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Problem Statement: What are the recommended parameters to monitor with regard to APC applications' health on each server? | Solution: The table listed below is also available in the attached document, and it outlines the important processes, log files, parameters, etc. that can be monitored to check APC application health.
DMC Machine
Aspen Watch Machine
PCWS Machine
Processes
A? control.exe (one per DMC controller)
A? cimio_dmcp_dlgp.exe
A? dmcp_datapump.exe
A? dmcp_dataworker.exe (can be more than one)
A? iq_datapump.exe
A? iq_dataworker.exe (can be more than one)
A? iqp_main.exe (one or two per IQ application)
A? apollo_datapump.exe
A? apollo_dataworker.exe (can be more than one)
A? apollo_ctrlr.exe (one per apollo application)
A? apollo_cpp.exe (one per apollo application)
A? RTEService.exe (if APC Builder Online is running)
A? RTEApplication.exe (one per APC controller)
A? AWCollect.exe
A? Watchdatapump.exe
A? MSCWatch.exe
A? PIDCollect.exe
A? WebDataProviderSvc.exe
Ports
Refer to solution Id- 123707 for details
Services
A? ACO Utility Server
A? Aspen APC DMCplus Data Service (dmcp_datapump.exe)
A? DMCplus Context Service (cimio_dmcp_dlgp.exe)
A? Aspen APC Inferential Qualities Data Service (iq_datapump.exe)
A? Aspen APC Nonlinear Controller Data Service (apollo_datapump.exe)
A? AspenTech Production Control RTE Service (RTEService.exe)
A? Aspen APC Message Log Service (AspenTech.ACP.Services.MessageLogSvc.exe)
A? Aspen APC Performance Monitor Data Service
A? Aspen InfoPlus21 Task Service (tsk_server.exe)
A? Aspen APC Web Provider Data Service (WebDataProviderSvc.exe)
Logs
A? Valid.err
A? .eng
A? .prt
A? Cimio_msg.log
A? MPF Messages
A? Dmcp.err
A? Dmcp.out
A? DMCplusRepositoryErrors.log (DMCplus)
A? AspenIQRepositoryErrors.log (IQ)
A? ApolloRepositoryErrors.log (Nonlinear)
A? NodeRepositoryErrors.log (APC Controller)
A? Awlog.txt
A? Upgrade.out
A? RepositoryErrors.log
Event Logs
A? Application (Windows event log)
A? System (Windows event log)
A? Aspen DMCplus (DMCplus mssages)
A? Aspen IQ (IQ messages)
A? Aspen Nonlinear (Nonliner messages)
A? AspenRTE (APC Controller messages)
A? Application (Windows event log)
A? System (Windows event log)
A? Application (Windows log)
In addition to these, it would also be a good idea to monitor the Elapsed Times (DELTAT) and CPU Times (DELTACPU) for each controller application. You can configure miscellaneous tags in AspenWatch to collect these parameters from the DMCplus Context. It would also be a good idea to add WatchDog Counters in the controllers to monitor the connection between the DMC Machine and the DCS.
System Parameters- Disk space, Memory usage, CPU usage.
Keywords: Monitor APC Application Health
Troubleshooting APC Applications
References: None |
Problem Statement: How to configure PIMS Adapter? | Solution: This KB article provides you the detailed procedure for PIMS Adapter configuration.
PIMS Adapter configuration
Make sure that all the Adapter needed components are installed in your machine (EIF, mMDM)
Configuration for 32 bit OS
Use ODM=N
Copy all the files in register files folder to your testing machine (you can place these files in any locations)
Double click the register files ‘TurnOnLoggingPimsAdapterV2009.06.16.reg’
Click OK/Yes when the system asking you whether you want to add the info to the registry.
Open Integration Adapter designer from start menu -> Aspen Configuration -> Integration Adapter Designer.
Click Open file icon (or from menu File-> Open), and then browse to open the configure file, AtlwaAdapterConfig.xml, under the following directory:
C:\Program files\AspenTech\AEP\EnterpriseConnect\IntegrationPacks\pims\Adapter\etc\xml\
Expand node Global Variables, and then make sure the value for UseODM is ‘NO’
Use ODM=Y
Copy all the files in register files folder to your testing machine (you can place these files in any locations)
Double click the register files ‘TurnOnLoggingPimsAdapterV2009.06.16.reg’
Click OK/Yes when the system asking you whether you want to add the info to the registry.
Open Integration Adapter designer from start menu -> Aspen Configuration -> Integration Adapter Designer.
Click Open file icon (or from menu File-> Open), and then browse to open the configure file, AtlwaAdapterConfig.xml, under the following directory:
C:\Program files\AspenTech\AEP\EnterpriseConnect\IntegrationPacks\pims\Adapter\etc\xml\
Expand node Global Variables, and then make sure the value for UseODM is ‘YES’. If the value is not YES, change the value in RAW value field to ‘YES’
Change the value for ‘ODMWorkSpaceName’ to ‘Default_Database’. (the default value is ‘Default_File’)
Save the changes and then exist the Aspen Integration Adapter Designer.
Restore the model related ODM bak files to the SQL Server
(Note: If no ODM bak file provided, you can create one mMDM DB by yourself, and please make sure all the needed facility, material, location, etc are created and configured correctly) (refer to DOC Aspen PIMS Integration user guide, section 5)
Launch Aspen mMDM Administrator V10, and then enter all the necessary info according to the wizard. (refer to DOC Aspen PIMS Integration user guide, section 6)
Configuration for 64 bit OS
Copy all the files under PIMS-200864bit folder to:
C:\Program files\AspenTech\AEP\EnterpriseConnect\IntegrationPacks\pims\Adapter\etc\xml\ and replace the original ones.
(Note: you’d better backup the original files before replacement)
After the replacement, all the other configuration is the same as the 32 bit OS.
KeyWords
PIMS Adapter, Integration Adapter Designer
Keywords: None
References: None |
Problem Statement: Can aspenONE Engineering and aspenONE Manufacturing applications run on the same computer? | Solution: Yes, you can run both aspenONE Engineering and aspenONE Manufacturing applications on the same computer. However, both suites need to be at the same version. Mixed versions of Engineering and Manufacturing suites are currently not supported.
Keywords: AES,
MES
aspenONE
References: None |
Problem Statement: Why are the Help files not present when installing aspenONE using a silent deployment package? | Solution: When installing aspenONE using a silent install package, if the Help files are not present, then they were not included in the silent install package when the package was originally created.
To fix this, copy the HtmlHelp self-extracting exe files from the original location on the media at:
<media_root>\aspenoneengdvd\core\HtmlHelp (Engineering) or
<media_root>\aspenonemscdvd\core\HTMLHelp (Manufacturing and Supply Chain)
Next, paste the files in the same location in the silent deployment package.
Keywords: Help files
packaged silent installation
References: None |
Problem Statement: How to model a two stage compression, split pressure level propane refrigeration process in HYSYS? | Solution: In this document, a typical two stage, split level propane refrigeration process model is presented, along with several possible integrations with other parts of a plant. The source and detailed discussions of the process can be found in reference [1] and [2].
Figure 1 shows a two stage, split level refrigeration process (GPSA, 1987, Figure 14-7), and its operating conditions.
Figure 1. Two Stage Split Level Propane Refrigeration Process
This process provides two cooling duties at different temperatures. Only a portion of propane is circulated to the low pressure chiller, and thus saving horsepower compared to a simple refrigeration loop.
Typically, propane refrigeration process is only part of a plant model, such as, NGL plant. The cooling duties for both high pressure and low pressure exchangers are determined by the process streams exchanging heat with the refrigeration loop. From modeling standpoint, the refrigerant flowrates through low pressure and high pressure exchangers have to be calculated by the program from the requested duties and the outlet conditions of the two exchangers. This is the central feature of this model, i.e., the interactions between the refrigeration process and the process streams requesting cooling.
Figure 2 shows the base model developed in Aspen HYSYS. Separator unit is used to model receiver, and suction drums. Two Compressor units are used to represent stage 1 and 2 compression.J-T expansion is modeled with Valve unit. A Cooler unit is presented to model air cooler, and it can be replaced with Air Cooler unit.
The base model is a faithful representation of a typical process shown in Figure 1 except the addition of unit TEE-101 and stream LP Extra and HP Extra. These additions do not model actual unit or line on the plant, but are necessary to get a robust model. Users are encouraged to experiment with the attached base case using different model setup.
In Aspen HYSYS basic training course, we show that for a simple propane refrigeration loop or a propane refrigeration loop with economizer, the refrigerant flowrate can be calculated from duty, and be propagated backward throughout the flowsheet. In this case, the approach does not work properly. The low pressure line is the liquid outlet of the high pressure suction drum. The flowrate on this line is calculated by HP Suction Drum. But, to meet the duty demand of LP Exchanger, the flowrate on this line has to be calculated by LP Exchanger. The addition of unit TEE-101and stream LP Extra allows for the flowrate of the liquid outlet from HP Suction Drum and that of stream 12 to be different, while the material balance around TEE-101 is always satisfied. As a result, the flowrate on LP Extra may be positive when the flowrate of stream 10 is larger than that of stream 12, or negative when the flowrate of stream 10 is less than that of stream 12. The intended flowrate for LP Extra is zero, and a scheme to achieve this is presented later in this document.
Stream HP Extra is added for the similar reason. The flowrate of stream 3 is user specified. The flowrate on stream 4 is calculated by HP Exchanger. The inlet to TEE-100 is determined by Receiver. The addition of HP Extra allow the material balance of TEE-100 to be met under all situations. However, the intended flowrate for this stream is zero.
Figure 2. Base Model of a Two Stage Split Level Propane Refrigeration Process
The remaining issue in base model is to capture the operating conditions so that the flowrates of streams LP Extra and HP Extra are at zero. Earlier, we mentioned that the flowrate of stream 3 is user specified. Changing this specification will directly change the flowrate on liquid outlet of HP Suction Drum, and in turn change the flowrate of stream LP Extra. Based on this understanding, an Adjust unit is used to change the specified flowrate on stream 3 until the flowrate of LP Extra is zero, see Figure 3 for the setup. As a result, the liquid outlet flowrate calculated by HP Suction Drum equals to the flowrate of stream 12 determined by the requested duty on LP Exchanger. Now, the sum of flowrates of stream 3 and 4 matches the inlet of TEE-100, stream 2, and the flowrate of HP Extra is always zero.
Next, the model is converted to templates based on the anticipation of two typical applications. The first is to interact with other part of a plant through energy streams. In this situation, the duties for both exchangers are provided by other part of the model, and the propane refrigeration process model only calculate the refrigerant flowrates to support the duties. The second is though two sided heat exchangers. The refrigerant flows in the shell side, while the process streams flow in the tube side. In this case, the process streams need to be fully calculated at inlet, have pressure (or can be calculated via pressure drop specified in the exchangers) and temperature at the outlets. The program will calculate the duty for a exchanger, then determine the refrigerant flowrate based on duty. The UA of the exchange will also be calculated.
Figure 3. Updated Model of a Two Stage Split Level Propane Refrigeration Process
Finally, four technically possible ways in HYSYS to integrate propane refrigeration process model to your plant are presented.
The simplest integration is to specify the duties for low pressure and high pressure exchangers. In this setting, the refrigeration process is imbedded in subflowsheet. The duties calculated by Cooler units are used as feeds to the subflowsheet. Only the energy exchange is model, while the feasibility of the heat transfer is not considered.
The more straightforward integration is to bring the refrigeration process as part of the model. Two sided exchangers are shown in the provided flowsheet, but Heater units can be used in place of the two sided exchangers. The feasibility of the heat transfer is part of the modeling concern here.
The third integration reveals the two exchangers on the main flowsheet, but hides the rest of the refrigeration process in subflowsheet. Recycle units are not necessary. It is critical to specify the transfer basis in the subflowsheet correctly. In this example, the transfer basis for stream 5 has to be VF-P, because these are specified variables on the outlet of the high pressure exchanger. The transfer basis for stream 9 has to be VF-T, because temperature and vapor fraction are specified on the outlet of the low pressure exchanger.
The forth integration uses a convenient feature of Heat Exchange unit, i.e., it allows streams from different flowsheet for different sides. Only streams for one side are shown on the main flowsheet. The flowsheet appears less busy.
For the details of different integrations, please see attached demo file.
List of File Attachments
1) C3 Refrigeration Base Case.hsc -- Base model shown in Figure 2.
2) C3 Refrigeration Updated.hsc -- Updated model shown in Figure 3.
3) C3 Refrigeration Sub1.tlp -- Subflowsheet which interacts with process streams via energy streams.
4) C3 Refrigeration Sub2.tlp -- Subflowsheet which interacts with process streams through two sided exchangers.
5) Integration of two exchangers.hsc -- Demo of four ways to use propane refrigeration process model
A note is available in models and subflowsheets with detailed specifications throughout the model.
Keywords: Propane, refrigeration, C3, two stage, split level, compressor, adjust
References: s
[1] Oilfield Processing of Petroleum: Natural Gas, Francis S. Manning, Richard E. Thompson, published by PennWell Books, 1991, ISBN 0878143432, 9780878143436.
[2] Encyclopedia of Chemical Processing and Design: Volume 45 - Project Progress Management to Pumps, John J. McKetta, William A. Cunningham, published by CRC Press, 1993, ISBN 082472495X, 9780824724955. |
Problem Statement: How do I model solid solubility in a flowsheet?
See the attached files: dissolid.bkp and dissolid.inp The backup file will run in Aspen Plus 10.2 and higher. The input file will run in 9.2 and higher. | Solution: A partially dissolved solid can be modeled in Aspen Plus by specifying a physical property chemistry paragraph or object containing an equilibrium salt reaction. This method will enable the physical property system to perform solubility calculations for all streams and blocks within any flowsheet section that references the Chemistry paragraph or object. Equilibrium salt reactions are normally used with electrolyte systems, but can also be used with other physical property option sets to model the precipitation of any conventional solid if equilibrium data are known. A chemistry paragraph or object is created in the ModelManager by pressing the New button on the Reactions / Chemistry Object Manager form. If using input language, the equilibrium reaction is specified within a Chemistry paragraph.
In this example, the solubility of sucrose in water is calculated between 0 and 100C. The attached files contain a Property Analysis and Heater block to illustrate the implementation of this approach. The following steps are required:
1. The solid component must be defined as two components, once as a dissolved component and again as the precipitated solid. In the GUI, the dissolved component must be declared as a Conventional type and the precipitated solid as a Solid type.
2. A precipitating salt reaction must specified on the Reactions / Chemistry form in the Data Brower, or in an input language Chemistry paragraph.
4. The True-component approach must be used in order for the precipitated and dissolved salt concentrations to be reported separately.
5. The equilibrium constant for the equilibrium constant (K-SALT) must be regressed from solubility data using the Data Regression System (DRS) if not known. The equilibrium constant has the form: ln(K)= A + B/T + C*ln(T) + D*T.
6. After doing the regression, the values for K-SALT must be specified with the reaction on the Reactions / Chemistry form.
7. The Run Type on the Setup / Specifications form can be changed from DRS to FLOWSHEET to build and run a flowsheet.
To illustrate the suitability of this method, solubility data from the Handbook of Chemistry and Physics, 35th edition, page 1629, are compared with the regressed polynomial:
Temperature
Sucrose Solubility
Sucrose Solubility
(deg. C)
(Wt.%)
(Calculated Wt.%)
0
64.180
64.182
5
64.870
64.889
10
65.580
65.611
15
66.530
66.411
20
67.090
67.121
25
67.890
67.914
30
68.800
68.761
35
69.550
69.575
40
70.420
70.448
45
71.320
71.350
50
72.250
72.281
55
73.200
73.237
60
74.180
74.222
65
75.880
75.565
70
76.220
76.267
75
77.270
77.320
80
78.360
78.404
85
79.460
79.500
90
80.610
80.630
95
81.770
81.771
100
82.970
82.940
The coefficients were found to be A=233.5378, B=-5602.269, C=-42.62564, and D=.0865879 using DRS.
The attached file contains the necessary input to perform the regression, and a Property Analysis and small flowsheet using the NRTL property method. The run type can be changed from Flowsheet to Data Regression or Property Analysis to view each section separately in the Graphical User Interface.
Notes:
1. Most Property Methods can be used with the true component approach. (The KSALT parameters for sucrose were regressed using NRTL, RK-SOAVE and the IDEAL Property Methods. All gave the same analysis and regression results.)
2. Solid Heat of Formation (DHSFRM) and Solid Heat Capacity (CPSPO1) parameters were entered for the solid sucrose. Without these parameters the enthalpy of the solid is incorrect.
3. K-SALT and activity coefficient model parameters are not independent of each other.
Keywords: None
References: None |
Problem Statement: Aspen EDR design templates enable process engineers to perform preliminary sizing of heat exchangers using design standards created by the company experts. EDR design templates can be created to enforce geometry and design specifications preselected for an exchanger type. | Solution: The objective of this solution is to understand:
· Why one should use EDR Design templates
and demonstrate how to:
· Create a Heat Exchanger Design Template
· Use the template to size a Rigorous Heat Exchanger model from a Process Simulator (Here Aspen HYSYS)
· Review resulting Heat Exchanger Model
· Revert back to a simple End Point model, if required
In addition to the guide, an Aspen HYSYS case file and an Aspen EDR template file are provided to let you try the sizing process for yourself.
Keywords: None
References: None |
Problem Statement: Incorporating rigorous heat exchanger models in process flow sheets helps process engineers quickly evaluate feasible heat exchanger design alternatives and assess its impact on capital and operating expenditures. This is achieved by means of accurate thermal and hydraulic process simulation models that rigorous heat exchangers help create. | Solution: This example demonstrates the above value by incorporating a rigorous Plate-Fin Heat Exchanger Model in an Aspen HYSYS Flowsheet.
Plate-fin heat exchangers are critical to many cryogenic gas separation processes and are increasingly found in many processing plants. Significant capital and operational savings can be realized with the high thermal effectiveness provided by this technology. Plate fin exchangers can handle many process streams in a single exchanger to provide for a high degree of thermal integration. This not only minimizes consumption of primary energy but also brings benefits in modular construction and plant layout.
Aspen Plate Fin Exchanger performs a detailed simulation of multi-stream plate-fin heat exchangers made from brazed aluminum, stainless steel or titanium. The models and correlations within the program are recognized as the industry standard, based on over 40 years of Aspen HTFS research. It can be used standalone by the thermal specialist for exchanger design or as an integrated product with AspenTech's steady-state process simulation program, Aspen HYSYS®
The attached example demonstrates how a company benefited from collaboration between thermal equipment specialists and process engineers through the integration of the Aspen Plate Fin Exchanger and Aspen HYSYS programs.
In this example you will learn:
· Why one should incorporate rigorous heat exchanger models in process flow sheet?
and learn How to
· Examine a ‘simple’ heat exchanger model in an Aspen HYSYS Flow sheet
· Convert the simple model to an EDR plate-fin model by importing a plate fin exchanger model
· Examine the model
· Use the model to decide between two alternative feed purchase options
Keywords: None
References: None |
Problem Statement: Where do I find examples on flowsheet of rate-based model CO2 capture with an absorber and regenerator? | Solution: Beginning with Aspen Plus V8, we have introduced aspenONE Exchange, which contains many examples and flowsheets.
There are different examples on CO2 capture Flowsheet with Ratebased models are available with Physical as well as Chemical Solvents in below location
From the Aspen Plus ribbon, click on "Exchange" then type "CO2" then click on search:
Alternatively user can look for many examples provided in below location on CO2 Capture Rate-Based Distillation
C:\Program Files (x86)\AspenTech\Aspen Plus V8.0\GUI\Examples\Amines_ELECNRTL
C:\Program Files (x86)\AspenTech\Aspen Plus V8.0\GUI\Examples\Amines_ENRTL-RK
C:\Program Files (x86)\AspenTech\Aspen Plus V8.0\GUI\Examples\Physical Solvents
Keywords: CO2 capture flowsheet example, Rate-based CO2 capture
References: None |
Problem Statement: How do you obtain properties for streams from the main and sub-flowsheets using Excel VBA? | Solution: This example macro demonstrates how to extract data across all streams from the main flowsheet and 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. The user can expand the variables by modifying the following code segment in the Excel file attached with this solution.
For Each hyStream In fs.Streams
'If this is a material stream
If Not hyStream.IsEnergyStream Then
i = i + 1
j = 0
Range(Loc).Offset(i, j - 1).Value = fs.Name
Range(Loc).Offset(i, j).Value = hyStream.Name
'Temperature
j = j + 1
Units = Range(Loc).Offset(0, j)
Range(Loc).Offset(i, j).Value = hyStream.Temperature.GetValue(Units)
'Pressure
j = j + 1
Units = Range(Loc).Offset(0, j)
Range(Loc).Offset(i, j).Value = hyStream.Pressure.GetValue(Units)
'Mass flow rate
j = j + 1
Units = Range(Loc).Offset(0, j)
Range(Loc).Offset(i, j).Value = hyStream.MassFlow.GetValue(Units)
'Molar flow rate
j = j + 1
Units = Range(Loc).Offset(0, j)
Range(Loc).Offset(i, j).Value = hyStream.MolarFlow.GetValue(Units)
'Actual volume flow rate
j = j + 1
Units = Range(Loc).Offset(0, j)
Range(Loc).Offset(i, j).Value = hyStream.ActualVolumeFlow.GetValue(Units)
'Molecular weight
j = j + 1
Units = Range(Loc).Offset(0, j)
Range(Loc).Offset(i, j).Value = hyStream.MolecularWeight.GetValue(Units)
'Molar density
j = j + 1
Units = Range(Loc).Offset(0, j)
Range(Loc).Offset(i, j).Value = hyStream.MolarDensity.GetValue(Units)
'Mass density
j = j + 1
Units = Range(Loc).Offset(0, j)
Range(Loc).Offset(i, j).Value = hyStream.MassDensity.GetValue(Units)
'Vapour fraction
j = j + 1
Units = Range(Loc).Offset(0, j)
Range(Loc).Offset(i, j).Value = hyStream.VapourFraction.GetValue(Units)
Keywords: VBA, Sub-Flowsheet, Stream Properties
References: None |
Problem Statement: How to generate an Ideal Pump Curve from Aspen HYSYS. | Solution: For generating Idea Pump curves, users can use Generate Curve option available in HYSYS pump operation. Please follow the steps listed below to generate the curves.
1. Add and converge a simple pump Unit Operation in your flowsheet. You can fully define the inlet stream and then specify the outlet pressure.
2. Nest, go to Rating> Curves and click “Generate Curves� button. Then, provide the design flow, design head and design efficiency values. If you know the design speed, you can also input that value.
3. After you hit “Generate Curves� button in the window, three curves should be generated in the list. You can also check the data in each table.
4. If you want to see the plot with your current operation point, you can click plot curve button. You will see a beautiful plot.
5. You can check the Use Curves box to use it in the simulation.
In the attachment, an example file (V8.6) has been made. Please refer to that file for more getting a better idea about the generated curves.
Keywords: Ideal Pump Curve, Generate Pump Curve, HYSYS
References: None |
Problem Statement: How do I use Aspen HYSYS to analyze column relief loads using the Unbalanced Heat Method? | Solution: The Property Balance Utility can be used to analyze the unbalanced heat loads on a Column. The steps to complete the analysis are shown in the PDF attached using the HYSYS example called " Atmospheric Crude Tower.hsc" Please note you will find this file directly from Resources tab > Examples
          Â
Keywords: PSV, Unbalanced Heat Method, Property Balance Utility
References: None |
Problem Statement: In one Aspen Plus or Aspen Properties simulation using data regression to estimate the binary interaction parameter UNIQ for the UNIQUAC activity coefficient model, if the ternary diagram is created using the “Aspen Plus Ternary Diagram” the effect of changing the binary parameters can be observed. However, if you use “Distillation Synthesis ternary map” to generate the diagram and you modify the binary parameters, then the changes do not take place.
Workaround( | Solution: )
This problem is caused by user-entered binary parameters being silently replaced with the regressed values if a Regression section is defined.
The workaround to solve this problem is (applies for Aspen Plus and Aspen Properties):
1. Update the binary parameters first, and then delete the Regression section.
2. Save the file as a different name and close Aspen Properties.
3. Open the .aprbkp file saved in step 2 with Aspen Properties.
4. Generate ternary diagrams with Distillation Synthesis.
Fixed in Version
CQ00556369: Targeted for a future release
KeyWords
Ternary diagrams, Distillation Synthesis, UNIQUAC, binary parameters.
Keywords: None
References: None |
Problem Statement: Aspen Capital Cost Estimator (ACCE) v8.4 and v8.6 crash/freeze when working on a dual monitor desktop computer. | Solution: When working on a dual monitor desktop computer, sometimes you select an option that will display another window inside our Economic Evaluation software and you will note that the program will freeze after making a click on this selection. This only happens on a dual monitor desktop computer. To avoid this behavior, always use your first monitor to avoid crashing and freezing when working on Aspen Capital Cost Estimator, Aspen Process Economic Analyzer, or Aspen In-Plant Cost Estimator.
Keywords: Freeze, Crash, dual monitor, desktop
References: None |
Problem Statement: Can Aspen Simulation Workbook V7.3 or the Aspen Plus and Aspen Properties Excel Add-In run on Windows 7 (64bit) together with Excel 2010 (64bit)? | Solution: No.
Aspen Simulation Workbook (ASW) V7.3 and the the Excel add-in for Aspen Plus and for Aspen Properties do not support 64 bit Excel.
ASW and the Excel add-in for V7.3 will run on Excel 2010 x 32 bit (or on lower versions of Excel).
There is a patch available for ASW V7.2 to support Excel 2010 (which came out after our V7.2 release).
Fixed in Version
V8
Keywords: None
References: None |
Problem Statement: After adding Ammonium Bisulfate (NH4HSO4) to the Chemistry in my simulation, it fails with missing parameters.
****PROPERTY PARAMETER ERROR
SOLID FREE ENERGY OF FORMATION (DGSFRM) MISSING
FOR COMPONENT "AMMON(S)". UNABLE TO CALCULATE REACTION CONSTANT.
! Calculations stopped because of missing property parameters | Solution: The solid free energy of formation for Ammonium bisulfate or Ammonium Hydrogen Sulfate (NH4HSO4) is missing from our databank (value of zero stored). The calculated equilibrium constant would be in error, possibly causing incorrect results, and that is why we now terminate the calculations.. If no precipitation is expected, then there would not be an issue. In that case, you could set a very small value for DGSFRM parameter of AMMON(S), say 0.0001, to proceed with the calculations as before.
These K-SALT parameters for NH4HSO4 were regressed and will be added to the Electrolyte Wizard reaction databank in a future release.
Values are:
A=104.6591 B=0 C=-26.57429 D=0.1453109
Keywords: None
References: : CQ00555850 |
Problem Statement: I have edited the pure component and binary interaction parameters inside Aspen Plus. When exporting the Aspen Plus property package into Aspen HYSYS I do not get identical values when comparing the results between both the simulation packages.
Applicable Version(s)
Aspen HYSYS and Aspen Plus versions 2006 and above | Solution: When exporting the Aspen Plus property package into Aspen HYSYS only the original component properties and binary interaction parameters from the selected databanks are exported into the Aspen HYSYS simulation. Any specified parameters by the user inside Aspen Plus do not pass into Aspen HYSYS. For this reason, under identical process the conditions, the simulation results between Aspen HYSYS and Aspen Plus will be different.
Workaround
No workaround currently available
Fixed in Version
CQ00548281: Currently no fix.
Keywords: Aspen Plus, Aspen HYSYS,Export, Property Package
References: None |
Problem Statement: In Safety Analysis | Exch. Tube Rupture, when the user tries to input a negative value for Operating Temperature at High Pressure Side, an error message appears "Number is outside allowable range." as shown below: | Solution: This is an known issue in V8.4 and V8.6 HYSYS, which has been fixed in HYSYS V8.8.
The current workaround is to change the Units Set to EN from the Home Tab, then input temperature values in degree F(Fahrenheit). Change the Units back to SI where HYSYS will accept the converted negative values.
If the desired temperature is very low, e.g. below -17.7 degree C, then the user has to upgrade to HYSYS V8.8.
Keywords: Safety Analysis, Exch. Tube Rupture
References: None |
Problem Statement: How do I prevent the error message, "Configuration unsupported for Miller charts for tee K=1 used"? | Solution: In Aspen Flare System Analyzer, the tee calculations uses a K factor which is interpolated using Miller Curves, which are functions of the flow and area ratios of the branch to the total flow as well as the branch angle. These charts do not cover all possible configurations of tee and so in these cases Aspen Flare System Analyzer simply uses a K value of 1.0. You cannot specify the values.
There are two ways to solve it:
1. The suggested method is to combine the flows such that the combined stream exits Downstream instead of the Branch, in order to be consistent with the Miller charts.
2. Use another metho:, for example, the Gardel method.
Keywords: Miller Method, Error message.
References: None |
Problem Statement: When trying to perform a full install of the Aspen OnLine components on a Windows 7 operating system there is no option to install the Aspen OnLine Server component. | Solution: Typically, the Aspen OnLine Server component runs as a service on a server class operating system. Due to some changes in the configuration of the Aspen Properties Enterprise Database (APED) on a server class operating system, the Aspen OnLine Server component can now only be installed on a server class operating system. Currently Windows Server 2008 R2 or Windows Server 2012 is supported for Aspen OnLine V8.4 and V8.5. Note the Aspen OnLine Client program can be installed on a server class or non-server class operating system like Window 7.
Keywords: AOL install, Aspen OnLine install, AOL Server, Windows Server 2008 R2, Windows Server 2012
References: None |
Problem Statement: How can I design a Plate Fin / LNG using Aspen Exchanger Design & Rating (EDR) in Aspen HYSYS? | Solution: Steps to design a Plate Fin inside Aspen HYSYS using EDR.
1. You need to create a Simple Weighted Plated Fin in HYSYS, it has to be fully defined
2. Open EDR, open a “New� case, select Plate Fin Exchanger (PlateFin).
3. Then go to the “File� Tab and select “Import From� and select the HYSYS version you have been using.
4. Select your Hysys Model, previously saved with your Plate Fin, HYSYS will open with the case.
5. In EDR select your exchanger,
6. In EDR in Input > Problem Definition> Application Options > Calculation mode select Design.
7. Run the model
8. Now go to the “Run� tab and select “Update file with Geometry- PlateFin
9. Save the case and close EDR.
10. Open the HYSYS file go to Plate fine model and change Rating Method to EDR-PlateFin. And delete all specifications in the outlet streams and pressure drop if you have defined any.
11. Go to EDR Plate Fin tab, and select Import,
12. Now in the LNG Pass Name select the corresponding streams, like it is shown below.
Keywords: Plate Fin, EDR, Design, LNG
References: None |
Problem Statement: In some Aspen Flare System Analyzer case files that contain glycol, there is big difference in temperature for Knock-Out drum in Aspen Flare System Analyzer and Aspen HYSYS. | Solution: Peng Robinson in Aspen Flare System Analyzer does not handle the glycols like TEG very well. This is why in Aspen Flare System Analyzer, glycols are often modeled as hypothetical HC - which can affect results significantly.
In general, Aspen HYSYS and Aspen Flare System Analyzer PR should be close in most cases but with following exceptions:
1. Aspen Flare System Analyzer PR does not handle the glycols like TEG very well. This is why in Aspen Flare System Analyzer glycols are often modeled as hypothetical HC which can affect results significantly.
2. Hypo component estimation methods are not part of property package and are different in Aspen HYSYS and Aspen Flare System Analyzer .
3. Binary coefficient may be different
If we remove the glycol and hypo in the Aspen Flare System Analyzer case file, you will find the calculation results is much similar with Aspen HYSYS.
Keywords: Glycol, Hypo, Flarenet
References: None |
Problem Statement: The depressuring tool in Aspen HYSYS allows the user to study a scenario in which a depressurization in a reactor takes place maybe due to a fire or a blowdown. In order to study this scenario, the user must define certain valve parameters. One of the specifications is the Vapour Flow Equation, in which the user needs to select the equation to be used.
One of these equations is the General equation and when opening the spreadsheet, in which all the calculations are shown, the equation specified for the gas specific heat ratio (K) implies an empirical factor (1. - .12/11900 * (P -100)), instead of using the Ideal Gas simple equation (API: k = Cp/Cv). | Solution: The empirical factor as specified in the general equation was originally used in the utility "Depressuring - Original". This is left unchanged in the new version for backward compatibility. The user can make changes in the spreadsheet and modify the equation to the one that they want to use (ideal or semi-ideal equation).
Keywords: Depressuring utility, General equation, Gas specific heat ratio.
References: None |
Problem Statement: I get the error below trying to use the Import Sources option. | Solution: This error is common when you have multiple versions installed. You must set the current version as the default one. For V8.6 go to All Programs | AspenTech | Process Modeling V8.6 | Aspen HYSYS | Set-Version Aspen HYSYS V8.6. Please note you require administrator rights to do so.
Keywords: import error, import sources, HYSYS stream sources
References: None |
Problem Statement: What should I do when I get warning "Solid particles (e.g. ice pellets) have been detected inside pipe"? | Solution: This warning is displayed when either:
The temperature somewhere in pipe segment is below 0C AND water is present in the stream
OR
The inlet stream has a solid phase
In the event of this warning the user should check the hydrate formation temperature and compare this with the temperature profile of the pipe.
In Aspen HYSYS V7.3 and newer version, the pipe segment contains Flow Assurance calculations. The users can compare the hydrate formation temperature profile with the fluid temperature in the pipe. See the screenshot below.
If the hydrate formation temperature is higher than the actual fluid temperature then the user may consider using hydrate inhibitors in order to suppress the hydrate in the pipe. The warning is intended to inform the user to take the appropriate preventative measures.
Keywords: Pipe Warning, Flow Assurance, Hydrate Formation Temperature
References: None |
Problem Statement: Where can users find the supportive packing materials to export from HYSYS to KG tower in tray sizing utility? | Solution: HYSYS exporting to KG tower feature only supports a few packing materials. Users can open a tray sizing utility and go to export tab.
After clicking "export to KGtower", users can select Packing radio button and check the box for displaying KG packings. If the packing materials that you select are in this list, you will be able to check the box on the tray list and export them.
Please remember that users have to install KG tower before you launch this function.
Keywords: Tray sizing, Export to KG towers, Supportive packing materials
References: None |
Problem Statement: How can I model a thermal fluid heater? | Solution: Many plants furnish heat to individual users by means of an intermediate heat transfer medium, which is normally mineral or synthetic oil. A fired heater is typically used to elevate the temperature of this heat transfer medium. The fluid normally remains in the liquid state from inlet to outlet. This kind of equipment can be modelled with Aspen Fired Heater
The general practice in the industry for this exchangers is to use a radiant-only helical coil heater because it has a simple/cheap construction and can achieve a high efficiency
This are the specifications used in this example:
Fuel: Oil No. 2
Thermal Fluid: DOWTHERM Q. The properties for this fluid were taken from the product datasheet and entered manually as user defined properties.
Geometry: Helical coil bare tube design (3 pass, 7 tubes in series), Vertical orientation
Further customization is possible with Aspen Fired Heater. For instance:
-Horizontal or Vertical configurations, as required to meet the physical limitations of the facility
-Combustion air preheating
Keywords: Thermal fluid heater, Fired Heater, Thermal Fluid, Helical Coil
References: None |
Problem Statement: How do you find the layered temperature for the pipe in an Aspen Hydraulics? | Solution: In Aspen Hydraulics pipe model you can provide heat transfer parameters and add insulation layers as given below.
The Hydraulics then calculate the fluid temperature, temperature of fluid in contact with pipe, temperature of pipe/insulation, the temperature on the surface of the insulation and ambient temperature. The temperature profile is available in the Performance page under Insulation as shown below.
Keywords: Layered Temperature
References: None |
Problem Statement: 错误消æ�¯â€œNot licensed for Crude Distillation (Distillation of high NBP hypothetical components)â€�有何å�«ä¹‰ | Solution: å�¯ä»¥è®©HYSYSè¿�行的许å�¯æ–‡ä»¶æŽ§åˆ¶ç�€ç”¨æˆ·å¿…é¡»è¦�使用的功能和选项。其ä¸æœ‰ä¸€ä¸ªâ€œCrudeâ€�选项，如果没有勾选这一选项，当è¿�行塔模拟程åº�时，仅é™�有é™�个数的物质组分，例如“Not licensed for more than 25 components with columnsâ€�。在这ç§�情况下，程åº�会冻结ä½�并将物质组分个数设为最大数目25.
而且如果精é¦�塔设置了多过25个物质组分的时候，如果其ä¸ä¸€ä¸ªç‰©è´¨çš„常沸点高于533K（NBP>533K），程åº�也会出错。例如24个组分（其ä¸ä¸€ä¸ªç‰©è´¨NBP>533K）是没有问题的，å�Œæ ·çš„26个组分，æ¯�一个的NBP都å°�于533K也是没有问题的。
有50ä¸ªæ— æœºè™šæ‹Ÿç»„åˆ†çš„ä¾‹å�，å�³ä½¿æœ‰äº›è™šæ‹Ÿç»„分的NBP>553K，程åº�也是å�¯ä»¥è¿�è¡Œçš„ã€‚è¿™æ˜¯å› ä¸ºå�ªæœ‰æœ‰æœºçš„虚拟组分会调用这个检查了。
唯一的解决方法是有“Crude�选项的许�文件，或是包括Crude和Oil选项的Refinery选项
Keywords: Crude，Oil，物质组分，虚拟组分，�制，没有许�文件，NBP, CN-
References: None |
Problem Statement: Do I need a license to access PVT Pro from Schlumberger? | Solution: If you have Aspen HYSYS Upstream access then you should have access to PVT Pro.
The program allows you to open .pro files and install the characterization in Aspen HYSYS, as well as characterize an assay using PVT Pro EOS.
To access PVT Pro in the Properties Environment go to PVT Laboratory Measurements.
Then go to Add Package, name it and Select DBR PVTPro. Click on Launch Engine, DBR PVT Pro should start.
To review a detailed sequence of how to install a .pro file go to Solution 119956, How to import PVT data from a third-party modeling software?
Keywords: PVT Pro, HYSYS, License, PVT laboratory Measurement.
References: None |
Problem Statement: What is the impact of coking and what are the general guidelines to avoid excessive coking in Fired Heaters? | Solution: Coking is the formation of carbonaceous deposits and is an important side reaction in many industrial processes, but it can become a problem in fired heaters and fired reactors as they accumulate inside the coils or tubes. It is recognized that coking is a problem to be avoided
In general (without getting into the specifics of the formation mechanisms), coking formation depends upon: fluid Composition (e.g. if there are unsaturated hydrocarbons in the feed), residence time, wall temperature (if it rises above critical values)
These are some of the detrimental effects of coking in the operation of fired heaters:
-Pressure drop increase inside tube
-Poor Heat transfer hence reducing the thermal efficiency
-Increase on tube metal temperature which can lead to tube failure. The TMT (Tube Metal Temperature) is a primary indicator for fouling/ coking services.
Fig. 1. Impact of coking on the tube metal temperature1
The reduction or elimination of coke formation often results in constraints on the operating conditions to be applied. Here are some recommendations and design practices to control or avoid excessive coking:
1. Coking can be controlled by controlling the steam/carbon ratios in the feed. Steam and hydrogen are the most important retarding reactants2. The coking deposits are formed at certain steam to carbon ration which means that in many cases the equipment most operate with a surplus of steam, the drawback is that a larger heater might be required. In Aspen Fired Heater There is an option to inject steam.
2. There is widely accepted a rule of thumb, mass flux (mass flow rate per tube cross sectional area) should not be less than 1000 kg/m2 s. This value is drawn from many years of experience.3
3. Limit vaporization, 20 to 60%
4. Limit the maximum heat flux
At the flow rates and qualities used in fired reboilers, the flow pattern that will occur over the majority of the length of a heated pipe, both upward and downward flow was found to by annular by Chong4. Annular flow is characterized by a liquid film flowing in a channel with a central gas core that may or may not contained droplets entrained. In simple terms, the goal of these recommendations (2,3 & 4) is to try to maintain the annular flow pattern, so the walls are always wetted.
1Sahu, Ruby Fired Heater for Process Plants. Foster Wheeler
2 J.R Rostrup-Nielsen, Catal. Today, 18 (1993)
3L.Y. Chong, B.J. Azzopardi, D.J. Bate, Calculation of Conditions at Which Dryout Occurs in the Serpentine Channels of Fired Reboilers, Chemical Engineering Research and Design, Volume 83, Issue 4, April 2005, Pages 412-422
4 Chong, L.Y, 2003, Annular two-phase flow in straight and serpentine channels, PhD thesis, University of Nothingham.
Keywords: Coking, Fired Heater, Process Heater, Fired Reboiler
References: None |
Problem Statement: The compressor inlet stream vapor fraction is less than 1 but there is no warning about liquid in the inlet stream. | Solution: The reason why we are not seeing an error message in the trace window or on the compressor object view is because of the tolerance based on which we check if there is Liquid in the inlet feed stream. The tolerance we use in this case is 0.999 and compressor will only warn if the vapor fraction of inlet stream to the compressor falls below (actually less than or equal to) this value.
Keywords: Compressor, Vapor fraction, Liquid In inlet stream
References: None |
Problem Statement: HYSYS invokes the incorrect solver for an Aspen Custom Modeler exported model. (ACM Op). This may cause convergence failure. It should be using by default the sparse solver with block decomposition, but it is incorrectly using the sparse solver without block decomposition. | Solution: Create a script in the model in Aspen Custom Modeler with the name EBSOLVE with the following instructions;
SOLVER DECOMP_SPARSE
SOLVE
Export the model from Aspen Custom Modeler. The purpose of this change is to create an OOMF initialization script. Note that if there is a Presolve VBScript in the model it will be automatically invoked when the SOLVE command is issued.
The example attached illustrates the problem as well as the work around: demo_model works correctly, and demo_model2 illustrates the problem. You can see on the screen captures where you can control which solver is actually used.
This is fixed in v8.8.
Keywords: CQ00554454, ACM, DECOMP_SPARSE. DSPARSE, SPARSE, solver, defect
References: None |
Problem Statement: How do I customize the Plate Databank in Aspen Plate Exchanger? | Solution: The Plate Databank can be edited by opening the Mdb file located in the program directory. These steps are described below.
1. Open Windows Explorer and navigate to C:\Program Files (x86)\AspenTech\Aspen Exchanger Design and Rating V8.4\Dat\Mdb.
2. Open the file PlateDb.mdb
3. Add an index and Manufacturer Name on the "Manufacturers" Table
4. Add indexes and plate geometry details on the "Plates" Table
Keywords: Customize, Plate Databank, Plate Geometry
References: None |
Problem Statement: When installing Aspen Basic Engineering from DVD 1 of V8.6, we cannot load any information on this program since the Aspen Basic Engineering Server is not available. We select all the options within the ABE group and the installation fails to register the server settings, like the Data Services folder. | Solution: The Aspen Basic Engineering Server is no longer included on the Aspen Basic Engineering section, you will need to go to the Server Tools group and select the Aspen Basic Engineering server so it can be installed on your machine.
Keywords: V8.6, Data services, Fail, Server, Aspen Basic Engineering
References: None |
Problem Statement: What is the geometry definition of Open distance at top (bottom) of layout/ Open distance on left (right) of layout/ Shell ID to outer tube limit diametric clearance? | Solution: Here is the sectional drawing of a shell and tube exchanger. The blue line refers to outer tube limit diametric clearance. The red line refers to the baffle outer diameter. The black line refers to Shell ID.
Open distance at top/bottom/left/right of layout share the same definition. It means the outmost tube edge distance to shell ID at that location(gold line to gold line).
Shell ID to outer tube limit diametric clearance means the distance between Shell ID and OTL(Double the distance of Blue line to Black line)
Keywords: Open distance at top (bottom) of layout, Open distance on left (right) of layout, Shell ID to outer tube limit diametric clearance
References: None |
Problem Statement: How can I use the Aspen Exchanger Design and Rating (EDR) programs when in the supercritical region? | Solution: There are two ranges of pressure which can be termed ?supercritical? for anything but a pure component. One is above the criconbar, which is the highest pressure at which two phases can exist and the other is between the critical point and the criconbar, where two phases can exist, but unusual behaviour can occur, such as the vapor mass fraction decreasing with increasing temperature.
The key to calculations in either of these regions is getting the physical properties correct. It is also preferable that the pressures you chose at which properties will be specified are all in the same region, avoiding having some pressures above the criconbar and others below. This is not normally a problem since exchangers usually operate well below the critical point or well above the criconbar, to avoid the uncertainties and instabilities associated with a region where phases can appear and disappear.
In the supercritical region well above the criconbar the steam will behave like a liquid at low temperatures and like a vapor at higher temperatures, but there is no well defined boundary between these regions. Property packages such as Aspen Properties and ComThermo use liquid property calculation methods at low temperatures and vapor methods at higher temperatures, switching between the two at some arbitrary temperature. Calculated properties will be broadly correct, but there will be an abrupt change in quality (vapor mass fraction) that has no physical reality.
This can be handled in two ways. One is to change all the zero qualities to be unity (at all pressure levels), so the substance is treated by the EDR program as if it were a gas. Another is to specify additional temperature points in the region where the apparent liquid-gas transition occurs. These extra points will give increased accuracy in this region and reduce the size, and hence importance, of the physically unreal liquid-vapour transition region.
Adding extra points in and near this region can be achieved by
a. Input | Property Data | Hot/Cold Side Properties select "Specify points" for the Temperatures
b. The background colour of the Temperature will change in the Property table, where for the point you can over write the temperatures. Enter temperature points near the transition temperature.
c. Click on "Get Properties" where the property data will then be generated at the temperature points entered.
Using this method will minimize the "apparent" two phase region and also generate points near the critical temperature where the specific heat capacity can vary considerably with temperature.
Then in Input | Program Options | Methods/Correlations depending if the supercritical stream is being heated or cooled;
Heated: In vaporization tab, for "Subcooled boiling accounted for in", select "Not allowed for"
Cooled: In Condensation tab, for "Desuperheating heat transfer method", "Dry-wall"
A slightly more subtle procedure is first to "Get Properties", with a reduced number of points, say from 22 to 18. Then when you select "specify points" you can add new ones in the transition region on to the end of the table. This avoids the need to overwrite any existing points. There is no need for the points to be supplied in order of temperature, but if you find it convenient to see them in the correct order, you can cut and paste to move some if the temperature up and then add tie new temperature points in the gap created, before you perform a "Get Properties" for the selected temperatures.
Keywords: Wet wall desuperheat
References: None |
Problem Statement: What is the meaning of Results Warning 1923? | Solution: Warning 1923 means that the Reynolds number is less than 5 low Reynolds (Re) number for the cross flow in the shell side. This warning is based on the investigation done by the HTFS group where they found adverse effects in heat transfer due to poor shell side mixing. The conclusion of this analysis brought a correction factor in the RS 1195 (HTFS Research Network) corresponding to Re greater than 5. (For further information you can review the RS1195 on the HTFS Research Network http://htfs.aspentech.com/resnet/resreports/2007/rs1195.pdf , separate license is required)
You can monitor the crossflow which is the big responsible for this warning under Results -> Thermal / Hydraulic Summary -> Flow Analysis -> Flow Analysis tab. Then you will note that the cross flow fraction should be low ( this is only that small percentage of the total flow is flowing in the baffled region perpendicular to the tubes contributing to the heat transfer)
Keywords: Crossflow, baffle pitch, warning 1923
References: None |
Problem Statement: When I run the EDR file in simulation or rating mode, I get input warning 1107: The tube count from the tube layout differs from the effective tube count. | Solution: This warning is due to inconsistencies between the inputted number of tubes and the calculated number of tubes based on the bundle specifications. This can be fixed by navigating to Input | Exchanger Geometry | Geometry Summary and deleting the specified number of Tubes. The value will be automatically calculated based on the bundle geometry, and it will be displayed in red.
Keywords: Input Warning 1107, effective tube count, bundle
References: None |
Problem Statement: What’s the Configure Online Server? | Solution: It’s a utility designed for Aspen Process Controller (RTE) and Aspen Online Deployment (AOD). It’s NOT suggested to be used for configuration of traditional DMCplus, IQ and Nonlinear controllers.
The Configure Online Server dialog box enables you to:
- Set up the current machine as an Aspen Process Controller (RTE) online server, running deployed Aspen Process Controller applications.
- Configure the quantity and intervals at which application snapshots and history data are stored on the server.
- Configure the security roles and permissions for the users who access the server or the online applications and data that are hosted on the server.
- Identify one or more input / output (IO) sources that can interface between the online applications, which are residing on the current server, and the plant distributed control systems (DCS).
For additional information of Aspen Online Deployment configuration, please refer to solution 138269 How do I configure Aspen Production Control Web Server to display an Aspen Online Deployment application?.
Keywords: Configure Online Server, Aspen Process Controller, Aspen Online Deployment
References: None |
Problem Statement: Is there a legend for the internal parts shown in the tubesheet layout? | Solution: While there is no separate documentation of how the items are drawn, you can see the item in the drawing. You can display the items in red by selecting the item category on the top of the window and the click the corresponding column on the bottom of the window as illustrated on the screen capture.
1. Navigate to Results, Mechanical Summary, Setting Plan, Tubesheet Layout
2. Select the item from the pull down list on top of the window
3. Click the items you want to highlights from the table below the drawing
4. The items are displayed in red on the drawing
A list is present in Help under Shell and Tube Results, Mechanical Summary, Tubesheet layout.
The tube layout diagram includes the following data:
· Shell Side Inlet and Outlet Nozzles
· Shell Cylinder (Shell Kettle Cylinder - if K Shell)
· Tube Locations
· Pass Partition Lanes
· Baffles
· Tie Rods
· Impingement Plate
· Sealing Strips
· Bundle Runners
· Longitudinal Baffle
· Pass Partition Lane Sealing Strips
The following tables can be selected to view the data associated which each item:
· Bundle Limits
· Pass Regions
· Nozzles
· Baffles
· Tie Rods
· Tube Lines
· Impingement Plate
· Sealing Strips
· Bundle Runners
· Longitudinal Baffle
· Pass Partition Lane Sealing Strips
Keywords: drawing
References: None |
Problem Statement: Why are there different values for overall tube length using Aspen Shell & Tube Exchanger vs. Shell & Tube Mechanical? | Solution: The reason that the setting plans are different in the two programs is that- currently, the default calculations for exchanger geometry lengths are different in thermal and mechanical. So as a result, under some circumstances, geometric dimensions will not be identical in both programs, for example-when the mechanical constraints dictate different dimensions. But in the absence of those constraints, the dimensions should be identical.
It is advised to use the mechanical results for fabrication, after both thermal and mechanical have been successfully run.
Note: If you make changes to the dimensions in Shell and Tube Mechanical, it is strongly recommended to re-run the case in thermal again. This is to ensure that the final/updated geometry is still capable of handling the required heat duty.
Keywords: Setting plan layout, Shell and Tube, Shell and Tube Mechanical, EDR, geometry, results
References: None |
Problem Statement: In the Aspen Exchanger Design and Rating "Optimization Path", what is the difference between OK and (OK) between brackets? | Solution: Aspen Exchanger Design and Rating searches to find a design that satisfies the following:
1. Enough surface area to do the desired heat transfer (Area Ratio (AR) >= 1). Area Ratio is the ratio of calculated surface area to required surface area for the desired heat transfer.
2. Pressure drops (at both shell and tube sides) meet constraints (Pressure drop Ratio (PR) ≤ 1). Pressure drop Ratio is the ratio of the calculated pressure drop to allowable pressure drop.
3. Physical size within acceptable limits
4. Velocities within an acceptable range
5. Mechanically sound and practical to construct
The “Design Status� in the optimization path for each selected design will be marked as “OK�, “(OK)�, or “Near� based on the following criteria:
1. The design is OK, if the AR ≥ 1, PR ≤ 1, and it meets TEMA unsupported length or nozzle rho-V-squared limits.
2. The design is (OK), if the Area Ratio ≥ 1 and the Pressure Ratio ≤ 1, but it fails to meet TEMA unsupported length or nozzle rho-V-squared limits.
3. The design is Near, if 0.8 ≤ Area Ratio < 1 and 1 < Pressure Ratio ≤ 1.5.
Keywords: Optimization path, Design, Shell & Tube, Area Ratio, Pressure drop Ratio, OK, Near
References: None |
Problem Statement: Are there built-in in kinetics for the thermal decomposition of a polymer for recycling applications? | Solution: Segment-based kinetics can be used to simulate the reaction steps involved for thermal decomposition or de-polymerization. For this purpose, we need to know the relative amount of different segments and monomers present in the bulk polymer. Once that is determined, we may write the key reaction sets with appropriate parameters (pre-exponential factors and activation energy). For example, the key reactions may be:
1. Polymer > Segment 1 + Segment 2
2. Segment 1 > Monomers; Segment 2 > Monomers
Key Words
Polymer, Recycling, Segment, Monomer
Keywords: None
References: None |
Problem Statement: What are XDEF Variables? | Solution: XDEF variables are created to establish the connection between calculator block and other unit operation variables. The links are known as connection equations which cause the two EO variables to be equal at solution. If we look at following EO variables (in the picture below this sentence), the connection equation for these two variables is:
CALC.XDEF.BTMS_TEMP - COLUMN.BTMS.STR.TEMP = 0
Key words
Calculator, EO
Keywords: None
References: None |
Problem Statement: User of Aspen Plus can further rigorously design/rating the heat exchanger in Aspen Plus process simulation through the integration of Aspen Exchanger Design & Rating program (EDR). | Solution: To integrate EDR into Aspen Plus, HeatX model in Aspen Plus should be used to simulate the heat exchanger.
Procedures below show how EDR will work in Aspen Plus.
1. Select HeatX model in Aspen Plus to simulate heat exchanger under Shortcut/Detailed method (Or select the existing HeatX model in process flowsheet which running in Shortcut/Detailed method). Aspen Plus simulation must need to RUN first before proceed to the next step.
2. Select Rigorous calculation method instead of previous Shortcut/Detailed method. Then decide type of calculation (either Design/Rating/Simulation) as per screenshot below: (Design mode will create new EDR file while Rating or Simulation type will need to have existing EDR with geometries information. More detail of calculation type, please refer Help file)
3. Once changed the calculation mode from shortcut to Rigorous, the left hand side navigation pane will showing “EDR Options� in RED. Go to this section and key in the file name for the EDR file that going to create by Aspen Plus if a new heat exchanger is going to create with Design mode. Or existing EDR file can be browsed here to integrate with Aspen Plus.
4. When typed in new name (create new heat exchanger) to create new EDR file for this HeatX model, after RUN Aspen Plus, a warning message that telling Aspen Plus couldn't found this file and new file with this name will be created. There is nothing need to worry as the warning message will be gone in next RUN.
5. If the following error message has been found when open up the EDR Browser, there are a few possible causes.
· It can be user has copied the Aspen Plus file into another folder (or other machine) without copying the EDR together and put in the same folder as Aspen Plus file.
· The simulation in Aspen Plus has never RUN yet, the link between Aspen Plus and EDR has not been establish. Reinitialize and RUN the simulation will fix this issue.
6. The results of the EDR can be directly view in Aspen Plus Navigation Pane as per screenshot (left circle) or inside EDR Browser Results summary.
Additional Notes:
1. Once any changes has been done in EDR browser eg. Geometry, it is recommended to Reinitialize the simulation before RUN to make sure the newly changes is counted.
2. The newly created EDR file under Design mode will be placed at the same folder as the Aspen Plus file. If a new Aspen Plus simulation is created from scratch, please do save the Aspen Plus file first before create the new EDR file using Design mode to make sure Aspen Plus program place the newly created EDR file at the same folder as the Aspen Plus file.
3. If existing EDR file are going to integrate with the Aspen Plus simulation, the EDR file should be copied in the same folder as the Aspen Plus simulation file.
4. The EDR file created through the integration can be individually open in Aspen Exchanger Design & Rating program.
Keywords: Aspen Plus, Aspen Shell & Tube Exchanger, EDR, Aspen Exchanger Design & Rating, Aspen Aircooled Exchanger, Aspen Plate Exchanger, HeatX, Heat Exchanger, Design
References: None |
Problem Statement: When defining non-conventional components in the component list, for example when simulating Biomass cases, it is often observed that NC Solid tab in the Stream Definition Form does not become active even though the stream class MIXCINC or MIXNC is selected in the Setup Folder>Specification>Stream Class Drop down list. What could be the reason for this? | Solution: In order to avoid this issue, the user should include a solid component in the components list. An example can be COAL defined as a Solid under the 'Type' column definition drop down list. Once completed the NC Solid and CI Solid tabs will become active in the simulation environment. Enter the values for flow and composition on the NC tab only and the CI Solid stream tab will become inactive. An illustration of this is described in the attached example file.
Keywords: Non-conventional components, MIXCINC, MIXNC
References: None |
Problem Statement: Error "Unable to load simulation engine, Probable cause: Insufficient disk space or memory" when launching Aspen Plus. | Solution: This error may be seen when you have a 3rd Party Software name "KEYLOK" is installed on your computer, which shares a common component, ppmon.dll, and causes this issue.
To resolve, please follow these steps:
1. Go to C:\Windows\System32 and rename ppmon.dll and ppmon.exe
2. Go to C:\Windows\SysWOW64 and renamed ppmon.dll and ppmon.exe.
3. Launch Aspen Plus to verify steps 2 and 3 resolved the problem.
Note: Renaming the above files will not affect the KEYLOK license software.
Keywords: Memory low
Disk space
Insufficient
Load simulation engine
Aspen Plus
Launch
KEYLOK
References: None |
Problem Statement: What error messages will I receive in Aspen Process Explorer V8.x if it loses connection to the license server? | Solution: Note: for information about the different licensing states that impact the functionality of Aspen Process Explorer, please refer to KB article 139163.
This Knowledge Base article describes the behavior of Aspen Process Explorer when the connection to the License Server is lost, and shows the error and warning messages that can be seen depending on the licensing state.
If Aspen Process Explorer loses its connection to the license server, the following will occur:
· Initially enter into a license time out period for 15 hours and Aspen Process Explorer will continue to function.
· If the connection to the license server has not been re-established within the 15 hours, then Aspen Process Explorer will enter into a 10 day grace period. The application will continue to function.
· Once the 10 day grace period is over, Aspen Process Explorer will no longer function, unless it has been reconnected to the license server.
At any point during the license time out period or the grace period the connection to the license server has been re-established, the license for Aspen Process Explorer will continue to be checked out until Aspen Process Explorer has been closed. Once Aspen Process Explorer has been closed, the license will be returned to the license server.
Below are screenshots of Aspen Process Explorer’s license behavior after losing the connection to the license server.
Aspen Process Explorer has lost connection to the license server (Double-click the icon in the lower left corner).
Aspen Process Explorer has entered into the 15 hour license time out period (hover over the icon in the lower left corner).
Aspen Process Explorer has entered into the 10 day grace period (hover over the icon in the lower left corner).
Aspen Process Explorer is still using the license while in the license time out period and grace period (Click the Aspen Process Explorer File button and select Process Explorer Options > About > Licensing Information).
Keywords: Process Explorer, PE, license time out period, license grace period
References: None |
Problem Statement: How can I modify the significant digits in the heat exchanger output in the performance tables? | Solution: Formats defined in the Preferences file will not affect the Performance Tables in the Heat exchanger datablock.
Therefore if you want to increase the number of significant figures in a unit operation property report you need to make some changes in the .rdf file associated to that unit operation.
You will find the heatexch.rdf file at the following location (we would suggest you also saving a copy of this file before you proceed):
C:\Program Files (x86)\AspenTech\Aspen HYSYS VX.X4\Support folder with this new file.
Following are the instructions to modify the file:
1. Go to C:\Program Files\AspenTech\Aspen HYSYS xxxx.y\Support
2. Make a copy of heatexc.rdf file and save it in some other location, if you want to revert these changes in future.
3. Now open the heatexch.rdf file using note Wordpad or Notepad.
4. Go to "Performance Datablock Contents"
5. Then go to each phase property and change "Format "%.2f"" to "Format "%.4f"" to give 4 significant figures. You can put any number you want.
6. See below as an example to vapor density:
NumberField TableSSVapDensity
Size 12 1
Label Centre "Density;"
Units WithLabel
Moniker ":MassDensity.300.1.[]"
Format "%.4f"
HideModifyState
Shade 10
ShadeLabelOnly
End
Keywords: significant digits, rdf file
References: None |
Problem Statement: Is it possible to add a new solvent for the NRTL-SAC model to investigate solid solubility issues with Aspen Solubility Modeler? | Solution: It is not possible for the user to modify the template files delivered in the Aspen Solubility Modeler files, as the regression spreadsheet is protected with a password and the variables used in the calculation spreadsheet are not formally documented.
However it is possible to proceed with Aspen Properties (or Aspen Plus) user interface directly. The purpose of the excel spreadsheet delivered as Aspen Solubility Modeler is to make very easy to perform the regression of solid solubility data and investigate solubility using the NRTL-SAC model. If you are familiar with Aspen Plus or Aspen Properties you can replicate the same calculations using the application directly.
The file nrtl-sac-new-solvent.aprbkp can be used to learn the procedure. The idea is to first make sure all the pure component parameters are available for the new solvent. This can be achieved in various ways (experimental data, estimation from the molecular structure, critical analysis of the relevance of the parameters). In this file, the component SOLVENT is assumed to be unavailable in the databank (we use the data of toluene to make the example realistic). The important parameters are MW (molecular mass) and PLXANT (saturation pressure). The other parameters are given dummy values to allow the calculations to complete (density and enthalpy will be incorrect but this is not relevant for the investigation of solid solubility). For the regression of saturation pressure parameter PLXANT (extended Antoine equation) you need experimental saturation pressure as a function of the temperature. This is specified in the data set D-6 (it was generated using toluene saturation pressure). You need a least 3 data points (more is better). The regression case DR-1 is used to regress PLXANT/1, PLXANT/2 and PLXANT/3 (this is the typical set of parameters to get a reasonable saturation pressure model). Actually the saturation pressure is not needed for the solid solubility investigation, but it is required to be able to characterize the solvent with the NRTL-SAC attributes X, Y+, Y- and Z.
To find the NRTL-SAC attributes X, Y+, Y- and Z values, the essence of the work is similar to the solid solubility investigation. You need vapor-liquid or liquid-liquid experimental data with binary mixture with the solvent and other solvents for which NRTL-SAC parameters are already available (make sure to select NRTL-SAC databank in the component specification form). In this example we have copied experimental data using the NIST database without a critical selection of the data set, as this example is only for illustrating the work flow. We have selected an hydrophile solvent (water), an hydrophobic solvent (n-hexane), some polar solvents (DMSO, DMF) and methanol (more solvents would be better but it is critical you select solvents of the 4 different natures, it is not useful for example to have only solvents in the same family (e.g. adding nC7, nC8 would have little impact). The data sets D-1 to D-5 contains those data (for the LLE dataset toluene/water, we have combined two experimental data sets as you must always specify liquid 1 and liquid 2 compositions otherwise regression fails even if the data set seems complete. For vapor-liquid experimental data, it is better to have both liquid and vapor composition, but if vapor composition is missing regression may proceed correctly). The regression case DR-2 (which will be run after DR-1) is specified to use those binary data, and regress the t-dependent parameter XYZE.
The values found are quite close to the databank values XYZE of toluene. The databank has been regressed more carefully and the databank values should be used when available.
You can then turn the simulation to property analysis or use Aspen Plus sensitivity analysis block with a heater to work out solubility (assuming you have regressed the NRTL-SAC parameters for your solid already). You can also use the Excel Aspen Properties add-ins to set up your own calculation (the principle of the calculation spreadsheet is to use the Flash function with an excess of solid to ensure saturation).
Finally if you are prepared to take the risk, you could replace one of the solvents from the 130 solvent file delivered with NRTL-SAC folder with your own solvent if you wish to use the regression or the calculation spreadsheet. Make sure to properly document your change to avoid confusion. Customization of the calculation or regression spreadsheet is not supported.
Keywords: solid, solubility, ASM, Aspen Solubility Modeler, NRTL-SAC
References: None |
Problem Statement: When you export an adiabatic valve specified in Aspen Plus with the option "Adiabatic flash for specified outlet pressure (pressure changer)" to Aspen Plus Dynamics, the valve is specified at arbitrary position of 50% and a valve coefficient C0max is calculated based on pressure drop and flow rate. What is the relation between C0max of simple valve and industry standard Kv valve coefficient? | Solution: Let's first set the definition of Kv, the flow factor. The definition in metric units is:
Kv = Q * sqrt(rho/1000 * 1 / dp)
where
Q = flowrate in m3/hr
rho = density in kg/m3
dp = pressure drop in valve in bar
Kv relates to C0max in the simple valve model with the following equation:
C0max = sqrt(2000) / (position/100) * Kv
The factor 2000 comes from the 1000 in the Kv definition and the factor 2 in the pressure drop equation in Dynamics. You need to specify the position (probably this will be 100%, in which case the formula is C0max = sqrt(2000) * Kv.
For the units of C0max you must select "m1.5 kg0.5/hr/bar0.5" (Metrics).
You can view the equations being used in the Valve model in Aspen Plus Dynamics on-line help or with the option "View Active Model" on a block.
// pressure drop
out_p_P = In_F.P - P_drop; // need the sign of P_drop (if we use "P_o = P - P_drop" then P_drop is always +ve)
// simple pressure/flow relation
F * Mw * 2/C0max = C0max*(PosA/100)^2 * Pdropc * Rhos / (abs(F)+eps);
C0*100 = C0max*PosA;
F = Fvol*Rhos;
The conversion formula can be obtained by identifying the terms used in the equation with the original definition of Kv.
When you specify the valve coefficient CV in Aspen Plus, this will be exported as a rigorous valve. In this case the industry standard definition of valve coefficient is used (we use the calculation method described by the ISA publication). Roughly speaking, a CV of 1 gives a pressure drop of 1 psi for a flowrate of 1 gallon/min (there are further correction factors for compressible flow, etc).
Kv = 0.865 * CV
The attached example shows VALVE1 specified with 1 m3/hr as feed, 1 bar as pressure drop with water at 25C. VALVE2 is 1 gal/min, 1 psi pressure drop, CV=100. This evaluates the position (using linear characteristic) of 1 (which is exactly how CV is defined). VALVE1X is using the same feed conditions as VALVE2, but uses the "simple valve" model. The following equations have been added to the flowsheet constraints to show the relation between Kv, CV and C0max.
CONSTRAINTS
// Flowsheet variables and equations...
Kv as realvariable;
Kv = streams("FEED1X").Fv * sqrt(streams("FEED1X").Rhom/1000/blocks("VALVE1X").pdropc);
Kv1 as realvariable;
Kv1 * sqrt(2000) / (blocks("VALVE1X").pos/100) = blocks("VALVE1X").C0max;
Cv as realvariable;
Kv = Cv * 0.865;
END
The Cv calculated from these expression is 1, which demonstrates the conversion is correct.
Keywords: valve, C0max, Kv, CV, ISA
References: None |
Problem Statement: Does Aspen HYSYS calculate the Acceleration Pressure Drop for single phase flows in a pipe segment? | Solution: For single phase streams, Aspen HYSYS uses the Darcy equation for pressure drop predictions. This equation is a modified form of the mechanical energy equation, which takes into account losses due to frictional effects as well as changes in potential energy.
The acceleration term (acceleration dP and acceleration gradient) is always zero for single phase flow in the Aspen HYSYS pipe segment since the Darcy friction factor is used in calculating the friction pressure gradient.
Keywords: Acceleration Pressure Drop, Acceleration gradient, Single phase, Pipe segment, Darcy equation
References: None |
Problem Statement: Is it possible to copy streams and unit operations from the main flowsheet into a Hydraulics sub flowsheet? | Solution: Copying a stream or unit operation from the main flowsheet to paste in Hydraulics sub flowsheet is not a supported function in Aspen HYSYS.
THe Hydraulics sub flowsheet has its own unit operations palette. It only supports specific unit operations. For streams, those available in the hydraulics sub flowsheet are different from streams on the Main flowsheet.
Therefore, a user cannot copy items from the Main flowsheet to paste in the Hydraulics sub flowsheet.
The same rule applies to copying from Main flowsheet into the Column subflowsheet.
The work around for copying streams from the Main flowsheet to a Sub flowsheet is to create a connection between the stream on the Main flowsheet and a stream in the Hydraulics subflowsheet. This will then transfer across the appropriate data like composition, pressure, temperature etc.Â
For unit operations, users have to use those available on the sub flowsheet palette.
Keywords: Hydraulics, Sub flowsheet, Main flowsheet , Column subflowsheet
References: None |
Problem Statement: Aspen Properties in Aspen HYSYS does not launch in Windows 8. | Solution: When Aspen Properties is added in HYSYSÂ the data is written in a temporary folder. If this folder is Read Only then the users may not be able to add Aspen Properties in HYSYS. The solution will be to launch HYSYS with an administrator.
Right mouse click on Aspen HYSYS and then select Run As Administrator.
Keywords: Windows 8, Aspen Properties, Aspen HYSYS
References: None |
Problem Statement: How do I find the stream using the "select object" operation? | Solution: When you right-click on the PFD and pick "select object" to search for a specific stream/unit operation, only the streams and unit operation that are visible appear in the list. If the stream/unit operation is hidden, you won't see it in the list. To see it: right click on the PFD=>Reveal hidden objects=>choose the desired stream and click Ok. Now if you pick "select object'; it should appear in the list.
Keywords:
References: None |
Problem Statement: I am unable to gain access to the internet version of Aspen Process Manuals. Can you please tell me the reason for this even though I have a valid support account and have supplied the correct log in credentials? | Solution: Aspen Internet process manual is available only for universities and customers who are doing an online evaluation.
Current commercial customers will need to set up this manual as an intranet version which is hosted internally by the company. Information on how to install and configure the intranet version of Aspen Process Manual can be found on our support site:
https://support.aspentech.com
From the left navigation pane select > Documentation folder and select product: Aspen Process Manual.
Information about the installation and configuration of Aspen Process Manual V8.6 is available in manual:
aspenONE V8.6 Engineering Installation Guide, chapter 4 Individual Product Installation Notes and section Aspen Process Manual Installation Notes (page 69)
https://support.aspentech.com/CustomerSupport/Documentation/V8.6/aspenONE%20Engineering/Aspen%20Engineering%20General/AspenEngineeringSuiteV8_6-Inst.pdf
Keywords: Aspen Process Manual, Internet, Intranet
References: None |
Problem Statement: How can I specify two vapour relief valves in the depressuring utility? | Solution: Provided you are not interested in the liquid flow from the vessel, you can use the liquid valve as the second vapour valve by changing it's position. After setting up the depressuring utility;
- If you are using HYSYS 2006 or an earlier version, make sure you have turned on the Aspen Fidelity licence by going to the Simulation menu, click Integrator and select the Options tab on the window that appears.
- Click the "Access Fidelity License Options" Checkbox.
- Open the Depressuring utility Subflowsheet, where you then open the Vessel (Separator) window.
- Click on the Rating tab, then go to the Nozzles page.
- Under Nozzle Parameters, set the Elevation(% of Height) of the Liquid nozzle as 100%.
This moves the liquid nozzle to the top of the vessel, thereby converting the valve to a second vapour valve.
Keywords: depressuring, utility, vapour, relief, valve
References: None |
Problem Statement: Which is the license that I need to have in order to run Pipesys? | Solution: If your contract with AspenTech starts after October 31, 2010, AspenTech no longer offers the PIPESYS or OLGAS technologies from SPT Group as part of our aspenONE Engineering suite. Customers have to license either PIPESYS or OLGAS directly from SPT Group so you cannot check if the license exists in the Licence Profiler.
If you have an earlier contact with Aspen Tech and also have access to Pipesys or Olgas, their respectives licenses should be listed in the license profiler from Start menu> All programs> AspenTech> Common Utilites> License Profiler. After selecting the license file you need to check the presence and the expiration date of them. SLM_Extensions_OLGAS, SLM_Extensions_PIPESYS, SLM_HYSYS_OLGAS, SLM_HYSYS_OLGAS3P
For more information you can refer to the following solutions:
132181, 132660
Keywords: Pipesys, license
References: None |
Problem Statement: How to add critical properties to the work table? | Solution: You can add the critical properties of the streams you like in once table on the flow sheet.Below are the steps to do so;
1. Home Ribbon- Right side –Stream Analysis- Select Critical Properties.
2. Select Process Stream-
3. Then on the left navigation panel, go to the stream analysis and you should be able to view the critical properties-stream
4. Then go to the Data Tables- Add-Variable Navigator
5. On the Variable Navigator, left corner you should select analysis from the navigator scope.
6. Next, select object and variable. Then click place on flowsheet for a table on the flowsheet with the critical properties.
Keywords: Critical properties, worktable
References: None |
Problem Statement: Steam Ejector Extension Unit Operation for Aspen HYSYS with Aspen Properties. | Solution: Use the attached Ejector-V71.zip file for Aspen HYSYS version V7.1.
Use the attached Ejector-V72.zip file for Aspen HYSYS version V7.2.
Please note that the ejector extension given in solution document 110065 does not work only when you use Aspen Properties with streams involved with ejector extension unit operation.
The extension provided with this document works with HYSYS components as well.
Note: This Automation application has been created by AspenTech as an example of what can be achieved through the object architecture of HYSYS. This application is provided for academic purposes only and as such is not subject to the quality and support procedures of officially released AspenTech products. Users are strongly encouraged to check performance and results carefully and, by downloading and using, agree to assume all risk related to the use of this example. We invite any feedback through the normal support channel at [email protected].
Keywords: ejector, extension, Aspen Properties.
References: None |
Problem Statement: 在HYSYS管道模型中怎样计算滞涩流物性 | Solution: 请查看附件，其中对在HYSYS管道模型中怎样计算滞涩流物性有详细的介绍。
注意事项
您可以在以下两个地方看流场信息：
a. On the Performance Tab (of Pipe) ll Slug Results page ll Status column;
b. On the Performance Tab (of Pipe) ll Profiles Page ll View Profile button ll Flow Regime column
如果用户在Design|Parameters 页面修改了关联方法，而且如果关联方法使用了流场图，那么不同的流场就可以看到。例如，如果用户选择了Duns & Ros，那么简况中的这一列（如b所说的）就会变为滞流。
Performance|Slug Results页的状态列（如a所说的）不是被关联方法（Design|Parameters）预测的流场。这个流场是由设计的计算方法预测的，在Slug Option标签页中。这是一个从压降计算方法分离出的稳定计算方法。
Keywords: 滞流,管段模型,CN-
References: None |
Problem Statement: How to change the display icon of the column after user customizes in the sub-flowsheet? | Solution: 1. Right click the column and pick "change icon" button.
2. Choose the proper icon from different types of columns.
Keywords: Change display icon, Customization
References: None |
Problem Statement: I would like to perform Design Specs calculations as in Aspen Plus for manipulating a specified input variable to achieve a particular value of a flowsheet calculated variable. How do I do that in Aspen HYSYS? | Solution: In Aspen HYSYS steady state the equivalent to the Design Specs of Aspen Plus is the Adjust block.
An Adjust block is one of the available logical unit operations in Aspen HYSYS however this is not available in Aspen HYSYS Dynamics as logical unit operations are not supported instead PID controllers are used.
The Adjust block manipulates the value of one variable (independent variable or adjusted variable) to meet a required value in another variable (dependent variable or target variable). It uses mathematical algorithms to find the target value.
Keywords: Aspen Plus, Design Specs, Adjust block, Aspen HYSYS
References: None |
Problem Statement: What is Column Component Recovery specification? Is it a ratio spec? | Solution: Yes, this is a ratio specification. The spec is the molar, mass, or volume flow of a component (or group of components) in any internal or product stream draw divided by the flow of that component (or group) in the combined tower feeds. As the recovery is a ratio between two flows, you specify a fractional value. Also, there is no need to specify a flow basis since this is a ratio of the same component between specified streams and the combined tower feeds.
If you want to read more about this specification or check the definition of other specs please look for “Column Specifications List” into the Aspen HYSYS On-Line Help.
Keywords: HYSYS Column, Specifications details, Component Recovery, On-Line Help.
References: None |
Problem Statement: Are the "Exposed" and "Wetted" areas in the Safety analysis forced to be the same? | Solution: No, they aren't supposed to be the same.
Let's refer to the PDF contained in solution 140064 related to the Fire Overpressure Analysis inside Safety Analysis. If you refer to Fig 41, you will see an Exposed area and if you continue looking you will see under Fig 45. A Wetted surface area different than the Exposed area reported in Fig 41. The difference comes from the calculation method.
The calculation method assumes that the "
Keywords: Exposed, wetted, area, safety analysis
References: Stream" selected by the user represents the feed to the vessel at normal operating conditions (which are specified on the Equipment tab).
Then, the reference stream is brought up to relieving pressure via a constant bulk-density flash1. At relieving T and P, the liquid volume is often significantly different from operating conditions. The Exposed Area on the main page (Fig 41) represents the wetted area at normal operating conditions, whilst the one in the flash table (Fig 45) represents the wetted area at relieving conditions, so, they could be different. |
Problem Statement: How to change the text/title from multiple lines to one line?
Before adjustment, the title looks like this.
After adjustment, the title looks like this. | Solution: Users can use "size mode" under flowsheet/modify tab to drag and size the text.
Keywords: Size, Multiple lines, Title
References: None |
Problem Statement: I am unable to delete a fluid package even though it is not used anywhere. How can I fix this problem? | Solution: The first step is to ensure that the fluid package which you wish to delete is not being used anywhere.
1. In the Simulation environment, go to the Home tab. Ensure that the solver is set to On Hold. Click on Fluid Package Associations.
2. Ensure that the fluid package which you are trying to delete is not being used in any of the flowsheets. If they are, change them out.
3. On the left hand Navigation pane, click on the Workbook form and navigate to the Workbook tab.
4. Ensure that the box labeled Show Subflowsheet Objects is unchecked.
5. Click on Order/Hide/Reveal located just under Show Subflowsheet Objects. Ensure that no streams are being hidden.
6. At the bottom right hand side of the Workbook, select the fluid package which you want to delete from the Fluid Pkg drop down. In this case, we are trying to delete FPkg1. This will filter the streams to only show the streams using FPkg1 as the fluid package.
7. View the streams in the Workbook. If there are no streams showing, you have ensured that the fluid package you are trying to delete is no longer being used in the flowsheet. If there are still streams using this fluid package, go to them in the flowsheet and change their fluid packages.
8. Switch the solver back to Active.
9. Go back to the Properties environment and attempt to delete the fluid package.
In V8.6 and earlier, you may get this warning message when you try to delete the fluid package.
In steps 1 through 7, we verified that the fluid package is no longer being used. However, the program still thinks the fluid package is being somewhere used because it is still written in the memory. This is a defect that was fixed in V8.8 (see solution ID 145017).
If you are using V8.6 or an older version, the workaround is to save the file, close out of HYSYS, then reopen the file. It may also be necessary to re-run the file. This can be done by ignoring a block and then un-ignoring it, which will trigger the solver and cause it to re-solve. This will purge the memory and allow you to delete the fluid package.
Keywords: Fluid package delete
References: None |
Problem Statement: How do I increase the font size of the labels on the PFD? | Solution: -
We can find this option in ribbon bar Format tab .
The steps are as follows:
1. Select the label you want to format. In this example it is CondDuty.
2. In the Ribbon bar, go to the Format tab
3. Here you have option to increase or decrease font size. In the following example, I increased the CondDuty Size to 22.
Keywords: Font Size, PFD, Format, Ribbon
References: None |
Problem Statement: Is there a way to use HSR in my physical computer with Aspen HYSYS installed in a remote application? | Solution: You cannot run Hysys Stream Reporter in your actual computer while running Aspen HYSYS in a server. HSR is a prebuilt macro that works by pulling out the stream properties by using it's corresponding HYSYS type library which is included which will be in the computer if HYSYS is installed.
Still, there are some options you can follow:
1. Run HYSYS and HSR in the same environment,
2. Build your own macro to connect HYSYS in the remote application
3. You can use ASW that actually has a remote execution. For more information on how to use Aspen Simulation Workbook please refer to solution 138913
Keywords: HSR, Remote execution, ASW
Â
References: None |
Problem Statement: The standard method that Aspen HYSYS uses to calculate flash point in the Cold Properties Utility is API procedure 2B7.1. The same method is used in stream properties (from correlation manager in Refsys) to estimate the flash point. However, the results of these two scenarios are different. | Solution: The Flash Point Correlation property and the Cold Properties Utility are both using the same correlation to estimate the flash point, the API 2B7.1 method. However, the D86_10% temp which is used into the correlation is differing in the two scenarios. The correlation property is using the more recent Refsys estimation methods to calculate the D86_10%, but the Cold Property Utility is using the legacy estimation methods for the same. Since fixing the legacy code in Cold Property Utility is time consuming and is not recommended, we always recommend user to use Refsys correlations to get the cold property estimates.
Keywords: Flash point, Cold Properties Utility, correlation manager
References: None |
Problem Statement: What is difference between partial, total and reflux column condenser type in Aspen HYSYS? | Solution: • Partial condenser: Has both vapour (vent gas) overhead product and distillate (liquid) draw. This will increase the required number of DOF specification by 2 over a base case of just an absorber column.
• Full Reflux condenser: All liquid from the overhead receiver is refluxed back to the column. There is only vapor (vent gas) overhead product from the reflux drum condenser and no liquid (distillate) draw. Only one additional DOF specification is required.
• Total condenser: All products are condensed into liquid. The condenser will have only distillate but no vapour overhead draw. Only one additional specification is required.
Keywords: Partial,Total, Reflux, Condenser type, Distillate, Vent gas
References: None |
Problem Statement: Is it possible to define selective conditions for activating HYSYS tabular properties? For example, could I use tabular properties for only a set of pressures and for the rest of the conditions the default methods? | Solution: This is not possible because once a Tabular Property is active, the parameters will be regressed to match data and will be used for the entire simulation with that property package.
Particularly when dealing with Enthalpy related properties, the entire envelope curve changes in order to fit the input data.
NOTE- As solution 118369 mentions, for Enthalpy related properties two of the three properties available must be active to allow the simulator to match parameters. Having the three activated will also cause errors in the results as the regression will be over specified. It is strongly recommended to have data for the two activated properties as having two active but only one set of data will cause inconsistencies in the regressed parameters
Keywords: Tabular properties, Enthalpy, Regress parameters
References: None |
Problem Statement: æ€Žæ ·å°†Aspen Properties/Aspen Plus文件导入到Hysysä¸ | Solution: 自HYSYS V7.0 以æ�¥ï¼Œç‰©æ€§åŒ…和二元交互å�‚æ•°å°±å�¯ä»¥ç‹¬ç«‹çš„导入到HYSYSä¸ï¼ˆä¸�包括PFD）
导入æ¥éª¤å¦‚下：
1. 建立一个新文件；
2. 在Fluid Package æ ‡ç¾é¡µé�¢ï¼›
3. 点击Import按钮；
4. 在文件类型ä¸é€‰æ‹©Aspen Properties文件类型
注�事项
1. å½“ä½ åœ¨HYSYSä¸ä½¿ç”¨Aspen Propertiesæ—¶ï¼Œä½ ä¸�需è¦�Aspen Properties的认è¯�许å�¯æ–‡ä»¶ã€‚åœ¨ä½ å®‰è£…Hysysçš„å�Œæ—¶ï¼ŒAspen Properties就会自动安装。这个功能仅在V7.0或是更早的版本有效；
2. å�ªæœ‰ç‰©æ€§ç›¸å…³çš„ä¿¡æ�¯ï¼ˆç‰©æ€§ç»„分，物性方法，用户定义的å�‚数，化å¦å��应）会被导入到HYSYS。æµ�è‚¡ä¿¡æ�¯ï¼Œæ¨¡å�—，物料图和PDF图ä¸�会被导入；
3. 为方便用户，å…�许å�Œæ—¶å¯¼å…¥.bkp å’Œ.aprbkp文件到Hysysä¸ã€‚
优点
在炼油和油气工业ä¸ï¼ŒHYSYS的用户å�¯ä»¥æ¨¡æ‹ŸåŒ–å¦åˆ¶å“�，è�¯å“�，è�šå�ˆç‰©å’Œç”µè§£è´¨ã€‚例如Aspen Plus有NRTL-Electrolyte物性包，以å‰�çš„HYSYS用户å�ªèƒ½é“¾æŽ¥ç¬¬ä¸‰æ–¹è½¯ä»¶OLI_Electrolyteæ�¥æ¨¡æ‹Ÿè¿™ä¸€ç³»ç»Ÿã€‚Aspen Propertieså�Œæ—¶ä¹Ÿæœ‰ä»ŽNISTæ•°æ�®åº“æ›´æ–°çš„çƒåŠ›å¦æ•°æ�®ã€‚
Keywords: Aspen Plus, Aspen Properties, 文件，模�文件，导入，�体，�体物性包, CN-
References: None |
Problem Statement: USGPM units not available for Actual Liquid Flow within Aspen HYSYS Stream Reporter. | Solution: The USGPM is not allowed because the list of conversions in HYSYS Stream Reporter can only be 255 characters long-conversions. After this length, they are truncated and placed as not selectable.
The USGPM conversion can be added to the Actual Liquid Flow list, you just have to do the following:
1. In the Stream Reporter (Excel), right-click on the name of the Setup tab and click "Unhide"
2. Select the "Settings" sheet and click "OK"
3. Click "GetPossibleUnits" so that the build for the visible units is updated with the currently linked version of HYSYS.
4. In column K locate "Actual Liquid Flow".
5. In the same row as "Actual Liquid Flow" in column M, add "USGPM" to the beginning of this list:
"USGPM,m3/h,m3/min,m3/s,..."
6. In the Setup sheet, clear the "Properties to report" section.
7. Re-select the desired properties to report and click "Use"
8. Click "Write Table"
The table should be written with "USGPM" for Actual Liquid Flow.
Keywords: USGPM, Stream Reporter, Actual Liquid Flow
References: None |
Problem Statement: Is there a way to use HSR in my physical computer with Aspen HYSYS installed in a remote application? | Solution: You cannot run Hysys Stream Reporter in your actual computer while running Aspen HYSYS in a server. HSR is a prebuilt macro that works by pulling out the stream properties by using it's corresponding HYSYS type library which is included which will be in the computer if HYSYS is installed.
Still, there are some options you can follow:
1. Run HYSYS and HSR in the same environment,
2. Build your own macro to connect HYSYS in the remote application
3. You can use ASW that actually has a remote execution. For more information on how to use Aspen Simulation Workbook please refer to solution 138913
Keywords: HSR, Remote execution, ASW
Â
References: None |
Problem Statement: The standard method that Aspen HYSYS uses to calculate flash point in the Cold Properties Utility is API procedure 2B7.1. The same method is used in stream properties (from correlation manager in Refsys) to estimate the flash point. However, the results of these two scenarios are different. | Solution: The Flash Point Correlation property and the Cold Properties Utility are both using the same correlation to estimate the flash point, the API 2B7.1 method. However, the D86_10% temp which is used into the correlation is differing in the two scenarios. The correlation property is using the more recent Refsys estimation methods to calculate the D86_10%, but the Cold Property Utility is using the legacy estimation methods for the same. Since fixing the legacy code in Cold Property Utility is time consuming and is not recommended, we always recommend user to use Refsys correlations to get the cold property estimates.
Keywords: Flash point, Cold Properties Utility, correlation manager
References: None |
Problem Statement: What is difference between partial, total and reflux column condenser type in Aspen HYSYS? | Solution: • Partial condenser: Has both vapour (vent gas) overhead product and distillate (liquid) draw. This will increase the required number of DOF specification by 2 over a base case of just an absorber column.
• Full Reflux condenser: All liquid from the overhead receiver is refluxed back to the column. There is only vapor (vent gas) overhead product from the reflux drum condenser and no liquid (distillate) draw. Only one additional DOF specification is required.
• Total condenser: All products are condensed into liquid. The condenser will have only distillate but no vapour overhead draw. Only one additional specification is required.
Keywords: Partial,Total, Reflux, Condenser type, Distillate, Vent gas
References: None |
Problem Statement: Does Aspen HYSYS have an option to include the wind/air speed into the Heat Loss Parameter for the Depressuring utility? | Solution: The convection part of the Detailed Heat Loss model assumes that the external ambient is air at atmospheric pressure and zero speed, and it’s not possible to modify this. The main reason for this is that the actual temperature of the "air" surrounding the vessel will depend on many things like: proximity of the flame, wind speed, ambient air temperature and orientation of the vessel, and HYSYS cannot take this into account. The only way to do this modeling correctly is to do a computational fluid dynamics (CFD) analysis.
Keywords: Depressuring, heat flux, heat loss parameters, air
References: None |
Problem Statement: How I can display in the strip-chart inlet/outlet vapour velocity for a pipe segment in dynamic mode. I tried using custom option to create the strip-chart but when I ran it vapour velocity, it is not shown on the chart. When I checked the historical data logger it is also empty. | Solution: The inlet/outlet vapour velocity for pipe segment applies only to the steady state model, and shows up as empty when in dynamics mode.
Steady state models slip, therefore you can get different vapor and liquid velocities. The pipe does not model slip in dynamics mode so it assumes that all phases are moving at the same velocity. This velocity is a different variable and is reported on the 'Performance' tab under the 'Holdup' plypicker selection. There is a velocity reported for each holdup, so if you want the inlet and outlet velocities, you would use the first and last holdup. Unfortunately these velocities are not available in the variable navigator, but you can drag and drop them from that page as a workaround. We are looking into adding them into the variable navigator. Note that these velocities are only used and are only valid in dynamics. If you switch back to steady state you'll want to use the inlet/outlet vapour/liquid velocities you mentioned earlier.
If you want to be able to model slip flow in dynamic environment, Aspen Hydraulics can do this
Keywords: Pipe segment, inlet vapour velocity, outlet vapour velocity, Aspen Hydraulics
References: None |
Problem Statement: How can I check the version and patch level of HYSYS? | Solution: If you would like to check the current version of Aspen HYSYS that you are using before installing any patches, or if you would like to know what patch level you have installed, then follow the steps mentioned below:
Step 1: Load the Aspen HYSYS application, which will be located in your start menu inside the AspenTech folder.
Step 2: Once the application has loaded you will then need to select “File” from the ribbon menu. Example shown below.
Step 2: Select “About”
Step 3: In this screenshot we can see the version number.
Below is the version breakdown, this structure will be the same for all versions:
Major
32
Minor
0
Revision
0
Build
8628
For example, if you apply CP1 your aspenONE HYSYS version will be V8.6 (32.0.1.8628)
We can see that the revision number will change.
Major: This release will have identifiable new features
Minor: This release will have existing feature improvements
Revision: This release contains bug fixes
Build: internal use for development
Please Note: Some patches do not change the version number. Make sure you check the knowledge base document of the patch to see if the version number will be changed.
Keywords: hysys version, build, about
References: None |
Problem Statement: How to prevent the warning, "Minimum tray residence time is smaller than 4 times the column integration step size". | Solution: When the calculated residence time number is below a certain number (four times the integrator step-size per the composition multiplier) then Aspen HYSYSÂ produces a warning message alerting the user that the dynamic transient calculations are not carried out rigorously enough.
To eliminate the warning you could:
1. Reduce the integrator step size
2. Change the execution rates to 1,2,2,4 or lower
Keywords: Minimum tray residence time, Column
References: None |
Problem Statement: What is the inlet stage convention adopted in Hysys column? | Solution: By default, the inlet streams entering a column in Hysys will be treated as on-stage convention. The following sequence is employed to establish the resulting internal product stream:
1) The entire component flow (liquid and vapour phases) of the feed stream is added to the component flow of the internal vapour and liquid phases entering the stage.
2) The total enthalpy (vapour and liquid phases) of the feed stream is added to the enthalpies of the internal vapour and liquid streams entering the stage.
3) HYSYS flashes the combined mixture based on the total enthalpy at the stage Pressure. The results of this process produce the conditions and composition of the vapour and liquid phases leaving the stage.
User can change to above-stage convention, where the vapor and liquid phases will be separated before entering the column. Thus, vapor will go to the stage above the inlet stage and liquid will go to stage same as the inlet stage number. To do this, user can check the “Split” checkbox under Flowsheet tab.
Keywords: On-stage, above-stage, inlet flow to column
References: None |
Problem Statement: Why do I see a "higher liquid inventory vaporizes" warning the in PSV Sizing & Depressuring Utility? | Solution: A higher liquid inventory only indicates a higher wetted area. With the API521 heat flux method, it would mean the heat transfer area is higher.
A higher liquid inventory also means a higher demand of sensible heat to heat the liquid inventory up to its bubble point so evaporation can begin. It could be a situation for higher liquid inventory case that before the vast of liquid phase begin to evaporate the vapour phase has been released enough by the vapour valve, so that the majority of the "liquid to vapour" flashing is not due to the liquid evaporation, but due to the declining trend of vapour pressure inside the vessel since the vapour valve is opened. In such a case, the higher liquid inventory case could have a smoother and more leveraged depressuring release process.
Keywords: API521 heat flux method, PSV sizing, Depressuring , Liquid Inventory, Wetted Area
References: None |
Problem Statement: I want to set the default PFD Table entries so I do not have to modify tables multiple times with the same variables. If you right click and select “Show Table” on a stream or unit operation, I want to immediately show the properties I have selected. | Solution: Go to File | Options | Simulation. Scroll down the Simulation Options window to the PFD Tables Content and Formats section.
Here you will find the available variables to display in the PFD tables for Material or Energy streams and Unit Operations.
Pick the desired entries and click on the OK button in order to keep the changes.
Keywords: PFD, table, options, formats
References: None |
Problem Statement: Why am I unable to register the Gas Quality Indicators extension? | Solution: In this knowledge base article we will be looking at how we can resolve the issue with registering this extension inside HYSYS.
The root cause of this issue is due to Administrator rights. Even if you have Administrator rights on your machine you still may have Microsoft Universal Access(UAC), which can restrict the application from performing certain tasks like registering extensions.
To resolve this issue you will need to do the following:
· Copy the extension files to the ‘Extensions' folder of Aspen HYSYS
· Right click on HYSYS V8.6 icon and then click on "Run as administrator"
· 64bit OS: C:\Program Files (x86)\AspenTech\Aspen HYSYS V8.6\Extensions
· 32bit OS: C:\Program Files\AspenTech\Aspen HYSYS V8.6\Extensions
· In the Customize Ribbon tab, choose ‘Register Extension'
· Search in the folder for the extension DLL file.
· Register the extension. Close Aspen HYSYS.
· Open Aspen HYSYS normally, you will find the Gas Quality extension in the Custom tab of the Model Palette.
Keywords: HYSYS V8.6
HYSYS extension fails
unable to register hysys extension
unable to register extension gas quality
gas quality extension
register
References: None |
Problem Statement: What is the definition of a "cell" with respect to a compressible gas pipe? | Solution: Cells represent the number of cells within the pipe (10-1000). When you are modeling multiple sections, faster and more stable convergence can be obtained if all cell sizes are similar. For a stable solution, the number of cells should be selected such that the following constraint is met:
The cells have to be sufficiently small to ensure that in any one time step there will be changes of sufficient magnitude in a sufficient number of cells to ensure that the solver used by the Compressible Gas pipe and the HYSYS dynamics pressure-flow solver interact correctly.
Keywords: compressible gas pipe, cells
References: None |
Problem Statement: When read xml file which is generated in a newer version of Aspen HYSYS (i.e. V8.6) is opened in an older version of Aspen HYSYS (i.e. V8.4), there is an error "This Beta - version case cannot be read by this version of HYSYS". | Solution: The reason why the xml file can't be opened with this error is because the case file contains extension unit operations object with invalid XML names. Please make sure the GUIDs of extension unit operation object used for naming begin with a letter or use a valid ProgID instead.
To avoid this error message:
1. Delete the extension unit operations of your case file in HYSYS V8.6
2. Save it as xml file
3. Open it in Aspen HYSYS V8.4 without any error
4. Add the extension unit operations deleted before in Aspen HYSYS V8.4.
However we usually don't recommend user to open the file created in a new version with the older version. New objects might be created in the new version (Hysys V8.6) which is not present in the old version and it would prevent opening of the file.
Keywords: XML, extension unit operation
References: None |
Problem Statement: How do I print documents from the documentation builder in Safety Analysis? | Solution: Although there is no menu option to print, you may still press "Ctrl - P" on the keyboard.
Keywords: Safety Analysis, documentation builder
References: None |
Problem Statement: How to generate a list of all the unit operations with their input process conditions in a table? | Solution: You can use Workbook to add a list of unit operations with the required process conditions.Below are the steps to do so,
1.Please go to the workbook on the home ribbon.
2.Then when you are on the workbook tab you can use setup for adding the equipment you want with the variables.
3.Then to add on the flowsheet, right click mouse and selected add workbook and then select what you want.
Keywords: workbook, unit operations, conditions
References: None |
Problem Statement: Missing PSV data with the following error message:
"The database file does not have an entry for this valve or scenario. This is most likely caused by opening the HYSYS case with a missing or inconsistent database file. It is recommended to re-open this case with the correct database file. To continue using this open case, then the valve or scenario should be deleted."
Why does that happen? How can we fix it? | Solution: In safety environment, Aspen HYSYS will generate both .hsc and .mdb file. HSC file is aim to carry all the regular simulation data and MDB file is to store all the data created in the safety environment. So if the information in the safety environment needs to be retained, the MDB file must be kept.
The easy way to avoid mistakes is to start saving as .hscz when user gets into the safety environment because it will keep hsc and mdb inside the file automatically.Â
However, if user still saves the file as .hsc and moves it without the MDB file, then the PSV data will be lost no matter what you do. Then user will occur the error message above.
One way to fix the problem is to find the MDB and then put in the same place (with the same name) as the HSC file. Aspen HYSYS will know what to do when opening.
Keywords: Safety Analysis, Missing Data, PSV
References: None |
Problem Statement: I have imported a template in my flowsheet but the fluid package in the imported template is different from the main-flowsheet. How do I change the fluid package for the template imported in the flowsheet? | Solution: The template inherits the fluid package used to create the template flowsheet. The user has the option to change the fluid package after importing this into the current simulation. The option is available in the Home page under Fluid Package Association as highlighted below.
The Fluid Package Manager will open when you click on Fluid Package Association.
The user can then change the fluid package (Basis-1) for the imported template to the fluid package used in the main simulation (GasPlant). In the above screenshot the template name is FLOW-1.
Keywords: Fluid Package Association, Fluid Package Manager
References: None |
Problem Statement: How do you get the CutYield% profile of a blend in the Petroleum Assay? | Solution: If user wants to blend assays in Petroleum assay, he has to blend the oil in the simulation environment using the Petroleum Feeder.
Â
Then get the output from the feeder which is a blend (Crude stream). From there, the user can save the output stream as assay.
Once it is saved, the blended assay will be available in the Properties Environment.
Keywords: Blend, Assay, Petroleum Assay, CutYield%
References: None |
Problem Statement: What does ‘Make FCC ready’ option for an assay mean? | Solution: The component list for FCC calculations requires a set of components. One way to add these necessary components to the list is to make the assay FCC ready.
When an assay is added, the component list generated does not contain the necessary components for FCC calculations. In order to add the missing components to the Component List, in the Properties environment, right-click the desired assay and select ‘Make FCC Ready’.
The attached document contains all the necessary components for th FCC.
Keywords: FCC, Make FCC Ready, Petroleum Assay, Component list
References: None |
Problem Statement: Petroleum-related properties appear incorrectly calculated in a stream resulting from blending in a mixer. | Solution: Incorrect calculation of stream properties from a mixer may occur if flow reversal is present, for example if negative flowrates are specified or calculated. In this case, splitting of a stream with unknown properties into two defined streams is being modeled. While a number of properties are well-calculated in this case, some of them (particularly related with petroleum) are not. For example, two streams with well-defined values of RON (research octane number) on one side of the mixer block, yield a single stream with RON =0 on the other side. The software does not display a warning or error message in these cases, and the user needs to take flow direction into consideration. Properties where this is observed include:
RON Clear
Cloud Point
Aniline Point
TBP for all percentages.
Curiously, values for MON are correctly predicted, and the problem is not extended to other blocks. For example, the case where flow reversal occurs over a splitter (Tee) is simulated correctly (in this case, mixing of two streams is effectively occurring).
Keywords: Mixer, Tee, Petroleum, Properties, Flowrate
References: None |
Problem Statement: How does the Delayed Coker Reactor deal with coke drum cycle? | Solution: The Delayed Coker model is not currently calculating a coke drum cycle. Right now the model is just assuming a drum cycle length (16 hrs) and solving according to that since the main purpose of the model is to predict steady state yields.
Keywords: coke drum cycle, delayed coker
References: None |
Problem Statement: The liquid level percent value in a column stage is not available as an exposed variable of the PID controller. How can I use it as the PV? | Solution: Inside the column subflowsheet open the stage section and go to Performance > Hydraulics. In this table there is a column names "Liquid Height in Tray" reported for each holdup volume.
You can then use the drag and drop capability of HYSYS to export the variable from the column subflowsheet into a Spreadsheet and then control the variable from the Spreadsheet cell.
Keywords: Trayed packed packing liquid %
References: None |
Problem Statement: When running a dynamics case, there is pop-up error that recommends a change to "User Specified Primary Components". Why do I get this error, and how to I prevent it? | Solution: To choose the “User Specified Primary Components� method, you could go to the Phase Order tab of the relevant Fluid package view within basis environment as below shown:
Â
The "Use User Specified Primary Components" option displays the Select Primary Phase Components group that allows you to specify which components should be in phase slot 1 and which components should be in phase slot 2. These checks are used to determine the phase order wherever the fluid package in question is used.
If there is only one non-vapour phase present and the mole fractions of the primary component adds up to more than the specified threshold, it is considered to belong in phase slot 1 and of type “liquid 1�. Otherwise the ratio of primary component for the two choices is examined.
This option is recommended when:
· A simulation is performed and it has more than one liquid phase.
· The densities of the two liquid phases may be close.
· One or more phases are close to being labelled either aqueous or liquid.
When you select the "User Specified Primary Components" method and go back to run the dynamics model, you will not see the error message.
Keywords: User Specified Primary Components, Dynamics
References: None |
Problem Statement: Is it possible to model a spray dryer that has more than one moisture components?
I am receiving an error:
MODEL IS ONLY APPLICABLE FOR SYSTEMS WITH ONE MOISTURE COMPONENT. | Solution: Currently the spray dryer model allows only for one moisture component. In the feed, there can only be one solvent, the moisture component, even if the additional liquid components are not defined as moisture. Other solid unit operation models such as the convective or short-cut dryer can consider multiple moisture components.
One work around for the spray dryer could be to define a composite component with average properties; however, the problem is that if you have liquids with very different vapor pressures you will not have a selective evaporation of these components. One could use the component with the lowest vapor pressure instead of the mixture to get a worst case estimate.
Keywords: None
References: None |
Problem Statement: How can I simulate the influence of methanol injection on hydrate inhibition? | Solution: Please note the information below is relevant up to version 8.6. For version 8.8 and after, please see the following links:
https://esupport.aspentech.com/S_Article?id=000030001
https://esupport.aspentech.com/S_Article?id=000040853
The Aspen HYSYS Peng-Robinson (PR) Property Package is recommended to simulate the influence of methanol injection on hydrate inhibition, as accurately as possible.
Even though the PRSV model tends to provide a better representation of the phase behavior of polar systems than the traditional PR model in general, it will not necessarily over-perform the Aspen HYSYS PR model for the systems with methanol injection. This is because the Aspen HYSYS PR model has the methanol related parameters regressed targeting hydrate inhibition processes. Also, the Aspen HYSYS PR model, along with the SRK model, gives access to the Hydrate Formation utility for hydrate prediction.
An Excel spreadsheet with validation data using Aspen HYSYS PR model is enclosed. Also enclosed you will find a Aspen HYSYS case (version 2004) where the validation data was obtained.
This case also provides one approach to determine how much methanol is required to eliminate the presence of hydrates in a gas stream. In this example, the Hydrate Formation Utility attached to stream "Feed With Hydrates" shows that hydrates are present at the stream condition (60 F, 3000 psia). An Adjust Logical Operation is used to determine how much methanol (20 wt% solution) we need to add to stream "Feed With Hydrates" to reduce the hydrate temperature below stream condition.
KeyWords
methanol, hydrates, inhibition, injection, PR, Peng-Robinson, PRSV, Property Package, model, prediction, reduction.
Keywords: None
References: None |
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