question
stringlengths 19
6.88k
| answer
stringlengths 38
33.3k
|
|---|---|
Problem Statement: Can I add a process utility stream such as high pressure steam in Aspen HYSYS? | Solution: In Aspen HYSYS, users may tag and designate material and energy streams as utilities. With this information Aspen HYSYS can calculate the utility consumption per utility type as well as total hot/cold utility consumption in the flowsheet.
This functionality is provided through the flowsheet summary (Home tab | Flowsheet).
To support this functionality, a process utility manager user interface is provided (Home tab | Process Utility Manager).
Aspen HYSYS provides a number of built-in utilities with defined heat capacity and temperature ranges as well as other physical properties. Users can customize this feature by adding user-defined utilities.
Keywords: utility, steam, cooling water, hot oil, utility stream
References: None |
Problem Statement: What are the Activated Analysis Dashboard in Aspen Plus? | Solution: Tools built-in to Aspen Plus to aid in process analysis and optimization
- Activated Economic Analysis provides high level cost estimates that can be used to compare process alternatives
- Activated Energy Analysis looks for opportunities to reduce energy consumption using pinch technology
- Activated Exchanger Analysis is allows quick access to rigorous heat exchanger design and rating programs from Aspen Plus
Keywords: Economic, Energy, Exchanger, Analysis
References: None |
Problem Statement: As a scheduler, most of the times the events scheduled vary from the actual scenario and the schedule prepared needs corrections,
In such a case, to edit all the events in a schedule one by one can be a tedious and painful process making the application difficult to use.
So how can we Edit multiple events at once in Aspen Petroleum Scheduler? | Solution: In APS, a functionality named Edit in Excel is available. This function has replaced the old application named as Multiple Event Editor which was available in previous versions before V9.
This functionality allows the Scheduler to edit and modify multiple events simultaneously in Microsoft Excel and Multi-Event Editor templates.
The Multi-Event Editor templates can be customized as per user model requirement and used for Editting events or the User can use Default templates that get invoked while trying to use this functionality,
In order to use the Edit in excel, here are the steps you can follow:
1) Open your APS Event Schedule Screen & Select All Events (as shown in the screenshot)
2) Right click on the Event Screen and click on Edit in Excel option
3) Once clicked, you will have the Default templates shown as follows
4) Click on one of the Event Type template and click Ok
5) You will now have an Excel sheet open with all your event specific to the type selected open for Editting
6) Once Editted, save the Workbook and click the Close button
7) The Event Schedule will refresh and the modified values/event data will now appear in the gantt screen impacting the overall Schedule.
This is the significance of the Edit in Excel functionality and can be best used to modify multiple events in a long term schedule.
Keywords: None
References: None |
Problem Statement: In version 2006 of Aspen Calc a new feature called 'Shared On-Demand Calculations' was introduced. Can these 'Shared On-Demand Calculation' be executed via Aspen SQLplus and see the results in window? | Solution: Yes, you can!
Please note that 'Shared On Demand calculations' are stored in InfoPlus.21 record sets called 'IP_CalcDef'. Through this IP_CalcDef record, we can fetch the formula defined in the 'Shared On-Demand Calculation' and execute the formula using Process data automation in SQLplus. Here is the sample query that does this:
LOCAL X, I INT, DS, QUERY, HIST, SAMPLES, SCRIPT;
X=CREATEOBJECT('ATPROCESSDATA.DATASOURCES');
DS = X('INAKUMARS1'); -- ADSA DATA SOURCE NAME
-- ONDEMANDMASS IS AN IP_CALCDEF RECORD NAME
SCRIPT = '';
FOR (SELECT CALC_LINE FROM ONDEMANDMASS) DO
SCRIPT = SCRIPT || CALC_LINE;
END
HIST = DS.TAGS.ADD(SCRIPT).HISTORY;
QUERY = HIST.QUERY;
QUERY.BEGINTIME= CURRENT_TIMESTAMP-24:00;
QUERY.ENDTIME = CURRENT_TIMESTAMP;
QUERY.MAXPOINTS=100; -- NUMBER OF RESULTS YOU WANT TO DISPLAY
QUERY.TYPE=0;
DS.READHISTORY(FALSE);
SAMPLES = HIST.SAMPLES;
WRITE SAMPLES.COUNT;
FOR I = 1 TO SAMPLES.COUNT DO
WRITE SAMPLES(I).TIME||' '||SAMPLES(I).VALUE;
END;
Keywords: Shared on demand
aspencalc
ad-hoc
ip_calcdef
References: None |
Problem Statement: Is it possible to get the historical data of a Strip Chart in tabular format in Aspen HYSYS Dynamics? | Solution: Users may set up as many strip charts as needed in Aspen HYSYS Dynamics to track the behavior of key process variables when running the model in dynamic mode.
However, there might be instances in which users might prefer to get the historical data of a strip chart in a tabular format rather than in a plot.
To retrieve the data points stored in a strip chart in tabular format, follow the next steps:
1) Make sure the model has been run in dynamic mode and stopped, as well as that there is at least one strip chart already defined with the process variables of interest.
2) Click on the ‘Strip Charts’ button on the ‘Dynamics’ ribbon.
Next, left-click once on the strip chart of interest and click on the ‘Edit’ button.
3) The property window of the strip chart will be displayed. Go to the ‘Historical’ tab, here the data points are stored as a function of time. These data can be directly copy-pasted in to MS Excel or be exported either as a *.csv or *.dmp file.
Keywords: Historical Data, Strip Chart, Data Points.
References: None |
Problem Statement: Why the main flow sheet stream hydraulics mass flow is different than sub-flowsheet? | Solution: The difference between the mass flow in the Hydraulics sub-flowsheet and the main HYSYS flowsheet is due to the linking of the two dynamic solvers.
The dynamic solver in Aspen Hydraulics requires a velocity boundary at the inlets and a pressure boundary at the outlets in order to solve the pressure-flow distribution in the pipe network.
In HYSYS dynamics, a pressure-flow matrix is solved for all of the operations on the flowsheet (see the dynamics help guide for more information, if necessary). This type ofSolution requires a pressure-flow relation for each unit operation so that they can be simultaneously solved. Therefore, in order to link Hydraulics to HYSYS, a pressure-flow relation of the form f' = f + df/dp(p'-p) must be used for the relation for Hydraulics at the outlets. Similarly, a p' = p + dp/df(f'-f) relation is used at the inlets.
At each time-step, Hydraulics solves its network then estimates a df/dp and dp/df and this equation is passed to HYSYS to put in its matrix equation. HYSYS then solves the matrix for the entire flowsheet, which means that the flow at the Hydraulics outlets and pressures at the inlets are calculated. Because the above equation is linear, it may/will not give the exact same results as the Hydraulics flow when there are large and rapidly changing pressures and conditions. Therefore, there can be a difference in the flows at the boundaries. I would expect that decreasing the time-step so that the changes are not as big would help in this issue.
Keywords: Hydraulics, Mass Flow, Inconsistence
References: None |
Problem Statement: What are the supported ProII Versions to import into Aspen Basic Engineering? | Solution: Please refer to the table below and make sure the ProII file is supported.
ABE Version Supported ProII Version
V8.0 with CPs Versions 5.01, 5.1, 5.11.1, 5.5, 5.55, 5.6, 5.61, 6.0, 6.01, 7.0, 7.1, 8.0, 8.1, 8.2, 8.3,9.0,9.1
V8.4 with CPs Versions 5.01, 5.1, 5.11.1, 5.5, 5.55, 5.6, 5.61, 6.0, 6.01, 7.0, 7.1, 8.0, 8.1, 8.2, 8.3,9.0,9.1
V8.8 Versions 5.01, 5.1, 5.11.1, 5.5, 5.55, 5.6, 5.61, 6.0, 6.01, 7.0, 7.1, 8.0, 8.1, 8.2, 8.3,9.0,9.1
V9.0 Versions 5.01, 5.1, 5.11.1, 5.5, 5.55, 5.6, 5.61, 6.0, 6.01, 7.0, 7.1, 8.0, 8.1, 8.2, 8.3,9.0,9.1
V10.0 with EP07 Versions 5.01, 5.1, 5.11.1, 5.5, 5.55, 5.6, 5.61, 6.0, 6.01, 7.0, 7.1, 8.0, 8.1, 8.2, 8.3,9.0,9.1, 9.3, 9.4, 10.1
V10.1 Versions 5.01, 5.1, 5.11.1, 5.5, 5.55, 5.6, 5.61, 6.0, 6.01, 7.0, 7.1, 8.0, 8.1, 8.2, 8.3,9.0,9.1
If you have any version other than that, please contact Aspen Tech Support ([email protected]) for help.
Keywords: ProII , Simulation Importer, Version Compatibility
References: None |
Problem Statement: How do I change the currency format based on region? | Solution: The currency format may be changed from Windows Settings | Control Panel | Region.
On the Formats tab, choose the appropriate format from the drop-down list.
On the Location tab, make the appropriate selection from the drop-down list.
Save your file, close the program and then re-open your file. The currency format should be updated accordingly.
Keywords: None
References: None |
Problem Statement: How do I get my Adjust, Set, or Balance to solve before my Column (or any other) operation? | Solution: An example where you may wish to do this is if you have an adjust operation that is setting one of the conditions (temperature, pressure or flow rate) of your feed stream to the column or operation. You may want the Adjust to solve first, so that your column does not have to solve every time the feed condition is adjusted.
To force the adjust to solve first, you will have to decrease its Calculation Level. Calculation levels can be accessed from the Home ribbon, in the Solver group, click to set calculation levels. The Calculation Order dialog box appears. (See Below Screenshot).
Specify a lower value to indicate a higher priority for the unit operation. Logical operations have calc levels of 3500 while a column operation has a calc level of 2500. Most other operations and streams have calc levels of 500. You can set the calc level of your adjust to 500 to ensure that it solves before the calculations in the column begin.
Keywords: calc levels, adjust, set, operation, solve first, solve before, column
References: None |
Problem Statement: This knowledge base article provides an example script which illustrates how to return all sub-batch start/end times and duration for a given batch using Aspen SQLplus. | Solution: The sample Aspen SQLplus script below calls the Aspen Production Record Manager Application Programming Interface (API) to return the start and end times and duration of all sub-batches of a batch within a specified time frame.
The query uses the following logic:
1. Query for the number of batches which have a start and end time within a given time frame
2. Loop through the batches returned to find how many sub-batches are associated with each batch
3. Loop through each sub-batch to return the start and end times of each sub-batch
The parameters are entered as macros in this simple example:
- The name of the data source
- The name of the batch area
- The start and end time of the desired time frame
Replace the parameter values below with your actual ones before running the script.
macro DATA_SOURCE = 'APRMSERVER';
macro AREA_NAME = 'Demo Area';
macro START_FRAME = '01-jan-19 00:00:00';
macro END_FRAME = '01-jan-19 12:00:00';
local data_sources;
local batchquery;
local batchlist;
local batch_hnd;
local char_hnd;
local i, j;
data_sources = createobject('AspenTech.Batch21.BatchDataSources');
batchquery = data_sources('&DATA_SOURCE').areas('&AREA_NAME').BatchQuery;
batchquery.timerange.start = '&START_FRAME';
batchquery.timerange.end = '&END_FRAME';
batchlist = batchquery.get;
write 'Number of Batches: ' || batchlist.count;
write ' ';
for i = 1 to batchlist.count do
batch_hnd = batchlist(i);
write 'Batch Number: ' || batch_hnd.characteristics.item('BATCH NO');
write 'Number of Subbatches: ' || batch_hnd.subbatches.count;
for j = 1 to batch_hnd.subbatches.count do
char_hnd = batch_hnd.subbatches.item(j);
Write 'Subbatch #' || j || ': ' ||
'Start=<' || char_hnd.characteristics.item('START TIME') ||
'> End=<' || char_hnd.characteristics.item('END TIME') ||
'> Duration=' ||
cast(cast(char_hnd.duration*24:00 as int) as char using 'ds12');
end
write ' ';
end;
Of course this is only a sample script. For example if you want the start time of a sub-batch called 'MIX' instead of the start-time of the j-th sub-batch, you will write:
char_hnd = batch_hnd.subbatches('MIX');
Note on format of duration
Aspen Production Record Manager returns the duration as a variant DATE. Aspen SQLplus converts the DATE value to a character value using the standard operating system conversion function. This default conversion is sufficient if the operating system settings do not use an AM/PM indicator and the duration is less than 24 hours. If this is not the case, you can format the value explicitly in Aspen SQLplus. Aspen InfoPlus.21 has some standard formats for delta times but they work on an integer number of tenths of seconds. The DATE is a number of days, which can include fractions of a day. So you need to convert the DATE value to an integer and then format it using an Aspen InfoPlus.21 format record.
Keywords: None
References: None |
Problem Statement: How do I split a stream and get outlets at the same temperature and pressure as inlet? | Solution: Here a scheme is presented to split a material stream into two with identical pressure and temperature.
1) Attach the material stream to a component splitter (X-100) as Inlet and attach two product streams to the splitter (1 and 2)
2) Attach an energy to the splitter (Q-100),
3) Set the intended splits for all components in the splitter property view (Design | Splits)
4) Select Calculate Equal Temperatures and Equalize All Stream Pressures, as shown below (Design | Parameters)
5) Add a Set unit to pass the temperature value from the inlet stream to one of the product streams
After the inlet and the splitter are calculated, stream 1 and 2 will have the same temperature and pressure as those of the Inlet.
Keywords: Component Splitter.
References: None |
Problem Statement: How to account for air preheating in a Fired Heater in EDR? | Solution: Air preheating is a common practice in Fired Heaters to increase the fuel efficiency. Using an oxidant (air) at a higher temperature than, for example, atmospheric conditions, could either decrease the amount of fuel needed to meet a specific outlet temperature of the process stream, or increase the outlet temperature the process stream could reach with a fixed amount of fuel.
EDR will allow you to specify if you want to model the air preheater along with the stack. You can select this under Input | Heater Geometry | Gas Flow | Stack | Included flue components (stack/preheater):
After selecting this, you also need to specify what will be the inlet temperature of the air to the burner (outlet temperature after the preheater). You can do this from Input | Program Options | Thermal Analysis | Air Preheat tab. Please note that if you do not specify this temperature, EDR will use the default of 20 C, which is like no preheating is taking place:
The effects on the Fuel Efficiency and/or the calculated Fuel Flowrate can be seen from the Overall Summary:
Keywords: Air preheater, fired heater, EDR, fuel efficiency
References: None |
Problem Statement: This | Solution: frames on how to configure one MV as Prediction only for a CV on DMC3 Builder V10
Solution
Prediction only feature is available from DMC3 Builder Version 10. When this feature is enabled we expect the controller to not use all models for control as some of the MVs will not move for certain constraints. In other words, using the Prediction only feature is the same as creating a copy of the MV as feedforward and moving the MV model to the new “Feedforward” variable. It has been noticed that when this feature is enable the move plan for this MV are not taken into account.
To enable this feature for a MV, please following the next steps:
1.- On DMC3 Builder go the Master model node of the controller
2.- On the top ribbon, go to Model Operation and click on the edit icon, this will display a sub menu where you can see the following options:
3.- Select Curve overrides and this will display a Matrix for the MVs and CVs. Select the MV/CV pair for which you want to set Prediction Only by checking the box on the top
4.- Change the Mv/CV pair from Always use to Prediction only, by selecting and clicking on the cell.
5.- Finally click on ok to save the change on the Model.
Keywords: DMC3 Builder, Prediction Only, Model
References: None |
Problem Statement: Is it possible to account for air recirculation effects in EDR? | Solution: Recirculation in an air cooled exchanger is a problem that can decrease the overall efficiency of a unit, especially for forced draught configurations.
Currently EDR does not model these effects as it is complicated to estimate what fraction of the air (gas) flow rate will be recirculated.
Nevertheless, if the recirculation and the total flow rates are known (the recirculation fraction is known), it would be possible to model this by connecting EDR to either Aspen HYSYS or Aspen Plus. A fraction of the air outlet stream would be mixed with the fresh air inlet, and the simulator would re-calculate the real performance of the unit considering this phenomenon.
Keywords: Recirculation, air cooler, EDR
References: None |
Problem Statement: What are the different types of Reactions that can be modeled in Aspen HYSYS? | Solution: In Aspen HYSYS, five types of Reactions can be modeled namely, Conversion, Equilibrium, Heterogeneous Catalytic, Kinetic and Simple Rate.
For creating a Conversion reaction set, users require the stoichiometry of all the reactions and the conversion of the base component in the reaction.
For creating a Equilibrium reaction set, users require the stoichiometry of all the reactions. The term Ln(K) may be calculated using one of several different methods.The reaction order for each component is determined from the stoichiometric coefficients.
For creating a Heterogeneous Catalytic reaction set, users requires the kinetics terms of the Kinetic reaction as well as the Activation Energy, Frequency Factor, and Component Exponent terms of the Adsorption kinetics.
For creating a Kinetic reaction set, users requires the stoichiometry of all the reactions, as well as the Activation Energy and Frequency Factor in the Arrhenius equation for forward and reverse (optional) reactions. The forward and reverse orders of reaction for each component can be specified.
For creating a Simple Rate reaction set, users requires the stoichiometry of all the reactions, as well as the Activation Energy and Frequency Factor in the Arrhenius equation for the forward reaction. The Equilibrium Expression constants are required for the reverse reaction.
Keywords: Reaction Types, Conversion, Equilibrium, Heterogeneous Catalytic, Kinetic, Simple Rate.
References: None |
Problem Statement: This Knowledge Base article shows how to resolve the following error message: Run-time error '91' : Object variable or With block variable not set.
One or both of the problems will be observed:
1. The AFW Security Client Service is not visible in the list of services.
2. The following error is observed when the AFW Security Client Tool is opened and Refresh Cache Now or Advanced Options... is selected. | Solution: 1. Open a command prompt window and cd to \Program Files\AspenTech\BPE - if you are running 32-bit version then specify Program Files (x86)
2. At the command prompt type: AfwSecCliSvc /unregserver to unregister the service
3. Reboot the computer and verify that the service is gone.
4. At the next prompt type: AfwSecCliSvc /service
5. Verify that the service is now listed in the services.msc Control Panel and that you can start it.
Note: The service will start with the Local System account but you can change this in the properties dialog for the service. Be sure there are no spaces at the end of either the /unregserver or /service command.
Keywords: AfwSecCliSvcAdmin
References: None |
Problem Statement: How to add static head contribution for vessel downstream pressure calculation? | Solution: By default, Contribution of static head on liquid outlet pressure is not incorporated. However, in models with a liquid holdup, we have the option of representing the effect of the liquid static head on the liquid outlet pressure.
This option can be enabled either from Global options or individual models.
For Global option:
In the Simulation Explorer, click the Globals folder, and in the Contents window, double-click DynamicsOptions to open the DynamicsOptions table.
Set the value of GlobalLiqHead to True.
For Individual models:
Right click on model, then Configure Form > Vessel > Check the hydrostatic head option
In either case, to add the value of vessel elevation, please right click on model > Allvariable form.
A representative model is attached.
Key Words
Hydrostatic Head, Pressure, Liquid
Keywords: None
References: None |
Problem Statement: How to resolve the Error-Failed to Launch Help received in APS when Help File is not found? | Solution: The root cause of this issue is that The Help file is missing from the Installation folder of Aspen Petroleum Scheduler i.e.
C:\Program Files (x86)\AspenTech\Aspen Petroleum Scheduler\HTMLHelp
To resolve this issue, two approaches can be followed:
1) You can copy this Default.htm file & the Content folder from a working APS machine with the same version and paste it in the foll. Path of the non-working machine ,path- C:\Program Files (x86)\AspenTech\Aspen Petroleum Scheduler\HTMLHelp\Orion
2) If these two files don't help,
Copy the entire Orion Folder from a working APS machine having the same version as that of the faulty machine,
Paste this Orion Folder in the following path: C:\Program Files (x86)\AspenTech\Aspen Petroleum Scheduler\HTMLHelp\Orion
3) Once copied, please re-open APS and then check if error is resolved by clicking on the Help button from the Menu bar
4) If the Help Topics page is launching and no error is received means that the issue is resolved:
Keywords: None
References: None |
Problem Statement: Can I perform Pipe Flow Assurance studies in Aspen HYSYS Dynamics? | Solution: Aspen HYSYS Pipe Segment Flow Assurance options allow users to check the physical structures of a pipe against the predicted wear caused by the type of fluid it is carrying to estimate the functional viability of the pipeline over time. In Aspen HYSYS Steady State, users can predict the formation of hydrates, the rate of corrosion, calculate the Wax Deposition rate, predict slug properties for horizontal and inclined two-phase flows in each pipe segment, and the physical erosion along the length of pipeline is extremely important during pipeline design and maintenance.
However, currently these flow assurance studies cannot performed in Aspen HYSYS Dynamics and Aspen Hydraulics Dynamics.
Keywords: Pipe Segment, Flow Assurance
References: None |
Problem Statement: How do I export the simulation workbook pages from Aspen HYSYS to Excel? | Solution: Please follow the workflow below to export the simulation workbook from HYSYS to Excel:
1. Select the Workbook button from the Home tab (top ribbon)
2. From the Workbook tab, click the Excel button from the Export section
3. Select pages to export
4. Finally, click Export to Excel button.
The workbook pages will be exported to a new Excel file.
The Workbook in the simulation can be configured with the required properties data and the data can be exported to Excel without requiring additional VBA macros.
Keywords: Workbook, Excel
References: None |
Problem Statement: Does RYield calculate adiabatic reactor temperature rise? | Solution: Yes. RYield calculates adiabatic reactor temperature rise.
For RYield, the duty is the difference between the inlet and outlet enthalpies. You do not need to specify heats of reaction, because Aspen Plus uses the elemental enthalpy reference state for the definition of the component heat of formation. Therefore, heats of reaction are accounted for in the mixture enthalpy calculations for the reactants versus the products. The temperature will change if the duty and pressure drop are 0.
Keywords: Aspen Plus, RYield, Reactor
References: None |
Problem Statement: Does Aspen Flare System Analyzer (AFSA) use rated flow or mass (design) flow for the pressure drop of inlet piping? | Solution: AFSA will use the design (mass) flow for inlet piping pressure drop calculations by default. However, you may set AFSA to make use of rated flow instead, by going to Calculation Settings | General | Rated Flow for inlet pipes.
Keywords: Inlet Pipes, Pressure Loss, Mass Flow, Rated Flow.
References: None |
Problem Statement: How to model tray types that are not available in the Column Internals database? | Solution: Tray types like Superfrac are proprietary and currently, the Column Internals database does not include the correlations for these tray types to perform the hydraulic calculations.
However, the user can select an existing valve tray type and modify the weir length to mimic the Superfrac tray. Weir Length can be modified using the Interactive view for the tray type (Geometry View)
Another option, the user can change is the system foaming factor and aeration factor to tune the results.
(Design Parameters View)
Keywords: Column Internals, Column Hydraulics, Superfrac, High Performance Trays
References: None |
Problem Statement: How can I add component mass fractions to a Workbook Report? | Solution: Open the Workbook and view the Compositions tab. From the Workbook tab in the top ribbon,click the Setup button.
Ensure the Compositions tab is selected and click the Add button.
You may type mass frac to auto-filter the variables. Click the arrow to add selected component mass fractions. Click Done when finished.
Keywords: Report, Workbook, Properties
References: None |
Problem Statement: How do I change a specification type for the column side operation? | Solution: The specification type used for a column side operation such as pump around can be changed following the steps given below:
1. Open the column and then select the Side Ops tab.
2. Select the side operation from the available list.
3. Click the View button.
4. Double-click on an Active Spec. This will open the available specifications for the selected side operation.
5. Change the specification type.
6. Enter a value for the spec.
Keywords: Column, Side Operation, Active specification
References: None |
Problem Statement: Can I run the Fired Heater in steady state? | Solution: Yes, the steady state Fired Heater model supports the specification of combustion efficiency and flue gas temperature and solves based on these parameters and fully defined feed and fuel / air streams.
In steady state mode, the fired heater supports multiple fuel and air streams. To facilitate the transition between steady state and dynamics, Aspen HYSYS will automatically merge all fuel streams created in steady state into one fuel and air stream in Dynamics. It will also split the same stream into air and one fuel stream when returning from dynamics to steady state.
To use the fired heater in steady state:
Ensure O2, N2, CO2 and H2O are in the component list
Define inlet streams for air, fuel to be burned and the process stream to be heated
Air stream is defined as an N2/O2 mixture
Heat transfer occurs in radiation zone only in steady state. Set up a dynamic model for convective and economizer zone calculations.
The HYSYS model may be linked to Aspen Fired Heater for rigorous design, rating or simulation.
Keywords: fired heater, steady state, furnace
References: None |
Problem Statement: If we open a stream property view, select Worksheet tab, Compositions page, and click on the button View Properties, we find a property Molar Volume as in the screen shot below.
What are the conditions at which the molar volume is calculated? | Solution: The is the same property known as GS/CS - Mol Vol, see screenshot using N2 as an example. Here GS denotes Grayson-Streed property package, while CS denotes Chao-Seader property package. This property is calculated from COSTALD at 25 C and 1 atm if Tc is higher than 300 K, or calculated using liquid density at 60 F for all other cases.
Keywords: Molar volume, GS, CS, mol vol.
References: None |
Problem Statement: How to Create a DFMS File for Aspen Enterprise Database Using Aspen Plus Engine | Solution: A DFMS (.dfm) file can be generated from an Aspen Plus or Aspen Properties simulation and used to create a custom user Aspen Properties Enterprise Database (APED) Databank.
This Solution explains how to create an enterprise database from a simulation model and requires the user to access the Aspen Plus User Interface to define the report options and generate the database files.
If the input data already exists as a compatible Aspen Plus Input File or the Aspen Plus Simulation is used to create a large data file but due to file size it may be faster to run the simulation through the engine. The Input file can be modified to add the DFMS report options to the Aspen Plus Customization Engine run.
First, set the correct options in the Input File so that so that Pure and Binary chemical parameters are generated.
The following keywords
REPORT NOADA
PROPERTY-REP NOPARAMS NOPCES DFMS NOPARAM-PLUS
will set up the Engine to create a report file (*.rep) and a DFMS file (*.dfm) with a list of chemical component IDs, pure and binary parameters with no property constant estimation parameters without other parameter reports.
This is the equivalent of setting the following options, In the GUI, Report Options| Properties Environment General Setup:
And Property Setup:
Next, launch the Customize Aspen Plus window and run the Input file to generate the reports as defined.
In the Customize Aspen Plus window, navigate to the directory with the Aspen Plus Input (*.inp) file, and use the command aspen inputfilenamenoextension and ENTER to run the file and generate report.
This will create the report file *rep and DFMS file *.dfm in the same directory
And as instructed in the same KB article 000025903 the DFMS file can be modified to be imported in Aspen Properties Enterprise DataBanks as a custom databank.
Attached is an Aspen Plus Input example file that can be used to create the DFMS report file. The proper keywords have already been set. To generate the files, simply follow the workflow for running the simulation in Aspen Plus Engine.
Keywords: Enterprise database, input file database, report from aspen plus engine, custom database from command line
References: None |
Problem Statement: Can I rearrange streams in alphabetical or any other order in HYSYS workbook? | Solution: Yes, you may rearrange streams in a workbook.
Please follow these steps:
Open workbook and then right click anywhere on the workbook.
Choose the option - Order/Hide/Reveal.
Choose the sorting order radio button. If you choose Manual, use the up or down arrow to move a stream up or down in the list.
Once you are done, click OK.
Keywords: Workbook, order, stream, ascending, descending
References: None |
Problem Statement: Why does the non-recoverable pressure loss equal total pressure loss when using either the Isothermal Gas or Adiabatic Gas pressure drop correlations for inlet piping? | Solution: The Adiabatic Gas and Isothermal Gas pressure drop correlations are closed form analytical equations (see the Help Menu Guide for details).
They only calculate the total pressure drop and not the individual parts of the pressure drop (e.g. pressure drop due to frictional / gravitational / acceleration effects). Therefore, non-recoverable pressure loss equals total pressure loss when using these correlations.
For example, in the image below, the inlet piping form of source (with no elevation changes) has a change of diameter from 6 in to 4 in. Using either the Adiabatic Gas or Isothermal Gas pressure drop correlations, the computed total pressure loss equals the non-recoverable pressure drop.
Now, using a pressure drop correlation such as Beggs & Brill, the computed total pressure loss results in a greater value than the non-recoverable pressure loss, as show in the image below:
Keywords: Total Pressure Loss, Non-recoverable Pressure Loss, Adiabatic Gas, Isothermal Gas, Pressure Drop Correlation.
References: None |
Problem Statement: Can I view individual heat transfer coefficients for the Aspen HYSYS Pipe Segment operation? | Solution: The individual heat transfer coefficients are available via the Overall HTC radio button on the Rating | Heat Transfer page.
Keywords: HTC, pipe segment, individual HTC, heat transfer coefficient, heat transfer
References: None |
Problem Statement: Why RBatch does not maintain mass balance around the block? | Solution: RBatch is a batch reactor used in a continuous flowsheet. Holding tanks are used to interface to steady-state simulations.
The mass calculation equations for RBatch are:
For charge stream:
Batch charge = F_charge * T_cycle
If T_cycle is missing, then
Batch charge = F_charge * T_feed
For product stream:
F_product = P / T_cycle
Where P = total mass in reactor = Batch charge + Continuous charge
If T_cycle is not specified, then
F_product = P / (T_stop + T_down)
Feed and product streams are time-averaged. As a result, transient calculations inherent to the RBatch may not maintain mass balance around the block.
Mass balance only closes if:
Total cycle time specified and there is no continuous feed
Total cycle time specified and continuous feed is not varying with time
Keywords: RBatch
Mass balance
References: None |
Problem Statement: Find Fouling calculation in Air Cooled Exchanger | Solution: Within EDR, there isn’t a specific ‘Find Fouling’ Calculation Mode as there is for S&T. However, Air Cooled Exchanger has 9 different variations for the Simulation mode.
One of these Simulation modes allows the user to calculate the Process fouling resistance and the X-side outlet temperature.
The outlet temperature of the process side needs to be specified, and a fouling resistance can be entered as an initial estimate, which will be recalculated by the program.
The attached file is an example of this type of Simulation calculation.
Keywords: Find fouling, fouling, air cooler, EDR
References: None |
Problem Statement: When is the “Tmom” parameter used in polymer procedures? | Solution: The third moment (TMOM) parameter is only used when the simulation model has included TMOM in the list of polymer attributes when setting up the properties or in the original Aspen Plus model. TMOM is required to calculate the Z-Average molecular weight, MWZ. The Free-Radical bulk, FR Emulsion, Ziegler-Natta, and Ionic polymerization models all support the third moment calculations, but it is optional (unless MWZ or DPZ is in the attribute list as these require TMOM).
Keywords: Third moment, tmom, polymers
References: None |
Problem Statement: What are the auto-recovery and backup settings options under File | Options |Preferences Simulation in Aspen HYSYS? | Solution: You have the ability to choose whether or not HYSYS will keep a backup of your cases or not. You have below options available under File | Options | Simulation | Auto-recovery Settings
1. Save Auto-recovery case: When this checkbox is active, HYSYS will save an auto recovery case every specified amount of time. Use the minutes field to specify the amount of time between every save. By default it is set to 15 minutes. The location of the autosave HYSYS file is displayed in the trace window at the bottom of your HYSYS desktop. Usually it goes to C:\Users\[User Name]\\AppData\Local\Temp but you should check your trace window. It has an extension of *.ahc. Files can be renamed to *.hsc files and treated as normal.
2. Save Auto-recovery case while Integrating: When this checkbox is active HYSYS will save an auto-recovery case every time the integrator is run. This checkbox is only available when the Save Auto Recovery Cases Every checkbox is active.
3. Number of case backups automatically maintained. By default, HYSYS maintains one case back-up when you save a case. However, please note that this is not done every 15 minutes. It is done each time you save your case. When you save the case and a version of this case already exists, the latest version of your case is saved with the extension *.hsc and the previous version is renamed with extension *.bk0. If you have the option to maintain 2 back-ups, then the previous case *.bk0 is renamed to *.bk1. This backup file is saved at same location where you save *.hsc file.
4. Cascade backups on every save: If this option is enabled, then HYSYS keeps a number of cascaded backups. Hence each time a case is saved, then the previous saved case is copied to a bk0 file, the previous bk0 file is copied to a bk1 file and so on. The default is to keep one cascaded backup. Internally bk# files are the same as standard hsc binary files, they can be renamed to *.hsc files and treated as normal.
Keywords: Backup, Auto-recovery
References: None |
Problem Statement: How Kappa (Isothermal Compressibility) is defined in Aspen HYSYS? | Solution: The isothermal compressibility is defined as:
b = -1/V*(dV/dP)(Tconstant)
It represents the change of volume that takes place when pressure changes at constant temperature. Unfortunately, HYSYS doesn't display the property values of Isothermal compressibility coefficient. You can implement this in a spreadsheet to perform the calculations.
The above equation is a simplified form, you may find this equation and calculation procedure in the followingSolution.
http://support.aspentech.com/webteamcgi/SolutionDisplay_view.cgi?key=125241
Using the attached HYSYS file on the above KB, you may compute the value of beta using spreadsheet.
Keywords: Kappa, Isothermal Compressibility, Aspen HYSYS
References: None |
Problem Statement: After the installation the web application fails to run and returns an error message referring to HTTP Error 500.21 | Solution: Many web applications use managed code from the Microsoft .NET Framework codebase. What this error is saying is that it does not know how to handle ASP.NET pages. This is in much the same way that if you received a Microsoft Word Document but you didn't have MS Office installed - the operating system would not know what to do with the file.
Administrators should install/uninstall ASP.NET 4.5 with IIS8 using the Turn Windows Features On/Off dialog, the Server Manager management tool, or the dism.exe command line tool. For more details please see https://docs.microsoft.com/en-us/iis/get-started/whats-new-in-iis-8/iis-80-using-aspnet-35-and-aspnet-45.
For example, open a command prompt window (Run as Administrator) and run the following Statement
dism /online /enable-feature /featurename:IIS-ASPNET45 /all
To complete the process, run iisreset.exe to reboot the Internet Information Services and then try the web application again.
Note, on older operating systems use the following statements instead:
%windir%\Microsoft.NET\Framework\v4.0.30319\aspnet_regiis.exe -i
-and-
%windir%\Microsoft.NET\Framework64\v4.0.30319\aspnet_regiis.exe -i
Keywords: Aspen AUP
A1PE
IIS
warning message
References: None |
Problem Statement: AspenONE Process Explorer Admin, and Trend search shows error code 500.
AspenONE Process Explorer Admin search error occurs “A connection with the server could not be established (error code: 500)” and the Tomcat Catalina.log file includes error “An attempt was made to authenticate the locked user “admin”.” The error is caused because Tomcat is not able to resolve the password for the “admin” user, to resolve the error follow the | Solution: below.
Solution
Edit the file
…\AspenTech Shared\Tomcat8.0.36\conf\tomcat-users.xml
Scroll to the bottom of the file and change the line with the encrypted password to admin. [see example below]
EXAMPLE;
Original,
<role rolename=AspenSearch/><role rolename=manager-gui/><user username=admin password=21232f297a57a5a743894a0e4a801fc3 roles=AspenSearch/>
Edit,
<role rolename=AspenSearch/><role rolename=manager-gui/><user username=admin password=admin roles=AspenSearch/>
Restart the Web Server with the command IISRESET, and restart the Apache Tomcat service
Verify that search functions as expected.
Reset the encrypted password.
Run AspenONE Credentials.
Select, Tomcat Basic Authentication for Search Security.
Verify the account is “admin”.
Enter and confirm the password “admin”.
Click Apply.
Restart the Web Server with the command IISRESET, and restart the Apache Tomcat service.
Verify that search functions as expected.
Keywords: Solr
Search
References: None |
Problem Statement: Sample calculation for NPSH | Solution: The following equations are used to calculate the available NPSH:
P1 - Pvap (V1)2
NPSHavailable = ------------- + ------
ρ * g 2g
where:
P1 = inlet stream pressure to the pump
Pvap = vapour pressure of the inlet stream
ρ = density of the fluid
V1 = velocity of the inlet stream
g = gravity constant
V1 is the fluid velocity of the inlet stream, hence in steady state, the available NPSH is calculated using the default nozzle size of 0.164ft (0.05m).
Keywords: NPSH, calculation
References: None |
Problem Statement: How to locate local help files for the Aspen Process Data Addins ? | Solution: The following locale install location contains a number of helpful files which cover the MES products.
C:\Program Files (x86)\Common Files\AspenTech Shared\Help\En
The following files are the Aspen Process Data Addins.
ProcessDataAddin.chm
ProcessDataExcelAddin.chm
Keywords: How to use.
Process Data
Excel
Addins
References: None |
Problem Statement: For inlet piping, sources report ‘Piping non-recoverable pressure drop’, as well as ‘Piping pressure drop’. What is the difference between them? | Solution: Sources in Aspen Flare System Analyzer report both ‘Piping non-recoverable pressure drop’ and ‘Piping pressure drop’.
Their definitions are the following:
1) Piping non-recoverable pressure drop accounts for friction losses only.
2) Piping pressure drop includes static head as well as friction losses.
Keywords: Piping Non-Recoverable Pressure Drop, Piping Pressure Drop, Friction Losses.
References: None |
Problem Statement: Why does the distillation curve reported for an assay sometimes differ from the input curve? | Solution: The input curve might be just the distillation data. E.g., ASTM D86
However, one can enter additional data related to assay. Assay data of certain crude oils, especially light crudes, may contain detailed analysis of defined components, typically including methane through n-hexane. You can enter the fractions (on a mole, mass, or standard volume basis) of these light ends components. The presence of light ends can affect the distillation curve results.
Also, the curve fitting could be another cause for different distillation curve results.
Keywords: Light ends, curve fitting
References: None |
Problem Statement: In addition to built-in attributes, what are other properties calculated by Emulsion Polymerization? | Solution: For RBatch and RPlug reactor, the following additional variables are calculated when Emulsion Polymerization kinetics is selected:
Glass transition temperature of the polymer (°C)
Average number of radicals per particle
% Soap coverage of the polymer particles
Volume of the monomer droplet phase (m3)
Concentration of monomers in the monomer droplets (kmol/m3)
Volume of the aqueous phase (m3)
Monomer concentration in the aqueous phase (kmol/m3)
Volume of the polymer particle phase (m3)
Monomer concentration in the polymer particles (kmol/m3)
Monomer conversion
These variables are reported in RBatch/RPlug > Profile > User variables Table:
Key Words
Emulsion, User Variables, Profile
Keywords: None
References: None |
Problem Statement: After specifying a subcooled temperature for the condenser, stage 1 (condenser) temperature in TPFQ profile does not get updated. | Solution: The behavior you observed is by design. The convention is that the temperature in the TPFQ table is the equilibrium temperature of the stages. If you want to look at the subcooled temperature of the reflux stream, you could create a pseudo stream for the liquid stream on stage 1 (condenser).
Keywords: None
References: None |
Problem Statement: When trying to access to the Aspen HYSYS Online Help, the Help page does not open in Aspen HYSYS, how do I fix it? | Solution: This issue occurs due to a corrupted Aspen HYSYS installation since the help files could not be saved on the right folder. Hence, in order to solve this, one can condiser below two methods:
1. Repair the installation of Aspen HYSYS.
2. Please check the following directory: C:\ProgramData\AspenTech\Aspen HYSYS Vx.x\HtmlHelp, you will notice that the folder is empty, so we can provide with a copy of all the topics help files available for Aspen HYSYS and these can be pasted on this folder. Then as soon as one opens Aspen HYSYS, the Online Help content will be available.
Keywords: Help page, Online Help.
References: None |
Problem Statement: What are ‘Logical Connections For’ in Aspen HYSYS and how can users access them? | Solution: The ‘Logical Connections For’ property view enables you to determine simulation dependencies between objects which are not otherwise shown via connecting lines on the PFD. Certain HYSYS operations can write to any other object and if you are looking at the object being written to, they have no way of telling this, other than that the value might be changing. For example, one can determine if one spreadsheet is writing to another.
To access the Logical Connections for… property view of a HYSYS PFD object,
1) Open the object’s property view.
2) Right-click in an empty area of the object’s property view. The Object Inspect menu associated to the object appears.
3) Select Connections command from the Object Inspect menu.
The table in the Logical Connections for... property view contains the following columns:
a) Remote Name column displays the name of the operation or stream being written to or read from the active object.
Double-click on an entry of the Remote Name column to open the property view of the operation or stream.
b) Remote Type column displays the operation type (pump, valve, stream, and so forth) of the remote object from the current/active property view.
The Show All check box enables you toggle between displaying or hiding all the other operations and streams that the selected object knows about. Duplicate connectivity information may be shown otherwise (either via a line on the PFD or someplace else in a Logical operations property view, for example). Usually, you do not need to activate this check box.
Keywords: Logical Connections For, Simulation Dependencies, Object Property View, Operations, Streams.
References: None |
Problem Statement: What are the available options to manually enter the Petroleum Assay data? | Solution: Each option allows you to enter information differently:
Multi Cut Properties (default option) lets you specify mass, molar, or volumetric cuts of the crude assay sample with user defined initial and final boiling points.
Single Stream Properties, lets you define the distillation percent and temperature of individual streams.
BackBlending, allows you to define feed streams by blending their associated products. The input products are typically defined in commercial distillations that have significant overlap across products. BackBlending creates an assay from these characterize feed assays by defining data and conditions for their outlet mixtures. BackBlending creates an assay from these overlapping measurements that can be used as a HYSYS Petroleum Refining feed stream.
Keywords: Aspen HYSYS, Petroleum Assay, Data
References: None |
Problem Statement: How do we understand the back pressure when choking happens downstream PSV in Aspen Flare System Analyzer (AFSA)? | Solution: In Aspen Flare System Analyzer, if you use a required mass flow > critical mass flow of the PSV orifice (rated flow of a PSV which is choked in other words), that would be an physically incorrect boundary condition and your back pressure results would be wrong.
At the point of secondary chokes in the downstream pipeline, the AFSA calculates the upstream pressure, to achieve the specified mass flow in the choked conditions. The backpressure results calculated this way are correct. There is a theoretical possibility though that supersonic flow/shock develops downstream of the choked location. The limitation of Flarenet is that it does not handle this case correctly (in practice this is not likely unless you put a specially designed supersonic nozzle in your pipeline to achieve supersonic flow).
It is not recommended the Flare network operating at choke conditions. Most users use Mach Number less than 0.7 for new systems and less than 0.8 for capacity expansion of existing systems.
Keywords: Back pressure, Choke flow
References: None |
Problem Statement: How shall I use Symbol Replication Tool to improve the Symbol Loading experience in Drawing Editor? | Solution: Symbol Replication tool can download the Symbol Library from the server to local client machine. It will speed up the performance of each client machine when a PFD in drawing editor is loaded.
This application can be launched from the start menu (Start > Aspen Basic Engineering > Symbols Replication) on a client machine
2. Browse to the “Master Symbol Library” location, this will be to the Workspacelibraries share location which is typically on the server machine
Server = Server name
Share = Share name on the Server
3. For the “Replication Directory (local copy)” field, browse to a known location on the client machine (note: the default directory shown in the application is not existent and will give an error when you try to replicate)
4. The “Local Symbol Library” field will get dynamically updated when the “Replication Directory (local copy)” and “Master Symbol Library” directories are selected
5. Click Replicate, for the process to start. Once this has been completed, a confirmation dialog will be generated.
6. Open the windows file explorer and browse to the “Local Symbol Library” directory to see the replicated symbols on the client machine
7. To use these symbols in the Drawing Editor, the client will need to open this application, select File à Symbols Location… and browse to the “Local Symbol Library” directory
8. Once the above steps are completed, user can connect to the workspace in the Drawing Editor and create diagram without any issues.
Keyword
Symbol Replication, Loading Symbol
Keywords: None
References: None |
Problem Statement: Are Heat Ports from ACM supported in Aspen HYSYS? | Solution: If an ACM model containing Heat Ports is exported to Aspen HYSYS, these won’t be available (HYSYS does not support these ports).
As an alternative, the heat duty calculated by the ACM model could be exported to a Spreadsheet block, and from there, even to an Energy Stream if additional manipulation is necessary.
Keywords: Heat port, ACM, HYSYS
References: None |
Problem Statement: When defining inlet pipe segments for sources in Aspen Flare System Analyzer (AFSA), does AFSA imply that an expander/reducer exists between each segment? Does it account for the pressure loss caused by the expander/reducer? | Solution: For different inlet pipe segment diameters, AFSA does not consider that a swage exists between two different sizes, so the pressure loss due to the change of pipe sizes is not considered. As a workaround you may enter an equivalent length for each pipe to account for such pressure loss.
Keywords: Pipe Segment, Inlet Pipe, Swage, Pressure Loss, Equivalent Length.
References: None |
Problem Statement: I have set up a Storage Tank Protection object in Safety Analysis, but even though there are results for Normal Venting, no results are shown for Emergency Venting. Why? | Solution: A 'Storage Tank Protection' object may be correctly set up, but the 'Bottom Tan Above Grade' and 'Flame Height from Grade' values might not be right, thus no results will be computed for Emergency Venting.
The 'Flame Height from Grade' value must be greater than the 'Bottom Tan Above Grade' plus the vessel ‘Height’ to have Safety Analysis compute the emergency venting calculations.
If, for example, for a 30ft tall vessel one sets the Bottom Tan Above Grade=5ft and Flame Height from Grade=30ft (default value), the emergency venting calculations will then be performed.
Keywords: Storage Tank Protection, Safety Analysis, Emergency Venting, Height, Bottom Tan Above Grade, Flame Height From Grade.
References: None |
Problem Statement: Why is the specified number of Tie Rods not being used for the Tubesheet Layout results? | Solution: The user-defined number of tie rods is accepted if it is above the TEMA minimum (usually >6) or zero. The user can always edit the number of tie rods on the tube layout, and reposition them. The tie rods have no effect on other calculated results, unless they occupy a potential tube location, in which case there will normally be a very small effect (no relevant from a thermal perspective).
Keywords: Tie rods, tube layout
References: None |
Problem Statement: In HYSYS, how to calculate the heat of mixing of electrolyte | Solution: ? For example, the heat of mixing sulfuric acid with water.
Solution
1. In Properties environment, choose Aspen Properties when adding component list. Add sulfuric acid with water.
2. Choose Aspen Properties when adding fluid packages. The reason we choose Aspen Properties here is because Electrolyte NRTL is not available in HYSYS fluid packages.
3. Under Fluid Packages, choose Electrolyte NRTL.
4. Click Electrolyte Wizard at the bottom to generate the chemistry. You can optionally include reactions of “Salt formation”, “Water dissociation” and “Ice formation” based on your electrolyte system and operating conditions. Then click “Get Reactions”. You can double check the reaction set to see if the chemistry is correct. Click OK.
5. Then go to simulation environment. Use a mixer to mix two streams. The mixture temperature will be increased due to the heat of mixing. Then use a cooler to bring the temperature back to the original temperature. The Q in the cooler will be the heat of mixing.
Keywords: Electrolyte NRTL
Heat of mixing
Aspen Properties
References: None |
Problem Statement: How to give pipe specifications for all the pipe segments in Aspen Hydraulics? | Solution: Users can use pipe segment editor under Piping Network Ribbon in Aspen Hydraulics to give specifications for all the pipelines together.
In the editor, users can specify pipe details quickly in an grid similar to excel. Also, it is possible to apply the properties values to all the pipes together.
Keywords: Pipe Segment Editor, Apply all
References: None |
Problem Statement: I would like to track the erosion rate for the whole pipe network in a Hydraulics subflowsheet, similar to what I see in pipe segment. How do I accomplish this? | Solution: Unfortunately there is no direct way to show the overall erosion rate as in a pipe segment. There are three options we can use to get this:
1.- Get the report for each pipe. Enter to the Hydraulics subflowsheet, and fro each pipe select the Flow Assurance tab where you can sactivate the Erosion Speed analysis.
2.- We can build a table to report erosion rate for all the pipes. Inside the Hydraulics property view, select the Variables tab and add the variable Pipe Erosion Rate for each segment. Unfortunately, there is no way to graph the data with this option. It is necessary to send the data to Microsoft Excel.
3.- To keep the data updated, we can make use of Aspen Simulation Workbook (ASW) (for more information, please refer to thisSolution Jump Start: Aspen Simulation Workbook in Aspen Plus V8) and call the variable Pipe Erosion Rate for each segment. In this option you can graph the performance using Microsoft Excel capabilities.
Keywords: Erosion rate, ASW, Microsoft Excel, Upstream, Flow Assurance, plot
References: None |
Problem Statement: When running the Icarus Excel reports, a message pops up referring to an Excel Report Header Error and/or the named range does not exist in the template | Solution: These error messages may come up for one of the following reasons:
1. If you use or have modified the Reporter_User.accdb file (found in C:\Program Files (x86)\AspenTech\Economic Evaluation VX.X\Program\Sys\Reporter\Database). Where VX.X represents your current version.
If a new Excel report was added in 'Stored Reports' table (within the Reports_User.accdb) without any corresponding modification to 'Stored Queries', when you run the Aspen Icarus reporter, you will receive an error message display: There is no stored query for the report ....... and There is no data for the report .....
2. Validate Named Range: Check to see if a named range is deleted in the report template. If that report is run, an error message would display indicating that the name range is missing.
Please check your template (found in C:\Users\Public\Documents\AspenTech\Shared Economic Evaluation VX.X\Reporter\Templates).
The error message will point to the template sheet where the issue could be generated
3. One of your installed applications (Microsoft Office), corrupted some of the Microsoft Excel .dll files, which won’t allow the report to be generated.
Uninstall Microsoft Office and reinstall. Download and install all patches and service packs for Microsoft Office from the Microsoft web site.
Keywords: Excel, Template, Error 430, Error 91, Icarus, Reports, Reporter, Header, Named range, Column header
References: None |
Problem Statement: Can I connect my Aspen HYSYS model to ASW if they are from different versions? | Solution: You can have different versions of ASW and Aspen HYSYS installed on your machine and still connect your process model to ASW.
For example, if you have the ASW V9.0 add-in installed and activated on your machine, and Aspen HYSYS V10 installed as well, you can still have ASW V9.0 connect to your HYSYS V10 model.
What you need to do is to go to the Organizer | Configuration | Simulations form and set the 'Version Option' to 'Exact Version' and type in 'V10.0' right on the 'Version String' field, as shown in the image below:
Basically, you are telling ASW which HYSYS version to use to launch the simulation file.
Keywords: Add-in, Organizer, Configuration, Version String.
References: None |
Problem Statement: What is the definition of the Vessel Base Elevation Relative to Ground Level and Nozzle Elevations on the Rating tab of a unit operation? Do they influence pressure drop calculations? | Solution: 1) The 'Base Elevation of Inlet Relative to Ground' field allows users to specify whether the process equipment's bottom head touches the ground or not, it is, if the vessel is located at ground level.
2) The 'Elevation' fields on the Nozzle Parameters section refer to the location of the feed and product nozzle(s).
'Elevation (Base)' refers to the elevation of a nozzle with respect to the base / bottom head of the vessel.
On the other hand, 'Elevation (Ground)' is pretty much the same as the above, but this once also accounts for the 'Base Elevation of Inlet Relative to Ground' of the vessel. It is, the Elevation (Ground) = Elevation (Base) + Base Elevation of Inlet Relative to Ground.
3) The elevation inputs described in 1) and 2) above do only have an effect in dynamic mode, not in steady state and should be enabled in the Integrator. Aspen HYSYS Dynamics will therefore account these heights to consider static head contributions in the system (an important term for pressure drop calculations).
Keywords: Base Elevation Relative to Ground Level, Nozzle Elevations, Pressure Drop Calculations, Static Head Contributions.
References: None |
Problem Statement: How is the Operating Weight of a Kettle exchanger calculated in Shell and Tube Mechanical? | Solution: Shell & Tube Mechanical (EDR) considers the normal liquid level to calculate the Operating Weight. The normal liquid level is taken as 25-50 mm above the OD of the highest tube row in the bundle, since the bundle must be covered by the boiling liquid.
Keywords: Operating weight, kettle, mechanical
References: None |
Problem Statement: Is it possible to have Aspen HYSYS save a copy of the Steady State model when switching to Dynamic mode? | Solution: It is a best practice to always keep a copy of the steady state file used when switching from steady state to dynamic mode. Unfortunately, users may forget sometimes to do so and that can become a problem.
For this reason, it is possible to set up Aspen HYSYS to save a copy of the steady state model once the user jumps straight to dynamic mode. The only thing to be done is to go to File | Options | Simulation | Dynamics and mark the checkbox for the ‘Save Steady State Case on Switch to Dynamics’ option, as shown in the image below:
When switching to dynamic mode, a copy of the steady state case will be saved in the location where the file is found. Note that this copy will be named with the ‘_ss0’ suffix.
Keywords: Steady State, Dynamics, Switch, Save, Simulation Options.
References: None |
Problem Statement: I have built an AFSA model in which I set up tear streams in the flowsheet, but the model comes across convergence issues. What I can I do to overcome them? | Solution: There might be some cases in which Aspen Flare System Analyzer (AFSA) models set up with tear streams will not be able to be solved with the default solver settings.
An example of this kind of situations would be KO Drums set up with dual feeds, as shown in the image below:
To overcome the convergence issues, the user can switch the ‘Structure Analyser’ setting from default ‘Convergent’ to ‘Simultaneous’, as shown in the image below.
In general, the ‘Simultaneous’ loop analyser is faster and more reliable than the ‘Convergent’ analyser and will calculate better initial estimates. The ‘Convergent’ analyser should be used for compatibility with legacy AFSA cases or when usera wish to force a set of pipes to be used as tears and/or flow estimates. More information on these methods can be found on the Help Menu Guide.
Keywords: Tear Streams, Loops, Convergence, Convergent, Simultaneous.
References: None |
Problem Statement: Why Integrator may fail if default bed discretization method is changed? | Solution: In Aspen Adsorption, the default discretization method for the gas_bed model is UDS1 (Upwind Differencing Scheme). UDS1 works very efficiently for almost all gas bed configuration and should not be changed if there is no specific reason.
While using other methods, user should be aware that other methods can have convergence problems that UDS1 does not. All discretization methods other than UDS1 are higher order methods, and theSolutions can oscillate about the true physicalSolution. This can lead to errors such as a variable near zero becoming negative, which may not be allowed for that variable type. User may need to change the bounds on some variable types to enable the model to solve.
Key Words
Adsorption, Discretization, Convergence
Keywords: None
References: None |
Problem Statement: How to model double-wall tubes in EDR? | Solution: The following description and attached example illustrate how to model double-wall tubes in EDR.
Specifications:
Tube OD
For the Tube OD, use the outer tube OD of the double-wall tube.
Contents between walls
To simulate the contents between the double-wall, select a fouling layer thickness equal to the difference of the inner tube wall OD and the outer tube wall ID. Then add the thermal conductivity of the medium in between. The program lowest value now is 0.058 BTU/(ft-hr-F). A typical entry might look like this:
Make sure no fouling resistance is entered in the tube side so the program can calculate it from the above entries. The program calculates the reduction in flow areas due to the fouling layer and the consequent increase in the tube side pressure drop.
The reduction in flow area due to the fouling layer thickness also directly affects the relevant stream heat transfer coefficients, the heat transfer area on which the fouling occurs, and the Reynolds numbers. The presence of a fouling layer of finite thickness may therefore cause changes in the clean heat transfer coefficient reported in the output, though these will normally be minor, because the effect of the increased mass flux will often be compensated for by the change in local heat transfer area.
Tube thickness
For tube thickness, you could specify the inner tube thickness only since the metal thermal conductivity for this type of calculation is insignificant, so we could ignore the outer tube wall thickness. However, doing this could affect pressure drop calculation in the tube side (depending on the contribution of the outer thickness to the overall tube thickness), so it’s better to use Tube thickness = outer wall tickness + inner wall thickness. In thermal calculations, the program internally sets the tube ID = bare tube ID + fouling thickness.
Keywords: Double wall, tube wall, EDR
References: None |
Problem Statement: This article explains how to resolve an incomplete trip time and distance error. Occasionally a User will receive the message “Cannot add shipment to transport because of incomplete trip time information” from the Aspen Fleet Optimizer that a shipment cannot be added to a transport:
This error is shown when the Optimizer cannot calculate the trip time and distance of one of the legs of the journey. | Solution: A journey for a truck making a delivery generally consists of at least 2 locations:
The Terminal where the truck starts his day (typically the same terminal where he will load his first load) and often the same he returns to for another load to be loaded after a delivery.
The Station he is making the delivery to (Customer)
Trip times and Distances must be entered into the Fleet Optimizer system so that the system can calculate an optimized schedule based on driving time and transportation costs between terminals and customers and between customers and customers.
If the truck starts at another terminal than the one he needs to load from (or returns to a different terminal), then additional elements of Trip Times and Distances need to exist in the database.
The Trip Time and Distance from the First (or starting terminal) to the Second (or loading terminal)
The Trip Time and Distance from the Loading Terminal to the Station for delivery
The Trip Time and Distance from the Station to whatever Terminal the truck will return to
As you can see, any additional location that is added to a trucks journey entails additional Trip Time and Distance information for the drive out and back to any other location on the journey. If this information is missing, you will receive this message.
To add Terminal-Customer trip time:
On the Customer Setup dialog box click View | Trip Times and Distances | Terminal-Customer…
To add Customer-Customer trip time:
On the Customer Setup dialog box click View | Trip Times and Distances | Customer-Customer…
T
o add Terminal-Terminal trip time:
On the Terminal Setup dialog box click Edit | Terminal-Terminal Trip Info…
Keywords: RSO, Resource Scheduling Optimization, manual fit
References: None |
Problem Statement: I have exported my Aspen HYSYS SM model to EO, but the EO tab is locked up. Why? | Solution: When the EO (Equation Oriented) sub-flowsheet is opened by right-clicking on the EO icon, the EO tab in the sub-flowsheet will be locked up, as shown in the images below:
To enable the EO tab in the sub-flowsheet, the user must double-click on the EO icon and click on the ‘Sub-Flowsheet Environment’ button. The EO tab will be enabled.
Keywords: Equation Oriented, Sub-Flowsheet, Locked, Tab, Enabled.
References: None |
Problem Statement: I had a customized crude library (System Crude Library) created on an older HYSYS version. Now, I migrated to a newer version of HYSYS. What are the steps to restore my old library on the newer HYSYS version? | Solution: The location where you can find the UserAssayLibrary.aal file (where the customized library is automatically stored) is:
C:\Users\USERNAME\AppData\Local\AspenTech\Aspen Assay Management\Vx.
Then, you can move to the folder of the newer version and replace the default *.aal file with the old one.
Remember that HYSYS can only store one single UserAssayLibrary.aal file and because of that you can only have one single System Crude Library.
Keywords: aal, RefSYS, Petroleum Assay, Import Assay, Library, customized
References: None |
Problem Statement: Which gas bed discretization method is recommended for highly nonlinear adsorption cases? | Solution: For highly non-linear adsorption phenomena and where breakthrough curves are very steep, the recommended discretization methods are: Biased Upwind Differencing Scheme (BUDS) and Flux Limiter. These two discretization methods handle near equilibrium behavior which happens in highly nonlinear adsorption cases.
The options are in Gas Bed > Configure > General form:
Key Words
Discretization, Non-linear, Isotherm
Keywords: None
References: None |
Problem Statement: Suppose the following conversion reactions have been added to a reaction set:
R1) A + B ==> C + D
R2) F ==> B + G
If the reactor feed contains only A and F, reaction R1 will not take place unless some B has been produced via reaction R2. It appears that HYSYS calculates R2 first followed by R1, thereby evolving C and D. I would like reaction R1 to solve first, followed by reaction R2. How can I specify the order in which HYSYS calculates a set of conversion reactions? | Solution: If you manually rank each reaction, you can dictate the order that HYSYS uses to calculate overall conversion. By default, HYSYS will automatically assign a rank to each reaction in a set by examining the dependencies that exist between reactants and products. To override the default behavior, view the desired reaction set and click on the Ranking button. You can then use integer numbers to assign a priority to the reaction; the higher the rank number, the later the reaction will take place.
Keywords: conversion, reaction, priority, rank
References: None |
Problem Statement: What is the maximum number of connections to an Aspen Cim-IO server? | Solution: The Aspen Cim-IO Core limits each program to 128 connections to a Aspen CimIO server. Note; Prior to Aspen Cim-IO v10.1 the limit was 64 connections.
If the maximum number is reached the following message appears in the CIMIO_MSG.LOG file.
CIMIO_MSG_CONN_FULL
Multiple connections are typical with Aspen Cim-IO configurations. Each Aspen Cim-IO client task and service associated with the logical device will make a connection to the Aspen Cim-IO server.
Note: This is a Aspen CIM-IO Kernel limit, therefore it applies to any Aspen CIM-IO Server
Keywords: Maximum connections
CIMIO kernel
CIMIO_MSG_CONN_FULL
References: None |
Problem Statement: What is the compatibility of Aspen Capital Cost Estimator with Primavera P6? | Solution: The Icarus Project Scheduler (IPS) requires the installation of Primavera P6 Professional Project Management software. The following table list the current compatibility:
Aspen Economic Evaluation Primavera P6
V8.6, V8.8, V8.8.2 Primavera P6 Professional 8.2
V9, V9.1, V10, V10.1 Primavera P6 Professional R15.2
Refer to the following article to troubleshoot the Primavera P6 Link: I am having problems with my installation link between Economic Evaluator and Primavera; what can I do?
For further information, see the related Primavera installation documents on Oracle's website: https://www.oracle.com/mx/applications/primavera/products/project-management.html
Keywords: Primavera P6, Oracle, Icarus Project Scheduler.
References: None |
Problem Statement: _TANKS table value does not match with the TNKINV value of the tank inventory, is this a defect? | Solution: This is by design,
If the inventory volume is greater than 0 and less than 3.21e38f then the starting volume of the tank is the value specified in the TNKINV table and the weight is calculated.
Else if the weight of the tank in the inventory table is greater than 0 and less than 3.21e38f then the starting weight of the tank is the value specified in the inventory table and the volume is calculated from the weight.
Else the volume is set to the trace volume in the config table and the weight is set to 0.
When publishing trace volume means a publish value of 0.
Note: Config table entry PUBLISH_AT_10_SEC with a value of Y will help to publish the simulated values at 10 seconds for the initial values in table _TANKS. You can find information of the uses of PUBLISH_AT_10_SEC in the following KB Articles:
Why are the published data for derived properties wrong at model start date? https://esupport.aspentech.com/S_Article?id=000032436
Is there a way to force publishing of day 0 to be done after POST sheet in APS?
https://esupport.aspentech.com/S_Article?id=000014797
Keywords: None
References: None |
Problem Statement: Why do I see XAML naming error when I register extensions with a specific name (i.e. satu$rate.dll)? | Solution: Aspen HYSYS shows XAML naming erros (and even sometimes crashes) because V10.0 can only handle alpha-numeric characters when constructing an XAML name (based on DLL name) as the Aspen HYSYS Palette was rebuild.
For example: extension with name satu$rate.dll or saturate.0.dll will show this problem. By changing the name to saturate_0.dll error is gone. Keep in mind that you need to change also all of the associated files similarly.
On the following link you can read more about extensions What are extensions and how do I create them?
Keywords: Palette, alpha-numeric characters, dll, XAML, customization, register, extension, EDF
References: None |
Problem Statement: Does Aspen calculate shear-dependent viscosity for melted polymers? | Solution: The viscosity of melted polymer is usually very high, and it is a function of shear rate (shear thinning/shear thickening). Therefore, melted polymer is a non-Newtonian fluid. The shear effect on melted polymer viscosity needs to be considered when doing equipment design and rating, like heat exchangers.
However, Aspen Polymer does NOT correct melted polymer viscosity to shear rate. It only calculates zero shear viscosity using equations like Mark-Houwink and van Krevelen. Therefore, it is the user’s responsibility to calculate or measure the polymer’s viscosity under shear.
If you are using Aspen Plate Exchanger, you have the option to customize the physical properties for non-Newtonian fluids like polymer. But Aspen does not automatically generate it, and you'll have to manually specify the parameters like the non-Newtonian K value and n value. For more details, please read this KB article: https://esupport.aspentech.com/S_Article?id=000044642
Keywords: Polymer viscosity
Non-Newtonian fluid
Shear thinning
Shear thickening
References: None |
Problem Statement: When trying to write values with over eight digits into Aspen InfoPlus.21 the last digit is usually incorrect in the value written.
The precision problem is not actually a problem within IP.21 but with the conversion to a real value: IP.21 will save the value after a conversion to real was made at the computer chip level. This follows the IEEE (Institute of Electrical and Electronics Engineers) 754 standard, so the value is saved as a single-precision floating-point value, this is a 4 bytes (32 bites) value with 7 digit precision (the whole standard is available for download in the IEEE page here: http://ieeexplore.ieee.org/xpl/mostRecentIssue.jsp?punumber=4610933). The conversion process is well documented and it can b tested with online tools (like this http://www.h-schmidt.net/FloatConverter/IEEE754.html) to see the result of the an eight digit value conversion, basically it will be the same as the value displayed by IP.21. | Solution: To keep precision for values with more than 8 digits it is necessary to use a record which value field has been set to use a Double Precision Real value; IP_AnalogDef is not designed to work with this, but it is possible to create a custom definition record that accepts these values. Having this it is possible to have values up to 16 digits:
Here the record NumTypeTest belongs to a custom record made to show the precision for a single and double precision real value as well as signed and unsigned integer. Basically, the double precision real field will hold values up to 16 digits and then the conversion will throw unexpected values just as in the single precision eighth value. The integer value for records provided in IP.21 is a 16-bit values, so that the signed integer hold value from -32767 up to 32767 while the unsigned will hold values up to 65635 but only positive.
Keywords: InfoPlus.21
Double Precision
Single Precision
References: None |
Problem Statement: In the Aspen Plus manual Getting Started Modeling Processes with Solids, the following stoichiometry is used for coal drying:
COAL(wet) -> 0.0555084 H2O
Where is this particular number of 0.0555084 coming from? | Solution: Aspen Plus treats all non-conventional components as if they have a molecular weight of 1.0. The reaction indicates that 1 mole (or 1 lb.) of coal reacts to form 0.0555084 mole (or 1 lb.) of water. Therefore, 0.0555084 is coming from 1/ 18.01528 (the molecular weight of H2O). It's used to keep the mass balance.
Keywords: Modeling Processes with Solids
Stoichiometry
Mass Balance
References: None |
Problem Statement: How to modify the exchanger weight that is used for Lift Lugs calculations? | Solution: Shell & Tube Mechanical designs each lift lug to lift the entire vessel. So, 2 lift lugs are designed for 2X the vessel weight, 1 lift lug for 1X the vessel weight, etc.
Even when the program calculates the vessel weight, this can be overwritten to account for any additional weight:
1. Go to Input | Program Options | Loads-Ext/Wind/Seismic/Weights/Ins/Den | Weights/Insulation, and enter the Exchanger weight empty you want to use in the calculations:
2. After the run, check the Results | Code Calculations | Lift Lugs. You will see your input was used for the calculations:
Keywords: Weight, lift lugs
References: None |
Problem Statement: How to vary the solid phase heat capacity in different nodes of the bed layer? | Solution: By default, Aspen Adsorption is going to use a constant solid phase heat capacity for the entire bed. However, since V9, we added a new feature to allow the customer to vary the solid phase heat capacity in different nodes of the bed layer from a user submodel. This allows the heat capacity to vary axially, and in a 2-D bed, also radially.
To use this option, please select User Submodel for Solid Phase Heat Capacity under the Energy Balance tab of the gas layer configure form.
Then use the gUserCps submodel to specify values for the heat capacity. Here is an example:
Model gUserCps
//Define parameters and variables
Layer_ID as IntegerParameter(1);
FDESet as IntegerSet([1:20]);
W(FDESet,ComponentList) as g_loading; //kmol/kg
C(FDESet,ComponentList) as g_Conc_Mol; //kmol/m3
T(FDESet) as Temperature_k; //K
P(FDESet) as Pressure; //bar
Cps(FDESet,ComponentList) as g_heat_capacity; //MJ/kmol/K
// Calculate solid phase heat capacity
/* Sample default to ensure problem remains square
Cps = 0;
*/
Keywords: Solid phase heat capacity
User submodel
References: None |
Problem Statement: This | Solution: frames on the Use Double and Single precision on IP21 and the effect related to DCS and DMC3 controller.
Solution
IP.21 will save the value after a conversion to Real made at computer chip level. This is following the IEEE 754 standard, so the value is saved as a single-precision floating-point value, this is a 4 bytes (32 bites) value with 7 digit precision (the whole standard is available for download in the IEEE page here:
http://ieeexplore.ieee.org/xpl/mostRecentIssue.jsp?punumber=4610933).
The conversion process is well documented, and you can test online tools (like this http://www.hschmidt.net/FloatConverter/IEEE754.html) to see the result of an eight-digit value conversion, basically it will be the same as the value displayed by IP.21.
So, if you want to keep precision for values with more than 8 digits you will need to use a record which value field has been set to use a Double Precision Real value, neither IP_AnalogDef or IP_SetDef is designed to work with this, so you will need to create a custom record for this value. Having is it possible to have values up to 16 digits:
Here the record NumTypeTest belong to a custom record made to show the precision for a single and double precision real value as well as signed and unsigned integer.
Basically, the double precision real field will hold values up to 16 digits and then the conversion will trough unexpected values just as in the single precision eighth value. The integer value for records provided in IP.21 is a 16-bit values, so that the signed integer hold value from -32767 up to 32767 while the unsigned will hold values up to 65635 but only positive. Also, please consider that IP_SetDef are no longer supported and they’re on IP.21 just to keep backward compatibility, it is recommended to changes the use of this records for IP_AnalogDef record.
Keywords: IP21, DMC3
References: None |
Problem Statement: I have an Aspen Properties Fluid Package using the Peng-Robinson EOS as the property package, but critical properties cannot be calculated for my material stream(s). Why? | Solution: The ‘Critical Properties’ analysis tool in Aspen HYSYS can only be used when users set up a HYSYS Fluid Package with either the Peng-Robinson or SRK cubic EOS, as shown on the images below:
So, if the Fluid Package is an Aspen Properties one, even using either Peng-Robinson or SRK, the analysis will fail, and no results will be computed.
Keywords: Fluid Package, Property Package, Peng-Robinson, Aspen Properties, Critical Properties.
References: None |
Problem Statement: For the Continous Catalyst Reforming (CCR) reactor model, does the model assume any value for carbon on the regenerated catalyst (COR)? Would it be possible to study the effect of COR on the product spec? | Solution: The CCR reactor model basically assumes that the coke on catalyst is zero for the regenerated catalyst. How much would the COR vary? For the most part, it would be close enough to zero to not matter, but if users want, they can shift to specifying the coke-on-catalyst (COC) for reactor 1 and add whatever value available for the COR, since such value will be calculated assuming that there was zero COC at the inlet of the reactor.
Keywords: Carbon, Regenerated Catalyst, Continous Catalyst Reforming, Reactor, COC, COR, CCR.
References: None |
Problem Statement: Which heat capacity ratio should be used for API relief calculations? | Solution: We advise the use of the Ideal Gas Cp/Cv method if doing the analysis in the Aspen HYSYS V10 Safety Analysis Environment. In fact, the Ideal Gas Cp/Cv was added to the stream properties view just for this purpose (i.e. facilitation of relief valve rating calculations using the Ideal Gas Cp/Cv), as shown in the image below:
Keywords: Heat Capacity Ratio, Ideal Gas, Cp/Cv, API, Relief Calculations.
References: None |
Problem Statement: In Aspen Plus Dynamics, how can I know what are the names of both the PV and OP variables of a controller? | Solution: To know the PV and OP variables of a controller in Aspen Plus Dynamics, just right-click on the inlet and outlet signal streams of the controller and go to the Forms | AllVariables sheet. The inlet signal stream will show what is the PV and the outlet signal stream the OP, as shown on the images below:
Keywords: Controller, PV, OP, Signal Stream.
References: None |
Problem Statement: I recursed compositions for C4M in upstream submodel and created depooling structure as below.
Why do I get error ' *** Error. Distribution of XXX to YYY in ZZZ is not Permitted'? | Solution: The error is related to the structure of error distribution and PDIST table.
There is a pool, C4M in the PIMS model.
The compositions for C4M are recursed with the recursion row, RC4UC4M and RC4IC4M.
And they will be used by E-row, EC4UC4M and EC4IC4M in depooling structure.
But this is not permitted because the last 3 characters of E-row is same as the pool tag.
The error distribution coefficients are defined by table PDIST, even if not defined by user, PIMS automatically generate PDIST internally.
The column name of PDIST is pool tag and row name is the destination that is the last 3 characters of row name.
The row names in PDIST must be different from the pool tag.
For example;
----- This is not permitted.
If I change the row name to EC4UALK, the PDIST is,
----- This is OK.
So you should rename the last three character of the row in depooling structure, it is recommended to use the submodel tag, if possible.
Keywords: Error distribution, E-rows, depooling
References: None |
Problem Statement: For a compressible fluid the velocity at the outlet of pipes is always greater than the velocity at the inlet. Why? | Solution: In compressible pipe flow this behavior is expected due to the following:
1) Velocity rises along the length of the pipe as density decreases when the fluid is moving from higher to lower pressure.
2) Temperature decreases because internal energy gets converted into kinetic energy (as velocity increases).
Keywords: Compressible, Velocity, Outlet, Inlet, Pipe, Density, Pressure, Temperature, Internal Energy, Kinetic Energy.
References: None |
Problem Statement: What is Aspen Hydraulics and how does one use it? What features of Aspen Hydraulics are currently available in Aspen HYSYS Upstream? | Solution: Aspen Hydraulics enhances the pipeline simulation of pipes and pipeline objects like junctions, mixers, swages, and valves within Aspen HYSYS. Pipeline and hydraulic network simulations can be solved in Steady State mode or Dynamic mode on a single network, with the ability to switch between the two modes and also switch between solvers.
In Dynamic mode (transient multiphase flows), theSolution engine solves mass, momentum and energy equations for each phase using a one-dimensional finite difference scheme. Appropriate flow pattern maps and constitutive relationships are provided for wall and interfacial friction as well as heat transfer, and a model for multi-component phase-change is included.
The subflowsheet for Aspen Hydraulics can be added directly from the Flowsheet menu bar. Choose Flowsheet | Add Operation from the main menu (or click F12) then use the Upstream Ops filter to select Aspen Hydraulics Sub-Flowsheet. Once added, the options available within the Aspen Hydraulics subflowsheet are exactly the same as the those available in the HYSYS PFD property view. The only difference between the standard HYSYS PFD and the Aspen Hydraulics PFD is the reduced number of unit operations available in the latter.
The solver method to be used in steady state is shown on the Steady State tab as in the figure below:
The solver control table is used to modify the parameters for the numerical solver. These parameters affect the calculation time and converged values.
The Dynamics tab enables us to configure the solver options used to solve the Aspen Hydraulics flowsheet in dynamic mode.
For more information, refer to the Aspen HYSYS Help guide.
An steady state Aspen Hydraulics example (V8.8) is attached to thisSolution. In this example four streams are entering the flow network and pressure at the end of pipe line is specified. The flow in each loop is calculated.
A second example is attached that can be run in dynamics mode. In this model, the Aspen Hydraulics unit operation is AH-100.
Note that an Aspen HYSYS_Upstream license is needed in order to use Aspen Hydraulics.
Keywords: Aspen Hydraulics Example, pipe segment, HYSYS Upstream
References: None |
Problem Statement: How to resolve the error message “unable to validate server response. HTTP code:510” in A1PE? | Solution: When trending some tags in A1PE, user might get the following error message.
To resolve this error, please follow the below steps.
Launch AspenONE Credentials as shown below
2. Disable Domain Security and hit Apply as shown below
Keywords: HTTP code: 510
A1PE
References: None |
Problem Statement: How to force liquid entrainment in vapor line in case of pressure relief scenario? | Solution: By default, vapor port connected to any vessel (like flash tank, reactors) only allows vapor flow through it. But in some cases, specially pressure relief scenarios, swollen liquid may also need to be pass through vapor line.
To enable this option, please right click on vessel to access Forms > Configure > Vessel
And check the following option :
Once this option is selected, overfilled liquid in vessel will flow thorough relief valve once set pressure is reached.
Key Words
Overpressure, Liquid, Disengagement
Keywords: None
References: None |
Problem Statement: What is the difference between heat exchanger and LNG exchanger in Aspen HYSYS? | Solution: Below is the difference between heat exchanger and LNG exchanger on HYSYS:
Heat Exchanger:
- Used to model heat transfer between two process streams (hot & cold).
- Select preferred Heat Exchanger Model depending on required simulation detail.
- For rating calculations to calculate heat transfer coefficient and pressure drop, exchanger geometry must be entered.
- Aspen EDR rigorous modelling software can be accessed through Heat Exchanger.
LNG Exchanger:
- LNG Exchanger can be used to represent heat transfer between multiple hot and cold streams.
* Note: LNG Exchanger can also be used for two-stream heat transfer.
- Various heat transfer specifications can be provided: outlet temperatures, UA, temperature approach, etc.
- TwoSolution approaches:
* For single unknown, exchanger energy balance is computed.
* For multiple unknowns, iterative calculation is used to satisfy energy balance and any exchanger specifications.
- Can be integrated with Aspen Plate-Fin Exchanger for rigorous rating of a wound-coil type heat exchanger
Keywords: Aspen HYSYS, Heat Exchanger, LNG Exchanger
References: None |
Problem Statement: How to initialize RCSTR with padding gas? | Solution: RCSTR can be initialize with a padding gas for specified reactor pressure. To enable that Please select the Configure form > Hold up > select “Pad Component”
Then Check and specify initial Pressure. Once complete, please run the “Initialization” mode.
Key Words
Initial, Padding gas, Pressure
Keywords: None
References: None |
Problem Statement: What is the difference between pump efficiency and driver efficiency? | Solution: When specifying a pump, you will see two efficiencies. One is the pump efficiency, and the other one is the driver efficiency.
Pump efficiency is the ratio of the fluid horsepower to the brake horsepower. It includes the effects of slurry characteristics, frictional losses in seals, capacity losses due to seal flushing and bearing losses.
Driver efficiency is the ratio of brake horsepower to electrical horsepower. It includes the losses in the electric motor.
When calculating the overall efficiency, you should include both pump efficiency and driver efficiency.
Keywords: Pump efficiency
Driver efficiency
Fluid horsepower
Brake horsepower
Electrical horsepower
References: None |
Problem Statement: Why excel files are being unattached and PIMS model file (pimx file) is deleted, and how can I solve it? | Solution: The excel files are not attached in the model when opening the pimx file because PIMS cannot read the pimx file. This pimx file is an encrypted, xml file.
Please install Microsoft's KB updates: KB954430 and KB973688 or get the MSXML 4.0 DLL from another machine to copy to the problematic machine.
Keywords: None
References: None |
Problem Statement: Can EDR Air Cooler model condensation on the outside of the tubes? | Solution: As stated on the Help Guide, the program does not calculate outside condensed liquid when Gas (property specified or from Databank) is selected for Outside tube application. The program can calculate outside condensed water only when Humid Air option is selected, and even then, it will not report an outside liquid phase flow.
However, there is a potential workaround via using Shell & Tube thermal to model this application by setting up a Shell & Tube case using an X-type shell (cross flow). Each Shell Side inlet represents one Air Cooler bay.
Attached example has 2 Shell Side (outside on the Air Cooler model) inlets, so it can be interpreted as 2 Air Cooler bays. The process fluid on the Shell Side is a mixture of gases that represents the Air Cooler outside stream (Gas or Humid Air).
Please see the attached EDR file.
Keywords: EDR, Air, Cooler, Condensation, Outside, Shell
References: None |
Problem Statement: Why are the MIP threshold values for a product not being honored? | Solution: This Tech Tip explains why sometimes it looks like the MIP threshold values for a product are not being honored and how to attend this issue.
To do the following demonstration we used the Demo model located in C:\Users\Public\Documents\AspenTech\Aspen Petroleum Scheduler\Demo\Access, we will use all the components of the product U87, and the blend event 227.
1. Select the threshold values as in the picture by going to Menu Model|Products
2. Open Blend event 227, then go to Optimizer and check the option MIP Recipe, note that this event has the option Fixed Recipe enabled, if this option is enabled the threshold value will not be respected, you can note that the Optimize NLP button is greyed, also note that when you select the option MIP Recipe the value that is not being honored turns red.
3. Once the Fixed Recipe option has been unchecked the Optimize NLP button will be enabled.
4. Once you click on the Optimize NLP button the threshold value will be honored and the red message Blend Composition: At Least One Spec Not Met: will be gone also the BUT component will be in black colored text.
Keywords: None
References: None |
Problem Statement: How do I calculate/report the Combustion Temperature of a fuel stream? | Solution: The Combustion Temperature is not reported in Aspen HYSYS as a default variable/property. However, you can obtain the combustion temperature from the flue gas of a fired heater model. The flue gas temperature is calculated by combusting the fuel streams with the air stream and transferring a percent (determined by the specified efficiency, which can be zero) of the energy released to the process fluid.
To get the combustion temperature for a stream using the fired heater, do the following:
Connect the stream (for which the combustion temperature is to be determined) as the fuel inlet to a fired heater
Set up any arbitrary inlet/outlet streams for the process fluid.
Connect an 'air' stream of almost pure oxygen with a very small amount of nitrogen (the fired heater expects there to be some non-zero amount of nitrogen in the air stream, but this can be extremely small). Do not specify a flow rate.
On the fired heater Design/Parameters page, specify zero efficiency and zero excess air percent, so that it uses just the stoichiometric amount of oxygen to burn the fuel and there is no heat transfer to the process fluid.
The combustion temperature is the reported temperature of the flue gas/combustion product
Keywords:
References: None |
Problem Statement: I would like to track the erosion rate for the whole pipe network in a Hydraulics subflowsheet, similar to what I see in pipe segment. How do I accomplish this? | Solution: Unfortunately there is no direct way to show the overall erosion rate as in a pipe segment. There are three options we can use to get this:
1.- Get the report for each pipe. Enter to the Hydraulics subflowsheet, and fro each pipe select the Flow Assurance tab where you can sactivate the Erosion Speed analysis.
2.- We can build a table to report erosion rate for all the pipes. Inside the Hydraulics property view, select the Variables tab and add the variable Pipe Erosion Rate for each segment. Unfortunately, there is no way to graph the data with this option. It is necessary to send the data to Microsoft Excel.
3.- To keep the data updated, we can make use of Aspen Simulation Workbook (ASW) (for more information, please refer to thisSolution Jump Start: Aspen Simulation Workbook in Aspen Plus V8) and call the variable Pipe Erosion Rate for each segment. In this option you can graph the performance using Microsoft Excel capabilities.
Keywords: Erosion rate, ASW, Microsoft Excel, Upstream, Flow Assurance, plot
References: None |
Problem Statement: When running the Icarus Excel reports, a message pops up referring to an Excel Report Header Error and/or the named range does not exist in the template | Solution: These error messages may come up for one of the following reasons:
1. If you use or have modified the Reporter_User.accdb file (found in C:\Program Files (x86)\AspenTech\Economic Evaluation VX.X\Program\Sys\Reporter\Database). Where VX.X represents your current version.
If a new Excel report was added in 'Stored Reports' table (within the Reports_User.accdb) without any corresponding modification to 'Stored Queries', when you run the Aspen Icarus reporter, you will receive an error message display: There is no stored query for the report ....... and There is no data for the report .....
2. Validate Named Range: Check to see if a named range is deleted in the report template. If that report is run, an error message would display indicating that the name range is missing.
Please check your template (found in C:\Users\Public\Documents\AspenTech\Shared Economic Evaluation VX.X\Reporter\Templates).
The error message will point to the template sheet where the issue could be generated
3. One of your installed applications (Microsoft Office), corrupted some of the Microsoft Excel .dll files, which won’t allow the report to be generated.
Uninstall Microsoft Office and reinstall. Download and install all patches and service packs for Microsoft Office from the Microsoft web site.
Keywords: Excel, Template, Error 430, Error 91, Icarus, Reports, Reporter, Header, Named range, Column header
References: None |
Problem Statement: How can whole crude property update process in the EIU be simplified? | Solution: In order to import Assays information you can use EIU, the import process is described in kb article How do I add new crudes to APS model?, this can consulted in the following link: https://esupport.aspentech.com/S_Article?id=000014626; this process requires additional clean up with Whole Crude Data worksheet.
To simplify the previous process, you can use the attached EIU workbook, that contains a VBA macro to extract crude names and whole crude properties from the assay file, follow the next steps to use it:
Copy your assays PIMS model table into the OUTPUT worksheet, make sure there are no spaces in column A until the end of the file. The macro sees spaces as an indication of the end of the file.
In WholeCrudeProps worksheet, create map of whole crude property (WCP) name with the row number in the OUTPUT worksheet corresponding to the WCP. This gives you control of which whole crude properties to load from the assay file.
Go to PIMS_ASSAY_XREF worksheet and click on Update APS Assay Sheets
Note
The Knowledge Base examples are provided for academic purposes only and as such are not subject to the quality and support procedures of officially released heritage-Hyprotech products. Users are responsible for the implementation and maintenance of this macro, therefore we strongly encouraged to check performance and results carefully and, by downloading, agree to assume all risk related to the use of these examples. We invite any feedback through the normal support channel at [email protected].
Keywords: None
References: None |
Problem Statement: How can I model a rate-based packed tower in Aspen Plus? | Solution: When modeling distillation towers, equilibrium stage efficiencies are sometimes employed to account for the fact that the amount of mass transfer between liquid and vapor phases may not be sufficient to result in thermodynamic equilibrium being reached. While utilizing equilibrium stage efficiencies can be useful, the efficiencies are functions of column conditions (flow, temperature, pressure, etc.) and generally do not extrapolate well to other conditions. On the other hand, rate-based distillation models, once calibrated to one set of conditions, generally extrapolate better to other conditions than columns utilizing equilibrium efficiencies. Rate-based models utilize mass and heat transfer correlations and tray/packing geometry to more rigorously predict column performance. The attached file includes a Methanol-Water distillation column with 1.5 in Pall packing.
Notes:
The Aspen Plus Resources tab provides the access to a number of additional examples of rate-based distillation distillation (e.g. the CO2 capture process by MeOH from a gas mixture of Methane, H2, CO2, CO, N2, COS).
Keywords: mass transfer
transport
internals
rigorous
References: None |
Problem Statement: How do I prevent the “Results Warning 1527: The HTFS Condensation Mass Transfer method failed, or was applied to an inappropriate system. The program used the default method (Silver-Bell) for the gas-phase resistance in condensation”? | Solution: From Input Program Options | Method/Correlations | Condensation | Condensation heat transfer model, there are two options:
HTFS – Silver-Bell: is the standard method for mixture condensation or condensation from a non-condensing gas in Shell&Tube, is an adaptation by HTFS of the Silver (Bell and Ghaly) method
HTFS – Mass Transfer: an adaptation of the Colburn-Hougen method for condensation of a vapor from a non-condensing gas. This is a mass-transfer model which requires additional data relating to the diffusion coefficient, or properties from which it can be calculated. The method is used with the integral condensing curve which you supply (or which Shell&Tube calculates). This method as implemented in Shell&Tube will not provide additional information on the distribution of components between the liquid and vapor phase.
Note: The standard Silver-Bell condensation method in Shell&Tube does not model the mass transfer effects explicitly, but incorporates an additional thermal resistance relating to the vapor phase, which has a comparable effect on the overall heat transfer
The HTFS – Mass Transfer condensation method can only be used for a binary mixture with one liquid phase present in the fluid. Otherwise, the Silver method will be employed. If the HTFS – Mass Transfer condensation method is selected and the diffusion coefficients are not available for the components, or the number of components exceeds the two then warning 1527 is displayed and the Silver-Bell method will be selected by the solver.
Note: While using the Activated EDR feature within Aspen Plus/HYSYS, the HTFS – Mass Transfer method cannot be used, since it needs Pure Component properties, and the data gotten from the simulators is considered as User specified properties.
Keywords: Warning 1527, HTFS condensation method, Silver-Bell, Colburn-Hougen.
References: None |
Subsets and Splits
No community queries yet
The top public SQL queries from the community will appear here once available.