripchart so that you do not lose any desired historical information (by default this is set at 300). To do this, open the databook (i.e. select Tools | Databook from the main menu) then click on the SETUP button found on the Strip Charts pagetab. In the ensuing Logger Set-Up window, change the Logger Size (# Samples) to the required value.
Keywords: databook, data, logger, stripchart, chart, plot, graph, dynamics
References: None
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Problem Statement: How do I provide specifications for the MASSBAL equation based solver?
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Solution: Specifications used for the MASSBAL equation-based solver can be populated on the Parameters page. The Create Specs button is useful in that it gives the user a good start. What it does is check for unit operations/streams (except SOURCE streams) with specified values and add them to the list of specifications.
Keywords: MASSBAL, populate specifications
References: None
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Problem Statement: Why does the status bar on my heat exchanger read insensitive?
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Solution: The insensitive message in the status bar of a heat exchanger is the equivalent of having a column not converging. At one point during the iterations, the error is not changing anymore.
To work around this problem, the specs for the heat exchanger can be changed to first solve (converge) the heat exchanger. Then, you can try to solve the heat exchanger using the desired specs, starting from a convergedSolution.
Keywords:
References: None
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Problem Statement: Can I see the results for other variables in the Case Study which are not selected as dependent variables?
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Solution: For each calculated state, the Databook tracks only the dependent variables, thus it is not possible to see the results for other process variables that have not been selected as dependent variables in the Case Study.
If desired, it is possible to add more dependent variables even after running the Case Study, however you will need to re-run the Case Study again in order to generate the results for the newly added variables.
Keywords: case, study, results, dependent, variable, add, data, databook
References: None
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Problem Statement: How can I access mixed phase (combined liquid) properties via OLE Automation?
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Solution: The HYSYS Fluid object offers properties (.VapourPhase, .LightLiquidPhase, .HeavyLiquidPhase) which can be used to get objects, of type FluidPhase, for the vapour, light and heavy (usually water) liquid phases of the stream. There is no direct way to obtain a combined liquid phase object. However, this can be done by mixing together Fluid objects for the light and heavy phases in the stream. The code section below illustrates this:
'Initialise the fluid objects
'- here hyStream is a ProcessStream object representing a stream with two liquid phases
' and hyOverallFluid and hyCombLiq are objects of type Fluid
Set hyOverallFluid = hyStream.DuplicateFluid
Set hyCombLiq = hyStream.DuplicateFluid
hyCombLiq.Erase
'Get the light liquid phase into the 'combined' liquid object
hyOverallFluid.ExtractPhase ptLiquidPhase, hyCombLiq
'Mix in the heavy liquid
hyCombLiq.AddPhase hyOverallFluid.HeavyLiquidPhase
'Do a flash
hyCombLiq.EquilibriumFlash
'Use combined liquid properies
dblMoleFlow = hyCombLiq.MolarFlow.GetValue(kgmole/h)
In practice error checking would be needed to make sure that the source stream has two liquid phases. The attached Excel example file illustrates how this might be done.
There is also an extra complication: some properties which are available for a FluidPhase object (for example: Cp/Cv (Gamma), Kinematic Viscosity, Thermal Conductivity, Viscosity) are not available for the HYSYS Fluid object. In order to obtain these properties it is necessary to use a HYSYS backdoor variable method; this is also illustrated in the attached file.
For troubleshooting advice on common HYSYS / OLE Automation errors, seeSolution #112361.
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 AspenTech products. Users are strongly encouraged to check performance and results carefully and, by downloading, agree to assume all risk related to the use these examples. We invite any feedback through the normal support channel at [email protected].
Keywords: Mixed Phase, Combined Liquid, ExtractPhase, AddPhase, Fluid, FluidPhase, Backdoor
References: None
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Problem Statement: The default calculation mode inside Aspen Properties is Property Analysis. How do you change the run type to something else such as Data Regression or Assay Data Analysis?
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Solution: If you want to perform Data Regression, Estimation or Assay Data Analysis. Aspen Properties will allow you to enter the data, but the regression forms are not enabled by default. Go to the Tools pull-down menu and change the Calculation type to Regression. You will see Regression in the top frame of options in the Tools items. Then the Regression form will be exposed. In Aspen Plus you would change the run type on the Setup | Specifications form. In Aspen Properties, you change the run type from the Tools menu.
Keywords: Run type, regression, Aspen Properties, calculations, TOOLS
References: None
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Problem Statement: How can I eliminate the message Error in retrieving the list of available PVT Engines?
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Solution: A HYSYS Upstream license is needed to access the features and functionality of the PVT Environment. If you don't have the appropriate license for HYSYS Upstream, you will receive the message Error in retrieving the list of available PVT Engines if you attempt to access these features. Note that the HYSYS Crude license only enables the use of the oil characterization feature within the HYSYS Oil Environment.
To remove the aforementioned error without acquiring a HYSYS Upstream license, you will need to delete all entered PVT information. To do this, navigate to the Basis Manager and click the Enter PVT Environment button found near the bottom left corner of the Simulation Basis Manager window. Select each added PVT entry on the Engine Setup pagetab and press the Remove button.
For more information on the PVT Environment, refer toSolution document 119955.
Keywords: error, PVT, engines, PVT engines, available
References: None
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Problem Statement: How do you select components in Aspen Properties Mobile?
|
Solution: To select components, follow these steps:
(1) Tap the Components icon on the navigation bar at the bottom of the screen to start selecting components (chemical species).
(2) Tap the ?+? button on the upper left side of the screen to open the Search Components screen
(3) Select the search mode - you can search by name, chemical formula, for CAS (Chemical Abstract Service) registry number. Start typing the search target using the on-screen keyboard. As you type the application will provide a list of components that match your search string. Tap any component name to select or deselect the component.
(4) Tap to view static properties of selected components.
(5) Tap the Done button to add the selected components to the component list.
You can tap the Edit button to select and delete components from the list. You can also repeat the search process to add components to the list.
Aspen Properties Mobile includes access to the Aspen Pure Component Database and the NIST Source database. Together, these databases cover tens of thousands of pure components. In addition, your company may opt to include additional in-house databanks using Aspen Properties Enterprise Database.
Aspen Properties Mobile is not designed for petroleum fluids (pseudo components or assays), polymers, or non-conventional solids such as coal.
Keywords: None
References: None
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Problem Statement: When all parameters are entered after a regression, then regression is executed again the model does not seem to start at the point where the previous regression ended. Why would this happen?
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Solution: When you run a problem containing multiple regressions, the regressed parameter values from one regression are used automatically in the subsequent regressions. However, if you re-run a regression, it may not start at exactly the same point as the previous regression ended, and the residual (RMS and/or SSQ) may be greater. This occurs because:
Different algorithms are used on initial and later iterations. By default, the Deming algorithm is used for 20 iterations, then Britt-Luecke is used. These methods use different objective functions that lead to different residual calculations. You can change these algorithms on the Regression | Algorithm sheet.
The values for adjusted variables (those with non-zero standard deviations in the regression) are not saved, and may not start at the same values as they had in the previous run. Initial values can be specified on the Regression | Parameters sheet.
Keywords: DRS
Data Regression
References: : CQ00476733
|
Problem Statement: Is it possible to automatically save a converged simulation prior to entering dynamic mode?
|
Solution: New in Aspen HYSYS 2006, you can set Aspen HYSYS to save the Steady State case automatically before you switch the case to Dynamics. This option can be set via the Simulation | Dynamics pagetab as shown in the figure below:
With this checkbox active, HYSYS will automatically save a copy of your steady state case before switching to Dynamics. The saved case will have the same name as the original, however Aspen HYSYS will append '_SS#' to the end of the filename, where '#' is a number. The primary purpose of this feature is to prevent the loss of converged results when a case is switched back to Steady State mode from Dynamic mode.
Keywords: dynamics, steady, state, save, auto, automatic, automatically, preferences, option
References: None
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Problem Statement: I have written some VB code to launch Aspen HYSYS, but when I run the code, the Aspen HYSYS splash screen appears, and then nothing else. Why did Aspen HYSYS not open?
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Solution: If you check in your Task Manager, you should see hysys.exe running in the list of Processes. This means that Aspen HYSYS did open and is running. It is just that it is running in invisible mode. You will need to add the following line into your code to make the running instance of Aspen HYSYS visible:
hyApp.Visible = True
Keywords: excel, vb, visual basic, code, running, invisible, visible
References: None
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Problem Statement: How do you manually restore the APV80, NISTV80, and FACTV80 databases in Aspen Properties Database?
Occasionally from installation problems or other changes in the Aspen Properties Enterprise Database, the APV, NISTV and FACTV databases provided by AspenTech will not be created in the Aspen Properties Database Manager and therefore will not be available to use in Aspen Plus, Aspen HYSYS and other Aspen Tech software programs. If you try to restore or register the databases in the Aspen Properties Database Manager and the procedure fails then restore the databases manually.
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Solution: This knowledge base describes how to manually restore the Aspen Engineering Suite (AES) V8.0 databases on Windows XP. If you need to restore AES V7.xA databases seeSolution 124819 for details.
First check for the existence of APV80.MDF, NISTV80.MDF and FACTV80.MDF and corresponding *.LDF files in the folder:
C:\Documents and Settings\All Users\Application Data\AspenTech\APED V80\ (Windows XP)
If there are files here, back them up by copying them to another folder, then delete the files in the folder named above.
To restore the databases, execute the following commands from a DOS window:
(For your convenience, attached to thisSolution is the batch file for all the commands below)
set DatabaseFolder=C:\Program Files\AspenTech\APrSystem V8.0\PropertiesDatabase\Database
rem Set your SQL server name below in machineName\instanceName format
rem If you have SQLExpress installed do not change following line.
rem Note that .\ refers to This machine.A If the server is elsewhere, give its actual name.
set ServerName=.\SQLEXPRESS
RemA A A A A A A A A A A A A A A A A A A use the following 2 commands to add apeduser account
sqlcmd -E -S %ServerName% -Q EXECUTE SP_ADDLOGIN 'apeduser', 'Aproperty88#', 'master'
sqlcmd -E -S %ServerName% -Q EXECUTE SP_ADDSRVROLEMEMBER 'apeduser2', 'sysadmin'
RemA A A A A A A A A A A A A A A A A A A Drop the current databases if available
sqlcmd -U apeduser -P Aprop100 -S %ServerName% -Q Drop Database APV80
sqlcmd -U apeduser -P Aprop100 -S %ServerName% -Q Drop Database NISTV80
sqlcmd -U apeduser -P Aprop100 -S %ServerName% -Q Drop Database FACTV80
RemA A A A A A A A A A A A A A A A A A A Add the 3 databases used
sqlcmd -U apeduser -P Aprop100 -S %ServerName% -Q restore database APV80A A from disk='%DatabaseFolder%\APV80'A A WITH MOVE 'APV80'A A TO 'c:\Documents and Settings\All Users\Application Data\AspenTech\APED V8.0\APV80.MDF',A A MOVE 'APV80_Log'A A TO 'c:\Documents and Settings\All Users\Application Data\AspenTech\APED V8.0\APV80_Log.LDF'
sqlcmd -U apeduser -P Aprop100 -S %ServerName% -Q restore database NISTV80 from disk='%DatabaseFolder%\NISTV80' WITH MOVE 'NISTV80' TO 'c:\Documents and Settings\All Users\Application Data\AspenTech\APED V8.0\NISTV80.MDF', MOVE 'NISTV80_Log' TO 'c:\Documents and Settings\All Users\Application Data\AspenTech\APED V8.0\NISTV80_Log.LDF'
sqlcmd -U apeduser -P Aprop100 -S %ServerName% -Q restore database FACTV80 from disk='%DatabaseFolder%\FACTV80' WITH MOVE 'FACTV80' TO 'c:\Documents and Settings\All Users\Application Data\AspenTech\APED V8.0\FACTV80.MDF', MOVE 'FACTV80_Log' TO 'c:\Documents and Settings\All Users\Application Data\AspenTech\APED V8.0\FACTV80_Log.LDF'
In the code quoted above, you may need to change the following:
1. set DatabaseFolder: Change the APrSystem foldera??s version to your version, and to C:\Program
Files (x86) if the OS is 64bit.
2. set ServerName: Add your SQL Server Service name. This located in Windows Services under SQL Server. The ./ means This Machine.
(Leave a??.\SQLEXPRESSa?? if you are using the SQL Server Express edition that was included on the Aspen DVD).
Again,this database restore procedure is also available in the attached batch file that can be run in a DOS window. You can modify this file for the above mentioned features.
Keywords: Aspen Properties Database Configuration, Manual Database Restoration for AES V8.0, Batch file
References: None
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Problem Statement: Where can I find stream and other results calculated by the MASSBAL subflowsheet?
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Solution: In MASSBAL flowsheet mode, the Massbal flowsheet writes out calculated values to streams and pertinent unit operations. Users can also look on the Results page in the MASSBAL Op (PH1 and PH2 files) for any other results.
In Sequential Modular flowsheet mode, the MASSBAL flowsheet solves using the HYSYS solver. You have the option of running MASSBAL on the existing operations. The only difference is that the stream results of MASSBAL won't be printed to any of the streams in Sequential Modular mode.
Keywords: MASSBAL stream calculated results
References: None
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Problem Statement: I have specified all inlet streams and have specified nothing in the outlet streams. Why am I getting a consistency error?
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Solution: In this type of scenario, it is likely that a stream variable has been specified in both the main PFD and in the column environment. For example, the pressure has been specified in the feed stream in the main PFD and also in the feed stream in the column environment (i.e. the same pressure has been specified twice).
To eliminate this error, delete the extraneous specification from the column environment, as the main flowsheet will provide the value to the column environment.
Keywords: consistency, error, column, message, solver
References: None
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Problem Statement: Is it possible to call Aspen Properties Excel Add-In functions from VBA?
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Solution: No, you cannot call the Aspen Properties Excel Add-In functions (such as a TPFlash function) from VBA. These functions are Private and can only be called by the Add-In itself.
In order to develop some applications (or engineering calculations) using the Aspen Properties Excel Add-In that requires the ability to set input, get output etc. using VBA, users should use the Aspen Properties Excel Add-In to define the components, properties, and various input and functions (flash, etc) that are needed. Then they can write some VBA code that deposits values to the appropriate cells and retrievse results that are needed from other cells. Additional calculations can be made in the VBA code to display the results on the Excel sheet. They can add buttons and other design elements to the Excel sheet as needed.
Keywords: None
References: : CQ00354977
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Problem Statement: Why IAPWS-97 is not implemented in Aspen Properties?
Isn't the IAPWS-97 better than IAPWS-95?
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Solution: The IAPWS-95 formulation is actually a better formulation to use, in particular in process simulation. It provides a reliable, continuous property values and derivatives with respect to temperature and pressure. While the 95 version is a rigorous equation of state (Helmholtz energy-based), just like the steam NBS equation and any traditional equations of state, the 97 version consists of a large number of empirical equations that are curve-fitted to the data to represent different regions of the valid temperature and pressure domain. For example, one equation might be used for the subcritical region for liquid properties and another equation is used for a certain portion of the critical region and so on. The main advantage of the 97 version is the speed of calculations. However, a serious drawback when used in Aspen Plus and Aspen HYSYS is the lack of continuity of property when going from one region of the curve-fit to another. The derivatives can also be very wrong. In the simulation environment, we also need ?extrapolated? properties, e.g., a vapor property at a given temperature and pressure while in nature (at that temperature and pressure) water does not exist as ?vapor?. In this situation, the 95 formulation will return reasonable and continuous results, while the 97 formation may not. These drawbacks will cause failure of equation oriented (EO) and dynamics simulations. We have seen this problem with the ASME 1967 steam table correlation, which is also a collection of special curve-fit equations.
Therefore, we have implemented the IAPWS-95 formulation and we did not and shall not implement the 97 formulation.
Keywords: IAPWS-95, IAPWS-97, IAPWS, 1995, 1997
References: None
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Problem Statement: The following error message is generated when the calculator is launched:
Error in getting units from Units.dat file in /Engine/xeq. Please check if the file is missing or corrupted.
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Solution: This error occurs when the Aspen Properties Excel Calculator needs to be added to the Excel environment. This is known to occur when using the Lite Client.
To add the Aspen Properties Excel Calculator to the Excel environment:
Open Microsoft Excel 95, 97 or 2000.
Go to the Tools menu and select Add-ins. The Add-ins dialog box appears.
Click on the Browse button, move to the directory ...\Aspen Properties 10.2\Engine\xeq on the file server, locate and select file Aspen Properties.xla. You must respond No when asked whether or not to copy the Excel Add-In file to your local drive. In other words, don''t copy file Aspen Properties.xla to your local drive. A new menu item - Aspen Properties will appear on the main menu bar of Microsoft Excel.
Keywords: Aspen Properties, Excel Calculator, calculator, lite client, installation, units, dat, xla, add-ins
References: None
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Problem Statement: What formats does Aspen HYSYS support when importing oil assay information?
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Solution: Previously, only assays in binary *.oil format could be imported. New in Aspen HYSYS 2006.5, PIMS-generated assay files in *.csv format can be imported directly into the Oil Environment. Since many of the commercial assay generator tools can convert their assay format to PIMS *.csv format, this new feature opens the possibility of importing assays from many third party vendors. Note that Aspen HYSYS does not support detailed petroleum properties (such as sulphur or RON), so when these properties are imported from PIMS, assay values are stored as user curves.
Keywords: oil, manager, import, assay, PIMS, csv, user, property, curve
References: None
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Problem Statement: Are there resources available that contain the measured mixture data (i.e. TXY, PXY, etc.) that went into creating the binary pairs for Aspen Plus/Properties in v7.2. Is there any document or location where users could access this data? Is that data made public?
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Solution: The experimental binary data used to regress the binary parameters in the databanks are not available to customers; however, the NIST ThermoData Engine (NIST-TDE) will have binary data in V7.3 and higher.
Keywords: None
References: None
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Problem Statement: Why doesn't my bubble point match the pure component NBP?
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Solution: For equation of state based models (such as PR or SRK), the bubble point of a pure component is based entirely on the critical properties contained in the Aspen HYSYS component database. Although all equations of state will ultimately use the same pure component input parameters to calculate the bubble point, each thermodynamic model will deviate from the displayed normal boiling point accordingly, as a consequence of the individual differences between the models.
When using an activity coefficient model (such as UNIQUAC) to calculate the VLE for a mixture, the phase distribution for a given component is defined in terms of the vapour phase fugacity and liquid phase activity coefficient. In this context, the vapour pressure used in the calculation of the standard state fugacity is based on the Antoine coefficients specified for the pure component (i.e. on the TDep pagetab of the pure component view):
Thus, when using an activity coefficient model, the predicted bubble point temperature for a pure component at atmospheric pressure will also differ somewhat from the displayed normal boiling point since it is dependent on an entirely different set of data.
Keywords: bubble, dew, point, NBP, pure, component, Antoine
References: None
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Problem Statement: Where did the property package options go?
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Solution: In previous versions of HYSYS, the calculation options available for Property Package were scattered in the SetUp tab. This made it difficult for users to find and select the different calculation methods they want to apply.
To increase the convenience of selection for the desired property package options, all of the options for the Peng-Robinson (and PR derived), SRK (SRK derived) properties packages have been moved to the Parameters tab in Aspen HYSYS 2006.
Rather than a mixture of check boxes and radio buttons, all of the options are available via drop down lists.
Each row in this table corresponds to a check box or radio button in previous versions of Aspen HYSYS. Cases built in prior versions will be recalled with the same options.
The Enthalpy Row corresponds to the EOS Enthalpy Method Specification radio buttons. The Equation of State label has been replace with the label Peng-Robinson Equation.
The Density Row corresponds to the Use EOS Density checkbox. The ?unselected? option is now labeled COSTALD which is the default Aspen HYSYS density method.
The Modify H2 Tc and Pc row corresponds to the Modify H2 Tc and Pc Checkbox.
The Indexed Viscosity row corresponds to the Indexed Viscosity checkbox. The ?unselected? state in labeled ?HYSYS Viscosity?
The Peng-Robinson Options corresponds to the Peng Robinson Options Radio buttons.
A new Volume Translation option has been introduced for PR and SRK in HYSYS 2006. This option appears when the Use EOS Density option is selected. Note that a column of Volume translation parameters appears when Use EOS Density is selected. These values can be used to make corrections to the density value calculated (using EOS) for each component in order to make them match experimental data. If all Volume Translation values are set to zero (as they are by default) the fluid package will behave as if the Use EOS Density option is selected in Aspen HYSYS 2004.2. These corrections can be entered manually or estimated using one of two methods: COSTALD and RACKET. To estimate values, select the preferred method and press the Estimate Vol. Trans button.
Changing the Volume Translation values adjusts only the density of the liquid state and does not affect the vapour fraction or composition of the liquid or vapour phase.
Attached with thisSolution is a quick demo. You are more than welcome to download it and take a look at it.
Keywords: EOS, equation of state, volume translation, Set up, Parameters, view, viscosity, COSTALD, PR, Peng-Robinson, SRK, enthalpy
References: None
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Problem Statement: What is NPSH for a pump?
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Solution: Net Positive Suction Head (NPSH) is an important factor to consider when choosing a pump. Sufficient NPSH is required at the inlet of the pump to prevent the formation of small bubbles in the pump casing which can damage the pump. This is known as cavitation. For a given pump, the Net Positive Suction Head required to prevent cavitation, (NPSHrequired), is a function of the capacity (volumetric flowrate) and speed of the pump. To prevent pump cavitation the NPSHavailable must be greater than the NPSHrequired.
NPSH data can be entered in HYSYS and used in dynamic mode. NPSH curves cannot be used, however, in Steady State mode, although you can calculate the NPSHavailable by opening the pump Rating tab | NPSH page and clicking on the calculate button.
For more information on available NPSH calculations, please seeSolution # 121590
Keywords: NPSH, pump, cavitation, curves
References: None
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Problem Statement: Does Aspen Solubility Modeler support electrolytes calculation with ENRTLSAC property method?
|
Solution: Aspen Solubility Modeler does not support electrolytes. The property method used in Aspen Solubility Modeler is the NRTL-SAC and the databank used is called NRTL-SAC . This databank contains parameters for more than 100 common solvents. This parameter contains a representation of each of these solvents as a combination of the four types of segments used in the NRTL-SAC property method.
The property method ENRLSAC was available in the version V7.0. However, starting from the version V7.1, the Solubility Modeler does not contain this feature anymore.
In Aspen Plus and Aspen Properties, ENRTLSAC and also NRTLSAC are present in the drop down list of the property methods which can be selected in Aspen Plus and Aspen Properties, however they are superceded by the NRTL-SAC, as one can see when hovering them with the mouse (see the image below).
In fact, NRTLSAC and ENRTLSAC are still kept in Aspen Plus and Aspen Properties for the purpose of upward compatibility, but it is recommend not to use them for new simulations. Instead, NRTL-SAC should be used. The NRTL-SAC databank can be selected from Components | Specifications | Enterprise Database sheet.
Keywords: Solubility Modeler, ENRTLSAC, NRTLSAC, NRTL-SAC
References: None
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Problem Statement: When we changed a computer name, Aspen Properties stopped working. How do we fix this?
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Solution: Aspen Properties uses SQL database which by default gets register for the machine name on which you have installed Aspen Properties. When you change computer name to new computer name Aspen Properties still refers to old computer name and that is the reason it stops working.
To solve this problem, all you need to do is register the Aspen Properties database by using Aspen Properties Database Manager application which we can find it from Start menu > Programs > AspenTech > Process ModelingA A > Aspen Properties option.
Once the Aspen Properties Database Manager is open, right click on Aspen Physical Properties Database option and select Register a database option. You need to select Server Name, Login name, Password and Database name in Register a Properties database window.
You will need to register three databases: APXXX, NISTXXX and FACTXXX where XXX can be replaced by version number. You will need to repeat the Database registration process three times. The default Login name and password are apeduser and Aprop100 respectively. You will also need to register any user databases if you have them.
Keywords: computer name, machine name, change name
References: None
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Problem Statement: What is velocity in the slug tool?
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Solution: Velocity in the slug tool is defined as the slug translational velocity. It determines the frequency of the slug fronts but does not determine the liquid flowrate occurring in slugs. Think of a wave travelling round a sports stadium. At any one time there may be 100 people (slug volume) with their hands in the air and the wave is travelling at 10 m/s (slug translational velocity) round the stadium. There is no net lateral movement of people though (zero flowrate).
Keywords: Velocity, translational velocity, Slug Tool
References: None
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Problem Statement: In the Performance tab of the LNG heat exchanger, how Aspen HYSYS calculates the LMTD value, which does not correspond to a calculation based on a overall energy balance.
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Solution: The steady state model of an LNG in Aspen HYSYS is based on the concept of energy integration. Aspen HYSYS generates two composite curves, the cold composite curve combines all cold streams connected to the LNG. The hot composite curve will do the corresponding combination for all hot streams. Aspen HYSYS splits both curves in intervals and calculates the LMTD value for each interval, based on Equation 1.
(1) Aspen HYSYS calculates the energy interchanged (Qn) in each interval and then the UA for each interval by using Equation2.
(2) Aspen HYSYS reports the overall LMTD based on Equation 3 (Performance tab | Results (SS) page | Overall Performance box).
(3) For example, assuming that the composite curves are split into four intervals (see Figure 1), the corresponding LMTD and UA values for each interval will be calculated by:
Figure 1. Composite curves split into four intervals.
Enclosed to thisSolution there is a simulation case (S118684_20042.hsc). In this example, two cold streams recover energy from one hot stream. The composite curve is shown in Figure 2.
Figure 2. Composite curves in the Aspen HYSYS simulation.
The overall LMTD values will be:
And is reported in the Performance tab | Results (SS) page shown in Figure 3.
Figure 3. Results reported by Aspen HYSYS.
Please note that the above equations are not valid for the dynamic model of the LNG.
Keywords: LMTD, LNG, UA
References: None
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Problem Statement: My feed is not all reacting (or my reaction is not going to completion). What should I check?
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Solution: Check that the base component for your reaction is set properly. For example, if your reaction is: CH4 + 2O2 -> CO2 + 2H2O
and you expect it to reach to 100%, make sure that your base component is CH4. Also, check that you have enough reactant and check that your stoichiometric coefficients are set properly. Reactants should have a negative stoichiometric coefficient and products should be positive. For the above reaction the coefficients will be:
CH4 = -1
O2 = -2
CO2 = 1
H2O = 2
Reactions are created in the Basis environment. See the Simulation Basis Guide Chapter 4 for more details.
Keywords: stoiciometric coefficients, reaction, conversion, completion, combustion
References: None
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Problem Statement: How to access the number of the feed stage knowing the name of the feed stream or vice versa through automation.
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Solution: 1. You have to use the tray section object that is inside the columnsubflowsheet.
2. This object has a FeedStages object that contains the collection of all feed stages
3. Each FeedStage object in this collection has a name property which is the stage name where the feed occurs
4. Each FeedStage object in this collection has a FeedStreams collection that has the list of all streams feeding on this particular stage (as you could have more than one stream on a given stage.
Sample code:
Sub main()
Dim hyApp As HYSYS.Application
Dim hyCase As HYSYS.SimulationCase
Dim hyCol As HYSYS.ColumnOp
Dim hyColfs As HYSYS.ColumnFlowsheet
Dim hyTray As HYSYS.TraySection
Dim hyFSs As Object
Dim hyFS As SeparationStage
Dim hystr As ProcessStream
Set hyApp = CreateObject(HYSYS.Application)
Set hyCase = hyApp.ActiveDocument
Set hyCol = hyCase.Flowsheet.Operations.Item(T-100)
Set hyColfs = hyCol.ColumnFlowsheet
Set hyTray = hyColfs.Operations.Item(Main TS)
Set hyFSs = hyTray.FeedStages
msg =
For Each hyFS In hyFSs
msg = msg & FeedStage : & hyFS.Name & Chr(10)
For Each hystr In hyFS.FeedStreams
msg = msg & Chr(9) & FeedStream : & hystr.Name & Chr(10)
Next
Next
MsgBox (msg)
End Sub
Sample File: Refer to attached sample file. It runs with Aspen HYSYS V7.1. To run in V7.1, the line with code
Set hyApp = CreateObject(HYSYS.Application)
is modified to
Set hyApp = CreateObject(HYSYS.Application.V7.1)
To run the code, open the attached excel file. Click Alt + F11 on the keyboard to go the VB code. And then press F5. It will generate the following message box. Please make sure to keep only one HYSYS file running before running the code.
Keywords: automation, tray, feed, stage, stream, ole
References: None
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Problem Statement: How can I change the units and scale of a HYSYS plot?
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Solution: By default, HYSYS plots will display all variables using the active unit set, however each variable on a plot can be modified as desired. To change the display units for a specific variable, follow the steps outlined below:
- Right-click on the graph and select Graph Control from the ensuing menu.
- In the Graph Control window, open the Axes tab and highlight the axis you wish to modify from the matrix.
- Deactivate the 'Use Default Units' checkbox in the Label group box.
- Select the desired unit from drop-down list.
If you want to modify scale of x-axis/y-axis:
- Right-click on the graph and select Graph Control from the ensuing menu.
- In the Graph Control window, open the Axes tab and highlight the axis you wish to modify from the matrix.
- Deactivate the 'Use Auto Scale' checkbox in the Bounds group box.
- Specify minimum and maximum value for the scale.
Key words
graph, plot, performance, scale, units
Keywords: None
References: None
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Problem Statement: Sometimes it is desirable to have a second stream act as an exact mirror of the original stream, so that whenever the original stream's state changes, the change is reflected in the mirror stream automatically.
|
Solution: There are several methods that can be used to achieve this effect within Aspen HYSYS. One of the simplest ways is to leverage the functionality of the BALANCE and SET operations. The BALANCE operation is used to ensure that compositions are preserved by selecting MOLE as the balance type (via the Parameters page tab), and the SET operations are used to relay pressure and temperature to the mirror stream. See the attached case for the general configuration of such a flow sheet.
Keywords: mirror, duplicate, multiple, stream, connection
References: None
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Problem Statement: How can I open the Calculation.xls file from the Aspen Solubility Modeler folder without error messages?
Opening the file from the directory the C:\Program Files (x86)\AspenTech\Aspen Solubility Modeler VX.X\NRTL-SAC, this error message appears on screen:
! Unable to generate PDF file from C:\Program Files
(x86\AspenTech\ Aspen Solubility Modeler
V8.0\NRT-SAC\NRTL-SAC_Solvents_43_Excipents.aprbkp, the
package would not be imported.
Then, clicking on ‘OK’ and the following messages will be shown:
Failed to resolve Property Package C:\Program Files (x86\AspenTech\ Aspen
Solubility Modeler V8.0\NRT-SAC\NRTL-SAC_Solvents_43_Excipents.aprbkp
and Excel has to close
Then,
No Property Package has been resolved. Please select property package first.
|
Solution: As program Files is a protected directory, sometimes the user may have some problems trying to open the Calculation.xls file from the Aspen Solubility Modeler directory. However, if one copies the .xls Excel file, as well as the file NRTL-SAC_130_Solvents_43_Excipients.aprbkp to a new created folder, for example on my documents or desktop and then open from there, a message like this one will appear:
This workbook contains links to other data sources.
- If you update the links, Excel will attempt to retrieve the latest data.
- If you don't update the links, Excle will use the previous information.
Note that data links can be used to access and share confidential information without your permission and possibly perform after harmful actions. Do not update the links if you do not trust the source of this workbook.
Click on ‘Don’t Update’. Then there will be a message:
This workbook contains one or more links that cannot be updated.
- To change the source of the links, or attempt to update values again, click Edit Links,
- To leave the lins as is, click Continue.
Click Continue.
The Excel file is now accessible, so click on ‘Change Aspen Properties File…’ button on the Excel spreadsheet and open the Aspen Properties (.aprbkp) file from the new folder created. Then, click on OK again.
Now the results from that file are obtained and shown.
See .PDF document file attached for further details.
Keywords: Aspen Solubility Modeler, Aspen Properties, Calculation.xls.
References: None
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Problem Statement: What equipment-specific information is needed to convert a case from steady-state to dynamics?
|
Solution: The purpose of the attached document is to provide simple and straightforward advice to enable engineers to produce dynamic models of real operating units using Aspen HYSYS. This guide details the basic steps to follow in order to convert a steady-state case into a dynamic case and presents the minimum process data required for each unit operation.
It is assumed that the user of this guide is familiar with the HYSYS interface and is comfortable creating steady-state models.
Keywords: dynamics, control, dynamic, simulation, weir, height, sump, level
References: None
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Problem Statement: A sample of Aspen HYSYS extension reaction kinetics in Visual Basic .NET
|
Solution: First: Download and unzip the attached zip file, bring up Microsoft Visual Studio 2005, load theSolution and build it, you will see the binary dll file is generated in .\bin\debug folder. Copy the EDF file to same folder as DLL file.
Next: Bring up Aspen HYSYS 2006 and register it, close Aspen HYSYS and reopen it again. You can then test it with the case file attached. It is a Glycol Reaction Extension Package.
Finally, go into Basis manager reaction page and add a reaction of new type labelled as test new env and proceed from there.
Note: You'll need both Visual Studio 2005 and Aspen HYSYS 2006 installed on the same machine in order to compile and run the extension. However, to distribute it to other machines, only .Net run time is required with the dll and the edf files.
Note: VB.NET extension are supported from HYSYS 2006 and later versions.
Keywords: .NET, extension, VB.NET, sample, Visual Basic, reaction extension
References: None
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Problem Statement: This knowledge base article provides an overview of FIXA option in CMAN table.
|
Solution: FIXA is a Plant Scheduler simulator option found in CMAN (FIXA) .It can be set to YES or NO. When set toYES, the simulator does not move fixed activities. An activity is known to be fixed if its hierarchy level in MAKI (LEV) is greater than the fixed level in HIER (FIX, LEV).
As an example, on the planning board, if the user drags a non-fixed activity and drops it on top of a fixed one, the dropped activity will be scheduled by the simulator after the fixed one. And, if there are other fixed activities after that, the simulator will schedule it at the first time where it can fit without moving a fixed activity. In simple terms, simulator determines the actual start (AS) time for each activity so that no activity overlaps. The activities are processed in scheduled start (ST) time order. If any activity overlaps, it is scheduled to start (Actual Start) at the end of the one it is overlapping and the Scheduled start (ST) sequence is preserved.
The most common fixed activities are downtimes but, the user can fix production activities by raising their hierarchy levels. FIXA is not enabled on facilities with embedded shutdowns.Â
With FIXA on, the Actual Start for the fixed activities is determined first. Once the fixed activities have their Actual Starts set, then the un-fixed activities are processed in Scheduled Start (ST) order.
There may be situations when the users may move activities on the Planning Board. Also, a macro can be used to move activities with command like M RESCHE, which is the command that runs when a user drag-n-drops. These actions can change the schedule and activities scheduled start (ST) times. Then simulator runs and determines the earliest Actual Start (AS).
Keywords: None
References: None
|
Problem Statement: Why does the status bar on the Deposition | Methods page of my pipe segment indicate Not Calculated?
|
Solution: As in the figure at the bottom of thisSolution document, the status bar on the Deposition | Methods page the pipe segment may indicate Not Calculated for a variety of reasons:
1. The stream or associated pipe segment does not have enough information to run.
2. The ProFES wax calculation method does not have sufficient information to run.
3. The Do Deposition Calcs checkbox has not been activated.
Keywords: wax, deposition, pipe, segment, ProFES
References: None
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Problem Statement: When starting Aspen Rxfinery, this error occurs:
Window Title: Critical Error
Error in ConnectServer(), module Com2Dcom. Error message:Method 'GetSimulationEngine' of object 'IAPEngConnect' failed
-OK-
|
Solution: One of the Rxfinery components registers an older version of a type library. If the products are installed in the correct order, i.e. Aspen Plus 11.1, Rxfinery 11.1, Aspen Plus SP1, Rxfinery SP1, this problem does not occur. If installed in any other order, the Dcom error noted above may occur.
TheSolution is to reregister that type library through this process:
Start / Programs / AspenTech / Aspen Engineering Suite / Aspen Plus 11.1 / Aspen Plus Simulation Engine to open a grey command line window
Use cd to navigate to AspenTech\Aspen Plus 11.1\Engine\xeq
Enter regsvr32 ascclasslib.dll
To prevent the problem, install the products in this order:
Aspen Plus 11.1
Rxfinery 11.1
Aspen Plus SP1
Rxfinery SP1
Fixed in Version
This is fixed for 12.1.
Keywords: aspen refinery dcom com service pack registry type libraries
References: None
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Problem Statement: Is it possible to see Description instead of Tags of Nodes on the Maps?
|
Solution: Yes, from Program Options | Map select ‘Use Description’ for Label Type
Keywords: DPO Map description
Map Description
Map Label
References: None
|
Problem Statement: Freeform line is defined but the freeform data in the Results window does not represent the same. Why?
|
Solution: Free-form points allow you to more realistically depict the path of a transportation arc. Segments are the building blocks for defining routes.
The 'Show Point to Point Transportation' shows the transportation arcs as a straight line (as the crow flies) from the source node directly to the final destination. The results that are displayed also based on this option.
Deselect the 'Show Point to Point Transportation' option to show the Freeform data in the results Window.
Keywords: None
References: None
|
Problem Statement: The error message 'Cavett parameter calculation did not converge' is observed when exiting the Oil Manager. What causes this?
|
Solution: The error message 'Cavett parameter calculation did not converge' is caused by a failure in the iterative estimation method for the Cavett parameter. This parameter is used to calculate heat of vaporization whenever an ACTIVITY model is used. If you are using Equation of State (EOS) based model, however, this parameter is not used hence this error message can be safely ignored (in an EOS model, the liquid enthalpy is determined by the EOS directly, therefore the Cavett parameter is not used to calculate heat of vaporization).
This error message frequently appears when an Assay has components with NBPs above 2000F at the upper end of its boiling range. Whenever you receive such an error message, we recommend evaluating your results carefully (note that you can view the estimated value of the Cavett parameter from the Point pagetab on the pure component view).
In certain cases, this error message can be avoided by changing the Extrapolation Method for the Assay (while in the Oil Manager environment, view the selected Assay and open the Calculation Defaults pagetab). For example, you can try changing the extrapolation method for the distillation data from Probability to Lagrange, because the Lagrange method tends to estimate somewhat lower temperature values for the heavy ends.
Another possible option is to manipulate the assay data. An example would be to reduce the temperature(s) for the final data point(s). If either of these option allows you to avoid the error message, it is recommended that you use your engineering judgment to assess the significance of the impact the data modification has on your results.
Keywords: Cavett parameter, error, oil manager, heat of vaporization
References: None
|
Problem Statement: Occasionally from installation problems or other changes in the Aspen Properties Enterprise Database, the APV7x, NISTV7x and FACTV7x databases provided by Aspen Tech will disappear in the Aspen Properties Database Manager and therefore will not available to use in Aspen Plus, Aspen Properties and other Aspen Tech software programs. If you try to register the databases in the database manager and the procedure fails then you may have to restore the databases manually.
|
Solution: If you need to restore the databases on the server manually, first check for the existence of APV7x.MDF, NISTV7x.MDF and FACTV7x.MDF (where ?x? is your version number) and corresponding *.LDF files in the folder:
C:\ProgramData\AspenTech\APED V7.x\ (Windows 7)
or
C:\Documents and Settings\All Users\Application Data\AspenTech\APED V7.x\ (Windows XP)
If there are files here, back them up by copying them to another folder, then delete the files in the folder named above.
To restore the databases, execute the following commands from a DOS window:
Windows 7 (V7.3 and below)
set DatabaseFolder=C:\Program Files\AspenTech\APrSystem 7.3\PropertiesDatabase\Database
set ServerName=.\SQLEXPRESS
sqlcmd -E -S %ServerName% -Q EXECUTE SP_ADDLOGIN 'apeduser', 'Aprop100', 'master'
sqlcmd -E -S %ServerName% -Q EXECUTE SP_ADDSRVROLEMEMBER 'apeduser', 'sysadmin'
sqlcmd -U apeduser -P Aprop100 -S %ServerName% -Q Drop Database APV73
sqlcmd -U apeduser -P Aprop100 -S %ServerName% -Q Drop Database NISTV73
sqlcmd -U apeduser -P Aprop100 -S %ServerName% -Q Drop Database FACTV73
sqlcmd -U apeduser -P Aprop100 -S %ServerName% -Q restore database APV73 from disk='%DatabaseFolder%\APV73' WITH MOVE 'APV73' TO `C:\Users\All Users\AspenTech\APED V7.3\APV73.MDF', MOVE 'APV73_Log' TO `C:\Users\All Users\AspenTech\APED V7.3\APV73_Log.LDF'
sqlcmd -U apeduser -P Aprop100 -S %ServerName% -Q restore database NISTV73 from disk='%DatabaseFolder%\NISTV73' WITH MOVE 'NISTV73' TO 'C:\Users\All Users\AspenTech\APED V7.3\NISTV73.MDF', MOVE 'NISTV73_Log' TO `C:\Users\All Users\AspenTech\APED V7.3\NISTV73_Log.LDF'
sqlcmd -U apeduser -P Aprop100 -S %ServerName% -Q restore database FACTV73 from disk='%DatabaseFolder%\FACTV73' WITH MOVE 'FACTV73' TO `C:\Users\All Users\AspenTech\APED V7.3\FACTV73.MDF', MOVE 'FACTV73_Log' TO `C:\Users\All Users\AspenTech\APED V7.3\FACTV73_Log.LDF'
Windows 7 (v7.3.2)
set DatabaseFolder=C:\ProgramData\AspenTech\APED V7.3.2
set ServerName=.\SQLEXPRESS
sqlcmd -E -S %ServerName% -Q EXECUTE SP_ADDLOGIN 'apeduser2', 'Aproperty88#', 'master'
sqlcmd -E -S %ServerName% -Q EXECUTE SP_ADDSRVROLEMEMBER 'apeduser2', 'sysadmin'
sqlcmd -U apeduser2 -P Aproperty88# -S %ServerName% -Q Drop Database APV732
sqlcmd -U apeduser2 -P Aproperty88# -S %ServerName% -Q Drop Database NISTV732
sqlcmd -U apeduser2 -P Aproperty88# -S %ServerName% -Q Drop Database FACTV732
sqlcmd -U apeduser2 -P Aproperty88# -S %ServerName% -Q restore database APV732 from disk='%DatabaseFolder%\APV732' WITH MOVE 'APV732' TO `%DatabaseFolder%\APV732.MDF', MOVE 'APV732_Log' TO `%DatabaseFolder%\APV732_Log.LDF'
sqlcmd -U apeduser2 -P Aproperty88# -S %ServerName% -Q restore database NISTV732 from disk='%DatabaseFolder%\NISTV732' WITH MOVE 'NISTV732' TO `%DatabaseFolder%\NISTV732.MDF', MOVE 'NISTV732_Log' TO `%DatabaseFolder%\NISTV732_Log.LDF'
sqlcmd -U apeduser2 -P Aproperty88# -S %ServerName% -Q restore database FACTV732 from disk='%DatabaseFolder%\FACTV732' WITH MOVE 'FACTV732' TO `%DatabaseFolder%\FACTV732.MDF', MOVE 'FACTV732_Log' TO `%DatabaseFolder%\FACTV732_Log.LDF'
Windows XP (v7.3 and Below)
set DatabaseFolder=C:\Program Files\AspenTech\APrSystem 7.3\PropertiesDatabase\Database
set ServerName=.\SQLEXPRESS
sqlcmd -E -S %ServerName% -Q EXECUTE SP_ADDLOGIN 'apeduser', 'Aprop100', 'master'
sqlcmd -E -S %ServerName% -Q EXECUTE SP_ADDSRVROLEMEMBER 'apeduser', 'sysadmin'
sqlcmd -U apeduser -P Aprop100 -S %ServerName% -Q Drop Database APV73
sqlcmd -U apeduser -P Aprop100 -S %ServerName% -Q Drop Database NISTV73
sqlcmd -U apeduser -P Aprop100 -S %ServerName% -Q Drop Database FACTV73
sqlcmd -U apeduser -P Aprop100 -S %ServerName% -Q restore database APV73 from disk='%DatabaseFolder%\APV73' WITH MOVE 'APV73' TO `C:\Documents and Settings\All Users\Application Data\AspenTech\APED V7.3\APV73.MDF', MOVE 'APV73_Log' TO `C:\Documents and Settings\All Users\Application Data\AspenTech\APED V7.3\APV73_Log.LDF'
sqlcmd -U apeduser -P Aprop100 -S %ServerName% -Q restore database NISTV73 from disk='%DatabaseFolder%\NISTV73' WITH MOVE 'NISTV73' TO `C:\Documents and Settings\All Users\Application Data\AspenTech\APED V7.3\NISTV73.MDF', MOVE 'NISTV73_Log' TO `C:\Documents and Settings\All Users\Application Data\AspenTech\APED V7.3\NISTV73_Log.LDF'
sqlcmd -U apeduser -P Aprop100 -S %ServerName% -Q restore database FACTV73 from disk='%DatabaseFolder%\FACTV73' WITH MOVE 'FACTV73' TO `C:\Documents and Settings\All Users\Application Data\AspenTech\APED V7.3\FACTV73.MDF', MOVE 'FACTV73_Log' TO `C:\Documents and Settings\All Users\Application Data\AspenTech\APED V7.3\FACTV73_Log.LDF'
Windows XP (v7.3.2)
set DatabaseFolder= C:\Documents and Settings\All Users\Application Data\AspenTech\APED V7.3.2
set ServerName=.\SQLEXPRESS
sqlcmd -E -S %ServerName% -Q EXECUTE SP_ADDLOGIN 'apeduser2', ' Aproperty88#', 'master'
sqlcmd -E -S %ServerName% -Q EXECUTE SP_ADDSRVROLEMEMBER 'apeduser2', 'sysadmin'
sqlcmd -U apeduser2 -P Aproperty88# -S %ServerName% -Q Drop Database APV732
sqlcmd -U apeduser2 -P Aproperty88# -S %ServerName% -Q Drop Database NISTV732
sqlcmd -U apeduser2 -P Aproperty88# -S %ServerName% -Q Drop Database FACTV732
sqlcmd -U apeduser2 -P Aproperty88# -S %ServerName% -Q restore database APV732 from disk='%DatabaseFolder%\APV732' WITH MOVE 'APV732' TO `%DatabaseFolder%\APV732.MDF', MOVE 'APV732_Log' TO `%DatabaseFolder%\APV732_Log.LDF'
sqlcmd -U apeduser2 -P Aproperty88# -S %ServerName% -Q restore database NISTV732 from disk='%DatabaseFolder%\NISTV732' WITH MOVE 'NISTV732' TO `%DatabaseFolder%\NISTV732.MDF', MOVE 'NISTV732_Log' TO `%DatabaseFolder%\NISTV732_Log.LDF'
sqlcmd -U apeduser2 -P Aproperty88# -S %ServerName% -Q restore database FACTV732 from disk='%DatabaseFolder%\FACTV732' WITH MOVE 'FACTV732' TO `%DatabaseFolder%\FACTV732.MDF', MOVE 'FACTV732_Log' TO `%DatabaseFolder%\FACTV732_Log.LDF'
In the code quoted above, you may need to change the following:
1. set DatabaseFolder: Change the APrSystem folder?s version to your version, and to C:\Program
Files (x86) if the OS is 64bit.
2. set ServerName: Add your SQL Server Service name. This located in Windows Services under SQL Server. The ./ means This Machine.
(Leave ?.\SQLEXPRESS? if you are using the SQL Server Express edition that was included on the Aspen DVD).
This database restore procedure is also available in the attached batch file that can be run in a DOS window. You can modify this file for the above mentioned features.
Keywords: databanks, APED, Aspen Properties Enterprise Database, Aspen Properties Database Manager, Database restore
References: None
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Problem Statement: When a quoted cost item is entered, Aspen Icarus Process Evaluator (IPE) escalates the Adjusted Total Project Cost (cell C190 on projsum.ics) from the date of the cost engine (1Q98 for versions 5.0 and 5.1) as it does for all generated costs. This presents a problem since most quoted costs are entered in present day dollars.
|
Solution: In IPE, escalation is calculated simply, using a formula similar to the following: X = A(1 + RN)
where X = total cost, including escalation
A = 1Q98 base cost
R = rate of escalation per period (as shown in field C132 of ProjSum.ics) N = number of periods from 1Q98 to the Start Date of Basic Engineering
So to get around this, when entering current costs for quoted cost items, use the following formula to estimate a 1Q98 cost for your item, knowing N, R, and X, which would be your present day cost.
A = X / (1 + N*R)
Keywords: escalation
quote
References: None
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Problem Statement: How is the controlling product defined in Aspen Fleet Optimizer?
|
Solution: Within a given shipment, there can be more than one product to be delivered. A controlling product is a product that will run out first in a given shipment. In the detail window, the row that shows the controlling product of the shipment will be highlighted in red. This feature works only with a forecasted customer. With this feature, the user can pay close attention to the controlling product and manage deliveries more efficiently.
Keywords: None
References: None
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Problem Statement: Why is Wetted Area shown as <empty> on Heat flux page of the Dynamic Depressuring utility?
|
Solution: The wetted area used in the Dynamic Depressuring utility is defined as the surface area wetted by the internal liquid content of the vessel, and is effective in generating vapor when the exterior of the vessel is exposed to fire.
When you select Fire API521 as the operating mode for the Dynamic Depressuring utility (via the Design | Heat Flux pagetab), an equation is highlighted on the right hand side that is used in calculation of heat flux. Starting with Aspen HYSYS 2004 and onwards, the initial wetted area is not longer provided by user as it is automatically calculated in order to match initial liquid volume on the Design | Connections page of the utility. For this calculation, Aspen HYSYS will determine the initial wetted area assuming flat ends for the vessel. Note that the initial wetted area entry box is still available so as to ensure compatibility with old versions, however the value is shown as <empty> and cannot be edited.
If you wish to view at the wetted area of the vessel, it is now displayed in cell D8 of the ?Duty? Spreadsheet (inside the depressuring subflowsheet). Note that it only shows the current value when the utility is running.
Keywords: wetted, area, empty, dynamic, depressuring, utility
References: None
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Problem Statement: Tips for using Results Window.
|
Solution: This is a typical Results Window.
If you want to show the map only without the options, the simple way to do is to make the Option Window float first, then close this option window by clicking the 'x' on its top right.
To make the Option window float, click and hold the option window then drag it to the middle. Once it changes to the floating mode, it is an independent window. Then you can close it without affect the map window.
Keywords: Float
Results Window
Option
Graphical Results Window
References: None
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Problem Statement: Making Stream / Operation User Variables get data from Utilities...
|
Solution: I want to access data from a utility and use it in my user variable, but whenever the user variable runs all the data it tries to obtain is empty. Is there a way around this?
The problem here is that utilities attached to streams calculate after the rest of the flowsheet has solved, hence when a stream PostExecute() user variable runs then the utility won't have calculated.
The way around this is to use a combination of a stream user variable and a flowsheet PostSolve() user variable, which runs when the whole flowsheet has finished solving, and the utility has calculated values.
The enclosed case (HYSYS ver 2.2) gives a simple example of a stream user variable which gets data from a boiling point table utility. (As a demonstration it just outputs the 50% d86 temperature value)
The case contains two user variables:
A PreExecute() user variable on the stream (BPTableTest) - when the user variable is enabled this adds a boiling point table utility (if the stream doesn't already have one) and then puts a dummy value (0K) into the user variable, so that the other user variable knows to calculate it.
A PostSolve() user variable on the main flowsheet (FlwBPTableTest) - this uses a recursive (procedure calls itself) method to loop through all the streams in all the flowsheets in the case each time the flowsheet solves. If the stream has the dummy value in it's user variable then it calculates a value based on data from the streams attached boiling point utility.
A limitation of this method is that the stream user variable cannot be the target of an adjust since it's value is calculated after the adjust tries to solve, so the adjust only ever sees the dummy value.
The user variable code is as follows:
Stream User Variable:
Sub PreExecute()
'
'Description: Designed to be used with FlwBPTableTest Flowsheet level User Variable
' This procedure adds a boiling point table to all streams with it enabled, and marks
' it so the FlwBPTableTest UV knows to calculate the value
'
'Declare Variables
Keywords: None
References: None
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Problem Statement: What should I do when the binary interaction parameters are not available?
|
Solution: When the Binary Interaction Parameters (BIPs) for a thermodynamic model are not provided in Aspen HYSYS by default, it is usually due to one of the following two reasons:
1. The phase behavior of the binary system is very unusual, so that a single set of BIPs is not sufficient to accurately represent the mixture's phase behavior across its whole concentration range.
2. No literature data is available to us. We are a software company and don't have facilities to conduct experimental work for VLE measurements.
In a situation like this, we usually encourage users to look for the missing information from literature. Meanwhile, to get some directional results, you can also consider the built-in UNIFAC Estimation feature in the program. This feature is available for both NRTL and UNIQUAC models. As shown in the attached image file, you can choose to estimate the unknown BIPs for VLE or LLE applications. We strongly recommend that while using estimated BIPs for their simulations, users should always use their own engineering judgment and validate their simulation results with any plant/lab data they might have.
Keywords: missing BIPs, binary interaction parameters, UNIFAC estimation, VLE, LLE, estimate
References: None
|
Problem Statement: The economic summary table generated after executing a DPO model has a list of data entries in a column named Miscellaneous. This report provides a detailed description on the interpretation of these entries.
|
Solution: The 'Sample 2' model in the Aspen Supply Chain Planner folder is selected for illustration. A snap shot of the Economic Summary table (Run | Economic Summary) is given in Figure 1.
Figure 1: Economic Summary Report
As evident from Figure 1 the miscellaneous value for JAN is -34.4186. This value is the sum of Activities*Prices (Activities multiplied by Price) that are not included in the preceding categories of summary table in Figure 1. Preceding categories implies Sales Revenue, Exchange Revenue, Purchases Etc.,
In order to view the miscellaneous column breakdown value of -34.4186 for JAN in theSolution browser, launch theSolution browser from the run menu drop down of the tool bar (Run |Solution Browser). This opens a window as shown in Figure 2.
Figure 2: Getting theSolution Browser
Select case- A and click OK. The resultantSolution browser is displayed as Figure 3.
Figure 3:Solution Browser
From the tool bar of this window click Rows on Top. Then select Filter Non-0.0 Activities Bottom, finally from All Row Types pull down list, select OBJ. This results in Figure 4.
Figure 4: ModifiedSolution Browser
Now double click ?OBJ:JAN? in the upper window (Figure 4), which enables to see all columns intersecting the objective function for the period of JAN. Furthermore, Click All Display Columns to see additional columns (Figure 5).
Figure 5:Solution Browser with Miscellaneous Column Breakdown Highlighted
Now click column name in the lower window to sort the entries by column names. The rows highlighted in Figure 5 have the breakdown of the miscellaneous column value -34.416 for JAN. This can be verified by adding the entries in the Extended column: -1 + -0.3543 + -18.592 . . . + -1.5760 = -34.4186.
SEG are the segment columns and SEGC are segment integer columns. Both of them are not included in other categories of the economic summary report. Therefore they are aggregated to the Miscellaneous column.
Keywords: DPO Economic Summary Report, Miscellaneous Column
References: None
|
Problem Statement: Why is it called film holdup in Slug Tool? How does this differ from Liquid Holdup in the Pipe Profile?
|
Solution: In a slug, allowance is made for gas bubbles in the slug. The liquid holdup in the slug is the fraction of the pipe cross-sectional area occupied by liquid where this liquid/gas mixture bridges the pipe, with the liquid being the continuous phase. The model takes into account the shape of the interface from the back of one slug to the front of the next one. This is called the bubble region and the local film thickness is not uniform. The quoted film holdup for this region is the average liquid holdup from the back of one slug to the front of the next one.
Keywords: Film Holdup, Liquid Holdup, Slug Tool
References: None
|
Problem Statement: How does one correct the component density calculated by the GCEOS model?
|
Solution: The Generalized Cubic Equation of State (GCEOS) is an alternative to the standard EOS property models that enables the user to define and customize a cubic equation. This allows for volume translation correction thereby providing a better representation of liquid volume and density by the chosen property model.
The Parameters tab for the GCEOS consists of three group boxes as shown in the figure below:
1. GCEOS Pure Component Parameters
2. GCEOS Parameters
3. Initialize EOS
To correct the density calculated by the GCEOS model, the volume translation parameters found within the GCEOS Pure Component Parameters group box can be modified as appropriate. By default all the input values are set to zero, however these parameters can be modified by the user or estimated by HYSYS via the Estimate button. When the Estimate option is selected, the pure component volume translation parameters are estimated by matching the liquid volume calculated at the normal boiling point with the liquid volume obtained using an independent method (i.e. COSTALD).
Known Issues
In versions prior to Aspen HYSYS 2006, the Estimate button does not work as designed.
Keywords: GCEOS, volume translation parameters, density
References: None
|
Problem Statement: Do I need a license to access the OLI Electrolyte property package?
|
Solution: A separate license is required to access the OLI Electrolytes property package, however AspenTech does not provide this directly. While certain AspenTech products do have an interface enabling the use of this property model, the license itself is provided by OLI Systems, Inc. Contact information for OLI Sytems is provided below:
email: [email protected]
web: http://support.olisystems.com
Keywords: OLI, fluid, package, license
References: None
|
Problem Statement: What are the differences among heat transfer models available in the dynamic depressuring utility?
|
Solution: The differences among the different heat transfer models available in the dynamic depressuring utility are listed in Aspen HYSYS Operations Guide, which is available on the support website via the Documentation link. A summary table is included below for your convenience:
Keywords: depressuring, blowdown, mode, model, API521, fire, Stephen-Boltzman, adiabatic, utility
References: None
|
Problem Statement: How do you convert Aspen HYSYS files to use Exchanger Design and Rating (EDR)?
|
Solution: The attached converter allows you to convert Aspen HYSYS files that use the discontinued TASC and ACOL programs so that they will use the Shell&Tube and AirCooled models from Aspen Exchanger Design and Rating.
This converter is designed to work with Aspen HYSYS and Aspen EDR versions V7.0 with CP1 installed and later versions. If you have multiple versions, be sure that one of these versions is registered. Aspen TASC 2006.5 and Aspen ACOL 2006.5 must be installed. Patches for Aspen HYSYS 2006.5 (patch is due to release) and V7.0 must be up to date.
To convert Aspen Plus files, seeSolution 112077.
You must have installed both the program you are converting from and the program you are converting to.
To convert files using
You must have installed
TASC
Aspen TASC 2006.5, Aspen Shell & Tube Exchanger, and Aspen HYSYS
ACOL
Aspen ACOL 2006.5, Aspen Shell & Tube Exchanger, and Aspen HYSYS
Note:
The converter is compatible with files saved in older versions of Aspen HYSYS, but not with newer files. The current registered Aspen HYSYS version must be at least as new as the version under which the files were saved in order to use the converter.
If the source folder and destination folder are the same, the program creates a subfolder named ConvertToEDR under the destination folder. This prevents files being overwritten during the conversion.
To use it:
1. Download and install the files for the converter in any convenient folder, but do NOT install it in the same folder with your Aspen HYSYS files to be converted.
2. Run ConvertToEDR.exe from this folder.
3. At the top, select either Aspen HYSYS (*.hsc) for the type of file to be converted.
4. In the middle section, select the Source Drive and Source Folder where the converter should look for files to convert. The Aspen HYSYS .hsc files should be in this folder.
5. Select the Destination Drive and Destination Folder where the converter should write the converted files. It will use the same filenames as the source files, except that the extension of the .bjt files will be changed to .edr in the converted files.
Note: If Source Folder and Destination Folder are the same, the converter will create a ConvertToEDR folder within the source folder and store the converted files there, to avoid overwriting the original files.
6. In the Source File list, select the file(s) to convert. You can click Select All to select all the files. Then click Convert.
It will take some time as the converter calls Aspen HYSYS and EDR to convert the files. At the end you will be prompted when all the files have been converted.
7. Click OK.
If any problems are encountered in mapping the settings from the older program into Shell&Tube or AirCooled settings, a description of the affected setting is saved as a comment in the block with a description containing ToEDR conversion warnings. Click the Status Button in the Data Browser when open to this block to view the comments.
The following specifications in the programs converted by this converter are not supported by EDR. When they are encountered, the converter converts them as well as it can and leaves comments in the Trace Window describing the problem.
Keywords: Aspen HYSYS to EDR converter utility files, EDR, Converter, Converter Files
References: None
|
Problem Statement: Can I merge two component lists into one?
|
Solution: If you are trying to take oil hypotheticals or a group of hypotheticals from one list to another, there is a shortcut. Select the component list (where you want to add) || View || Hypothetical || select a Hypothetical Group (for oil it's a blend) || then click on Add Group.
There is no shortcut option to combine or merge pure components and/or individual hypothetical components of two component lists. You have to add the components all over again.
Keywords: combine, merge, component list, oil hypo, component
References: None
|
Problem Statement: For two same simulations with the same basis, I am getting two different results.
|
Solution: The most probable cause is that you binary parameters are changed manually. Please reset the binary parameters for both the files or make them same.
Path to reset the binary parameters:
Go to Simulation Basis Manager (Ctrl + B).
Click on Fluid Pkgs tab.
Select the fluid package and press View.
Click on the Binary Coeffs tab.
Click on Reset Parameters.
Keywords: Same basis, different results, reset binary parameters, reset binary coefficients.
References: None
|
Problem Statement: How to get mass enthalpy--temperature curve in heat exchanger?
|
Solution: Open the property view of a heat exchanger, and select Performance tab and Tables page. Here you find several columns of data following the flow path, temperature, pressure, enthalpy, heat flow, vapor fraction, and cumulative UA. For enthalpy, only mole based enthalpy is available.
If mass based enthalpy vs temperature curve is required, an Aspen HYSYS Spreadsheet unit can be used to convert the mole based enthalpy values to mass based enthalpy values.
The given steps should be followed:
1. Converge your model;
2. Add a Spreadsheet unit to your PFD;
3. Specify adequate number of column and row, and select proper engineering unit set.
4. Try to make both the property view of the heat exchanger and the spreadsheet to show at the same time (possibly one left and the other right);
5. Use drag-and-drop method to import enthalpy data from the heat exchanger;
6. Import molecular weight from the inlet or outlet for the side under consideration (shell side or tube side);
7. Enter cell formula to calculate mass based enthalpy from molar enthalpy divided by molecular weight;
8. Change variable type to Mass Enthalpy for cells with calculated values
Now you have the mass enthalpy along the flow path.
Note that the method suggested in KBSolution 120887 will not result in a match curve along the flow path.
Keywords: Mass enthalpy, heat exchanger;
References: None
|
Problem Statement: In the Twu options for PR and SRK. What does the option Water Gas Kij do?
|
Solution: Water in gas calculations refer to the special temperature dependant Kijs fitted for water - Argon, C1, C2, C3, H2, N2, and CO for the liquid and vapor phase Kijs.
Keywords: Water Gas, Twu, PR, SRK, Kij
References: None
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Problem Statement: How to use MIP type Linkage in Aspen Petroleum Supply Chain Planner
|
Solution: MIP type Linkage
Forces a more expensive transaction to limit theSolution before a less expensive transaction of the same type (material, transport mode, sub model operation, or capacity) can be included in theSolution. This is similar to PRIORITY column in PIMS
Objective of this modeling
Add the necessary MIP variables to ensure that the north pipeline’s new pricing structure is used versus the base rate for all volumes transported. (Example model attached)
Procedure
Need for new Mode PIPE2. Cost 0.92 is 80% of 1.15.
* TABLE
Modes
*
*
!
Mode
Description
PIPE
Pipeline
PIPE2
Link Pipeline
RAIL
Rail
TRUCK
Truck
Use linkage in Table Transport, Linkage use of MIP causes high cost option (limited at 30) to be used before low cost option.
* TABLE
Transport
*
*
!
Material
From
To
Mode
Cost
Max
MipType
* PIPE
DIE
WREF
DEPA
PIPE
0.5
DIE
DEPA
DEP1
PIPE
0.5
DIE
DEPA
DEP2
PIPE
0.5
*
GAS
EREF
DEP1
PIPE
1.15
30
GAS
EREF
DEP1
PIPE2
0.92
1000
Linkage
Results
OBJFN = 3164.42 for NPL_Incentive case.
Note activity of high priced GAS from EREF with mode (PIPE) is at maximum of 30.
Lower priced mode (PIPE2) provides balance of delivery.
Keywords: MIP
Linkage
References: None
|
Problem Statement: The Transportation Cross-Tab report in Aspen Petroleum Supply Chain Planner returns a Jet Engine error when you try to access it and it does not display data.
How do I fix this problem?
|
Solution: Delete the Results.mdb that stores all the output data so that it gets recreated. After you delete the Results.mdb file, run the model again.
The Transportation crosstab report should be accessible again.
Keywords: Transportation Crosstab report
Results.mdb
References: None
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