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Problem Statement: Processed, pipelined natural gas can be characterized by the term GPM (gallons per MSCF). What is the meaning of GPM and how can I calculate it? | Solution: GPM is the gallons of liquifiable hydrocarbons contained in 1,000 cubic feet of natural gas. Aspen HYSYS is not reporting the property of the stream. We can use the user variable to calculate for your desired stream. The attached user variable is an example of how to create the code and calculate the property. Since the parameters of the equations are experimental, you may need add more for other components.
Keywords: User variable, GPM, natural gas
References: None |
Problem Statement: A vortex tube is a mechanical device (with no moving parts) that separates compressed gas into hot and cold streams. The hot end can reach temperatures of 120-200 deg.C with the cold end as low as -50 deg.C. The air stream within the vortex tube can spin as high as 1,000,000 rpm and its operating principle is based on the law of conservation of angular momentum.
Is it possible to simulate such a device in Aspen HYSYS? | Solution: At this time, there are no Aspen HYSYS unit operations (available from AspenTech) that can rigorously design or rate a vortex tube. However, if sufficient process conditions from the inlet and outlet streams are known, Hysys can be used to perform the mass and energy balance across the vortex tube.
As an illustration, a simulation for the mass and energy balance is provided in thisSolution.
Keywords: vortex tube, vortex cooler
References: None |
Problem Statement: My regression converged, but the parameters calculated are at their initial values and show an extremely high standard deviation, what could be the problem? | Solution: When all parameters regressed keep stuck at their initial values and the quality of the fit is very bad, that is a clear indication that those parameters are not having any effect in the measurement data. The reason behind is that the model you are regressing the parameters for is not being used in the property method that is selected, or in other words, the model regressed is not active in the route involved in calculation of the measured property.
In the attached example, the regression DR-2 is trying to obtain the parameters for the PPDS equation for the heat capacity of the liquid (CPLPDS), but that model is not being used for ethanol so the fit is impossible. Although the route DHL09 is selected, the model won't be active if the parameters CPLPDS is not the only CPL parameter present. We can force the method to use CPLPDS by directly specify it in the thermo-switch (THRSWT/6). This way we are telling Aspen Properties System to use that parameter and then letting the regression to be performed:
In the example file provided go to THRSWT/6 and introduce 301, if you run the regression, it will now converge and adjusted to the experimental data correctly.
Another way to force Aspen Physical Property System to use that specific model is to delete the ethanol parameters for the DIPPR equation (CPLDIP) and add CPLPDS with a dummy value, that way it will become active in the property method.
Keywords: Regression, bad fit, standard deviation.
References: None |
Problem Statement: Is it possible to model the production of ethanol from corn stover? | Solution: In the Aspen Plus examples directory, there is an example of producing ethanol from corn stover. It is located by default in the C:\Program Files (x86)\AspenTech\Aspen Plus V8.6\GUI\Examples\Bioethanol from Corn Stover directory. You can also click on the Examples button on the Resources ribbon of the Aspen Plus graphical user interface to get to this directory. A Fortran compiler is needed due to the use of Common blocks and write statements in the Calculator blocks. For customers without a compiler, an Aspen Plus V8.6 .apwz file that does not need Fortran is attached to thisSolution. This version will be available in the examples directory in the next release.
Keywords: None
References: None |
Problem Statement: Is it possible to model crystallization of multiple isomers such as that of para and meta-xylene? | Solution: As long as both molecules have different properties, it should be possible to model them using Chemistry. Multiple solids can be precipitated using chemistry method.
In the Chemistry, a salt reaction is added for each solid isomer. For each reaction Heat of fusion (HFusion) in the pure component databanks), the melting point (Tmelt), and the difference between the liquid and solid Cp at the triple point (DeltaCP) are entered to predict the freezing of the isomers. These parameters were found in the pure component databanks. HFusion is HFUS. Tmelt is FREEZEPT. DeltaCP is DCPLS.
The Chemistry can be used in a Heater or in a Crystallizer. The results will basically be the same since the solid formation is driven by flash/chemistry. The Crystallizer would allow to set/calculate particle size information if desired. When Chemistry is selected in Crystallizer the selected Salt Component ID does not affect the solid formation (solid/liquid equilibrium) calculation. It is only affecting the block results Crystal product and Magma density which are both calculated based on the selected salt component. If particle size or growth kinetics are not of interest the user can use the Heater or Flash block.
Parameters have not been regressed to match the ternary eutectic diagram of xylene rigorously. This example should be seen as example on how such system could be modelled.
Keywords: xylene
M-XYLENE
P-XYLENE
O-XYLENE
References: None |
Problem Statement: Excel VB Example to extract critical properties for streams from the Main Flowsheet and Sub-Flowsheet | Solution: This example macro demonstrates how to extract data across all streams from all sub-flowsheet including sub-flowsheets within sub-flowsheets.
This requires a recursive function that can call itself on the given flowsheet's sub-flowsheets. The attached example case demonstrates this with some selected variable from the simulation.
Note: This Excel macros will only return values if the critical properties is compatible with the given property package.
Keywords: Critical Properties, VBA, Excel,
References: None |
Problem Statement: How do you transfer multiple conditions without using the set operations? | Solution: The Set operation in Aspen HYSYS is used to transfer a condition such as temperature, pressure, flow from one stream to another stream. This operation can be used as follows:
Y2 = m X1 + c
Where, X1 is the condition in the source stream 1, m is the multiplication factor and c the offset. The Y2 is the calculated condition applied to stream 2. The parameters page of the Set block is shown below.
One Set operation can be used to transfer one condition only. If you require to transfer conditions then multiple Set operations can be added. An alternative approach would be import the source in a spreadsheet, add equations to calculate the results and export the calculated values to the target streams. This also allows any form of equation not limiting to the linear form as in the Set operation. The screenshot below shows as an example how this can be implemented in the spreadsheet.
An example is attached in thisSolution.
Keywords: Set Operation, Spreadsheet
References: None |
Problem Statement: With a significant portion of global power used in buildings it is therefore important to use efficient ventilation recovery to give better indoor air quality and energy utilization. Is it possible to model a ventilation recovery system through Aspen HYSYS? | Solution: Buildings that have high ventilation rates can reduce their heating load by recovering energy from any exhaust air streams. One way in which this can be done is by use of a run-around loop shown in the process below. As shown in the example HYSYS simulation, a run-around loop consists of two conventional liquid to air cross-flow heat exchangers.
An example simulation case has been attached to thisSolution which uses ethylene glycolSolution with 35% mass percent glycol pumped at a rate m=1 kg/s through both heat exchangers. During winter operation, the glycolSolution is heated by the warm air exiting in the exhaust duct. The warm glycolSolution is then used to preheat cold air entering from outdoors through the ventilation duct.
Keywords: Ventillation Recovery
References: None |
Problem Statement: How do I model and optimize a flash dryer in Aspen Plus? | Solution: The attached Aspen Plus V8.2 demo will show you how an industrial flash dryer can be modeled in Aspen Plus and how such dryer can be optimized to reduce its energy demand. There is an associated PDF to guide you through the steps.
This example will cover
· Basic description of the flash dryer model
· Using the pipe line model to determine the pressure drop and the saltation velocity
· Demonstrating the Aspen Plus optimization capability to determine optimal operating conditions to reduce the dryers total energy demand
· How reducing the drying agent flow rate and heater outlet led to a reduction in the energy demand by 28.8%.
Keywords: Solids Capabilities, Unit Operations, Drying, Conveying, Energy optimization
References: None |
Problem Statement: Do you have an example of regressing parameters for an electrolye mixture? | Solution: See the attached example files.
In this example, vapor-liquid equilibrium data and
enthalpy data for an aqueous HClSolution are used
to regress chemical equilibrium constant,
Henry's law constant, and activity coefficient
model parameters. Note that the Henry's law constant and chemical equilibrium constant are closely correlated. Enthalpy data are essential to accurately determine both constants.
Vapor liquid equilibrium data at 25 C,
Exp Val Est Val Exp Val Est Val Exp Val Est Val Exp Val Est Val
PRES PRES MOLEFR MOLEFR MOLEFR MOLEFR MOLEFR MOLEFR
X X Y Y Y Y
HCL HCL HCL HCL H2O H2O
torr torr
21.80 21.76 0.0306 0.0305 0.0001 0.0000 0.9999 1.0000
20.01 19.65 0.0520 0.0510 0.0003 0.0002 0.9997 0.9998
18.03 17.26 0.0745 0.0717 0.0018 0.0016 0.9982 0.9984
15.55 14.82 0.0978 0.0934 0.0095 0.0112 0.9905 0.9888
14.42 13.87 0.1099 0.1031 0.0222 0.0251 0.9778 0.9749
13.28 13.11 0.1223 0.1129 0.0512 0.0538 0.9488 0.9462
12.89 12.71 0.1350 0.1239 0.1156 0.1172 0.8844 0.8828
13.15 13.23 0.1479 0.1360 0.2433 0.2443 0.7567 0.7557
15.80 15.87 0.1612 0.1491 0.4462 0.4469 0.5538 0.5531
25.62 23.08 0.1747 0.1631 0.6676 0.6709 0.3324 0.3291
38.87 39.72 0.1887 0.1780 0.8361 0.8365 0.1639 0.1635
73.85 75.62 0.2029 0.1942 0.9276 0.9275 0.0724 0.0725
146.41 141.00 0.2175 0.2106 0.9576 0.9671 0.0424 0.0329
280.60 261.57 0.2324 0.2291 0.9699 0.9852 0.0301 0.0148
517.88 504.76 0.2478 0.2539 0.9944 0.9937 0.0056 0.0063
902.30 823.21 0.2635 0.2791 0.9975 0.9968 0.0025 0.0032
Enthalpy data at 25 C and 760 mmHg,
Exp Val Exp Val Est Val
MOLEFR HMX HMX
X LIQUID LIQUID
HCL
J/kmol J/kmol
0.5 -203690000 -202180000
0.4 -224570000 -224590000
0.3333 -237540000 -238690000
0.2857 -245730000 -247910000
0.25 -251500000 -254100000
0.2 -259250000 -261490000
0.1667 -264150000 -265800000
0.1429 -267520000 -268740000
0.1111 -271850000 -272610000
0.0909 -274510000 -275050000
0.0625 -278150000 -278490000
0.0476 -280020000 -280280000
0.0323 -281920000 -282130000
0.0196 -283470000 -283660000
0.0099 -284640000 -284820000
0.0025 -285530000 -285710000
Keywords: gmelcc
henry
k-stoic
kstoic
water
References: None |
Problem Statement: How to create streams in a loop by calling a sub-procedure. | Solution: The attached example in VB.NET illustrates how to create streams in a loop by calling a sub-procedure. The sub-procedure that creates the streams can be used for future projects. The code will allow to:
· Create a new Simulation
· Enter components and property method
· Create several streams in a loop by calling a sub-procedure
· The sub-procedure takes as arguments: name, temperature value and units, pressure and units and molar flow rate.
Keywords: VB.NET, COM Interfaces, Automation, create streams.
References: None |
Problem Statement: Optimization tool not taking into account input variables and is not showing any results after I run the simulation, even if it is specified properly. | Solution: When specifying the optimization tool and constraints it is important to remember to include in the calculation variables which are in active streams and blocks. If the blocks or streams which are included in the optimization input specification are deactivated, then Aspen Plus will not take these into account during the calculation and this is the reason why no results are shown in the optimization folder.
Activating the streams and blocks, containing the variables will allow Aspen Plus to compute the calculations properly and show all the results.
In the attached file you will find an example which shows how the optimization tool behaves when the value from a deactivated stream is used. To check if results will appear, right click on the EFFLUENT stream, select activate, reinitialize/reset simulation and run it again.
Note: The example was prepared based on available opt.bkp example from AspenTech KBSolution #102315
Keywords: Optimization, Deactivated Variables
References: None |
Problem Statement: How do I model and optimize mill drying in Aspen Plus? | Solution: The attached Aspen Plus V8.2 demo will show you how a mill drying can be modeled in Aspen Plus and how such dryer can be optimized to reduce its energy demand. There is an associated PDF to guide you through the steps.
This example will cover
· Basic description of the dryer model
· Using a convective dryer, crusher and sifter model to model drying, communition and classification inside the mill
· Demonstrating the Aspen Plus sensitivity analysis to determine optimal operating conditions to reduce the dryers total energy demand and at the same time fulfill the product specifications with regard to moisture and particle size distribution
Keywords: Solids Capabilities, Unit Operations, Drying, Crushing, Energy optimization
References: None |
Problem Statement: C# example: Creating a new simulation from the ground up through Automation. | Solution: This attached example in C# illustrates how to set up a simulation from the ground up through ActiveX interfaces in
Aspen Plus.
The code will allow you to:
· Create a new simulation
· Entering components and selecting the property method
· Create streams and a heater block
· Attach the streams to the block ports
· Entering stream specifications and block operating conditions
· Run simulation
· Console window feedback
Keywords: Aspen Plus interfaces example, ActiveX, Automation, C#, C sharp
References: None |
Problem Statement: For an activity coefficient model such as NRTL-RK, how do I get the mixture density to fit better. | Solution: Most activity coefficient property methods use the Rackett/Campbell-Thodos Mixture Liquid Volume model. This model has a binary parameter RKTKIJ. This parameter can be regressed for a better fit of mixture density data.
In the attached example file that can be opened in V7.3 and higher, liquid density data from NIST-TDE for a water-glycerol mixture is regressed.
Keywords: None
References: None |
Problem Statement: How RSTOIC, the stoichiometric reactor, calculates the heat of reaction. | Solution: Attached is an example from Chemical Engineering Design: Principles, Practice and Economics of Plant and Process Design by Towler and Sinnott (Second Edition, Copyright 2013) , Chapter 15, pages 643 to 645.
The reaction is the pyrolysis of 1,2-dichloroethane (C2H4CL2) to Vinyl Chloride (C2H3CL) and Hydrochloric Acid (HCl).
C2H4CL2 --> C2H3CL + HCL
In the Aspen Plus file, the conversion of 1 mole of C2H4CL2 at standard conditions (vapor at 1 ATM and 25C) is calculated for the RSTOIC reactor BASECALC using ideal properties to keep the hand calculation simple.
The hand calculation starts with the definition of the heat of reaction. For a case with no Heating or Cooling Duty,
Heat of Reaction = Enthalpy Leaving block - Enthalpy Entering block
Heat of reaction = enthalpy of products - enthalpy of reactants
As perSolution 3169, enthalpy can be written as the following expression,
H(T,P) = HIG(T) + DH(T,P)
With no phase change and ideal properties, the enthalpy departure DH(T,P) is zero, and the enthalpy (H) is simply the ideal gas enthalpy (HIG),
The ideal gas enthalpy (HIG) is the differences of the Heat of Formation (DHFORM) at the reference temperature.
HIG = DHFORM + Integral CPIG (from reference Temp. to system Temp.)
HIG = DHFORM at reference temperature
The Heat of Formation of the components in the reaction are as follows:
Data set
Units
Parameters
Component
Component
Component
HCL
C2H4CL
C2H3CL2
DHFORM
kJ/kmol
1
-92310
-129790
28450
Hence, the heat of reaction is
Heat of reaction = heats of formation of products - heats of formation of reactants
Heat of reaction = DHFORM(C2H3CL) + DHFORM( HCL) - DHFORM(C2H4CL2)
Heat of reaction = (28450) + (-92310) - (-129790)
Heat of reaction = 65930 kJ/kmol
This agrees with the results for the duty of the RSTOIC block BASECALC.
The heat of reaction from the reference is 70,224 kJ/kmol.
The same conversion of 1 mole of C2H4CL2 at standard conditions (vapor at 1 ATM and 25C) is specified for the RSTOIC reactor BASESPEC; however, in this case the heat of reaction is specified as 70,224 kJ/kmol. For this case the duty of the block is 70,224 kJ/kmol.
This case is simplified to a case of all vapor for illustration purposes to simplify the calculation. In reality, the feed is a liquid and the products are vapor at 25C. If you allow for a liquid phase for the feed, the duty of the reactor will rise to 105287.142 kJ/kmol since the heat of vaporization of the feed is also included.
Keywords: RSTOIC, thermodynamic, outlet, enthalpy, temperature, specific heat
References: None |
Problem Statement: How can I model a crusher specifying both inlet and outlet PSD as well as the power? | Solution: In a crusher you can either specify the PSD at the outlet or the power required along with the distribution function.
In case you want to have a particular power and a particular PSD outlet, the best option is to specify the outlet PSD and then add a Design Spec that changes the Hardgrove Grindability Index to adjust the power that you desire.
To use a particular outlet PSD, in the Specifications tab of the crusher unit operation, select Specify Outlet PSD. You can use a distribution function if you have one, if you have the PSD directly you can also use it.
In the design spec you need to specify the power as Block Var>BlockName>POWER. You will need to vary the HGI defining it as Block Var>BlockName>HGI>CIPSD. You will need to provide variable limits.
Attached is an example file where Jaw1 unit operation is specified with Outlet PSD and a design spec called JAW1DS contains the specified and varied variables. This file can be opened in Aspen Plus V8.4 and higher.
NOTE-This should be used if you have experimental data of the outlet PSD and the power used. If you know the material you should check the calculated HGI is in the range of that material, otherwise you might be getting unrealistic results.
Keywords: Aspen Plus, crusher, PSD, HGI, design spec
References: None |
Problem Statement: The density of fructose | Solution: s is poor. I have some data. What parameters should be regressed?
The attached concentration tables are based on the Handbook of Chemistry and Physics 70th Edition. found at
http://us.mt.com/us/en/home/supportive_content/application_editorials/D_fructose_de_e.html
D-Fructose
Concentration vs. density (20?C)
A % by wt.
Density [g/cm3]
0.50
1.0002
1.00
1.0021
1.50
1.0041
2.00
1.0061
2.50
1.0081
3.00
1.0101
3.50
1.0120
4.00
1.0140
4.50
1.0160
5.00
1.0181
5.50
1.0201
6.00
1.0221
6.50
1.0241
7.00
1.0262
7.50
1.0282
8.00
1.0303
8.50
1.0323
9.00
1.0344
9.50
1.0365
10.00
1.0385
11.00
1.0427
12.00
1.0469
13.00
1.0512
14.00
1.0554
15.00
1.0597
16.00
1.0640
17.00
1.0684
18.00
1.0728
19.00
1.0772
20.00
1.0816
22.00
1.0906
24.00
1.0996
26.00
1.1089
28.00
1.1182
30.00
1.1276
32.00
1.1372
34.00
1.1469
36.00
1.1568
38.00
1.1668
40.00
1.1769
42.00
1.1871
44.00
1.1975
46.00
1.2080
48.00
1.2187
50.00
1.2295
52.00
1.2404
54.00
1.2514
56.00
1.2626
58.00
1.2739
60.00
1.2854
62.00
1.2970
64.00
1.3086
66.00
1.3204
68.00
1.3323
70.00
1.3443
Solution
Using a Run type of Data Regression on the Setup | Specification | Global sheet, you can evaluate the parameters in Aspen Plus or regress new ones from data.
To do an evaluation run, specify a Calculation type of Evaluation for the Regression.
The result for fructose is quite poor.
To regress parameters, switch from Evaluation to Regression. The Rackett model is commonly used to calculate liquid molar volume. The parameter to regress for this model is named RACKET.
Regressing only one element gives a much better fit:
See the attached Aspen Plus V7.3 .bkp file.
Keywords: None
References: None |
Problem Statement: Is it possible to use Excel to control a RadFrac distillation column in Aspen Plus | Solution: Attached is an example of a MethylChlorate RadFrac distillation Column in Aspen Plus running in Excel using Aspen Simulation Workbook (ASW). This model illustrates the integration of ASW with an Aspen Plus model of MethylChlorate production by esterification.
In the following example, several features of Aspen Plus are illustrated using the Aspen Simulation Workbook. - *Reactive Distillation
*Three Phase Distillation
*Column with Total boilup
*Internal column specification with feed flow manipulation
*This application uses a decanter model.
The column contains temperature specifications that can be controlled from Excel using ASW. At the same time, the file can have plant data for model comparison.
A zip file is available for V8.4, V8.6 and V8.8 with the ASW file and a pdf with a detail description of the model.
To run the file please follow the instructions:
1) Download the zip file that corresponds to the version of Aspen Plus you have.
2) Open the Aspen Simulation Workbook file with Excel.
3) If ASW does not start running immediately go to the ASW tab and enable it.
4) Activate the simulation by clicking on the following button.
6) After that you should be able to interact with the Aspen Plus bkp file that is embedded inside the Excel file.
Keywords: Aspen Plus, ASW, Reactive Distillation, Tray Rating, Plant Data, Example
References: None |
Problem Statement: Using the demo file and this walkthrough, the user will learn how to properly use Activated Energy Analysis in Aspen HYSYS to revamp the existing heat exchanger network in order to reduce energy consumption in the developed process model. In order to access the Activated Energy Analysis features, Aspen HYSYS V8.4 and Aspen Energy Analyzer V8.4 or later versions must be installed. | Solution: The demo file is based on a simplified natural gas processing plant, modeled in Aspen HYSYS. Raw natural gas stream is first sweetened to remove the acid gas, and then the water content is removed in dehydration section. The dehydrated gases is cooled down by recovering cold heat source from the top of de-methanizer column and then further cooled by the refrigeration before being separated in the de-methanizer. The overhead from the column is further compressed and cooled before being sent to the gas pipeline for sales. The bottom liquid product is separated in the downstream columns for NGL recovery, which is not modeled in this example file.
Keywords: Activated Energy Analysis, NGL
References: None |
Problem Statement: Let's say that I have a stream with the following solids and I want to separate them for example by using a screen:
- Solid A: 50 kg/h SiO2 with PSD: 100% --> 0:20 mu;
- Solid B: 50 kg/h NaCl with PSD: 100% --> 180:200 mu.
How can I set my model with Aspen Plus? | Solution: The attached file shows how theSolution explained below is implemented in Aspen Plus v8.0.
To model the solids with a particle size distribution (PSD), we select the MIXCIPSD stream class under the Simulation environment, Setup | Specifications.
Since 2 different solids are present in this case, we have to specify 2 CIPSD substreams: one for each component. If we were putting both solids in the same substream, this would represent solid particles which are a mixture of the two components. To create a second CIPSD substream, go to the Setup | Solids | Substreams sheet, enter a name in Substream column (e..g CIPSD2), select the type CISOLID and select the PSD mesh ID as PSD.
Once this new substream CIPSD2 is created, go to the Setup | Stream Class, and on the Stream Class sheet, select the MIXCIPSD. Click the CIPSD2 in the Available substreams, then click the > button to bring it into the Selected substreams column. The substreams for the modified MIXCIPSD stream class will be:
MIXED
CIPSD
CIPSD2
In the input data for the streams, the solid A should be specified in the CIPSD substream, as one can see in the stream S1 of the attached file, and the solid B in the CIPSD2 substream, as per the stream S2 definition.
To illustrate this solid separation in Aspen Plus, one can use a SCREEN block. Other models dealing with solids can be used in a similar way.
The streams S1 and S2 are mixed for creating the stream S3, that is fed to the SCREEN block. In this block the cut size is set to 100 mu and the Rogers function is selected, then the screen is capable of separating two streams:
the overflow (stream S4): constituted mainly of B component with larger particles;
the underflow (stream S5): constituted mainly of A component with smaller particles.
Keywords: SCREEN, solids, CISOLID substream
References: None |
Problem Statement: How do I configure the controlled flow blowdown using depressuring utility in Aspen HYSYS? | Solution: The depressuring utility can be configured to implement controlled flow blowndown. The user can specify the vapour mass flow and bypass any valve equation. The mass flow rate can be specified in the spreadsheet is located in the Depressuiring sub-flowsheet.
The specified value can be in any unused cell in the specified. The screenshot below shows the fixed vapour flow in cell B11. A conditional statement as shown below can be added modifying the calculation in this cell.
@if (B16>=B15, B11, 0)
The attached case serves an example illustrating how the controlled flow blowdown can be implemented in the depressuring utility. A similar configuration can be made for fixed liquid blowdown in the “LiquidFlowRate” spreadsheet.
Keywords: Controlled blowdown, Depressuring Utility
References: None |
Problem Statement: How do I simulate subcooling of a saturated liquid stream (e.g. separator or column bottom product) without using heat transfer, prior to entry to a pump in Aspen HYSYS Steady State?
Background
Subcooling of a saturated liquid stream prior to pump (e.g. centrifugal pump) entry is important in industry. If saturated liquid is fed into a centrifugal pump, it is very likely that there will be cavitation within the pump (leading to mechanical damage).
To produce subcooling (without physically cooling the stream), the pressure of the saturated stream is increased. This results in a subcooled liquid stream. To achieve this, the interconnecting piping from the vessel bottom connection to the pump inlet is designed for minimal pressure drop and a downward flowing, elevation profile so as to produce sufficient static head for subcooling. The target is to meet the required Net Positive Suction Head (NPSH) as advised by the pump vendor.
During the initial design (simulation) phase of the process, it is not typical to specify line sizes. As such, it may not be suitable to use a Pipe Segment in the simulation. However, a level of subcooling (i.e. pressure increase relative to saturation pressure) is normally specified, e.g. 100mbar subcooling. | Solution: In the attached example file:
1. Use a Balance block to transfer the Component Mole and Heat Flow from the saturated stream to a new stream.
2. Use a Set block to increase the pressure of the new stream (relative to the saturated stream). The Target Variable will be the new stream pressure with the Source Object being the saturated stream. In the Parameters tab, specify the level of pressure subcooling as the Offset (positive value).
Keywords: Subcooling, Separator liquid product, Pump suction, Cavitation, Balance, Set
References: None |
Problem Statement: Design and Simulate a Vertical Thermosiphon Reboiler Using Aspen Shell & Tube Exchanger | Solution: This new Design Guide offers step by step instructions for the design & simulation of vertical thermosiphon reboilers using Aspen Shell & Tube Exchanger. Thermosiphon reboilers are commonly used in chemical processing and refining for vaporizing lighter fractions at the bottom of a distillation column and returning them to the two-phase stream at the appropriate separation stage. They require less capital and maintenance costs, making them an attractive alternative to pumped systems with kettles or other forced flow reboilers.
In simulation the program will calculate what circulation rate can be achieved. It also checks for risk of instability. The guide also provides two additional recommendations to evaluate how to control operation with shell side flooding and how to trouble-shoot potential instability associated with clean start up conditions.
In addition to the document, two EDR case files have been included: one for the design, and one for the simulation to let you explore modeling for yourself.
Keywords: design, thermosiphon, simulation, shell & tube
References: None |
Problem Statement: How can a user design a distillation column using DSTWU unit? | Solution: In this series of knowledgebaseSolutions, we demonstrate column targeting using the tools available in AspenPlus. The background on column targeting can be found in the work of V. R. Dhole and B. Linnhoff [2]. We use the LNG fractionation unit considered in the research of H. E. Alfadala, B. M. Ahmad, A. F. Warsame [1]. An Aspen Plus V7.3 backup file is attached. This file will run in V7.3 and higher.
Before a column targeting study, we need to determine a conceptual design based on the separation requirements. In AspenPlus, DSTWU is a easy-to-use tool for this purpose. We use DSTWU to predict the number of stages, and estimate feed location.
The feed and products specifications of a LNG fractionation unit are as following:
Table 1. Feed and Products of LNG Fractionation Unit
Properties
Feed
Top
Bottom
Mass flow (kg/hr)
25736
10287
15449
Temperature (C)
77.4
Pressure (bar)
6.62
6.52
6.76
Vapor fraction
0.00
0.00
0.00
Mole fractions
Propane
0.05388
i-Butane
0.14808
n-Butane
0.29493
(LK) 0.55049
Methyl-Butane
0.13301
(HK) 0.26470
n-Pentane
0.12368
n-Heptane
0.23114
Benzene
0.00941
Toluene
0.00587
In Aspen Plus, we use UNIFAC as property method for this LNG column. In DSTWU unit operation, the reflux ratio is specified at 3.5, light key (n-Butane) recovery is 0.976, and heavy key (methyl-butane) recovery at top is 0.051.
The calculated minimum number of stages is 7, and feed location is stage 4.
The plot of reflux ratio vs. number of minimum stages is shown below.
Figure 1. Reflux ration vs number of stages
From the above results, we select 15 stages for RadFrac model in the next step, with the anticipation of reducing reflux ratio to 1.5 or 2.0.
Keywords: Column targeting, column design
References: s
[1] ?A Hierarchical Approach to Optimize LNG Fractionation Units?, H. E. Alfadala, B. M. Ahmad, A. F. Warsame, European Symposium on Computer Aided Process Engineering 15, 2005.
[2] Distillation Column Targets, V. R. Dhole and B. Linnhoff, Computers Chem. Engng, Vol. 17, No. 5/6, pp. 549-560, 1993. |
Problem Statement: VBA example for Automation Server in Aspen HYSYS. | Solution: Automation Server in Aspen HYSYS gives users the ability to programmatically interact with the application through objects exposed by the program. By using an Automation client like Visual Basic, the end user can write the code to access these objects and interact with HYSYS. The exposed objects make it possible to perform nearly any action that is accomplished through the HYSYS graphical user interface.
With the Automation interface, users can:
· Create new applications that invisibly use HYSYS in the background. Programs such as Microsoft Visual Basic and Microsoft Excel can use HYSYS as a calculation engine.
· Bring automation to their workflows, eliminating redundant tasks and increasing efficiency.
· Connect both the inputs and the results of HYSYS simulations to other applications such as design programs or databases.
· Write your own user interface to an HYSYS plant model. You can use this interface to distribute your plant model to others who can run the simulation case without learning to use HYSYS user interface.
The presentSolution provides an example of automation in HYSYS. The attached excel file includes VBA code that will allow to:
· Open any HYSYS case file.
· Change pressure, temperature, and flow in the streams selected by the user.
· Add a spreadsheet operation and link variables from a selected stream to another.
· Save and close the simulation
Keywords: ActiveX, VB, VBA, Visual Basic, Automation Server, getting started, examples.
References: None |
Problem Statement: How do I configure PQ curve for wellhead modelling in Aspen HYSYS? | Solution: In Aspen HYSYS V7.3 and higher versions the options for the wellhead PQ relationship is made available in the extension group (for V7.3) and custom group for V8.0 and higher versions.
Â
This extension allows the users to configure Flow vs. Wellhead pressure as shown in the screenshot below.
Â
Â
The regression coefficients for the curve can entered manually or regressed from the tabular flow vs. pressure data. You connect the well fluid as the product stream and specify a dummy stream for the inlet. The PQ curve calculates the flow in the product stream if the pressure is specified and vice versa.
See the attached sample HYSYS case for further details of the PQ relationship.Â
Keywords: PQ Curve, Wellhead
References: None |
Problem Statement: How do I model crystallization and consider economics for solids processing in Aspen Plus? | Solution: The attached Aspen Plus V8.2 demo will show you how a process that contains both fluids and solids can be simulated and optimized with Aspen Plus. The process involves crystallization, solid/liquid separation by hydrocyclones, drying, solid/gas separation by gascyclones, compacting, screening and crushing of particles. The demo uses activated economics to compare different design scenarios. There is an associated PDF to guide you through the steps.
This example will cover
· Optimizing the current layout of the process to allow for a higher production rate while fulfilling capacity constraints of the current equipment
· Considering an alternative design to fully utilize the capacity of the process and with this further increase the production rate
· Use activated economics to compare capital costs and payback period
Keywords: Solids Capabilities, Unit Operations, Crystallization, Hydrocyclone, Drying, Compacting, Screens, Activated Economics
References: None |
Problem Statement: Based on a conceptual design, how to model the column rigorously and generate CGCC(T-H) curve? | Solution: In this series of knowledgebaseSolutions, we demonstrate column targeting using the tools available in AspenPlus. The background on column targeting can be found in the work of V. R. Dhole and B. Linnhoff [2]. We use the LNG fractionation unit considered in the research of H. E. Alfadala, B. M. Ahmad, A. F. Warsame [1]. An Aspen Plus V7.3 backup file is attached. This file will run in V7.3 and higher.
In thisSolution, we continue to develop the LNG fractionation unit. In the previous step (KB 135408), a conceptual design is calculated. In this document, we transfer the results of the conceptual design to a rigorous distillation column model. In Aspen Plus, the rigorous distillation model RadFrac is used to model the LNG fractionation unit.
From conceptual design, we reached a column that has 15 theoretical stages, total condenser and kettle reboiler. The column will operate at reflux ratio 3.5 and distillate rate 179 kmol/hr.
For this column, we ?include column targeting thermal analysis?, with ?user defined? key components, n-butane as light key and methyl-butane as heavy key. The plot wizard will generate CGCC(T-H) curve, as shown below.
Figure - CGCC (T-H) curve for the base case
Next, we show the effect of adjusting the feed location.
Keywords: Column targeting, column design
References: s
[1] ?A Hierarchical Approach to Optimize LNG Fractionation Units?, H. E. Alfadala, B. M. Ahmad, A. F. Warsame, European Symposium on Computer Aided Process Engineering 15, 2005.
[2] Distillation Column Targets, V. R. Dhole and B. Linnhoff, Computers Chem. Engng, Vol. 17, No. 5/6, pp. 549-560, 1993. |
Problem Statement: Example of Liquefied Natural Gas Plant | Solution: This document tries to provide a model for the LNG process, it intended to:
? Provide an example of how to model the different sections of LNG process
Supply a starting set of components and physical property parameters for modeling processes of this type
The model is not intended for equipment design or for specifying other engineering documents without further review by a process engineer with experience of LNG processes.
The model includes:
A nominal set of chemical species and property parameters for this process.
Typical process areas including: Acid gas removal, Natural Gas dehydration, Propane Pre-Cooling Train, Compressor Train, LNG Section, and the main streams connecting these units and sections.
Key process control specifications such as mixed refrigerant flow rate.
Keywords: LNG Process, LNG Plant etc
References: None |
Problem Statement: Example case for calculating Latent Heat or Heat of Vaporization for a mixture in Aspen HYSYS. | Solution: Knowledge BaseSolution 105227 uses an example case to illustrate Latent Heat calculation for a mixture in Aspen Plus. Here is an example to illustrate the calculation in Aspen HYSYS. In Aspen HYSYS, the Heat of Vaporization of a mixture is defined as the enthalpy difference between the bubble point and the dewpoint at a fixed pressure (Knowledge BaseSolution 108992)
In the example, a heater block is used to perform the vaporization with zero pressure drop. The Mass Enthalpy difference between the feed and product stream indicate the Heat of Vaporization.
Keywords: Latent Heat, Example case, Heat of Vaporization
References: None |
Problem Statement: How do I configure the Recycle block for Backward transfer of a variable? | Solution: The default configuration of the Recycle block is set to run in Forward transfer mode. In this mode the Recycle block transfers variables from the inlet stream to the outlet stream. The transfer direction in this block can be set as Backward. In Backward transfer mode the selected variable(s) can be transferred from the product to the feed stream. The following steps illustrate how this can be achieved.
1. Open the attached case HYSYS case RECY1-F.hsc
2. Set the parameter of Mixer 1 “Equalize All”
3. Delete the pressure of stream RECY 1 Out. Check that this pressure is calculated by Mixer 1
4. Open RCY-1 and change the Transfer Direction for pressure Backwards
5. Now change the pressure of “LD1 Out” from 1725 to 1800 kPa.
You will see that pressure in LD1 Out is set by the REY-1 as 1725 kPa. The Backwards transfer mode transfers the pressure from the outlet to the inlet stream.
You can try changing the pressure of the Feed stream. You will see that the pressure of LD1 Out will be updated as you change the pressure of the Feed stream.
Note: When you transfer a variable in Backward make sure to have an initial value of that variable in the inlet stream. When the value changes in the outlet stream the inlet stream will be updated accordingly.
Keywords: Recycle Block, Backward Transfer
References: None |
Problem Statement: How to regress the aqueous phase heat capacity at infinite dilution (CPAQ0) | Solution: Related technical tip documents:Solution ID 128120: How do you regress enthalpy, heat capacity and VLE data for an electrolyteSolution?Solution ID 113569: How is Aqueous Heat of Formation Used?
The equation for the electrolyte NRTL enthalpy model (HMXENRTL) is:
The aqueous infinite dilution thermodynamic enthalpy Hk∞ is calculated from the infinite dilution aqueous phase heat capacity, as follows:
The aqueous phase infinite dilution enthalpies, entropies, and Gibbs energies are calculated from the heat capacity polynomial. The values are used in the calculation of aqueous and mixed solvent properties of electrolyteSolutions:
The Criss-Cobble correlation for aqueous infinite dilution ionic heat capacity is used if no parameters are available for the aqueous infinite dilution heat capacity polynomial. From the calculated heat capacity, the thermodynamic properties entropy, enthalpy and Gibbs energy at infinite dilution in water are derived:
In this document the regression of the heat capacity (CPAQ0) parameter is explained. A mixture data file of the heat capacity values (CPLMX) can be used for this purpose.
Obviously, a wider range in temperature and more data files will ensure a more accurate regression.
The property calculation method is selected to be the ELECNRTL.
In the parameter tab the CPAQ0 is selected and take note that the “element� field refers to the coefficients in the polynomial expression used to calculate this parameter.
The regressed values can be seen in the results folder.
Keywords: , Regression, CPAQ0, aqueous phase heat capacity at infinite dilution
References: None |
Problem Statement: Trying to get the Aspen hydraulics simple pipe segment to calculate the fluid mass flow across a large pressure drop returns incorrect pressure profile | Solution: In the example file attached you will notice that the Aspen Hydraulics sub-flowsheet has a single pipe modeled with only pressure as the boundary specifications. This is the normal workflow to enable Aspen hydraulics implementing a mass flow calculation, i.e, provide only the pressures of the inlet stream and the outlet stream attached to the pipe.
The boundary pressure specs are such that the user is anticipating a steep pressure drop across an 80 km pipe, hence simulating choked flow conditions across a long distance. Inlet pressure is at 5000 KPa while exit pressure is set at 100 KPa. You will notice that in the snapshot below, the pipe pressure profile shows a steady decrease along the length of the pipe, until about 40km. After that, the pressure drops to 100 KPa, which is the exit pressure, and remains constant for the remaining length of the pipe. See snapshot 1 below. This same model built with the Aspen Hysys pipe segment would typically give a choked flow error, but the Aspen hydraulics rigorous solver will converge the pipe, as shown in Pipe flow1.hsc.
Snapshot 1
To improve the solver and generate a more realistic pressure drop profile, go to the Steady State tab of the Aspen Hydraulics subflowsheet and reduce the Min. Jacobian flow step size, to say 0.001kg/h. This is implemented in Pipe flow2.hsc. This is shown in snapshot 2 below, where the pressure profile shows a more consistent decrease in pressure until the pipe exit.
Snapshot 2
Please note that the pipe feed stream still needs a known temperature and stream reference conditions, as is the usual workflow in setting up a Aspen hydraulics flowsheet.
Keywords: Aspen Hydraulics, flow step size, pressure drop profile, hydraulics pipe, choke flow.
References: None |
Problem Statement: How would I use Aspen Simulation Workbook (ASW) to develop an interface for an Aspen Custom Modeler (ACM) model of the Batch Reaction for PVC? | Solution: PVC is the third largest commodity plastic manufactured in the world. Approximately 75% is manufactured via suspension polymerization. ThisSolution contains a description of the PVC Reaction Process in the attached Slides as well as files containing the ACMF, BKP and APRPDF files required to run the ACM model. An Excel sheet containing the ASW interface to the model is also included.
Keywords: Polyvinyl chloride, batch reaction, batch reactors, Aspen Custom Modeler, Aspen Polymers, Aspen Simulation Workbook, Excel Interface
References: None |
Problem Statement: How do I model crushing/milling and classification of solids in Aspen Plus? | Solution: The attached Aspen Plus V8.2 demo shows how a multi-step crushing and classification process can be simulated in Aspen Plus and how this process can be optimized with regard to energy demand. There is an associated PDF to guide you through the steps.
This example will cover
· Simulation of a grinding process with multiple crushers and screens
· Optimization study to increase throughput and decrease mass specific energy demand
Keywords: Solids Capabilities, Unit Operations, Crusher, Crushing, Grinder, Grinding, Milling, Classification
References: None |
Problem Statement: How do I generate saturation curves of water in nitrogen over a temperature and pressure range? | Solution: A simple model is set up to demonstrate the scheme of generating the saturation curves. Dry nitrogen at fixed flowrate (100 kmol/hr) and specified pressure is mixed with water feed in a mixer. The product of the mixer goes through a heater unit to reach a specified temperature. A design specification is defined to regulate the relative humidity on the outlet of the heater by adjust the flowrate of the water feed stream.
The curves are generated in sensitivity analysis. The pressure of the dry nitrogen stream and the outlet temperature of the heater are varied in the sensitivity analysis.Â
Keywords: Saturation, water saturation, water saturation curves.
References: None |
Problem Statement: When to consider feed conditioning in column targeting? | Solution: In this series of knowledgebaseSolutions, we demonstrate column targeting using the tools available in Aspen Plus. The background on column targeting can be found in the work of V. R. Dhole and B. Linnhoff [2]. We use the LNG fractionation unit considered in the research of H. E. Alfadala, B. M. Ahmad, A. F. Warsame [1]. An Aspen Plus V7.3 backup file is attached. This file will run in V7.3 and higher.
In this document, we consider the third step, feed conditioning, in column targeting discussed by V. R. Dhole and B. Linnhoff [2].
Following setting up the rigorous distillation model shown inSolution 135443, the feed stage location and reflux ratio can be adjusted as shown inSolution 135444 and 135445 respectively. Next, we add a pre-heater with a duty of 0.4 MMKcal/hr. Now the reboiler duty is reduced, and is closer to that of the condenser.
Figure - CGCC (T-H) curve after adding a pre-heater for the feed
Keywords: column targeting
References: s
[1] ?A Hierarchical Approach to Optimize LNG Fractionation Units?, H. E. Alfadala, B. M. Ahmad, A. F. Warsame, European Symposium on Computer Aided Process Engineering 15, 2005.
[2] Distillation Column Targets, V. R. Dhole and B. Linnhoff, Computers Chem. Engng, Vol. 17, No. 5/6, pp. 549-560, 1993. |
Problem Statement: Description on how to calculate the activity coefficients for a ternary diagram. An example file developed in V8.0 included as reference. | Solution: 1. Under Properties Environment, go to Setup | Specifications | Global and select Vapor-Liquid-Liquid as valid phases. Click Next button.
2. Select the components. Click Next button.
3. Select the property method. An activity coefficient model based method that can handle two liquid phases should be selected as this point.
4. Select the property to be used in the Analysis. For this purpose:
a. Go to Property Sets folder and create a New Prop-Set.
b. On Properties tab, select the physical property GAMMA. It represents the activity coefficient for a component in a liquid mixture. It is dimensionless.
c. On Qualifiers tab, select 1st Liquid and 2nd Liquid as Qualifiers, since for a ternary system, two liquid phases are expected. By default all the components are included in the calculations, so it is not necessary to specify the components under Qualifiers.
5. Create a new Property Analysis.
a. Go to Analysis folder (whether through the Navigation Pane or through Home Ribbon selecting Analysis) and create a new case. Enter a name or leave the default one (PT-1) and select type: Generic.
b. On System tab, select “Points along a flash curve”, select the component flow basis (mol, mass or Standard liquid volume) and set the flow of each component.
c. On Variable tab, specify the temperature and pressure of the system. As adjusted variables select the flow of each of the components of the system, this means there will be three adjusted variables.
i. Define the range of each adjusted variable. For this, select the variable, click Range/List and fill the Adjusted Variable Range/List Options window with the list of values or the Range and set Lower and Upper limits and the number of Points.
ii. Repeat this step for all the adjusted variables.
d. On Tabulate tab, select the property set created on step 4.
6. Run the simulation. You might expect to get a Warning message “Total flow is zero” if zero flow was included in the Range/List of the adjusted variables. If this is the case, in a certain point of the analysis all flows are zero, therefore, the Warning message.
7. Check the results under Analysis | PT-1 | Results.
Keywords: GAMMA, activity coefficient, ternary diagram
References: None |
Problem Statement: How to model Wax Deposition in HYSYS? | Solution: The topic is upstream. But the model does not require the upstream license to run. This concerns the calculation of wax deposition in the lines. The case has the correlations set up and it has some wax deposition tuning data in it. To get a good prediction of wax deposition, you do need some lab data for the tuning. To my knowledge there isn't a predictive method available for the moment that can give a reliable estimate of wax deposition without tuning data.
When doing an example on wax deposition, note that you have the enter an initial wax deposition thickness, although it is quite logical to take a starting point with no wax deposition at all, the default is just empty fields.
Keywords: Aspen Hydraulics
References: None |
Problem Statement: Is it possible to report the heat capacity of a non-conventional component, such as coal? | Solution: For reporting the heat capacity for NC components, one has to follow the steps below:
1. Define a new Property Set from the Simulation Environment. Select the ‘Substream: NCPSD’(see the image below);
2. Use the ‘Search’ button in the Properties sheet of the new Property Set and look for heat capacity. Select the property HEAT-CAP (Mass heat capacity of a nonconventional component in a solid phase), that the search brings up;
3. Under the Qualifiers tab, select the component and set Phase=Solid;
4. Include the property set in the stream report FULL from Simulation environment | Setup | Report Options | Stream sheet, click on the Property Sets and select the new property set;
5. Set the stream report format to FULL from the stream results and after running the simulation the heat capacity of the nonconventional solid will be displayed in the Stream Results.
An example file with the application of this workflow to a coal stream is attached.
Keywords: Non Conventional component, Cp, HEAT-CAP
References: None |
Problem Statement: When to adjust feed location in column targeting? | Solution: In this series of knowledgebaseSolutions, we demonstrate column targeting using the tools available in AspenPlus. The background on column targeting can be found in the work of V. R. Dhole and B. Linnhoff [2]. We use the LNG fractionation unit considered in the research of H. E. Alfadala, B. M. Ahmad, A. F. Warsame [1]. An Aspen Plus V7.3 backup file is attached. This file will run in V7.3 and higher.
In this document, we start the column targeting study as discussed by V. R. Dhole and B. Linnhoff [2]. The first step is to adjust feed location.
In the previous step (KB 135443), we converged a rigorous distillation model. Using RadFrad | Analysis, column targeting thermal analysis and hydraulic analysis can be generated. When feed location changes, the feed point will change. The goal is to select a feed stage so that the pinch point is shifted to right.
The first step in column targeting is to adjust the location of feed stage. The sharp enthalpy change between pinch point and stage below (stage 9 and 10) suggests that the feed location should be moving up. If we change the feed location from stage 10 to stage 7, the sharp enthalpy change disappears, and the projection of the pinch point is shifted to the right. This pinch point shift gives more space for adjusting reflux ratio, see the figure below.
Figure - CGCC (T-H) curve after feed stage is changed to stage 7
Keywords: column targeting, feed location
References: s
[1] ?A Hierarchical Approach to Optimize LNG Fractionation Units?, H. E. Alfadala, B. M. Ahmad, A. F. Warsame, European Symposium on Computer Aided Process Engineering 15, 2005.
[2] Distillation Column Targets, V. R. Dhole and B. Linnhoff, Computers Chem. Engng, Vol. 17, No. 5/6, pp. 549-560, 1993. |
Problem Statement: How do I use Conceptual Solids Modeling in Aspen Plus? | Solution: The attached Aspen Plus V8 demo will show you how to use conceptual solids models in Aspen Plus to model a solids processing step with only a few parameters. This conceptual model is used to gain an understanding of the impact of the processing steps on the entire BPA Production process at hand. There is an associated PDF to guide you through the steps.
This example will cover
· Basic description of the conceptual models available and why they are useful
· Using a conceptual model to describe a centrifuge and understand the impact of the rotation speed on the energy demand of the entire process
· Demonstrating how a conceptual model can easily be switched to rigorous so that it can further investigated.
Keywords: Solids Capabilities, Unit Operations, Conceptual Models, Shortcut Models, BPA Production
References: None |
Problem Statement: Example file of a script to create a column template that replaces a reboiler energy stream with a utility steam. | Solution: For the full procedure to create a column please reviewSolution 115038 for detailed information on the steps to create the column. The attached SCP file was created to provide an example of how this procedure can be automated using scripting language in Hysys. It is also intended to be used as a template to quickly create a column with a standard format that replaces the energy stream of the column Reboiler.
To run the script, download the SCP file and make sure you are in the Simulation Environment before running the script.
The column will use your default property package in many cases called Basis-1. Go to the Tools menu and select the Script Manager.
A window will appear and you will have to look for the file in the directory where you download it.
Look for the file, select it and click on play button to run the script.
Notes:Â
The script will create a column named T-100; if you have one column in your simulation named T-100 already, please rename that column before running the script.
Some advantage of using a script instead of VBA macro is that SCP files are not version dependent and there is no need to load reference library to run the file.
Script manager is all you need to run the SCP file and a regular text editor can modify the file.
If you will like to append streams in the parent environment that attaches to the column use the AttachObject sentence at the end of the Script as follows:
AttachObject FlowSht.1/UnitOpObject.400(T-100) :Stream.500.0 NullObject Create Steam_In
AttachObject FlowSht.1/UnitOpObject.400(T-100) :Stream.511.0 NullObject Create Ovhd Vapour
AttachObject FlowSht.1/UnitOpObject.400(T-100) :Stream.511.1 NullObject Create Distillate
AttachObject FlowSht.1/UnitOpObject.400(T-100) :Stream.511.2 NullObject Create Q-Condenser
AttachObject FlowSht.1/UnitOpObject.400(T-100) :Stream.511.3 NullObject Create Steam_Out
AttachObject FlowSht.1/UnitOpObject.400(T-100) :Stream.511.4 NullObject Create Liquid Bttm
Keywords: Script, Script Manager, Duty Stream, Column Reboiler, AttachObject
References: None |
Problem Statement: When to adjust reflux ratio in column targeting? | Solution: In this series of knowledgebaseSolutions, we demonstrate column targeting using the tools available in AspenPlus. The background on column targeting can be found in the work of V. R. Dhole and B. Linnhoff [2]. We use the LNG fractionation unit considered in the research of H. E. Alfadala, B. M. Ahmad, A. F. Warsame [1]. An Aspen Plus V7.3 backup file is attached. This file will run in V7.3 and higher.
In this document, we consider the second step, adjusting reflux ratio, in column targeting discussed by V. R. Dhole and B. Linnhoff [2].
Following setting up the rigorous distillation model shown inSolution 135443, the feed stage can be adjusted as shown inSolution 135444. The gap between the pinch point and the ordanite after analyzing the feed stage location suggests that the duties in the reboiler and condenser can be reduced by reducing reflux ratio. If we change the reflux ratio from 3.5 to 1.5, we observe significant reduction in conderser and reboiler duty on the CGCC(T-H) curve, see figure below.
Figure - CGCC (T-H) curve after reflux ratio is reduced to 1.5
Keywords: column targeting
References: s
[1] ?A Hierarchical Approach to Optimize LNG Fractionation Units?, H. E. Alfadala, B. M. Ahmad, A. F. Warsame, European Symposium on Computer Aided Process Engineering 15, 2005.
[2] Distillation Column Targets, V. R. Dhole and B. Linnhoff, Computers Chem. Engng, Vol. 17, No. 5/6, pp. 549-560, 1993. |
Problem Statement: How do I configure delayed blowdown using the depressuring utility in Aspen HYSYS? | Solution: The mass flow rate through the vapour valve is calculated in a spreadsheet for Supersonic, Subsonic, Masoneilan and General equations. The spreadsheet is located in the Depressuiring sub-flowsheet.
The user can modify the calculations in the spreadsheet “VapourFlowRate� and incorporate a delayed blowdown if necessary. To implement this the user needs to specify the time delay in a cell such as in cell B11 and then add a conditional statement in cell B12. The integrator time is in cell B16. The conditional statement can be as follows:
@if (B16>=B11, CalcFlow, 0)
The attached case serves an example illustrating how the delayed blowdown can be implemented in the depressurization calculation.
Keywords: Depressuring Utility, Delayed Blowdown
References: None |
Problem Statement: How do I use an in-line experimental correlation for calculating the Murphree stage efficiencies to be used in a RadFrac model? | Solution: One can use a Calculator block and write the correlation either via Fortran or Excel; the Calculator block has to be linked with the RadFrac block by accessing its efficiency sheet. One can select one of the following options from the RadFrac | Specifications | Efficiencies | Options sheet:
· Specify stage efficiencies;
· Specify efficiencies for individual components;
· Specify efficiencies for column sections.
According to which option is selected, the variable name to be specified from the calculator block has to be respectively:
· STAGE-EFF, with ID1 representing the stage number;
· COMP-EFF, with ID1 representing the stage number and ID2 the component ID;
· STEFF-SEC, with ID1 representing the section number.
In the attached example file, the Murhpree stage efficiency option is considered and a description of the workflow is provided below.
The Murphree efficiency option has to be selected in the RadFrac block under Block | B1 | Specifications | Efficiencies | Options. Then one can use the Vapor-Liquid sheet (image below) for inputing initial values for the stage efficiencies. These values will be overwritten by the Calculator block, but it is important to specify them for defining the variables that can be accessed.
The subroutine for calculating the Murhpree efficiencies has to be written inside the Calculator block C-1: one can use either a Fortran or an Excel subroutine.
For accessing and overwriting the stage efficiency values specified from the Block | B1 | Specifications | Efficiencies | Vapor-Liquid sheet, the variable STAGE-EFF must be used, where the ID represents the number of stage (see image below).
It is important to note that one can overwrite only variables that are input in the simulation then, in the example, according to the Vapor-Liquid, one can modify the efficiencies for stages 1, 2, 11, 12, 19, 20.
After running the simulation, one can then check the values of efficiencies taken into account by Aspen Plus into B1 | Profiles | Efficiencies sheet (print-screen below).
As an alternative, instead of providing stage efficiencies, one can also consider to use a rate-based modeling approach: this approach uses mass- and heat transfer correlations based on transfer properties and tray/packing geometry to predict column performance, without the need of efficiency factors.
Keywords: Murphree, STAGE-EFF
References: None |
Problem Statement: What's New in Aspen Plus V7.3.2 - Navigation and Forms | Solution: This tutorial reviews changes in forms and form navigation with the new Aspen Plus. In this animated tutorial you will learn how to use the navigation pane and how to use and manage forms.
Play viewlet now!
Keywords: None
References: None |
Problem Statement: What's New in Aspen Plus V7.3.2 - Creating and Editing Plots | Solution: Plotting is faster and easier than ever before with the new Aspen Plus. Watch this 4 minute tutorial to learn how to create and edit plots in the new Aspen Plus.
Play viewlet now!
Keywords: None
References: None |
Problem Statement: The sulfur recovery process involves many energy-intensive steps, where process streams must be heated and cooled to achieve conversion and sulfur removal. A bottlenecked sulfur recovery system can prevent processing of high sulfur feedstock leading to significant opportunity loss.
Tracking the sulfur content throughout the unit and considering catalyst degradation in the model of the SRU can help users better predict the performance. | Solution: The functionality available for decades as part of standalone Sulsim has been completely incorporated into Aspen HYSYS V9. AspenTech and Sulphur Experts have independently validated and verified that all pre-existing functionality works as designed in the Aspen HYSYS environment.
Added to Aspen HYSYS, the Sulsim property package, SRU sub-flowsheet environment, and unit operations can be used to accurately simulate all commercial process configurations for the Claus process with over 30 unit operations. Additionally, new features not available in the latest version of Sulsim were added in Aspen HYSYS V9.
Sulsim Sulfur Recovery adds to the recently added Acid Gas Cleaning technology in Aspen HYSYS. Optimizing the acid gas cleaning and sulfur recovery design and operations together can allow for more insight into the process, leading to better decision making. The two are closely connected and usually operate together creating process dependencies that cannot be efficiently optimized separately.
Learn about Sulsim Sulfur Recovery in Aspen HYSYS V9 with this 30-minute video.
Sulsim Sulfur Recovery in Aspen HYSYS V9 by Chad Mondor
Keywords: Sulfur Recovery, Claus Process, Sulsim, Sulphur Recovery, SRU
References: None |
Problem Statement: Aspen InfoPlus.21 Administrator 속성의 Record Utilization 에서 이미 사용한 license points 를 확인할 수 있지만 매개 definition family가 license points 를 사용한 내용을 확인할 수 없음. | Solution: 1. 사용한 licensed points 확인
Aspen SQLplus v2004.2에는 새로운 기능이 포함되였고 아래와 같은 명령어로 사용한 license points를 확인할 수 있음
WRITE GETPOINTCOUNT;
낡은 버전에서는 아래와 같은 명령으로 확인할수 있음
SELECT count(*) AS Total Licensed Points Used FROM ALL_RECORDS
WHERE DEFINITION IN
(SELECT DISTINCT name FROM DefinitionDef.1 WHERE history_field_pntr <> 0);
2. 매개 definition family에서 사용한 license points 확인
SELECT DEFINITION AS Definition Family, count(*) AS Total Licensed Points Used FROM ALL_RECORDS
WHERE DEFINITION IN
(SELECT DISTINCT name FROM DefinitionDef.1 WHERE history_field_pntr <> 0)
GROUP BY DEFINITION;
3. 모든 records가 사용한 license points 와 소속된 definition family를 나열
SELECT name AS Record Name, DEFINITION AS Definition Family FROM ALL_RECORDS
WHERE DEFINITION IN
(SELECT DISTINCT name FROM DefinitionDef.1 WHERE history_field_pntr <> 0)
ORDER BY name;
Keywords: license points
utilization
definition
definition record
definition family
definitiondef
KR-
References: None |
Problem Statement: 装置ごとのアラームサマリー、ログがアップグレード時に移行できない。 | Solution: 以下の４個のレコードを oktomodify.inpに追加する。
IP_PimsAlarmAckLine
IP_PimsAlarmLine
IP__AlarmAckCntrl
IP_AlarmLogCntrl
Keywords: oktomodify.inp
Upgrade Database
Alarm Summary
Alarm Log
Alarm Summary
Alarm Log
Japanese, 日本文
References: None |
Problem Statement: How to Cim-IO Interface ManagerConfigure the link with an OPC server using Cim-IO Interface Manager?
Cim-IO Interface Managerを使用したOPCサーバーとの接続方法 | Solution: 添付設定手順書参照
Keywords: Cim-IO Interface Manager
OPC Properties
Store & Forward
Japanese, 日本文
References: None |
Problem Statement: SQL스크립트에서 GetObject 를 실행하여 Excel파일의 데이타를 불러올때 아래와 같은 오류 발생
''Get object from ''<파일경로>\<파일명>.xls'' failed: Access is denied at line <number>.'' | Solution: 본 오류는 DCOM구성의 권한때문에 자주 발생합니다.
1. 시작클릭하고 제어판선택
2. 관리 도구에서 구성 요소 서비스를 선택
3. 구성 요소 서비스 확장
4. 컴퓨터 확장
5. 내 컴퓨터 확장
6. DCOM구성 확장
7. Microsoft Excel Application 을 오른쪽으로 클릭하고 속성 선택
8. 보안태그 선택
Windows XP 에서는 사용자 지정을 선택하고 편집 클릭
아래의 절차대로 시작 및 활성화 권한 를 편집
1. 만약 사용자 그룹 혹은 사용자가 포함되지 않았으면 추가 를 클릭하여 사용자 그룹 혹은 사용자를 추가
2. 추가한 사용자 그룹 혹은 사용자에서 모든 권한 부여. 예:로컬 시작, 원격 시작,로컬 활성화, 원격 활성화
3. 확인을 클릭하여 변경된 내용 저장.
아래의 절차대로 액세스 권한 를 편집
1. 만약 사용자 그룹 혹은 사용자가 포함되지 않았으면 추가 를 클릭하여 사용자 그룹 혹은 사용자를 추가
2. 추가한 사용자 그룹 혹은 사용자에서 모든 권한 부여. 예:로컬 엑세스, 원격 엑서스
3. 확인을 클릭하여 변경된 내용 저장.
Windows 2003 Service Pack 1 환경에서 디폴트 COM 권한이 변경되였기에 DCOM 이 정상적으로 작동되지 않는 문제가 있음. 아래의 사이트를 참조하여 문제를 해결할 수 있습니다.
''Microsoft Windows Server 2003 서비스 팩 1을 설치한 후 DCOM을 사용하는 프로그램이 제대로 작동하지 않는다''.
http://support.microsoft.com/kb/892500/ko
Windows 2003 에서는 사용자 지정을 선택하고 편집 클릭
아래의 절차대로 시작 및 활성화 권한 를 편집
1. 만약 분산 COM 사용자 그룹(Distributed COM Users)포함되지 않았으면 추가 를 클릭하여 분산 COM 사용자 그룹을 추가
2. 추가한 분산 COM 사용자 그룹(Distributed COM Users)모든 권한 부여. 예:로컬 시작, 원격 시작,로컬 활성화, 원격 활성화
3. 확인을 클릭하여 변경된 내용 저장.
아래의 절차대로 액세스 권한 를 편집
1. 만약 분산 COM 사용자 그룹(Distributed COM Users)포함되지 않았으면 추가 를 클릭하여 분산 COM 사용자 그룹을 추가
2. 추가한 분산 COM 사용자 그룹(Distributed COM Users)모든 권한 부여. 예:로컬 엑세스, 원격 엑서스
3. 확인을 클릭하여 변경된 내용 저장.
관리자는 반드시 도메인 계정을 아래와 같은 절차로 분산 COM 사용자 그룹에 추가하셔야 합니다.
1. 시작 클릭하고 관리 도구 에 들어가서 Active Directory 유저 및 컴퓨터 선택
2. 도메인 확장
3. Built-in 확장
4. 오른쪽으로 분산 COM 사용자 그룹(Distributed COM Users)을 선택하고 속성선택
5. 구성원 태그에서 추가를 클릭하고 사용자 그룹 혹은 사용자를 입력한 후 확인 클릭
6. 확인을 클릭하여 변경된 내용 저장.
Keywords: Excel
Word
SQL
DCOM
KR-
References: None |
Problem Statement: Aspen Process Explorer Ver.9 installation procedure in Japanese. | Solution: Aspen Process Explorer Ver.9 Installation procedure in Japanese with screen captures on Windows 10 and Office 2013.
Keywords: Aspen Process Explorer
Windows 10
Office 2013
Japanese
日本文
References: None |
Problem Statement: Legacy Process Data Add-in is not configured automatically and some client does not know its existence.
Legacy Process Data Add-in is useful to use the old work sheet customer created using old version of
Aspen Process Explorer. | Solution: Legacy Process Data Add-in configuration procedure in Japanese with screen captures is attached.
Keywords: legacy
process data add-in
Japanese
日本文
References: None |
Problem Statement: Which dialog controls in MIMI can only be used in workspaces? | Solution: MIMI includes numerous controls available for building custom dialogs and workspaces for MIMI applications. Several of the newer dialog controls can only be used in MIMI workspace dialogs. These controls include the following:
Tab Controls: Display a series of notebook-style tabs on the dialog; The number of tabs, text that appears on the tabs, and orientation of the tabs can be configured.
Property Sheet Controls: Consist of a series of dialogs that appear on notebook-style tabbed sheets.
Tree Controls: Display hierarchical data in a tree-like structure on the dialog.
These MIMI dialog controls are not available from the MIMI Dialog Builder. They must be added or created in the dialog by editing the dialog sets directly and are valid only in Version 2 dialog types.
The workspace-specific dialog controls are available only for Windows, and only on the MIMI Application Client.
Keywords: MIMI
workspace
dialod controls
References: None |
Problem Statement: You are attempting to export from Plant Scheduler - installed on Windows Server 2008 X64 - to an ASCC database server (housed on Windows Server 2003 x86). When this is attempted you receive an error- The specified DSN contains an architecture mismatch between the Driver and Application message is displayed.
Started At: Fri Jan 15 11:39:33 2010
&0 IN THE SQL SET EXPANDED TO ASCCOWNER
&1 IN THE SQL SET EXPANDED TO ASCCOWNER
&2 IN THE SQL SET EXPANDED TO Aspen100
CONNECT/encrypt syntax error (code=-1007).
AUTOCOMMIT is ON before CONNECT statement.
CONNECT Fail:
SQLSTATE = IM014
NATIVE ERROR = 0
MSG = [Microsoft][ODBC Driver Manager] The specified DSN contains an architecture mismatch between the Driver and Application | Solution: You should use C:\Windows\SysWOW64\odbcad32.exe [ other than default C:\Windows\System32\odbcad32.exe ] to configure the DSN, thus our SCM ( in 32bit ) can call the odbc driver correctly.
Keywords: ODBC
SQL SERVER
64 bit
References: None |
Problem Statement: InfoPlus.21 Tag Configuration Tool 시간하고 SQLplus 혹은 InfoPlus.21 administrator 시간과 틀리나요? | Solution: InfoPlus.21 Tag Configuration Tool Add-In 에 나타나는 시간은 UTC 포멧입니다.
Keywords: 시간
KR-
References: None |
Problem Statement: 以下の警告メッセージがAspenTech Process Data Add-insがロードされているスプレッドシートを開こうとしたときに発せられます。
このアプリケーションは、安全でないかもしれないActiveXコントロールを初期化しようとしている。あなたは、このファイルのソースを信頼する場合は、[OK]を選択し、コントロールが現在のワークスペースの設定を使用して初期化されます」。 | Solution: コントロール”MSGRID.OCX”が起こす問題です。このコントロールは標準の視覚化コントロールです。Windows Server 2003 R2ではデフォルトでインストールされません。”Aspen Process Explorer”と同時にインストールされます。Excelのバージョンによっては、”MSGRID.OCX”が安全に初期化できるとマークされていないとか、安全にスクリプティングできるとマークされていないためにロードできない場合があります。回避策はレジストリを変更することです。具体的には、以下の内容を含む.regファイルを作成し実行します。
REGEDIT4
[HKEY_CLASSES_ROOT\CLSID\{A8C3B720-0B5A-101B-B22E-00AA0037B2FC}\Implemented Categories]
[HKEY_CLASSES_ROOT\CLSID\{A8C3B720-0B5A-101B-B22E-00AA0037B2FC}\Implemented Categories\{7DD95801-9882-11CF-9FA9-00AA006C42C4}] @=Safe For Scripting
[HKEY_CLASSES_ROOT\CLSID\{A8C3B720-0B5A-101B-B22E-00AA0037B2FC}\Implemented Categories\{7DD95802-9882-11CF-9FA9-00AA006C42C4}] @=Safe For Initializing
Keywords: Process Data Add-in
ActiveX, Japanese, 日本文
References: None |
Problem Statement: 在Aspen Process Explorer中添加 IP_CalcDef record 的趋势图时，level 列显示为 Unknown Level (-1) status列显示为 Unknown Status (-32768). | Solution: 此问题是因为计算反馈的连续数值无status 和level。这是Aspen Calc会显示为Unknown Status 和Unknown Level.
上面的 TestCalc 计算的脚本如下：
IF (ATCAI < 8) THEN 0 ELSE 1
不需要创建新的tag,如果把计算脚本修改为如下就能看到status和level
IF (ATCAI < 8) THEN ATCAI * 0 ELSE ATCAI * 0 + 1
Keywords: Shared Calculation
On Demand calculation
CN-
References: None |
Problem Statement: 빠르게 Aspen InfoPlus.21를 새로운 하드웨어로 마이그레이션 하는 방법 | Solution: ** 아래의 내용은 고객의 내부 문서로서 Aspen InfoPlus.21(version 2.5 부터 2006.0 까지)하드웨어와 소프트웨어를 마이그레이션하는 방법을 소개합니다.**
V7.1버전부터 설치 데이터 및 설정이 변경되였고 본 문서에서 소개된 일부분의 내용이 이미 추가 되였습니다.
1. 새로운 컴퓨터를 도메인에 추가등 설정작업 진행
2. 새로운 컴퓨터의 네트웍을 끊고 Aspen Manufacturing Suite 설치
3. OS 충돌이 발생하지 않기 위하여 새로운 컴퓨터의 네트웍을 끊고 낡은 컴퓨터와 같은 컴퓨터 이름 지정.
- 이와 같이 작업을 진행하면 CIMIO store and forward를 설정할때 도움이 됩니다.
4. 필요한 Infoplus.21 내용을 낡은 컴퓨터(M_OLD)에서 부터 새로운 컴퓨터 M_NEW 로 카피.
- 설치 가이드 참조Aspen Infoplus.21 Installation Guide 2006.0, Appendix D - Migrating Infoplus.21 from one Computer to Another.
- 새로운 컴퓨터에서 InfoPlus.21가 정상적으로 작동할 수 있는지 확인.
5. 만약 새로운 컴퓨터에서 최신snapshot 와 history files 이 설정되였으면 낡은 컴퓨터(M_OLD)의 InfoPlus.21 다운시킴.
- 만약 S&F 가 설정되였으면 새로운 데이터는 CIMIO서버에 저장됨. 새로운 서버가 이후에 같은 컴퓨터 이름 하고 같은 IP주소를 사용하기에 store files삭제할 필요가 없습니다.
6.낡은 컴퓨터(M_OLD)와 새로운 컴퓨터(M_NEW)를 크로스케이블로 연결
- 이런 방식은 파일을 빠른 속도로 컴퓨터간에서 전송이 가능합니다.
- 낡은 컴퓨터(M_OLD) 와 새로운 컴퓨터(M_NEW)는 이름이 같아도 문제가 발생하지 않습니다.
7. snapshot 와 repositories 전송
- 경험에 의하면 ~10GB 데이터를 10분내에 크로스케이블로 전송 가능.
8. 새로운 컴퓨터(M_NEW)를 네트웍에 연결하고 낡은 컴퓨터의IP주소를 부여함.
9. CIMIO 연결 테스트
10. Infoplus.21시작
Contributed by:
Hariom Raval, Process Automation
RELIANCE INDUSTRIES-JAMNAGAR
Keywords: KR-
References: None |
Problem Statement: Is Aspen SCM V7.2 supported on Windows7 SP1 and Windows Server 2008 R2 SP1 operating system? | Solution: Aspen SCM V7.2 not officially certified on Windows7 SP1 and Windows Server 2008 R2 SP1.
AspenTech didn't do complete regression tests, So AspenTech cannot ensure the quality for the product that didn't undergo thorough tests.
Service packs for either one of the Operating system were not required for V7.2 platform specs.
Keywords: SCM
Support
Windows Server 2008 R2 SP1
Windows7 SP1
Service Pack
References: None |
Problem Statement: Attempting to install Aspen SCM, there is a failure with Noblenet Portmapper installation. | Solution: When the Noble Net portmapper does not install and start correctly it usually means that there is another application that is using the same port number that the Noble Net Portmapper wants to use.
To solve this instance there is a NT service that caused the problem.
Start the services applet from the Control Panel Administrative Services screen. Then look for the following service named Networker Remote Exec Service. Right click on this service and choose stop. Then install Aspen SCM.
The portmapper service that SCM is trying to install is named NobleNet Portmapper for TCP. There has been cases of other software installing a service named NobleNet Portmapper This service also can cause a conflict and should be stopped in the same way as the above example.
Keywords: None
References: None |
Problem Statement: This knowledge base article describes why the following error may be observed when installing Aspen SCM software.
Error 1920. Service NobleNet Portmapper for TCP (NobleNet Portmapper for TCP) failed to start. Verify that you have sufficient privileges to start system service. | Solution: Aspen SCM uses NobelNet PortMapper but this service may be blocked by anti-virus software. Open your anti-virus software, change the setting to allow the service to run then continue with the SCM installation.
Keywords: NobleNet
Port Mapper
References: None |
Problem Statement: The purpose of this tech tip is to explain with examples how to install the MIMI CAPS web help. | Solution: After your MIMI/CAPS installation, you will find the CAPS files in separate directories for each configured application under \Program Files\AspenTech\Aspen CAPs.
Note that web help requires a browser (IE 5.0 or Netscape Navigator 4.7).
To install:
Unzip file named <appl. code>_Help_<language code>_Vv-w.zip
Be sure to select check box Use Folder Names
Extract into default directory (to be created if not existing)
\Program Files\AspenTech\Aspen CAPs\CAPHelp\<appl. code>_Help\<language code>
You can choose to extract the files to a directory other than the default, but in that case you must enter that directory into the FMTFDEF table, HELPFILE and HELPPATH entries
<appl. code> - the configured application's code:
DM (Demand Manager)
DS (Distribution Scheduler)
IP (Inventory Planner)
PPS (Plant Planner and Scheduler)
PS (Plant Scheduler)
PP (Power Planner)
SP (Supply Planner)
<language code> - the language code:
Chinese
French
German
Italian
Japanese
Spanish
UKEnglish
USEnglish
v-w - the major and minor version of the configured application separated by a hyphen
For example, to set up the online help system for the Plant Scheduler CAP in US English:
Take file PS_Help_USEnglish_V3-0.zip in directory C:\Program Files\AspenTech\Aspen CAPs\Plant Scheduler V3.0
Unzip into your CAPs help directory for the Plant Scheduler,
e.g. the default C:\Program Files\AspenTech\Aspen CAPs\CAPHelp\PS_Help\USEnglish\
The procedure is a bit different for the Aspen Strategic Analyzer (ASA) configured application:
SA_Help_V3-5.zip contains the online help files for the ASA
Copy the zip file in \Mimi\Cases\ASA and extract the help files to \Mimi\Cases\ASA\Webhelp (the default)
If you want to select another default MIMI case directory, change the path in APPDATA(BATFILES,1) within ASA. The web help files should be extracted in the same subdirectory as file ASA.bat
Keywords: WEB HELP
CAPS
MIMI CONFIGURED APPLICATIONS
INSTALLATION
References: None |
Problem Statement: In Aspen SCM, how do I refresh the Planning Board? | Solution: There are two ways to refresh the Planning Board.
1. The M SIM command will rebuild the entire planning board. Before usingf M SIM, we suggest you consult the MIMI Help Files.
2. Under the Planning Board menu, click on View | Reset | Planning Board. This will also refresh the entire Planning Board.
Keywords: None
References: None |
Problem Statement: Is there any benefit to running Aspen SCM on a computer with dual processors? | Solution: Aspen SCM is a single-threaded application, which means that Aspen SCM native code will only function on a single processor at a time - no benefit to direct MIMI processes, although the server can manage other processes (Windows, Oracle, etc.) on the other server and dedicate a little more CPU time to Aspen SCM - probably negligible.
Most Aspen SCM processes are very fast. The exception is the optimization of very large problems. The basic simplex algorithm cannot be written to make use of multiple processors. However, the interior point and mixed integer applications can be sped up by running parts of the problem in parallel. For interior point, since the new DUAL algorithms, available in both CPLEX and XPRESS have become available, they are so much faster than interior point that there is no benefit.
In summary, the only value of multi-processor is when you want to run multiple large Aspen SCM applications on a single server. However, in many cases, the cost of a 2-processor Intel computer is more than twice the cost of a single processor. Thus, multi-processor computers may not be cost effective.
Keywords:
References: None |
Problem Statement: Where can I find the pre-loaded Configured Application (CAP) cases for V7.3.1? | Solution: The default locations for the CAP cases are:
? Windows Vista and Windows 2008 Server
C:\Users\Public\Documents\AspenTech\Aspen CAPS\
? Windows XP and Windows 2003 Server
C:\Documents and Settings\All Users\Documents\AspenTech\Aspen CAPS\
Keywords: Case files
Models
Standard CAP cases
References: None |
Problem Statement: The &TIME variable is not returning the correct system time. | Solution: In this situation, there is usually an incorrect setting somewhere on the PC. The first areas to check are the following:
1. Check to make sure the Time Zone on your PC is correct. Adjust if necessary.
2. Correct the Clock Time as needed.
3. Reboot your machine and check if the Time Zone and the Clock Time are still correct. (If it does not show up correctly, you may need to adjust the BIOS settings on your PC.)
If none of these suggestions correct the problem, try running our Time Test program. Download the program from thisSolution and copy it to your PC. Unzip the program and execute it from a MS-DOS prompt. If the program shows that SCM Time is the same as the System Time, then the SCM Time is correct. In this case, check the autoexec.bat file on your PC to make sure the Time Zone setting is not hard coded within.
Keywords: None
References: None |
Problem Statement: Remote sets and tables being created when saving an independent case. | Solution: The general cause of this problem is that the LOADCASE attributes somehow got corrupt and are not being recognized. A good way to test if this is definitely the problem is to load the case and bring up one of the remote sets. Look at the attributes and see if the LOADCASE attribute is set to Current Case. If the set were truly dependent, then the LOADCASE should be another CASE that is defined in $CASES; however, it will likely be set to Current Case indicating that it is independent. If this is the case, then the test confirms that an independent set is being recognized as dependent.
To fix this problem, reselect Current Case in the LOADCASE attribute pull-down menu and apply the change. Then, save the case and exit. Upon reloading the case, see if the number of remote sets decreases by 1. If so, then the cause of the problem is confirmed.
If there are a lot of independent sets and tables being loaded incorrectly as remote, then updating them manually could be quite an arduous task. Luckily, there is an easy way to fix this programmatically. Simply write a rule which will loop through SCAT and TCAT and alter the LOADCASE attribute correctly.
If you need assistance with this, please contact the help desk at [email protected].
Keywords: REMOTE
SETS
TABLES
OPEN
INDEPENDENT
LOAD
SAVE
References: None |
Problem Statement: What is the difference between MIMI Application Client and MIMI Limited Edition? | Solution: MIMI Limited Edition is the Application Client with some menu items and commands removed. This makes sure that the end user can only make changes through the menus and commands that the case writer lets them. Essentially the end user can not corrupt or change a case by mistake.
Keywords: mimile
mimile.exe
References: None |
Problem Statement: This applies to cases that use old library cases or user libraries when they are not differentiated in version numbers. You may have different copies of library cases with the same names in different folders. For example, you have older copies of DataView.cas in the default library folder, e.g., C:\Program Files\AspenTech\Aspen CAPs\Shared Libraries, and an updated version of Dataview.cas in local case directory.
When first loading a case, the $TCASES table will point to the standard CAPs library directory, C:\Program Files\AspenTech\Aspen CAPs\Shared Libraries. Assuming the new library is in your local case directory, you would change $TCASES to make sure the updated library cases are used, then save the case.
In doing this, it had registered the presence of some sets and tables that were in the library cases in the standard CAPs directory, and so they were now saved into the catalog. Upon reloading and pointing to the local libraries, it now won't be able to find the sets and tables that it had brought in from the old libraries. | Solution: Replace the old library with the new one in the standard library CAPs directory. If you forget to do so before loading the case, do not save the case and exit Aspen SCM. Then, follow the suggested steps to replace the old libraries in the CAPs standard directory first.
NOTE: If you had saved the case by any chance, you need to retrieve the case that does not register the presence of some sets and tables from the library cases in the standard CAPs directory, and then do the suggested above.
Keywords: $TCASES
References: None |
Problem Statement: The company is doing a Disaster Recovery exercise and needs to move their AspenTech license(s) to the Disaster Recovery server without disrupting production. | Solution: Whether you have a dongle or a dongle free license, you will need to request a temporary key for your Disaster Recovery server.
Aspen Technology Customer Care will help you with your request.
You can start the process via the AspenTech Support Website
On the left-hand side of the screen click Upgrades & Licenses and select Place a License Key Request.
Complete the Shipping and End-User information on the top part of the form.
Enter a reason for the temporary license key request, the version of AspenTech software you are using and what type of license you need.
Complete either the SLM or ALM sections of this form.
Enter the system name (system name for the Disaster Recovery server).
Attach the license key.
Network license key is located:
C:\Program Files\Common File\SafeNet Sentinel\SentinelRMS License Manager
Standalone license key is located:
C:\Program Files\Common File\Hyprotech\Shared
Select the type of license locking needed.
Click the Submit icon.
A new Customer Care incident will be created for you. There is a 5 to 10 day turn around for obtaining a license key. Please consider this in your Disaster Recovery exercise planning.
Keywords: Disaster Recovery
Moving a license
Temporary license
Duplicate license
References: None |
Problem Statement: When trying to run the OPT Command Aspen SCM V7.2, I get an error message Command OPT is not available. | Solution: The command OPT requires the CPLEX Optimizer license. The error message ?Command OPT is not available is flagged in V7.2 because the CPLEX Optimizer license is not present.
AspenTech no longer offers CPLEX Optimizer license and has announced the end of support dates for CPLEX Optimizer. Aspen SCM V7.2 uses FICO? Xpress Optimization which is delivered on the aspenONE DVD.
The CPLEX Optimizer has been an optional optimizer that clients could license as an alternative to XPRESS. Due to a lack of customer requests for CPLEX over the past 4 years, AspenTech will no longer offer the CPLEX license. Customers with current support contracts for Aspen CPLEX Optimizer will continue to receive support for the product through June 30, 2012.
To run the XPRESS optimizer the command XPRESS is used.
Transition Strategy
No significant transition work is required. The XPRESS optimizer provides the same functionality as CPLEX, but may require some changes to the optimizer settings to better mimic the CPLEX behavior. Please see the Aspen Plant Scheduler or the Supply Chain Planner Implementation Guide for the correct settings.
Any customer who wishes to obtain new CPLEX license or to enter into a support agreement on an existing CPLEX license may contact IBM directly.
Keywords: CPLEX
OPT
XPRESS
References: None |
Problem Statement: How do I add a new user in SCM V7.3.1? | Solution: 1. Open a case.
2. Select the Security icon in the Navigation pane (on the left-hand side of the screen).
3. Select User Management from the menu tree.
4. On the ribbon (top part of the screen) click Properties.
5. In the Add User section, enter the user name in Userid field.
6. Select a role from the Primary Role field drop down list.
7. Click Add.
Keywords: USERID
User role
User
References: None |
Problem Statement: When you go to the AspenTech License Key Request web page (ALM Web Licensing Portal) to generate a ALM license you get the following error: | Solution: The ALM licensing server is down. Please contact Aspen Tech support.
Keywords: Installation Key
Authorization code
References: None |
Problem Statement: What are the relevant Windows Services that are specific to aspenONE SCM v7.2? | Solution: The following are the relevant Windows Services for Aspen SCM:
AFW Security Client Service
Chesapeake Distributed MIMI Request Broker
NobleNet Portmapper for TCP
Keywords: None
References: None |
Problem Statement: A Microsoft patch was installed on the Aspen server and now Aspen case files will not open. | Solution: Ensure that the server was rebooted after the patch was installed.
Keywords: Runtime license
Auto detect license
References: None |
Problem Statement: When converting CAP cases, cas2dat/dat2cas will fail because all CAP cases are in version 3 format.
cas2dat/dat2cas can not convert version 3 format cases. | Solution: Use cmprcase instead of cas2dat/dat2cas.
Basically, cmprcase has all cas2dat/data2cas feature except converting binary case files to data files. More specifically, cmprcase can do the following
1. Rearrange the case file and eliminating wasted space in the case,
2. Eliminate invalid characters in the case using -f option,
3. Increase maximum number of sets and tables in a case use -S or -T option. Please note that the maximum number of sets and tables is 4000.
4. Compress to a different case using the -N option. In this case, by saving the compressed case to the specified name, the original case remains unchanged.
Keywords: None
References: None |
Problem Statement: You are installing ApsenTech SCM software and you receive Error 1327: Invalid Drive X:\ (X represents the drive letter). | Solution: There could be several reasons for this error:
1. The drive you are using no longer exists - check that the drive is a valid drive on your computer.
2. You are not mapped to the network drive referenced in the error message - Map the network drive via Windows' network drive mapping functionality using the drive letter represented in the error message. Go to Windows Explorer and choose Tools > Map Network Drive.
3. You are not connected to the network - check your network connectivity.
Keywords: Error 1327
Network Drive
Installation Error
References: None |
Problem Statement: After receiving a new network license, and after installing the Sentinel License Manager Service and the key, I find the service keeps stopping due to the following error: The SLM Service stopped - unable to bind to its socket. How can I resolve this? | Solution: Ensure Data Execution Prevention (DEP) feature is disabled against the Sentinel RMS service. Having this turned on prevents the service from running properly.
For more information about the DEP, see this article: http://support.microsoft.com/kb/875352
Keywords: None
References: None |
Problem Statement: The mouse scroll wheel works everywhere except on the Planning Board. | Solution: The likely cause of this problem is that the mouse driver is out of date. To update the driver, follow these steps:
Exit out of Aspen SCM.
Click on Start --> Control Panel.
Choose the System icon and then the Hardware tab.
Click on the Device Manager button and look for Mice and Other Pointing Devices in the list of available hardware.
Maximize that item by clicking on the + sign. There you should see the name of your mouse listed.
Right-click on the name of the mouse and choose Update Driver.
Follow the steps from Windows as indicated from that point forward.
Once the driver has been updated, reboot your PC.
Test the scroll wheel in the Planning Board again and the results should be successful this time.
Keywords: MOUSE
MICE
References: None |
Problem Statement: How often should dat2cas and cas2dat be run against my Aspen SCM case files? | Solution: Before using cas2dat and dat2cas, it's important to know what exactly they do. The purpose of cas2dat and dat2cas is to convert a binary file to character (then back) so the file can be transported to other operating systems. However, many customers do not realize the additional benefit to running cas2dat and dat2cas on a regular basis. These utilties not only remove wasted space from the case, but they also re-index the catalog of sets and tables. As a result, your case will run more efficiently.
Customer Support recommends that you perform cas2dat / dat2cas every day while the model is in development. Any time there are constant changes being made to the case, it's a good idea to include these utilities in your daily activities.
Once the case is in production, it is recommended that you perform cas2dat / dat2cas on a weekly basis.
For more information on cas2dat and dat2cas, please reference the SCM help files.
Keywords: None
References: None |
Problem Statement: After upgrading from 2006.5 to V7.1 you are no longer able to view the cascading menus: | Solution: Please turn on Options | System | System tab. TheCascading checkbox is located in the General Preferences section.
Then I can see the submenu.
I got the information from CAPs implementation guide.
Keywords: None
References: None |
Problem Statement: When I start MIMI, I get the error message MIMI failed to initialize. | Solution: The source of this problem is during the installation. During installation, the user selects as to whether the MIMI installation is a Plantelligence installation or not, and on some occasions, the user mistakenly picks the Plantelligence install. This sets two registry values which force MIMI to authenticate via an Aspen Framework Server, which the user would not have if he/she does not use Plantelligence products. To disable the Aspen Framework Server security authentication, set the following registry values.
Under the registry, in HKEY_LOCAL_MACHINE\SOFTWARE\AspenTech\AFW
Active =1
Advanced Settings=1
Set these two values to
Active =0
Advanced Settings=0
Reboot and the new registry settings will take effect, and MIMI will start properly.
Keywords: None
References: None |
Problem Statement: Is it possible to run the Supply Chain Management family applications in a VMWare environment? | Solution: AspenTech has performed selective testing on aspenONE for Supply Chain and found no problems running in a Virtual Machine (VM) environment. We are aware that various customers are successfully running some of our SCM applications in a VMWare environment; however, AspenTech cannot guarantee application compatibility with a specific customer architecture.
Keywords: VMWARE
VIRTUAL MACHINE
VIRTUAL PC
VIRTUAL SERVERS
VMWARE GSX SERVER
References: None |
Problem Statement: How do I publish the Planning Board (or interactive graphics and charts) on the web? | Solution: For the users who do not want to print the Planning Board (or interactive graphics and charts) but still need to display it, there is a way to publish it on the WEB. Although it is not possible to directly display the Planning Board, charts, or interactive graphics via the SCM Web Server, users can display a screen capture (snapshot) of the window using the command WINSHOT of SCM application and display it in the SCM Web Server Application.
Capturing the Planning Board (or interactive graphics and charts)
While in SCM application, open the Planning Board.
Use the Command Line (F3) and type in the command WINSHOT Window Name Output File. The Output File must have extension JPG, GIF, BMP or PNG. In most cases, GIF is the best. Example: : WINSHOT MAIN1 PLANBOARD.GIF (where MAIN1 is the name of the SCM Planning Board and PLANBOARD.GIF the snapshot image). The file will be save in the same directory of the CASE file.
Please note:
The command runs valid in Aspen SCM Application Client and Window NT only, from SCM 4.30 and further releases.
Client cannot be minimized.
Does not run on Application Server or Lite Client.
Displaying the Planning Board and Other Graphics in Your SCM Web Server Application:
To display a graphic on your SCM Web Server web page:
1. The file must be in a location published by web server. Example: c:\inetpub\wwwroot\mimiweb\ images\snapshot.gif
2.
Keywords: None
References: the graphic in the PRE or POST table via some HTML of the form: <IMG SRC=picture.jpg> or <IMG SRC=picture.gif>
3. The image must be in GIF or JPG format (not BMP).
4. The graphic file itself should be in one of the following directories:
o The same directory as the SCM Web Server executable (mimiweb.exe). (For security reasons, this is generally not recommended.)
o Or a directory that is directory accessible via a web browser. Examples: <IMG SRC=http://www.chesapeake.com/boat.jpg> <IMG SRC=../sailboat.jpg> In this example, if mimiweb.exe is located in /foo/cgi-bin, then sailboat.jpg should be located in /foo.
Should you need further information on how to install SCM Web, please contact SCM support. |
Problem Statement: You are receiving a STRGXI2.dll error when trying to run SCM. | Solution: The STRGXI2.dll file is associated with the Software License (SLM) tools and is located in the C:\Program Files\Common Files\Hyprotech\Shared folder.
Each version of SLM has a dedicated version of the STRGXI2.dll file. If you have install one version of SLM tools but then decide to uninstall it and install a different version, the STRGXI2.dll file associated with the uninstalled version of the SLM tools will not be deleted during the uninstall activities.
When you install the new version of the SLM tools the STRGXI2.dll file associated with this new version will not overwrite the previous version's STRGXI2.dll file on your computer. This mismatch of STRGXI2.dll file and version of SLM will cause an error when trying to open SCM.
When uninstalling SLM tool you must manually delete the STRGXI2.dll file from C:\Program Files\Common Files\Hyprotech\Shared.
Keywords: STRGXI2
References: None |
Problem Statement: When performing a numerical comparison in rules, such as GE after using ROUND function, the results are unexpected. Without using the ROUND function, the result is correct. Why? | Solution: In SCM, the value of a ?variable is stored in a buffer in the character string format. If the value is a number, the content in the buffer will be a numeric character string.
For example, if in a rule you assign ?RESMAX = AMERICA(0,X) where table cell AMERICA(0,X) contains integer 2376, the content of the buffer for variable ?RESMAX is numeric character string 2376.
Now, if you assign ?RESMAX = ROUND(?RESMAX, -4) the content of the buffer becomes numeric character string 2376.0000.
When SCM handles the comparison operation, it will first try to convert the operands in the character string format into numeric values. If the operands can be converted successfully, SCM will do a numeric comparison. Otherwise, it will do a string comparison.
There are some basic rules on numeric values when SCM converts the character string into a numeric value, one of which is that a valid numeric value can only have at most 7 digits in total. In this case, the value of ?RESMAX is 2376.0000, which cannot be converted. Therefore, the comparison is treated as a string comparison. You will get unexpected results, say if ?CAPFIX = 97.6 and ?CAPFIX GE ?RESMAX is evaluated as TRUE.
A possibleSolution to this problem is to make sure SCM knows that the ?variable containing the result of a ROUND function is a number.
For instance if you do:
?RESMAX = ?RESMAX + 0
before the test, ?RESMAX will be treated as a number in the test.
Also, as suggested in Knowledge BaseSolution 112671 (which gives details on the new switches for determining the way comparisons are performed inside rules), you can appropriately set setting SCMPM so that the comparison is done as numeric.
Keywords: ROUND
ROUNDING
GE, LE, GT, LT, EQ
COMPARISON
References: None |
Problem Statement: I receive an error message at the bottom of MIMI screen, P0265: Exceeded maximum PRO entries. please contact Chesapeake, when I try to start MIMI | Solution: Make sure in your license key, under Options, that PROlimit and MARlimit are both set to 00. Options is located near the top of the key file.
Example Appearance:
Options:
PROlimit:
00
MARlimit:
00
Keywords: None
References: None |
Problem Statement: Is there a way to change the font in Aspen SCM? | Solution: As per the Aspen SCM Help Guide, you do not have an option to change the FONT type in Aspen SCM. You can only change the FONT Formatting:
Applying Font Formatting
Important: The FORMAT command is available on the Windows Application Client only.
This FORMAT command syntax applies bold or italic formatting to:
A table cell
A table row
A table column
Table row or column headers
An entire table.
To remove formatting, see the Aspen Help section: Removing Table Formatting.
Syntax
FORMAT table({*|@|COLHDR|rowcode},{*|@|ROWHDR|columncode}) = {FONT BOLD|FONT ITALIC}
Examples
This example applies bold formatting to all cells in the LS column of the TDAT table.
FORMAT TDAT(*,LS) = FONT BOLD
This example applies italic formatting to the cell in the CAPA table to which the row and column indexes are currently set.
FORMAT CAPA(@,@) = FONT ITALIC
This example applies italic formatting to all the column headers in the CAPA table.
FORMAT CAPA(COLHDR,*) = FONT ITALIC
This example applies bold formatting to all the row headers in the CAPA table.
FORMAT CAPA(*,ROWHDR) = FONT BOLD
Description of Arguments
table: (Required) Name of the table to which you want to apply formatting.
({*|@|COLHDR|rowcode},{*|@|ROWHDR|columncode}): (Required) Indicates the cells, row, or column in table to which you want to apply formatting.
* indicates all rows or columns
@ indicates the Code entry in the row or column set to which the internal index is currently set
COLHDR indicates the column headings
ROWHDR indicates the row headings
rowcode indicates a particular Code from the row set
columncode indicates a particular Code from the column set.
{BOLD| ITALIC}: (Required) Specifies the formatting you want to apply to the specified cells:
BOLD: Bold formatting
ITALIC: Italic formatting
Keywords: user interface, formatting, font
References: None |
Problem Statement: How to modify the color of a product in the SCM Planning Board? | Solution: In order to modify the color of a product in the Planning Board, 2 tables and 1 set have to be considered: tables PCOLOR and MAKI and set SCOLOR.
1. The set SCOLOR lists the color codes and related color names (i.e. 0 = BLACK, 1 = MEDIUMBLUE, etc).
2. The table PCOLOR determines the color to be used for a given product in the Planning Board. Modifying the color code of a given product in the table PCOLOR will result in changing the color of the product wherever it is used in the Planning Board.
3. Product color may also be modified individually by changing the default value (-1) of an activity to a specific color code.
This is performed in the last column (COL) of the table MAKI.
The first column of the table determines the unique internal indixes assigned to the activities (notice that the first row, row zero, does not represent an activity. Valid activity has an IND >= to 1).
Keywords: None
References: None |
Problem Statement: When you drop any MimiX controls in an Excel spreadsheet you get an Error Cannot Insert Object. How can I resolve this? | Solution: Follow these steps:
1. First, close your Excel spreadsheet.
2. Open explorer and do a search for a file called MimiX.EXD.
3. Delete the file and go back to Excel and retry.
Keywords: None
References: None |
Problem Statement: When you open your case in SCM, turn trace on, and run the rule >RINVBL60, the case unexpectedly performs an exit.
When we run it the code unexpectedly performs an exit. In the trace, there is a point where we pull and check to see if ?TIER is eq 0. This should never happen, TEMP has values > 0. | Solution: You must make the following changes (highlighted with colors) to rule RINVBL65 to see if this solves the problem?
RINVBL65 --- NOW PROCESS SKUS WITH NEGATIVE INVENTORY
IF ?SKU = CODEOF TMPSET1(@)
AND ?ROW IN TEMPR
/* --- DO NOT DO THIS FOR TIER 1 */
AND ?ROW IN STLOCR
AND ?COL = TIER /* add this line */
AND ?TIER = TEMP(@,?COL) /* replace TIER with ?COL */
AND ?TIER EQ 0 AND EXIT OR ?TIER NE 1
..........
THEN RINVBL65_PROCESS_SKUS_WITH_NAGATIVE_INVENTORY
The reason you need to write the rule in this way is that TEMP is a dynamic table, which is dynamically changed by the APPEND command in the parent rule - RINVBL60. When SCM resolves set and table references as part of the linking process, the format or set Codes of the dynamic set or table may not match the set or table referenced in the rule, which could result in an error or some unexpected behavior. So, it is important to avoid referencing dynamic sets and tables in rules with the static row/column code, as noted in SCM Online Help ? Aspen SCM Development Tools ? Expert System Rules.
To avoid the potential problem in resolving dynamic table references in a rule, it is recommended to assign the row and column codes of the dynamic table to rule variables, then reference the table entry via the variables, as suggested above.
Keywords: None
References: None |
Problem Statement: You have recently upgraded Plant Scheduler. You change the library locations in $TCASES, closed the case and reopened, and then started reinstalling the libararies. Attempting to update the Plant Scheduler Library returns the following messages:
04/05/10 16:04:50 PSAMSG Possible problems:
04/05/10 16:04:50 PSAMSG
04/05/10 16:04:50 PSAMSG 1) SCAT or TCAT may be full.
04/05/10 16:04:50 PSAMSG 2) Check the library object [PUBLTAB(*)]. It may not exist in the
04/05/10 16:04:50 PSAMSG source model.
04/05/10 16:04:50 PSAMSG 3) Check the library object [PUBLTAB(*)]. It may already exist in your
04/05/10 16:04:50 PSAMSG model and conflict with the library. E.g. library defines
04/05/10 16:04:50 PSAMSG it as a set, yet your model defines it as a table.
04/05/10 16:04:50 PSAMSG 4) Check the library object [PUBLTAB(*)]. The set/table may be from a
04/05/10 16:04:50 PSAMSG dependent feature and may not exist in your model,
04/05/10 16:04:50 PSAMSG indicating a dependency issue. | Solution: The object in question, PUBLTAB, and it's feature Application Messaging are obsolete. You should avoid installing this feature into this new model.
Keywords: None
References: None |
Problem Statement: My workstation caches extensively to the hard drive when I use Aspen SCM. Error message is running out of virtual memory. What can I do to remedy this? | Solution: This problem occurs when the workstation has used up all physical RAM installed on the workstation, and the workstation has very little hard drive space on the hard drive. To fix this problem you can either:
1. Increase the amount of physical RAM on the workstation, or
2. Clear some space on the physical hard drive.
Keywords: None
References: None |
Problem Statement: What is MIMI3GB (Big MIMI)? | Solution: MIMI3GB is what we call the Aspen SCM executables that allow your model to use up to 3GB of virtual memory space.
No files exist for Aspen SCM versions earlier than 7.0.3.21.
There are different MIMI3GB exe files for the different Aspen SCM versions up to version 2004.0, which have to be asked to Aspen SCM Support.
You can find attached to thisSolution the executables for the main releases. Each zip file contains:
mimi_3gb.exe
(Application client)
mimias_3gb.exe
(Application server, to run cases in batch mode)
mimile_3gb.exe
(Limited Edition)
Starting from version 2004.1 and for all future versions you will not need any separate EXE's because the standard EXE's we deliver are already configured for the higher RAM limits. In that case you only need to have the proper operating system and have it configured properly for 3GB, as explained below.
Here is the information you need for the installation and use of MIMI3GB.
What operating system is required
We have tested Aspen MIMI3GB on a Windows 2000 or 2003 Server and on Windows XP Professional. Enterprise Edition (NTS/E), and Win2K Datacenter Server (Datacenter) should also be able to run applications over 2GB as they all have the /3GB boot switch (see below). You must have at least 4GB of physical memory.
What your system administrator needs to do
Add the /3GB switch in the boot.ini file. This increases the virtual address space of MIMI3GB. This switch signals to the operating system that it should partition the 32 bits space as 1 GB / 3 GB instead of 2 GB / 2 GB if requested.
Example of boot.ini file from a Win2000 Advanced Server machine:
[boot loader]
timeout=30
default=multi(0)disk(0)rdisk(0)partition(1)\WINNT
[operating systems]
multi(0)disk(0)rdisk(0)partition(1)\WINNT=Microsoft Windows 2000 Advanced Server 3GB /3GB /fastdetect
How to install MIMI3GB (only for versions 2004.0 and below)
The Aspen SCM executables that are enabled to use the large address space are delivered as separate files. First install Aspen SCM using the normal installation, then replace the existing executables with the 3GB ones, lets say mimi_3gb.exe and mimias_3gb.exe Rename the existing mimi.exe to another name and then rename the mimi_3gb.exe to mimi.exe. By doing this all Aspen SCM registry settings, shortcuts, etc. will stay in effect and no other changes will be needed, except for the boot.ini setting. The same procedure of renaming files for mimias.exe if you need to use also the Application Server for batch case files.
CAUTION:
Of course this means that if you have a version installed of MIMI3GB (e.g. for Aspen SCM 8.0) and you later install a service pack, then you obviously have to re-install the MIMI3GB executables, which must be the ones specific for the new version (e.g. 8.0.1). In fact the installation of the service pack overwrites the Aspen SCM executables. For assistance contact you local support center or select Submit Issues from the left-hand navigation pane at the online Technical Support Center.
Memory support and windows operating systems
Operating systems based on Microsoft Windows NT technologies have always provided applications with a flat 32-bit virtual address space that describes 4 gigabytes (GB) of virtual memory. The address space is usually split so that 2 GB of address space is directly accessible to the application and the other 2 GB is only accessible to the Windows executive software. However, on the 32-bit versions of the Windows 2000 Advanced Server (Win2K AS), the x86 version of NT Server, Enterprise Edition (NTS/E) and Win2K Datacenter Server (Datacenter), an administrator can enable the /3GB boot switch, which moves the division so that applications have 3GB of private memory and the system has 1GB.
You can have more information on memory support in the following Microsoft articles:
Memory Support and Windows Operating Systems
Information on Application Use of 4GT RAM Tuning
Keywords: MIMI 3GB
BIG MIMI
BOOT.INI
WINDOWS 2000 SERVER
WINDOWS 2000 ADVANCED SERVER
References: None |
Problem Statement: Is Aspen SCM V7.3 supported on Windows 7 Professional 64 bit operating system? | Solution: Aspen SCM V7.3 and its prior versions are not supported on Windows 7 Professional 64 bit operating system.
Keywords: SCM
64-bit
64bit
V7.3
Windows 7
Windows 7 Professional
References: None |
Problem Statement: This | Solution: explains what versions of CPLEX and XPRESS are embedded with a generic Aspen SCM release and how to find the version you are currently using.
Solution
When a new version of Aspen SCM is released, the latest major version of the optimizers is generally included.
The upgrades are done if they are requested from the clients or from Aspen and approved from the Aspen Release Board.
To see what version of CPLEX or XPRESS you are running, open a LP (Linear Programming) case and run the following commands from the Aspen SCM command line. The version information will appear in the message bar at the bottom left of the window. The screenshots below show the versions for Aspen SCM V7.1.
For XPRESS
Command: XPRESS VERSION
For CPLEX
Command: OPT VERSION
Note: The CPLEX optimizer is available through Aspen SCM V7.1. As of SCM V7.2, AspenTech no longer offers CPLEX Optimizer license and has announced the end of support dates for CPLEX Optimizer. Aspen SCM V7.2 and beyond uses FICO? Xpress Optimization which is delivered on the aspenONE DVD.
Keywords: SOLVERS
OPTIMIZERS
References: None |
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