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Problem Statement: The values of mass exergy reported for a stream are different than the ones the user is expecting. | Solution: This is most likely due to different reference conditions in the calculation. Even though for certain properties Aspen HYSYS uses 15 deg C (60 deg F) as the reference temperature, exergy uses by default a value of 25 deg. C. To change this, access the Correlation manager and set the desired values of temperature and pressure for the reference state.
The definition of exergy follows the expression described in KBSolutions 3384 and 109771.
Keywords: Exergy,
References: , Correlation Manager |
Problem Statement: Which Fluid Package in Aspen HYSYS do I use to model a system with Methyl-Mercaptan and Ethyl-Mercaptan with a set of light hydrocarbons? | Solution: A significant amount of work has been conducted in exploring the Vapor-Liquid Equilibrium (VLE) data between Mercaptan and Hydrocarbon mixtures. Denyer et al (1949) studied the azeotropic effect of Mercaptan and Hydrocarbons and Lee et al (1978) explored VLE data for H2S and light Mercaptan binary systems.
The paper by Twu et al. (2004) demonstrates the complexity involved modelling a Mercaptan and Hydrocarbon system. The work Twu was originally implemented in Aspen HYSYS as the clean fuel property package. The fundamental equation of state was implemented fully in the glycol fluid package. The Glycol fluid package has fitted parameters for Methyl Mercaptan and Ethyl Mercaptan with light hydrocarbons. The user should investigate the results with the glycol package for Methyl/Ethyl Mercaptan with Hydrocarbons. Users are still advised to use their own engineering judgment to decide whether the simulation results are reasonable for the process that is being modelled. Comparing the results with the plant data will always be the recommended practice.
Keywords: Mercaptan, Twu
References: s
1. Denyer, R.L., F.A. Fidler, and R.A. Lowry (1949), “Azeotrope Formation between Thiols and Hydrocarbons”, Ind. Eng. Chem., 41, pp. 2727-2737.
2. Lee, J.I., A.E. Mather, F.D. Otto (1978), “Vapor-Liquid Equilibria in the System Hydrogen Sulfide-Methanethiol”, J. Chem. Eng. Data, 23, pp. 78-79.
3. Twu, C.H., W. Tassone, and W.D. Sim (2004), “Accurately Predict the VLE of ThiolHydrocarbon Mixtures”, Chem Eng, Prog., 100 (9), pp. 39-45 |
Problem Statement: How can I minimize some objective functions, while maximizing others in the same Optimizer problem? | Solution: The individual items of the objective function are included in the Derivative Analysis associated with the optimizer. Some items may be associated with cost and some with revenue. The differentiation of cost and revenue items are done by the parameter called “Price” providing positive or negative value. A negative value can be entered for cost items and positive for the revenue items as illustrated in the screenshot below.
If the value for this parameter is positive then the function will be minimized or maximized according to what is defined in the Optimizer menu shown below (in this case, maximized)
.
If the value for Price is defined as negative, then the objective for that particular function will be the opposite of the one defined in the optimizer menu above (in this case, minimized).
Keywords: SQP Optimizer, Objective functions, Derivative Analysis
References: None |
Problem Statement: What are the various password security features available in Aspen HYSYS? | Solution: 1. Flowsheet Locking
The user is able to lock the process flow diagram (PFD) or a sub flowsheet. While it is locked they will not be able to create or delete model objects or change the topology. The user will be able to add certain logical operations such as set and adjust and use the spreadsheet function.
In order to lock a flowsheet in V8 and above, open the simulation case (crtl-m) and navigate to the locked tab. Enter a password. It is only possible to unlock the simulation if the user now re-enters the password. A screen shot showing where the user can enter the password is shown below:
It is possible to lock a sub-flowsheet. A similar operation can be conducted by double-clicking on a sub-flowsheet and defining the password in the lock tab.
2. File Access
You can also protect your file so that only authorized people can open the simulation. To access the case security option, click the arrow on the bottom right corner of the case group found in the home ribbon tab in V8.0 or in the customize tab in V8.4.
Through the case security option it is possible to lock the entire HYSYS case and set an expiration date for the user password. A step by step guide for the security option is documented in the Aspen HYSYS On-Line Help under ‘Case Security.’
WARNING: Please note that customer supports are unable to unlock or provide the password for protected cases. These functionalities are used at HYSYS user’s own risk.
Keywords: HYSYS Security, Flowsheet Locking, File Access
References: None |
Problem Statement: I have a 2 phase feed (a vapour phase and a 'water-containing' liquid phase) to my 3-phase separator. Why is Aspen HYSYS treating this liquid phase as a non-aqueous phase in my 3-phase separator? | Solution: By default (from version 7.1), for a liquid phase to be considered 'aqueous', EITHER of the two (2) conditions below has to be TRUE:
- If the mole fraction of the water is greater than 0.5 OR
- If the mole fraction of water is less than 0.5 but greater than the total hydrocarbon fraction
However, this 'aqueous definition' can be changed by the user from the Properties environment. With the fluid package selected, navigate to the “Phase Order” tab.
For a single liquid phase system (i.e. a system that can be single or two phase, but with only one liquid phase), the 'water-containing' liquid phase can be defined as 'aqueous' by selecting the Legacy Criteria from the Aqueous Phase Definition Criteria. See screenshot below.
Additionally, within this tab, the user has even more flexibility in setting their own criteria for what is deemed a liquid (non-aqueous) or an aqueous phase if they select the “Use User Specified Primary Components” option from the “Phase Sorting Method”. The user can set the components that constitute the aqueous and non-aqueous phases, as well as the limit for the sum of those component fractions that dictate whether the liquid is classed as aqueous or non-aqueous. See screenshot below.
Keywords: Aqueous, single liquid phase,
References: None |
Problem Statement: Whenever I try to vary the composition of a stream in a Case Study, the “Input Composition for Stream” window pops up as I run the case, and even when I click on OK the composition is still not modified in the results of the analysis. How do I fix this? | Solution: To modify the composition of a stream through a case study, you must use a Spreadsheet.
1. Define your stream of interest (Temperature/Pressure/Vapor Fraction Flow and Composition) add the spreadsheet to the simulation.
2. Within the spreadsheet go to Spreadsheet tab and in any column (i.e. column B) input the value 1 for as many components you have (for this example there are only 3 components) and in another column make equal to the one input value of the first one. (In this case A1 =B1, A2=B2 and A3=B3)
3. Go to connections tab and click on Add Export. Select your stream then Master Component Mole Frac and then all your components.
4. Once you have added all the components you will see that the cells assigned to them new cells. Select the dropdown arrow and match them to the cells containing the equation.
5. Create your case study and when you add the component fraction, instead of using master component of the stream, use the spreadsheet. Selecting the cell with user input values (in this case B1, B2 and B3)
6. Run your Case Study and the composition will vary through the different scenarios accordingly, without a problem.
Keywords: Spreadsheet, Case Study, Composition
References: None |
Problem Statement: When you right click on an unit operation and select Print Datasheet, the datasheet preview shows that the unit set is different to the current unit set showed in the flowsheet and workbook. | Solution: The unit set used for the datasheet can be modified using the Format / Layout button.
The default unit set is <Current>. However, this can be customized only for printing purposes.
Keywords: print, datasheet, unit set
References: None |
Problem Statement: Why does reactor appear to be solved (“OK� status and exit streams blue) when it has not? | Solution: This is because Aspen HYSYS activates (by default) the ‘Act as a Separator When Cannot Solve' checkbox to operate the reactor as a simple 2 phase separator whenever the reactor is not solved. This checkbox is only available for Conversion Reactors, and can be deactivated if you want HYSYS to report ‘not solved' when the reaction part has an error.
Keywords: Reactor, Separator
References: None |
Problem Statement: How to get transport properties (e.g. density, viscosity) from each tray in the column. | Solution: Transport Properties information for each tray comes under column performance tab.
Go to the column << performance << plots and select transport properties and say view table.
Keywords: Column, Tray , Transport Properties, Density, Viscosity, Performance, Plots
References: None |
Problem Statement: How do I set the default shutdown duration? | Solution: The default shutdown duration is determined by the combination of values for Minimum Lot Size and Process Time for Shutdowns in the table TDAT.
The Minimum Lot Size parameter should be set to the physical lower limit or the minimum volume that might be run between setups.
Process Time defines the amount of time required to complete the operation.
For more information on these parameters, please see the Aspen SCM Online Help files included with the product.
Keywords: EMBEDDED SHUTDOWNS
PLANNING BOARD
MAIN
References: None |
Problem Statement: How to get Gas Properties in Hysys Workbook tab? | Solution: Gas Properties (and other property values in Correlation Manager) can be retrieved on Workbook tab by selecting the Calculator option from the workbook SetUp àSelect Variable(s) ForMain option. See the following snapshot for the location of the same.
Keywords: Workbook, Gas Property
References: None |
Problem Statement: What is the Off-Design Correction option inside the compressor? | Solution: Two parameters can be entered for performance curves: Design Temperature and Design Molecular Weight. A screenshot showing this addition within the compressor form is shown below:
When these are supplied, HYSYS corrects the characteristic curves to the equivalent/corrected curves at operating conditions. To do so, design speeds, design head values and design flow rates entered in the curves are corrected to equivalent operating speeds, operating head values and operating flow rate values based on the quasi dimensionless equations shown below. In order to build the corrected characteristic curves, each data point (flow rate, head, speed) is corrected according to the following quasi-dimensional expressions:
1-Corrected volume flow in compressor characteristic curves
Where:
Tref = Temperature at reference/design conditions
MWref = Molecular Weight at reference/design conditions
Qact = actual volume flow in the curve
Qcorr = corrected volume flow in the curve
2-Corrected head in the compressor characteristic curve
Where:
Hcorr and Hact are the compressor's corrected and actual Head value in the characteristic curve.
3-Corrected Speed in the compressor characteristic curve
Where:
Ncorr and Nact are the compressor's corrected and actual speed in the characteristic curve.
Off-Design Corrections are supported in both steady-state and dynamics. Off-Design curve correction is not applied when you have a single curve and at this condition fan laws will be applied.
Keywords: Compressor Curves, Performance Map, Off-Design Correction
References: s
Dr. Meherwan P. Boyce , Centrifugal Compressors: A Basic Guide, PennWell Books
Chang, H. and Wu, C., ‘Corrected maps narrow Compressor performance prediction range’ Oil and Gas |
Problem Statement: I am converting a file from PROII to HYSYS. Where are the property packages defined in the PROII input file? | Solution: It is possible to use the PROII to HYSYS Convertor to change the simulation into a HYSYS file. Inside the PROII input file the property package is specified under the section entitled the Thermodynamic Data. An example from the PROII input file is found below:
THERMODYNAMIC DATA
METHOD SYSTEM=PR, TRANSPORT=PETR, MEOH=OFF, SET=PR01
WATER DECANT=ON, PROPERTY=SATURATED
METHOD SYSTEM=SRK, TRANSPORT=PETR, MEOH=OFF, SET=SRK01, DEFAULT WATER PROPERTY=SATURATEDMETHOD SYSTEM=GS,
The property package that will be imported into HYSYS will be labelled directly after the method system. The PROII code above is PR and SRK which is Peng Robinson and Soave-Redlich-Kwong property package respectively.
Keywords: HYSYS, PROII, Converter
References: None |
Problem Statement: Why the lbf*ft/lbm units change back to ft when I choose them for the Head Units in a Compressor curve? | Solution: The automatically change of lbf*ft/lbm to ft units by HYSYS in the Head Units cell of a compressor is by design, and it is an expected behavior since they are essentially the same. It would be redundant to have these two units separately.
Let’s examine the head produced by a pressure difference of 50 lbf/ft2 in a system pumping water.
As it is shown in the final equation, the number 32.174 appears in two places, once in the numerator as part of the unit conversion from lbf to ft*lbm/s2, and secondly in the denominator as g, the acceleration due to gravity. Because these two factors are numerically the same, they cancel (the numbers cancel, not the units), and expressions having units of ft*lbf/lbm and ft of head are numerically the same.
That’s why when you select lbf*ft/lbm in HYSYS it turns into ft. They are the same.
Keywords: Compressor curve, lbf*ft/lbm and ft units of head
References: None |
Problem Statement: Are there any tools available to help me decide which property package to use in my simulation? | Solution: New in Aspen HYSYS 2006, the Property Wizard is available from the fluid package window as shown in the figure below:
The Property Wizard can be used to generate a list of potential thermodynamic models based on some general process information provided by the user.
Note that detailed information for each of the different property models can be found in the Aspen HYSYS Simulation Basis manual. A link to all product documentation can be found on the left pane of the Aspen support website.
Keywords: property, package, wizard, tools, model, thermodynamic, assistant
References: None |
Problem Statement: How are Slug Length and Bubble Length defined in the Pipe Segment Slug Tool calculations? | Solution: For a given two phase system, the Slug Length is the average length of the liquid pocket at the indicated frequency. The Bubble Length is the average length of the gas bubble at the indicated frequency. If the Slug Length is greater than the pipe length, then there is no slug flow in the pipe.
Keywords: slug length, bubble length, slug flow, slug tool
References: None |
Problem Statement: How do I model Wound Coil Exchanger using Aspen HYSYS? | Solution: Wound Coil heat exchangers (WCHEs) are required for a wide range of applications involving fluid treatment. They must support broad temperature and pressure ranges as well as single- and two-phase streams.
To model Wound Coil (or Spiral Wound) Heat Exchanger (WCHE) we use LNG unit operation in Aspen HYSYS, which translates the geometric configuration of a WCHE into an equivalent configuration in Plate Fin mode.
Please review attached Wound Coil Heat Exchanger guide for detailed step by step instructions.
Keywords: Wound, coil, exchanger, spiral.
References: None |
Problem Statement: Can Aspen HYSYS validate hydrate formation prediction when a free water phase is in equilibrium with a liquid hydrocarbon phase? | Solution: Liquid phase hydrate prediction is a known limitation in Aspen HYSYS. The Vapour model is currently deemed the most suitable model for predicting liquid phase hydrates. The liquid phase hydrate prediction results should be checked carefully and compared with literature or field data whenever possible.
Refer to the attachment for the validation results in Aspen HYSYS.
Keywords: Liquid Phase Hydrates
References: None |
Problem Statement: How can I ignore or unignore a unit operation through automation? | Solution: Unit operations in HYSYS have the property .IsIgnored:
· .IsIgnored = True will ignore the unit operation
· .IsIgnored = False will unignore the unit operation
Attached is a sample Excel file with code to demonstrate how to do this. It can be used with an active HYSYS simulation.
Keywords: OLE, VBA, checkbox, ignored
References: None |
Problem Statement: When using Aspen Properties for a HYSYS simulation, several questions arise regarding the possibilities, benefits and limitations.
· When should I create an Aspen Properties package from HYSYS?
· When should I create it in Aspen Properties and import it?
· Should I customize it directly from HYSYS?
· What are the limitations that Aspen Properties has in Aspen HYSYS interface? | Solution: Aspen Properties is commonly used to customize property packages: estimating data, adding non-databank components, performing regressions of parameters, etc. It also contains all of the most important databanks of pure components, allowing the creating of robust property packages for simulation.
Since Aspen Properties can be used inside Aspen HYSYS it is important to understand that there are differences between using Aspen Properties to create a package to import and creating the Aspen Properties package from Aspen HYSYS.
If you only want to use Aspen Properties components and do not want to make any changes to the fluid package, then you can create it directly from Aspen HYSYS. Just be aware that you should not be performing any changes after that to the fluid package since not all the Aspen Properties features are visible in Aspen HYSYS GUI.
Now, if you want to customize the property package, perform estimations, regressions or modify the routes of calculations, then you should be working directly in Aspen Properties. There you should prepare your package until it is ready to be used for the simulation. This should also be your option if you are using your own databases for components and properties. Once your property package is ready then you should save it in an .aprbkp format to import it to HYSYS. Again, once it has been imported, not changes should be attempted for this package from Aspen HYSYS.
There are several features from Aspen Properties that although they are used inside the calculations, the tables and options are not visible from Aspen HYSYS. Some of these features are:
· Binary Parameters Databank selection tab
· Routes and model modification options
· Pure and Binary Parameters used for NIST equations
If you observe any issue or have any concern while using an Aspen Properties package inside Aspen HYSYS, do not hesitate in contacting our support team so your doubts can be addressed.
Keywords: Aspen Properties, Aspen HYSYS, Property Packages, Parameters,
References: None |
Problem Statement: How can I modify stream names for internal streams? | Solution: By default, HYSYS takes the name of the external stream and automatically re-name the internal stream with the name of the external stream attached.
If you want to modify the name of the internal stream so you have different names for internal and external streams (one name inside the column environment and another name outside), you just simply need to go to the Column Environment, open the stream of interest and rename it as any other stream.
When you go back to the main flowsheet, you’ll see the new name for the internal stream
Keywords: Internal stream, Column subflowsheet, re-names a stream
References: None |
Problem Statement: On the PSV Line Sizing results how are the Maximum DP In Line and Out line values calculated? | Solution: By default the Maximum DP In Line is calculated as 3% of Set Pressure. This can be modified in the Line Sizing Limit Settings editor. Click on the Constraint Setting button in the Line Sizing tab to customize this option.
According to the Default Valve Settings, the Out Line result is calculated as 10% of Set Pressure for Conventional PSV, 50% of Set Pressure for Balanced Bellows PSV and 75% of Set Pressure for Pilot Operated PSV. To modify this values go to Customize tab on the ribbon and click on the Valve Defaults button.
Keywords: PSV, Line Sizing, Maximum DP, Valve Defaults
References: None |
Problem Statement: Why are the Print and Print Snapshot options disabled in the Aspen HYSYS File / Print menu? | Solution: This behavior only occurs when trying to print an input form/window when working inside the Safety Analysis environment. The reason of this is that the Safety Analysis includes the capability to print out all the information present in the input and result windows through the Documentation Builder and/or the Built-in HYSYS Reports.
It is important to point out that the PFD can be printed even when in the Safety Environment.Â
Keywords: PSV Pressure safety relief scenario PRD
References: None |
Problem Statement: Can I use Critical Properties Utility with Sour PR fluid package?
I see the following message “Utility Critical Properties is not available with the property package being used.� | Solution: The Critical Properties Utility was written based only on Peng Robinson. In part this is because only the PR equation of state applies a correction for the molecular attraction term which involves the acentric factor. Sour PR is actually a 2-part property package: the vapor is modeled by PR but the liquid is modeled using a version of Wilson's (Activity Model) equation. For this reason, the critical properties utility cannot calculate using Sour PR as the property package.
In order to determine the critical properties in this case, you could follow:
1. Switch a stream in the affected sections back to PR (probably will need stream cutters to do this) and generate the critical properties on the stream with PR as the fluid package. SeeSolution ID: 109686
2. Use the Property Table utility to estimate critical temperature and critical pressure. You can generate the bubble point and dew point curves in the Property Table utility. These curves do not necessarily meet at the critical point. However, they at least approach to each other and you can get an idea where the critical point should be. SeeSolution ID: 109318
Keywords: Critical Properties utility, Sour PR, Peng-Robinson
References: None |
Problem Statement: Customer is not able to load any Hysys model that uses PIPESIMLINK. Will Aspen HYSYS Upstream license enable the PIPESIM functionality? | Solution: Aspen HYSYS Upstream license alone will not enable the PIPESIM functionality on any version of Hysys. The following two licenses are required for PIPESIM functionality in Hysys V7.2 and V7.3 :
1. Upstream RN_PML_HYSUPSTRM_R3 license from AspenTech
2. PIPESIM license which has to be purchased from Schlumberger
For Hysys version V7.2, in addition to the above two licenses customer should also apply CP2 attached to followingSolution
http://support.aspentech.com/webteamcgi/SolutionDisplay_view.cgi?key=130557
For Hysys version V7.1 customer should upgrade to V7.2 or higher
Keywords: HYSYS
Upstream
PIPESIM
Functionality
License
References: None |
Problem Statement: How do I use automation to add or remove components from a simulation? | Solution: To modify the components used in a given case, you must either access a specific component list, or the component list associated with a specific fluid package:
Set myBasisManager = myCase.BasisManager
Set myFluidPackage = myBasisManager.FluidPackages.Item(FP_Name)
myFluidPackage.Components.Add <Component_Name>
or
Set myBasisManager = myCase.BasisManager
Set myComponentList = myBasisManager.ComponentLists.Item(Comp_List_Name)
ComponentList.Components.Add <Component_Name>
In the above examples, the Component_Name used references the Sim Name shown in the Component List (this is the same name used in the simulation environment). To remove a component, the syntax is similar to above:
myFluidPackage.Components.Remove <Component_Name>
or
ComponentList.Components.Remove <Component_Name>
Keywords: Hysys Automation, add component, Fluid package.
References: None |
Problem Statement: How to model a Rupture disc in HYSYS Dynamics. | Solution: There is no direct way to model a Rupture disc in HYSYS. User can model a Rupture disc using a Relief Valve in HYSYS.
1. Assign the Set pressure = Full open pressure = desired rupture pressure.
2. Specify an Orifice Area and make the Discharge Coefficient = 0.62 for the Rupture disc.
3. Go to Dynamics tab and then check the 'Enable Valve Hysteresis' option. Assign Closing pressure and Reseating pressure to zero.
Once the process pressure exceeds the rupture pressure the Relief Valve will now act like a rupture disc and will remain open.
Keywords: Rupture Disc, HYSYS Dynamics, Relief Valve
References: None |
Problem Statement: Can Pipe Segment operation be used to calculate Pressure drop in slurry line? | Solution: Most of the pipe correlations for the Pipe Segment (e.g. Beggs & Brill and so on) were developed for 2-phase flow (vapour-liquid) and a few (e.g. OLGAS 3P) for 3-phase flow (vapour-light liquid-heavy liquid). But none of the pipe correlations in the Aspen HYSYS Pipe Segment will give reliable results when solids are present in the pipe (even just as ice or hydrates).
Theoretically, the results should be the same for the system with the solids that for the system without the solids. No modification is done in the viscosity of the liquid phase for the presence of the solids, because the correlations we use were developed for systems without solids in the process fluid. We also do not recommend modeling the slurry as a single hypothetical component, as the correlations used in Aspen HYSYS are not designed for this type of system.
AspenTech does have a product called Aspen Process Manual that can be used to design slurry based systems, however this is not a flowsheet oriented tool like Aspen HYSYS. Refer to KBSolution112569 for more details.
Keywords: Pipe Segment, Slurry, Solids, Aspen Process Manual
References: None |
Problem Statement: How to Ignore the Subflowsheet? | Solution: The Ignore check box option is available on the Parameters Tab.
To ignore a subflowsheet, double click on the Subflowsheet and go to Parameters TAB and check the Ignored check box.
Keywords: Subflowsheet, Ignore, check, box
References: None |
Problem Statement: Sometimes, we model two fluids using PIPESYS under similar Reynolds Numbers, but the the pressure drops are significantly different. | Solution: The explanation lies in the hydraulic treatment of flow pattern in PIPESYS. After the units are calculated, you can get the flow pattern on Results tab | Detail datasheet. PIPESYS only recognizes laminar and turbulent flow for hydraulic calculations. If one of your fluid is in laminar and the other is in transitional flow, the first one is treated as laminar flow and the second as turbulent flow. As a result, you will observe very different pressure drops, even though the Reynolds numbers are similar.
Keywords: .
Reynolds number, flow pattern, PIPESYS, pressure drop.
References: None |
Problem Statement: When the simulation includes a relatively large number of Adjust operations, it is often useful to quickly diagnose the status of these blocks, as their | Solution: is iterative (prone to convergence issues). Also, Adjust blocks may be used only sporadically to determine normal desired conditions (and be subsequently ignored).Solution
1. Using the Adjust manager.
Assuming that this is a problem relevant when you have multiple Adjust blocks, you can choose ‘SimultaneousSolution’ from the Adjust/Parameters tab in each Adjust. An overview of the Adjust blocks in the flowsheet and their Iteration Status can be accessed by clicking in Sim Adj Manager… in the Parameters tab of the block, or in the Home ribbon ‘ Adjust manager’):
In this menu, you can see if the blocks converged or not:
You can also see if blocks are ignored:
2. Using a HYSYS spreadsheet.
Compare the residual (you can access and import this variable directly from each block) and compare it with the respective specified tolerance (also importable). You can define a conditional expression to display a code for whether an acceptable residual was attained or not.
To capture in a HYSYS spreadsheet whether the Adjusts are ignored or not, open the Adjust window, click on the Ignored check box, drag and drop in the desired spreadsheet cell.
The result is (also works for other blocks, like recycles):
The iteration status in the Simultaneous Adjust manager can also be dragged and dropped into the flowsheet, you will see a numerical code associated with the status (0 for Incomplete, 1 for Not converged, 2 for Converged, 7 for Ignored).
3- Using Flowsheet Summary.
An overall view of the Adjust blocks in the flowsheet, can also be seen in the Flowsheet Summary (button in the Home ribbon). In the Recycle/Adjusts tab, you can list all adjusts in the flowsheet and filter the ones that have reached Max Iterations, and the ones that are ignored:
You can have the same information for Recycles by clicking the appropriate radio button.
Keywords: Adjust, Spreadsheet, Flowsheet, Adjust manager; Ignored; Converged
References: None |
Problem Statement: Why can I not specify certain shell types using the Aspen HYSYS heat exchanger model? | Solution: TEMA shell types G, H, X, J and K are currently unavailable because the required models have not yet been implemented in Aspen HYSYS. If a user attempts to select one of the aforementioned shell types, the following message will appear in the trace window:
G, H, X, J, K shell types are not supported yet.
This limitation only impacts the built-in rating models available in the Aspen HYSYS heat exchanger, and does not affect either of the design models.
Note that it is also possible to use the Tasc+ Engine (available on the Design | Parameters pagetab when Aspen Tasc+ is installed) to integrate Tasc+ exchangers into an Aspen HYSYS flowsheet. Using this approach, one can create rigorous rating models within Aspen HYSYS for heat exchangers with shell types other than E and F.
Keywords: TEMA, shell, type, G, H, X, J, K, TASC, Tasc+, heat, exchanger, configuration
References: None |
Problem Statement: How do I decide if I should select a direct action or reverse action on the controller interface? | Solution: When the setpoint value (SV) is fixed, the relationship between process value (PV) and manipulated Output Value (MV) can be direct action or reverse action as shown below and select accordingly.
Direct action: The controller action in which the MV increases as the process variable increases or decreases as PV decreases.
Example 1: If you have a valve at the vessel liquid outlet to control the vessel level, then you would like to set the controller as direct. As level increases you want to open the valve to let more liquid flow out to control the vessel level.
Example 2: If you are controlling the pressure of a vessel through a valve at the vessel vapor outlet, if the pressure in the vessel increases you want to open the pressure controller valve to bring the pressure (PV) to SV.
Reverse action: The controller action in which the MV decreases as the process variable increases or increases as PV decreases.
Example 1: If you have a valve at the vessel feed inlet to control the vessel level, then you would like to set the controller as reverse. As level increases you want to close the valve to let less liquid flow in to control the vessel level.
Example 2: If you are controlling the column bottom temperature through reboiler steam inlet, then when temperature increases you want to close the valve.
Keywords: Reverse, Direct, Action, Controller
References: None |
Problem Statement: I want to adjust the solubility of my components for my simulation. This is accomplished in SimSci Pro/II by adjusting the Henry's Law Constant. Does Aspen HYSYS have a compatible method to accomplish this? | Solution: Aspen HYSYS offers you the possibility to do it with the tabular options in the property fluid package.
1. In your simulation add the components you want to adjust its solubility.
2. Go to the Fluid Packages folder, select the package you are working with and go to the Tabular tab. In this, toggle “Enable Tabular Properties”
3. In Thermodynamical select K-value(V/L1)
4. Under Information select the component you want to modify, in this case Water. And modify the information.
· In equation shape you will be able to select the Henry Law like form equation.
· In y shape you will select Ln(y)
· In x shape you will select the shape of the variable x
5. Once done this, in a, b, c… you will adjust this equation as desired with your own data. You can also check how the property is being calculated in the box below the window.
When you go to your simulation environment the solubility of these components will follow the equation with the values you entered, hence calculated the way it has been previously specified.
Keywords: Solubility Adjustment, Henry’s Law, Tabular.
References: None |
Problem Statement: Extension source code built in VB6 is migrated to .Net and has been successfully complied to generate two dll files (name.dll and interop.Hysys.dll)
The extension, however, does not register successfully because it could not load the file or assembly Interop.HYSYS.dll
See error below.
Attempting to register the Hysys extension C:\ Users \ name.dll
Image Type: CLR
E10002: CLR Assembly registration extension.
Could not load file or assembly “ Interop. Hysys. Version=2.1.0.0 Culture=neutral. Public Key token=null” or one of its dependencies. The System cannot find the file specified.
FATAL ERROR:
Registration of Hysys extension name.dll failed. | Solution: This usually stems from a problem that Windows will search for dependencies in the path of the executable rather than the path of the target dll when registering a dll.
TheSolution is to copy the Interop.HYSYS.dll next to regextn.exe, which would be in C:\Program Files (x86)\AspenTech\Aspen HYSYS V#.#\, possibly without (x86) on a 32-bit machine.
At runtime the extension will be able to load the dependency of Interop.HYSYS.dll from next to the extension dll, but during registration regasm cannot find the dependency.
An alternativeSolution would be to build the VB.NET dll against .NET Framework 4.0 or newer, which allows for Embedding Interop Types into the target dll (this is a preference for each reference added to a project, Embed Interop Types = True and Copy Local = False). This will put the dependency on Interop.HYSYS.dll inside of the extension dll so there are no problems associated with loading it at registration or runtime.
Keywords: Extension, Interop, dll, VB6, .NET, .NET Framework
References: None |
Problem Statement: What is the application of the Feed Basis option of Carry Over Model in the 3 phase Separator? | Solution: The Feed Basis carry over model is applicable when the user intends to specify or knows how much fraction of a particular phase of the separator inlet feed stream is carried over in another phase of the separator product stream.
Refer to the attached simulation created to illustrate this.
10% of the light liquid phase flow from the inlet feed stream is required to be carried over in the product vapour outlet stream.
0.1 x 1517kgmole/h = 151.7 kgmole/h of light liquid phase in the vapour outlet stream
Also required is that 20% of the gaseous phase flow of the inlet feed stream should be carried over in the product light liquid stream.
0.2 x 2228 kgmole/hr = 445.6 kgmole /h of vapour phase in the light liquid product stream.
Keywords: Feed Basis, Carry Over Model, 3 phase Separator
References: None |
Problem Statement: The Quick Size utility in the Separator unit operation (Rating tab, Sizing menu) is a fast method for sizing a converged separator based on the criteria as stated in:
Evans, Frank L., Equipment Design Handbook for refineries and chemical plants - Volume 2, 2nd Edition, p. 154, Gulf Publishing Company, Houston, Texas, 1980.
Watkins, R.N., Sizing Separators and Accumulators, Hydrocarbon Processing, November 1967, p. 253.
However, users may find this criteria inappropriate for their particular application (or non-compliant with their design standards). | Solution: Use the Vessel Sizing utility from Equipment Design (accessible from the Navigation pane). A new vessel sizing case must be created, and the converged separator unit operation attached. The user will be able to specify the sizing criteria, construction and costing information from this utility. See image snapshot below:
Keywords: Separator, Quick Size, Vessel Sizing
References: None |
Problem Statement: Reports created by Report Manager can be printed as pdf's. However, users can also export the results and format to Excel. | Solution: 1) Open Report Manager and create report with desired Datasheets.
2) Enable the option ‘Text to File’ and click ‘Preview…’
3) In ‘Format’, configure how you would like the data to be displayed.
4) Check the format in ‘Preview…’ of the previous menu.
5) Choose ‘Print to File…’ and save as txt file.
6) Open this file in Excel and choose the appropriate options in the Text Import Wizard.
This leads to an Excel file with the Report Manager content and format.
Keywords: Report manager, Excel, txt, print
References: None |
Problem Statement: How do I avoid mass imbalance in Depressuring utility? | Solution: Mass imbalances when using Dynamic Depressuring utility with a zero liquid or vapor flow is a known issue. One way you can reduce the imbalance by using small time step size (~0.01 sec).
Using a greater step size, the vessel appears to relief more mass than it should actually relieve. Depressuring systems involve rapid transient states. The integration of the flow function for calculating the remaining vessel mass has inherent inaccuracies. In this case, mass flow vs time is a function that decreases with time, and this type of function may give an excessive error when integrating. Reducing the step size can mitigate this problem.
Keywords: Dynamic Depressuring Utility, Mass imbalance
References: None |
Problem Statement: The labels for all or some objects in the flowsheet have all disappeared. How can I restore them? | Solution: The labels may have been hidden or deleted, accidentally or on purpose, by the user or other users sharing the file. The following procedures should be able to restore labels in most cases:
Consider this example, where all labels are hidden:
1-Select all objects in the flowsheet (or just the ones with hidden labels).
3-Click on an object icon with the right mouse click. Make sure you are clicking in the actual icon and not in the flowsheet around the icon.
4-Choose ‘Format Label’ and then ‘Show Label’
In some cases, the problem persists in new files and even when adding a new object, in this case the user may want to load a new preferences file:
1. Download the default preferences file (.PRF) for the appropriate version of Aspen HYSYS you are using (attached).
2. Go to File | Options.
3. In the Simulation page, click on ‘Load Preference Set’. Choose the file. Click OK.
Keywords: Flowsheet, Labels, Preferences, Hide/Show
References: None |
Problem Statement: How to use the Script Manager. | Solution: 1. Find the script from the ribbon tab “Customize”.
2. Open the Script Manager. If you want to create a script, use Directories to locate the folder you want to store the script, and then press “New”. Be careful, if you are window 7 user, some of the directory is only for system administrator, and you may not be able to create a file there. If you want to play a script, use Directories to find the place where the script is, and then select the script from the upper window, then press Play.
3. Give a name to the script file. Don't use *.scp, it won't work. You can also write some description in “Description” field, but it is optional. Then press “Record”.
4. Once you start Record, you will see “Script Recording” on the right button corner.
5. Then, you can do whatever you plan to do using automation. After that, you can open the Script Manager, and press “Stop Recording”.
Keywords: script manager
References: None |
Problem Statement: When a gauge pressure is defined in a Set logical operation a warning message appears: Non-unity multipliers cannot be used with units that have offsets from the internal units used by HYSYS. This includes all forms of temperature and gauge pressure units as well as any user defined units that have non-zero offsets. Use a spreadsheet for this type of operation. Static units and consistent results are then assured.
Why it is not possible to define a Set logical operation with gauge units? | Solution: The normal pressure gauge units are not allowed to be used in the set block. If it were possible, every time a user changed the units of pressure, the results of the simulation would change without any warning.
Users can create their own pressure units by clicking on pressure units in the Units Of Measure (File | Options | AOM)
For more information about define a new Unit Set, please refer toSolution 109109.
Here, user can set a multiplier on the internal units used by HYSYS and then can use this unit in a set block with a non-unity multiplier and they can specify an offset of one atmospheric pressure.
Other than that, the only other option is to use a spreadsheet, since this ensures that the unit set is fixed.
If user changes the spreadsheet's units a warning is displayed, which informs them that the results of their simulation may change
Keywords: Set operation, spreadsheet, gauge pressure, Units of Measure, multipliers, offset.
References: None |
Problem Statement: List the Flow Regime code convention that Aspen HYSYS Upstream uses for Pipe Segments | Solution: The following table lists the Flow Regime code convention that Aspen HYSYS Upstream uses for Pipe Segments.
H----V Horizontal vapour only
H----L Horizontal liquid only
HB---- Horizontal bubble flow
H-A--- Horizontal annular flow
H--G-- Horizontal slug flow
H---S- Horizontal stratified flow
H-AG-- Horizontal annular/slug flow
H--GS- Horizontal stratified slug flow
H-A-S- Horizontal stratified annular flow
H-AGS- Horizontal stratified annular slug flow
V----V Vertical vapour only
V----L Vertical liquid only
VB---- Vertical bubble flow
V-A--- Vertical annular flow
V--G-- Vertical slug flow
V-C--- Vertical churn flow
V-AG--Vertical annular/slug flow
H-AGSD Horizontal dispersed stratified annular slug flow
H--GSD Horizontal dispersed stratified slug flow
H-A-SD Horizontal dispersed stratified annular flow
H---SD Horizontal dispersed stratified flow
H----O Horizontal oil only
H----W Horizontal water only
H---OV Horizontal oil/gas flow
H---VW Horizontal gas/water flow
H---OW Horizontal oil/water flow
H---SY Horizontal, stratified/wavy flow
H-A-SY Horizontal, stratified/wavy annular flow
H--GSY Horizontal, stratified wavy slug flow
H-AGSY Horizontal, stratified/wavy annular slug flow
XXXXXX N/A Error Indicator
------ Default indicator for Break/fill/valve/first cell
Keywords: Flow Regime, Hydraulics, Pipes, Hysys Upstream
References: None |
Problem Statement: What are the variables passed from Aspen HYSYS and retrieved from OLGA using the Aspen HYSYS-OLGA Link extension? | Solution: The Link extension passes a few key variables for the connected Inlet and Outlet streams.
For all streams, the temperature, pressure, gas fraction, and water fraction are passed to OLGA.
Additionally the total mass flow will be passed to SOURCE connections. In the case of a SOURCE connection, OLGA will use the total mass flow from Aspen HYSYS as a fixed and known value for the duration of that integration calculation.
In the case of a BOUNDARY connection in the OLGA model, the pressure from Aspen HYSYS will be fixed and set at that terminus NODE in OLGA.
The Link then retrieves from OLGA some key variables.
For a SOURCE connection (either Inlet or Outlet), the pressure is retrieved from OLGA and, optionally, along with the dP/dF (change of pressure with change in phase flow rates) derivatives, a pressure-flow relationship is enforced on the Aspen HYSYS model.
For a BOUNDARY connection, the total mass flow is retrieved from OLGA and, optionally, along with dF/dP derivatives, a pressure-flow relationship is enforced upon the Aspen HYSYS model. The temperature and phase flows (gas, oil, and water) are also retrieved in all cases and would be used to set the composition and temperature of the Aspen HYSYS stream where the direction of the flow dictates this.
Keywords: OLGA, variables
References: None |
Problem Statement: Why the pressure drop is decreasing in my system with a Swage instead of increasing | Solution: A smaller pressure drop in the system with a swage is because the pressure increases in your pipe is due to the diameter increases across the swages between the pipe segments of different sizes. Fluid flow across an expansion results in a decrease in fluid velocity and hence a recovery of velocity head as pressure head. It gives a DP smaller with the swage. This is an expected behavior.
Keywords: swage, pressure drop, pipe segment
References: None |
Problem Statement: After applying Emergency Patch 133193, OLGAS-2P correlation is not working anymore in Pipesys extension in Hysys V7.3 | Solution: In order to use OLGAS-2P correlation in Pipesys extension, you will need to follow the procedure in the knowledgebaseSolution (ID:115126) to download the license file and add the environmental variable.
Keywords: OLGAS , PIPESYS
References: None |
Problem Statement: By default, the Workbook in Aspen HYSYS displays the composition using the basis mole fraction. How this basis can be changed to mass fraction? | Solution: In order to change the basis of the composition in the main case and sub-flowsheets, users can follow the procedure below:
1. Go to the Home menu and select Workbook.
2. Go to the Composition tab.
3. Check the button Include Sub-Flowsheets located on the bottom right side.
4. Select Setup in the Workbook menu.
5. Then select Compositions in the Workbook Tabs > Select Delete in the Variables section
6. Click Add.. > Select Master Comp Mass Frac > click All > OK
Keywords: Workbook, setup, composition
References: None |
Problem Statement: Why is the Net Positive Suction Head available (NPSHa) reported in the pump unit operation greater than zero for a saturated liquid at the pump inlet? | Solution: The NPSHa calculation is based on the ADDITION of a static pressure term AND velocity head term. The static pressure term is proportional to the difference of the static pressure and vapour pressure terms (i.e. zero for a saturated liquid).
However, the velocity head term is not zero and is proportional to the square of the fluid velocity at the pump inlet. The fluid velocity is calculated based on the cross-sectional area of the inlet nozzle.
Keywords: Net Positive Suction Head available, NPSHa, Pump, static pressure, velocity head
References: None |
Problem Statement: How do I make the utilities show up on a material report print out? | Solution: When adding a report datasheet, you must select the Utilities button from the filter option.
Then select the utility objects:
Keywords: Utilities, report, print out
References: None |
Problem Statement: Referring to the curve fitting equation from | Solution: ID 133788, I understand that if I plot Q^2 vs H for a fixed operating speed, I should get a straight line. However, it does not give me a straight line which makes me wonder that if the curve is fitted to the mentioned equation in HYSYS. Please explain.
Solution
The method of fitting used in HYSYS may not guarantee the straight line. To prevent zero derivatives when the capacity or speed is zero, we add a linear term to the equation. We are fitting
(1-0.01b)*Q*|Q| + 0.01*b*Q = (1-0.01)*a*N*|N| + 0.01*a*N - b*H
However the linear term is small, and it numerical effect should be negligible. One thing needs to be pointed out is that the HYSYS uses a weighted least square curve fitting, and the fitting is carried out at every operating point. That means the curve points are recalculated using a set of weights and the weight for given point is
HeadCurveWeight[idpts] = (1.0 / (FlowDev + HeadDev+ SpeedDev))^2 EffCurveWeight[idpts] = (1.0 / (FlowDev + EffDev + SpeedDev))^2 where HeadDev = ((CurrentHead - HeadCurve_Offseted[idpts])/MaxHead)^2;
FlowDev = ((CurrentFlow - (*curve).GetFlowCurvePt(idpts, MassDensity))/MaxFlow)^2; EffDev = ((CurrentEff - EffCurve[idpts])/MaxEff)^2; SpeedDev = ((CurrentSpeed - curveSpeed)/MaxSpeed)^2;
That will actually make it possible that the calculated point is not on the original curve.
Keywords: Compressor Curve
References: None |
Problem Statement: How are pool fire and jet fire defined? | Solution: Pool fire: In a vessel containing a liquid, when the liquid spills out and ignites.
Jet fire: In a vessel containing only a gas, if the flange leaks and the high pressure gas escapes and ignites.
Key Words
fire, types, definition
Keywords: None
References: None |
Problem Statement: Aspen HYSYS V7.3 does not solve exchanger using EDR with Input error 1124 The data input for E-Shell inlet nozzle loc. A problematic case file and solved case file is attached to show the problem. | Solution: It happens with E-shell and D-shell case files built prior to EDR V7.3 integrated in HYSYS. When you load the old HYSYS models in HYSYS V7.3 you will see the message Input error 1124 The data input for E-Shell inlet nozzle loc. if there is any inconsistency between the inlet nozzle location and the distance between tube sheet.
To correct the problem in HYSYS V7.3 you have two options.
1. Go to EDR - Shell&Tube tab in Heat Exchanger and select Exchanger page to change the Flow Direction to Set default so that the program will set the direction of flow based on the specified Distance to Tubesheet under the Nozzles page.
2. If the flow direction set is correct then check the Nozzles page to see if the Distance to Tubesheet is correct. Sometimes this input item was used incorrectly in attempting to set co or counter current flow. To remove the inconsistency delete any values you have specified.
In HYSYS V8.0 and later you can open the full EDR Browser and make changes by clicking on Model Details.
Keywords: Error 1124, nozzle location, E-shell, D-shell
References: None |
Problem Statement: When trying to access the Documentation Builder in the Safety Analysis environment, it does not work. What could be the reason? | Solution: The reason could be related to the MS Access version installed on your computer. When the user clicks on the Documentation Builder button, the COM call to open the .mdb files is fired. This step can fail with MS Office 2007 because we use a 2012 version of Microsoft Office.Interop dll and backwards compatibility is not guaranteed by Microsoft. So, if you want to use the Documentation Builder with HYSYS version 8.6, you need to install the 2010 runtime version of MS Access (it can be downloaded for free from Microsoft at : https://www.microsoft.com/en-us/download/details.aspx?id=10910).
Please note that all the other aspects of the .mdb file should be fine (.mdb is the 2003 file save format).
Keywords: Documentation builder, Safety Analysis.
References: None |
Problem Statement: How to do I include the vapor properties such as density and viscosity in a column profile report using the Plots Datablock? | Solution: By default, Aspen HYSYS has activated the report option only for light liquid properties. If you want to include the vapour properties, you need to add them. This can be done as follows:
1. Go to Column editor in Performance tab > Plots section. Highlight Transport Properties and Click on View Table...
          Â
2. In the the new “Profile Tableâ€� window, click on the Properties… button           Â
3. A new window will be displayed “Properties View�. Please check the Vapor option in the Phase section. This will display the properties you’re interested in the “Profile Table�.
Try now to generate report. You should be able to see the vapor properties included in the Plots Datablock.
Keywords: Column Profile report, Column properties, Transport properties
References: None |
Problem Statement: Aspen HYSYS ActiveX: how to configure a user variable to apply a proportional ratio between component flows of different streams. | Solution: ThisSolution provides an example of how to link flowsheet variables in our simulation through a user variable, while applying some proportional criteria between them. In the example, the macro implemented will fix the component mass flow of the stream “2� as a proportion of the Ethylene mass flow present in the stream “1�. The ratio applied will be different for each component in the stream “2�. Then the component flow of the resulting product stream (stream “3�) will be used to define the composition and flow of the stream “4�, present in a subflowsheet, but excluding any remaining water in the stream.
These are the steps required to create a user variable:
1. Open any material stream in your simulation, and go to the User Variables page
2. Click on New User Variable icon at the top of the user variable table. The Create New User Variable property view will open.
3. Enter the information for the fields in the New User Variable property view, as specified in picture below:
4. Select the PostExecute() checkbox found on the Macro tab and enter the macro in the Code Editor. Click ok.
The example case file is attached with the aforementioned functionalities.
Keywords: ActiveX, VB, Macros, User variables, WinWrap.
References: None |
Problem Statement: Why are the critical temperature and pressure calculated by the Phase Envelope utility different from those calculated by the Critical Properties utility? | Solution: The two utilities use different algorithms and so discrepancies are expected between the two results.
The envelope is calculated on a dry basis, using the technique developed by Michelson and as a natural byproduct of theSolution sequence, the critical point is derived. Some special treatments are involved in the Envelope utility calculation to force the bubble point and dewpoint curves to match each other under critical conditions. In doing so, it may introduce certain discrepancy in the calculated critical properties.
The critical utility uses the method developed by Heideman and Khalil. The true critical properties are determined thermodynamically by satisfying both the quadratic and cubic forms in the expansion of the Helmholtz free energy as a function of the mole numbers as zero at a critical point. Details of critical point calculations can be found in the paper by Heidemann and Khalil (AIChE Journal, Vol. 26, No.5, p769-779, 1980).
Keywords: critical properties, phase envelope, critical temperature, critical pressure
References: None |
Problem Statement: How can I see Molecular weight , Density, Viscosity, Surface Tension and specific heat capacity for every stage in the column? | Solution: Procedure 1:
Double click on the column and click on Performance | Plots | Transport Properties | Select view table
It will display the transport properties listed above.
Procedure 2:
You can export the internal stream to the main environment and see the properties there.
Please follow theSolution below:
http://support.aspentech.com/webteamasp/KB.asp?ID=109247
Keywords: Tray by tray heat of vaporization, specific heat capacity of every stages.
References: None |
Problem Statement: How do you adjust the flowrate or the amine concentration in Makeup unit operation? | Solution: You can't adjust the amine concentration or amine flowrate using Adjust block because these variables are not exposed in Adjust block. However a workaround is available, by which you can access these variables.
If you create a HYSYS Spreadsheet, these variables can be dragged and dropped into the Spreadsheet, and you can add those from there to an Adjust function.
Steps are given the below:
1. Insert Spreadsheet unit operation on flowsheet. Open Spreadsheet tab
2. Drag-and drop the desired variable in the Desired cell on the Spreadsheet. For amine concentrations, click on the value, and then drag it. for the flow rate, click in the text box and the flow rate will be highlighted. At that point, hold over the highlighted text and drag.
3. Add an Adjust unit operation to the flow sheet. While adding the variables for the unit operation, select the Spreadsheet as the object from the Variable Navigator
Keywords: Amine, adjust block, spreadsheet,Makeup unit operation
References: None |
Problem Statement: What is the Off-Design Correction option inside the compressor? | Solution: Two parameters can be entered for performance curves: Design Temperature and Design Molecular Weight. A screenshot showing this addition within the compressor form is shown below:
When these are supplied, HYSYS corrects the characteristic curves to the equivalent/corrected curves at operating conditions. To do so, design speeds, design head values and design flow rates entered in the curves are corrected to equivalent operating speeds, operating head values and operating flow rate values based on the quasi dimensionless equations shown below. In order to build the corrected characteristic curves, each data point (flow rate, head, speed) is corrected according to the following quasi-dimensional expressions:
1-Corrected volume flow in compressor characteristic curves
Where:
Tref = Temperature at reference/design conditions
MWref = Molecular Weight at reference/design conditions
Qact = actual volume flow in the curve
Qcorr = corrected volume flow in the curve
2-Corrected head in the compressor characteristic curve
Where:
Hcorr and Hact are the compressor's corrected and actual Head value in the characteristic curve.
3-Corrected Speed in the compressor characteristic curve
Where:
Ncorr and Nact are the compressor's corrected and actual speed in the characteristic curve.
Off-Design Corrections are supported in both steady-state and dynamics. Off-Design curve correction is not applied when you have a single curve and at this condition fan laws will be applied.
Keywords: Compressor Curves, Performance Map, Off-Design Correction
References: s
Dr. Meherwan P. Boyce , Centrifugal Compressors: A Basic Guide, PennWell Books
Chang, H. and Wu, C., ‘Corrected maps narrow Compressor performance prediction range’ Oil and Gas |
Problem Statement: I am converting a file from PROII to HYSYS. Where are the property packages defined in the PROII input file? | Solution: It is possible to use the PROII to HYSYS Convertor to change the simulation into a HYSYS file. Inside the PROII input file the property package is specified under the section entitled the Thermodynamic Data. An example from the PROII input file is found below:
THERMODYNAMIC DATA
METHOD SYSTEM=PR, TRANSPORT=PETR, MEOH=OFF, SET=PR01
WATER DECANT=ON, PROPERTY=SATURATED
METHOD SYSTEM=SRK, TRANSPORT=PETR, MEOH=OFF, SET=SRK01, DEFAULT WATER PROPERTY=SATURATEDMETHOD SYSTEM=GS,
The property package that will be imported into HYSYS will be labelled directly after the method system. The PROII code above is PR and SRK which is Peng Robinson and Soave-Redlich-Kwong property package respectively.
Keywords: HYSYS, PROII, Converter
References: None |
Problem Statement: Can I include several objective functions in the same optimization problem in Aspen HYSYS? | Solution: In the Original optimizer, the user can only select one objective function. With the Hyprotech SQP optimizer, multiple objective functions can be handled. This option requires the previous setup of a Derivative Analysis.
In the Objective function menu of this analysis, add ObjFunc as shown below.
Keywords: SQP Optimizer, Objective functions, Derivative Analysis
References: None |
Problem Statement: Why do I see more wax deposits in a pipe when the inlet temperature increases? | Solution: There are two factors that can cause the wax deposition to increase with increasing temperature.
The first factor is that increasing temperature results in lower viscosity and higher diffusivity, both of which have the effect of increasing the mass transfer coefficient calculated using the equations inSolution 122699. There is a competing effect from the decrease in density, but it may be a less significant effect than changes to the viscosity and diffusivity.
The second factor is the change in the concentration differences between the bulk fluid and the pipe wall. The concentration difference between the bulk and the wall for the heaviest components may be larger at the higher temperatures, thus driving a higher deposition rate. This is a more complicated effect, dependent on the overall composition, the selected wax model, and the current temperature. For other conditions and/or wax model selections, this effect can be in the opposite direction (decreasing deposition with increasing temperature).
Keywords: Wax Deposition, Pipe
References: None |
Problem Statement: How to prevent the over-specified error when using the rigorous heat exchanger in Aspen HYSYS with vapour fraction specified. | Solution: When simulating the condenser/vaporizer with HYSYS methods (such as Simple Weighted), this calculates the heat overall transfer coefficient (UA). The calculated UA is based on specified outlet temperature or vapour fraction (VF =0, or 1). However, when the exchanger is linked with rigorous method using Exchanger Rating and Design (EDR) software, the exchanger geometry and detailed heat transfer coefficients are calculated by the rigorous method. The heat exchanger calculates the outlet temperature. Since the outlet temperature in the HYSYS is based on the specified vapour fraction, the exchanger will generate the over-specified error message. The solver can over-write the oulet temperature but not the vapour fraction. The user will require to delete the vapour fraction. This will enable the exchanger to solve without the error.
Keywords: Heat Exchanger, Sizing, EDR, Vapor fraction, Condensation, Vaporization
References: None |
Problem Statement: How to show replace the AspenTech logo with a custom logo on Aspen HYSYS reports. | Solution: By default Aspen HYSYS report file will show the AspenTech logo. However, it provides the feature to change the logo. To do that,
1. Open File|Options|, and then go to Report
2. Users can user “Select” button to load their own logo to replace Aspen Tech logo.
Users will have to make sure that the logo must be a bitmap with file extension as *.bmp. The file also has to be saved as 256 bit map file. The logo must fit in the area Aspen HYSYS provided, and user can resize the file using MS paint.
Keywords: logo, reporting, Aspen HYSYS
References: None |
Problem Statement: How is the relief load obtained in Safety Analysis in Aspen HYSYS? | Solution: Starting from Aspen HYSYS V8.3, user can use Safety Analysis to size PSVs in the process flowsheet. The PSV sizing requires relief load to be available. Currently, there are three ways to obtain the relief load:
1. Manual - User input relief load for sizing the PSV.
2.
Keywords: Relief Load, Safety Analysis
References: - Relief load is obtained from the selected stream in the Aspen HYSYS simulation.
3. Calculated - Relief load can be calculated for certain scenarios, whose has names are in bold in the table shown below.
If Calculated relief load is to be selected, the user needs to fill in the corresponding form and specify the values in blue.
For example in Fire scenario, the user needs to input vessel geometry, liquid level, wetted/unwetted information, environmental factor F, liquid fluid latent heat, etc. Then, the heat load input is calculated using API 521 standard, and the relief load is calculated as follows:
Relief Load = Heat Load Input / Fluid Latent Heat
The default value for Fluid Latent Heat is 27.80 kcal/kg, which should be modified with reference data or the mass heat of vaporization from Aspen HYSYS stream Properties.
The result summary of the relief load can be seen from PSV Reports | Reports | Relief Calculation, as shown below: |
Problem Statement: I need to use the backdoor method for certain variables. How can I find out their monikers? | Solution: Some variables used in Aspen HYSYS are not directly exposed as an automation interface, such as the variables used in the Performance Table of a Heater or a LNG Exchanger. Those variables have not been fully “wrapped� and cannot be directly accessed through Automation. However, the backdoor method can be used with the monikers of the variables you want get access to. In order to find out the monikers, you can use Aspen Workbook as shown in the image below:
Another option to reveal the moniker is to copy the variable in HYSYS and paste it in Excel as a link:
Keywords: Monikers, Backdoor method, Automation.
References: None |
Problem Statement: Where can I change component efficiencies calculated by the Amine Package for a column in Aspen HYSYS? | Solution: Aspen HYSYS estimates the stage efficiency for CO2 and H2S based on the tray dimensions. When the internal column diameter, the outlet weir length and the outlet weir height are known the AMSIM property package can estimate the stage efficiency base on that mechanical tray dimensions.
Tray dimensions can be entered in below path:
Column/Parameter Tab/Amines.
However, the user always has the chance to specify such efficiencies and overwriting the estimated values by selecting “Reset H2S,CO2� tab in Column/Parameters/Efficiency
Procedure:
Open the Column
1. Go to the tab Parameters | Efficiencies
3. Click on Reset H2S & CO2 button --> Efficiencies values change from black color to blue color
4. Enter for example 0.5 in the Eff. Multi-Spec
5. Select the entire column for CO2
6. Click on Specify tab
Same procedure can be followed to H2S as well
Keywords: Column efficiency, amine package etc;
References: None |
Problem Statement: How do I obtain the Heating Values and Wobbe Index of gas at normal conditions? | Solution: Aspen HYSYS gives the Heating Values and Wobbe Index at standard conditions (15 deg C and 1 atm). The users have the option to change the condition from 15 deg C to 0 deg C if the values are required at normal condition. This option is available in the correlation manager. The knowledge baseSolution ID 138937 describes how to find the Correlation Manager in Aspen HYSYS.
In the Correlation Manager the user can select the
Keywords: Normal Condition, Correlation Manager, Heating Values, Wobbe Index
References: Temperature options. See the screenshot below.
The reference temperature can be either 15 deg C or 0 deg C. The typical workflow is:
1. Select the variable such as LHV Vol Basis
2. Select the Ref Temp option
3. Click on the tick box to activate this correlation in the stream |
Problem Statement: How to change the fluid package of a single or multiple components in Aspen HYSYS V8. | Solution: The procedure to change the fluid package is no longer trough right click on the items but you need to go Home Tab> Simulation> Fluid Package association. In there you will be able to set the default property package to use for each flowsheet.
If you want to only change the property package for some items, the recommendation will be to combine them into a subflowhsheet (select all the items> right click and choose <combine into a sub flowhsheet), then go to Home Tab> Simulation> Fluid Package association and change the property package there.Â
Keywords: None
References: None |
Problem Statement: In the Parameters page of the compressor, you can specify the curve input options as Multiple IGV (Inlet guide vanes). What does this option mean? | Solution: The Multiple IVG option allows you to provide multiple sets of curves in the Rating Page / IGV Curve Collection.
Each set of curves corresponds to one IGV position value.
The Curve IGV allows you to specify the inlet guide vane position that the entered curve set data is at (or for).
The Current IGV specifies the current position that the compressor is operating at. The value is the percentage of the maximum opening position. The maximum value for current IGV is 100. The default value for current IGV is 25. This is based on best practices.
Keywords: Compressor, curve, IGV, inlet guide vanes
References: None |
Problem Statement: A user characterized the same crude in both HYSYS (using Peng-Robinson fluid package) and AspenPlus (using Peng-Rob property method) respectively, then set up the column with the same configuration in both simulators.
For the same feeds, the user gets slightly different results.
Why can't I get the crude distillation column results to match between Hysys and Aspen plus? | Solution: Historially, a significant amount of development work went into the improvement of Peng-Robinson fluid package. One of the areas of such development work is the estimation of binary interaction parameters (BIPs). HYSYS estimate BIPs for crude hypo components based on boiling point and density. The estimated BIPs play an important role in the accurate prediction of phase equilibrium behavior of the crude.
On the other hand, A+ does not provide BIP estimations for pseudocomponents representing a crude when Peng-Rob is the property method in use. The interactions between these pseudocomponents and other components, or the interactions between the pseudocomponents are not accounted for. This is the main cause of the discrepancy.
In this comparison, the results from HYSYS should be considered more accurate. If reliable plant data are available, a quantitative conclusion can be made on the results from either simulator.
Keywords: crude distillation, crude characterization, crude
References: None |
Problem Statement: How to hide/reveal streams from workbook table | Solution: Here are the steps you can follow to reveal all the streams' properties from workbook.
1. Open the work book by clicking “workbook” on the Home ribbon bar. Once you do that, HYSYS will show Workbook ribbon bar, and automatically bring you there.
2. Press the “Setup” on the right up corner to bring the Setup dialog box up.
3. On the left hand side, you will see all the existing workbooks. Highlight the one you want to modify (the one you want to bring the streams back). Then, press “Order…” to bring another dialog box over. You can then use the “Reveal…” button to reveal all the streams you have been hiding. After that, press OK to close the dialog box,
After that you will be able to see all the streams' properties from the workbooks.
Keywords: workbook
References: None |
Problem Statement: What is the role played by the “PV Work Term Contribution” option for vessels in dynamics mode? | Solution: The attached document discusses the impact of the PV work term option by comparing its influence on the results delivered by the simulator to the ones returned by hand calculations. It is accompanied by the simulation file “PV.hsc” in version V7.3.
Keywords: PV work term, HYSYS Dynamics, work energy, irreversibility
References: s
[1] “Thermodynamics: An Engineering Approach”, Çengel, Y.A., Boles, M.A.; McGraw-Hill, 1989. |
Problem Statement: Explanation of common run-time errors using the property ImportedVariable for a SpreadSheetCell class. | Solution: In Aspen HYSYS, a spreadsheet operation can be used to bind conditions of different streams and units by using the functionality of importing and exporting variables. Because it is an operation, variables are automatically updated. However, if we try to access the imported and exported variables through our VB code, there are some limitations that have to be considered; specifically when trying to import a component flow or fraction.
ImportedVariable is a property defined for a SpreadSheetCell class that requires a RealVariable object. However the property ComponentMolarFraction, for instance, of a ProcessStream object exposes a RealFlexVariable which is basically an array of RealVariable objects. If you try to assign one to the other, you will get a “type mismatch� error:
spsht.cell(0,1).ImportedVariable = importedStream.ComponentMolarFraction ‘It returns a type mismatch error
In other attempts, the code below tries to assign a double data type value to a property that requires an object, so we will get an “object required� error.
spsht.cell(0,1).ImportedVariable = importedStream.ComponentMolarFraction(1) ‘Object required
The reason is that the object, the RealVariable with the composition or flow of a certain component, is not exposed as an automation interface in Aspen HYSYS. If you configure manually a spreadsheet using the Hysys user interface, and select the molar fraction of a component as an imported variable, you will see that the object assigned is not accessible by any defined property from its parent class.
Keywords: ActiveX, VB, VBA, Spreadsheet, Imported Variables
References: None |
Problem Statement: What is retrograde region and retrograde condensation? | Solution: For multicomponent gas mixtures, the cricondenbar (point N) and the cricondentherm (point M) represent the highest pressure and temperature respectively where both liquid and vapor phase exist together. The critical point (point C) is where the bubble point (0% vapor) and dew curve (100% vapor) meet. Then we have the retrograde region where both liquid and vapor phases co-exist. The screen shot shows a typical P-T behavior for a multicomponent hydrocarbon gas mixture.
Retrograde condensation is the phenomenon that occurs when the temperature of a mixture is between the cricondentherm and the critical point, and the sample is at the dew point pressure. By lowering the pressure, some condensation will initially occur as the pressure is lowered into the two-phase region. Retrograde condensation is the formation of hydrocarbon liquids as the pressure is lowered. It occurs in a limited range of pressures and temperatures between the critical point and the cricondentherm
At 4000 kPa, for example, the mixture is in the vapour phase if the temperature is greater than 40°C. By cooling the mixture from say 60°C at a constant pressure of 4000 kPa, the line on the right side of the phase envelope would be intersected at about 40 °C. This means that at this temperature and pressure, the first droplets of liquid would form. This point is called the dew point temperature of this particular mixture, corresponding to this pressure. If a different pressure had been selected, then a different dew point temperature would have been obtained. The line connecting all of the dew points is called the dew point line.As the mixture is further cooled, the path proceeds to the left inside the envelope. By removing heat from the mixture, more of the material will liquefy, until the line on the left side of the diagram is reached. At this point, all of the material is in the liquid phase. This is the bubble point temperature at this particular pressure. The heat removed is the latent heat of condensation, or vaporization, if we had started on the left side, where the mixture is in the liquid phase. The line connecting all of the bubble point temperatures is called the bubble point line.
Keywords: ,
cricondentherm, cricondenbar, retrograde region, retrograde condensation
References: None |
Problem Statement: When importing a stream from one model to another, the following dialogue box is displayed:
The fluid package / template that is being imported contains different component data for a User Property that already exists in this case.
You have four options: [Create Local], [Update], [Ignore], [Create New].
What do these options mean? | Solution: Create Local - the imported component values of the user property is put into the property slate for the imported fluid package
Update - the existing user property will be updated with the all of the new data from the imported fluid package
Ignore - the old values for the existing user property will be kept
Create New - a separate new user property is created
Keywords: User Property, Import, Fluid Package
References: None |
Problem Statement: When a .csv file is imported into Aspen HYSYS petroleum assays then the stream associated with the csv assay reports 1.#Q000 for enthalpy, entropy and heat flow parameters. | Solution: The characterization feature allows the assay to be recut over a range of temperatures. With .csv files, only the data for a specific distribution of cuts are specified and there is not enough information inside the file for the assay to recut automatically. If the user experiences this error they will need to re-characterize for which the workflow is shown below as a series of screen shots.
The user will need to select the characterize feature which is located within the Assay Management Tab. Once the user has selected this feature the assay will be characterized with a focus of matching whole crude properties. The associated stream will now display the correct properties.
Keywords: CSV, 1.#QO000, Assay Management
References: None |
Problem Statement: Why the standard gas flow does not match with the actual volume flow at standard conditions? | Solution: The following screenshot shows that the standard gas flow and actual volume at standard condition do not match.
Standard gas flow is based on the molar volume of an ideal gas at standard conditions. It is a direct conversion from the stream's molar flow rate, based on the following:
• Ideal Gas at 60°F and 1 atm occupies 379.46 ft3/lbmole
• Ideal Gas at 15°C and 1 atm occupies 23.644 m3/kgmole
Note: In the Preferences, the users can use the default temperature conditions (60°F or 15°C) or specify different temperature for the standard conditions. The ideal gas molar volume will be based on the specified user supplied temperature.
The actual volumetric flow rate is calculated using a rigorous vapour density calculation at the actual stream T and P conditions, and reflects non-ideal mixing and compressibility effects.
Actual Gas Volume Flow = Molar Flow / Molar Density
This explains why the two volume flow do not match at the standard conditions.
Keywords: Standard Gas Flow, Actual Volume Flow, Standard Conditions
References: None |
Problem Statement: In the Fire Semi-Dynamic Flash calculation method in safety analysis, how is the temperature difference between each of the flash iterations calculated? | Solution: When conducting a Semi-Dynamic Flash the user can edit the temperature difference between each flash iteration step. The parameters to edit the iteration steps is within the ‘edit flash table’
Within the edit flash table the user can edit the maximum iteration temperature and ‘# of flashes.’ The relieving temperature and the temperature difference between each of flash iteration are related by the following equation:
Keywords: Safety Analysis, PSV, HYSYS
References: None |
Problem Statement: How do I ensure my company logo appears correctly in the datasheet report? | Solution: The company logo can be included in the datasheet report as shown below.
The logo can be added via Files/Options/Reports. See the screenshot below.
The logo should be saved as 16 or 256 colour bitmap file. If this is saved as 24 bit bitmap then the logo will not appear correctly in the datasheet report.
Keywords: Company Logo, Datasheet Report, Report Manager
References: None |
Problem Statement: In the Vessel Sizing utility how is the Total Length (reported under Performance tab | Sizing Results) of a vertical separator calculated? | Solution: The total length is calculated using one of two equations depending on the user specifications. In most situations these two equations should lead to the same length calculation.
Length = Diameter*L/D + 1/2*Diameter
-or-
Length = 1/4*Diameter + Demister Thickness + Inlet Nozzle To Demister + Sump To Inlet Nozzle + Demister To Head + Liq Surge Height.
The Demister To Head is the Demister To Top specification.
When surge heights and demister properties are specified the second equation is used to calculate length, diameter, and other parameters which aren't specified. When L/D and other similar parameters are specified the first equation is used and then the demister properties are found from there.
Keywords: vessel sizing, vertical separator, length
References: None |
Problem Statement: Is it possible to adjust tray efficiencies with the Sparse Continuation Solver? | Solution: The Sparse Continuation Solver is not designed to handle stage/component efficiency. As a limitation of the solver, the tray efficiency is not taken into account by the Sparse Continuation Solver. You should work with a theoretical number of stages.
To work with efficiency tray and two liquid phases, please refer to KBSolution 109406.
Keywords: Column, Solving Methods, Sparse Continuation Solver, Tray Efficiency, two liquid phases.
References: None |
Problem Statement: When I input my assay data as D2886, the results do not represent my crude correctly. Why? | Solution: The API methods used by Aspen HYSYS to convert from D2887 to TBP have some limitations. For the correlations to work, there is a maximum allowable temperature difference between cut points.
For example, the method has a maximum allowable temperature difference of 30 F for cut points in the 95 - 100% range. If my crude has a true boiling point of 710 F at 99%, and 1310 F at 100%, then this temperature difference is bigger than the allowed 30 F in the method and this will cause the calculations to be incorrect.
Even when the API methods are applied correctly, the average absolute error is still as big as the error generated by the assumption that D2887 data is equivalent to TBP data.
Due to the above mentioned reasons, the recommendation is to input the assay data as TBP in a mass basis.
You can follow thisSolution 118422 to check if your crude is being represented correctly:
Keywords: Assay, D2886, distillation curves, TBP
References: None |
Problem Statement: My depressuring utility returns the error Unknown Vessel Metal Thickness. How do I fix it? | Solution: Add the value for Vessel Metal Thickness in Design | Heat Flux | Heat Loss Parameters | Conduction:
Keywords: Dynamic, depressurization, thickness
References: None |
Problem Statement: You can develop a unit operation extension with different levels of access with the help of a licence file or key code. This allows developers to expose to the users more or less information by an appropriate configuration of the visibility manager in Viewer Editor (viewed.exe). However these hidden variables in the extension are still available for importation to a spreadsheet or to a PFD table. Is there a way to limit this access? | Solution: It is possible to limit access to a variable's value by manually modifying the edf file and implementing the VariableQuery function of the ExtensionObject interface in your extension model. The changes to the edf must be done in a text editor such as Notepad or Visual Studio and cannot be done in viewed.exe.
In the extension's edf there is a section named ExtensionVariables which lists all of the variables in the extension. For the variables which are listed as AttachmentVar, RealVar, TextVar, or EnumVar the 6th flag can be modfied to add a AndQueryNotify string to the parameter.
In a RealVar, TextVar, or EnumVar the TriggerSolve or NoTriggerSolve flag can be changed to TriggerSolveAndQueryNotify or NoTriggerSolveAndQueryNotify
In an AttachmentVar the AutoCompress or NoAutoCompress flag can be changed to AutoCompressAndQueryNotify or NoAutoCompressAndQueryNotify
For instance:
For all variables which are flagged with AndQueryNotify, a call will be made to VariableQuery function in the extension anytime the value of that variable is queried (such as the view for the extension being opened or the variable is exported to a spreadsheet and the spreadsheet's view is opened). The variable is passed to the function as an InternalVariableWrapper. Within VariableQuery, the InternalVariableWrapper's tag property will identify which variable's value is being queried and its value can be changed before returning based on the license status (for example, if a license is missing a parameter's value could be reset to HYSYS.EmptyValue_enum.HEmpty). Whatever value the variable contained within the InternalVariableWrapper has is what will be displayed from the VariableQuery. This will still change the value of the internal variable.
Keywords: HYSYS Extensions
References: None |
Problem Statement: Why Does the Tray sizing Utility give the warning: Downcomers are backed up? | Solution: This occurs when aerated liquid backs up into the downcomer due to increased tray pressure drop, liquid height on the tray or fractional losses in the downcomer apron.
When the back-up liquid in the downcomer exceeds the tray spacing, liquid accumulates on the tray above causing downcomer flooding.
Downcomer backup can be addressed by increasing tray spacing, decreasing the bottom downcomer frictional resistance, and/or lowering the overall tray pressure drop.
In Aspen HYSYS if a valve is being used as a tray internal, it is advisable to first of all go To the Design | Tray internals | Section and fill in the actual values for Valve Material and Hole Area % instead of using the default values to eliminate this warning.
If the warning persists then the options listed above can be implemented to address the warning.
Keywords: Downcomers, backed up, Tray sizing Utility, flooding
References: None |
Problem Statement: When should I use the Tray Packing Sizing and Rating (TPSAR) analysis? | Solution: Use the Tray Packing Sizing and Rating Analysis to perform rigorous design and rating/sizing calculations of a converged Acid Gas column. Packing or tray information can be specified relating to specific tower internals, such as tray dimensions or packing sizes, design flooding, and pressure drop specifications. Results include tower diameter, pressure drop, flooding, and tray dimensions.
Limitations:
- TPSAR is only available for columns using the Acid Gas property package. To perform tray or packed analysis for columns with a different property package, select the option Tray Sizing in the Equipment Design folder.
- This analysis can be calculated in Dynamics mode only when triggered on the Dynamics tab on the TPSAR analysis window.
Keywords: TPSAR, Acid Gas, Tray Analysis
References: None |
Problem Statement: I have several streams and unit operations in the main flowsheet. I want to transfer them into a subflowsheet. | Solution: Select all the streams and unit operations you want to transfer, then right click on the selected objects and use the Combine Into Sub-Flowsheet option.
After this, the selected items are transferred into a new subflowsheet.
For V7.3 and older versions, the option is included inside the Cut/Paste Objects.
Keywords: Main Flowsheet, Subflowsheet, Stream, Combine
References: None |
Problem Statement: I have a Fire scenario for a PSV, and I want to use the Supercritical calculation method. However, when I try to select it, it doesn't appear on the dropdown menu. | Solution: The supercritical option can be used to rigorously calculate the relief load for a vessel that contains only a single phase at relieving conditions, with no subsequent phase change during the fire.
There are two reasons why the Supercritical calculation method might not be appearing as an option for the calculation method:
1. The number of vessels is not 1.
2. The
Keywords: Safety Analysis Environment, emergency scenarios, relief load calculation
References: Stream is all liquid or two-phase at normal operating conditions. In this case, the only options available are the Unwetted (API) and Semi Dynamic Flash methods. |
Problem Statement: How to setup the Aspen HYSYS-OLGA Link extension? | Solution: A step-by-step procedure to use the Aspen HYSYS-OLGA Link extension is shown below:
1. Add the OLGA link located in the palette under Upstream buttons. The Aspen HYSYS Upstream license is checked out when the unit operation is placed on the flowsheet.
Â
2. Ensure that the OLGA and Aspen HYSYS servers are connected on the 'Server' page of the Setup tab of the link. From OLGA executable option, look for the location of the OLGA-5.X.exe executable file in the OLGA installation folder.
 Â
3. Specify the model path under OLGA Input Files.
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4. Ensure that the OLGA input file is loaded, before Aspen HYSYS streams can be connected to the link. Make sure the input file and the fluid package (*.tab file) are in the same folder in your disc.
5. Click Connect as shown below. When the connect button is hit, the OLGA license is checked.
Â
6. Then, go to the connections page and select the reference stream and mud reference stream. These are HYSYS streams used to calculate the composition of the non-drilling mud and drilling mud outlet streams.
Â
7. Then, select the HYSYS inlet stream and outlet.
Â
8. Select the OLGA Boundary/Sources for the inlet and outlet. These are OLGA streams and they should be available in a drop down menu if the link is correct.
Keywords: OLGA, link
References: None |
Problem Statement: 1) How can I select the appropriate pump for certain conditions?
2) How can I access pump data from several manufacturers from Aspen HYSYS?
3) How can I simulate a pump using incorporated data for a specific vendor’s model? | Solution: The answer to these questions is PUMP-FLO, the world’s largest database to size and select the right pump for your application. Access it through Aspen One Exchange in the button showed in the Design/Parameters menu of the Pump unit (available from V8.2).
This opens the Exchange tab, where PUMP-FLO can be selected.
Run the plug-in by clicking in the button .
In the first menu (shown below), you can choose a manufacturer and edit properties such as Head, Flow, Inlet temperature and fluid properties.
You can search pumps that are suitable for your process conditions, for a given manufacturer, and choose the appropriate one.
You can then select a pump and check the characteristic curve (the operating point is show by the red arrow).
If the pump is found adequate, you can click ‘Select Pump’. This will import the characteristic curve to the Rating tab of the pump (select ‘Use Curves’):
The data for the curve (Flow-Head-Efficiency) can be seen by clicking in ‘View Curve’.
Keywords: Pump, Characteristic Curve, Manufacturer, PUMP-FLO, Sulzer, Head, Efficiency, Selection
References: None |
Problem Statement: How are the liquid volume flows and liquid volume fractions calculated within the composition section of the material stream worksheet? | Solution: Calculating the liquid volume flow for each component:
The molar flow of a component in a stream is converted to a volume flow. The volume flow of each component can be viewed by choosing 'Liquid Volume Flow' as the Basis in the composition section of the material stream worksheet. HYSYS does the following conversion for each component from molar flow to volume flow:
Mass Flowcomponent= Molar Flowcomponent x MWcomponent
Std Volume Flowcomponent = (Molar Flowcomponent * MWComponent)/(Std Ideal Liquid Mass Denistycomponent)
Calculating the liquid volume fractions for the components in the vapor/liquid phase:
The component liquid volume fractions are then calculated by dividing each phases volume flow by the total volume flow of the stream. An ideal liquid volume flow is calculated for the vapor/liquid phase, and it is this flow upon which component vapor/liquid volume fractions are based.
The vapor component volume fraction:
Vapor Phase Std Volume Flowcomponent = (Vapour Phase Molar Flowcomponent* MWComponent)]/( Std Ideal Liquid Mass Denistycomponent).
Vapor Phase Component Volume Fraction = (Vapor Phase Std Volume Flowcomponent)/(Vapor phase Std Volume Flow Flow)
The liquid component volume fraction:
Liquid Phase Std Volume Flowcomponent = (Liquid Phase Molar Flowcomponent* MWComponent)]/( Std Ideal Liquid Mass Denistycomponent).
Liquid Phase Component Volume Fraction = (Liquid Phase Std Volume Flowcomponent)/(Liquid phase Std Volume Flow)
Please note that the property Actual Gas Flow is calculated using a rigorous vapor mass density calculation at the stream temperature and pressure, but the phase volume component fractions reported by HYSYS are based on ideal liquid densities.
Attached is an example simulation which demonstrates the above equations in a spreadsheet.
Keywords: Liquid Volume Flow, Liquid Volume Fractions, Material Stream
References: None |
Problem Statement: How do I extend SLI set? | Solution: SLI is automatically managed by the simulator. If you extend the TIM set, SLI will be automatically extended the next time the simulator is run.
For more information, please also refer about the SLI and DTU entries in SCM Help.
Keywords: SLI set
TIM
DTU
References: None |
Problem Statement: Simulator runs twice if the Planning Board is open. This occurs when user performs an activity on the Planning Board and when a routine executes the M SIM command. | Solution: It is by design that the simulator will run twice if the planning board is open and M SIM command is fired - once for the command and once because the planning board is opened. (M SIM runs when the planning board is opened).
Keywords: Simulator
References: None |
Problem Statement: Where does the built-up backpressure value (7.252 psi /0.5 bar) come from in Safety Analysis environment? | Solution: The 7.252 psi or 0.5 bar (depending on the units set) is a default value with no technical basis. The user can and should change this value for their particular analysis.
In order to changes this value go to the selected sizing scenario. In the Scenario Setup tab look for Total Backpressure and click on Edit button (Calc... in V8.3). The Backpressure (BP) Parameters window is displayed where you can modify the Built-up Backpressure as shown below.
Keywords: PSV, Backpressure, Built-up Backpressure, Safety analysis environment
References: None |
Problem Statement: Quick Start Deployment Guide for IP.21 Process Browser and Plant View | Solution: Plant ViewTM provides access to plant data within Aspen PlusTM or Aspen HYSYSTM so that plant data can be viewed side-by-side with simulation results. Â
Activating Plant View requires three components:
           1. Aspen InfoPlus.21 V8 or other plant data historian
           2. IP.21 Process Browser V8
           3. aspenONE V8 Engineering Suite of Products
www.aspentech.com
Worldwide HQ
200 Wheeler Road
Burlington, MA 01886
UNITED STATES
Contact:
http://support.aspentech.com
Configuration
Aspen IP.21 Process Browser must be installed and configured on a Windows 2008 R2 server which is in the application user's corporate domain and administered by a local administrator. When configuring the ADSA (Aspen Data Source Archive) settings for Process Browser, it can either be configured to point to an IP.21 or non-IP.21 data source server. If a non-IP.21 historian is being used, you must add the appropriate configured services to the ADSA client.
Keywords: IP.21, Plant View, Aspen HYSYS, Aspen Plus, product compatibility, interoperability
References: s are from the Aspen InfoPlus.21 Product Family Installation and Configuration Guides.
Typical Install for IP.21 Process Browser (Recommended)
Ø The Prerequisites for Installing the IP.21 Product Family are:
o Microsoft .NET Framework 3.5 SP1
o Microsoft .NET Framework 4
o Internet Explorer 9
o Latest version of Java (Version 7, Update 10)
Ø In IIS, select Windows Role Services-(Installation-Appendix C)
Ø In the IP.21 Custom Install, Choose Products in the MES family (Installation-Chapter 3):
o Administration Tools
o Web Server (This is the IP.21 Process Browser product)
Ø Critical patch for Aspen MSC v8.0 (Installation-Chapter 3).
Ø ADSA Configuration-to configure data source directory server (Configuration-Chapter 7)
o Name the Plant Data Server for the Directory Server
o Select Web Service
o Select User or Public Data Source
o Add Following Services (Specify data source location):
§ Aspen Process Data (Type of Data Source: IP.21 PI, PHD, Etc.)
§ Aspen Process Data Service
§ Aspen Process Subscription (Generic)
§ AspenSQLPlus Service Component
Ø Verify IP.21 Process Browser Installation (Installation-Chapter 4)
User Access
Desktop/Laptop: aspenONE Engineering Suite should be installed
*In the Plant View Environment, click the “Source� button on the ribbon to specify the web server: http://<servername>/web21/processdata/atprocessdatarest.dll
Use the Data Source drop down to specify the data source. |
Problem Statement: How do I change reference temperature for the calculation of HHV and LHV in Aspen HYSYS? | Solution: HHV and LHV reported under Gas Properties are calculated at 15C and 1 atm.
If required user can change this reference temperature to 0C from Correlation Manager | Gas.
Note: Heating values reported under standard properties are calculated at 25C and 1 atm.
Keywords: Heating value basis, LHV basis, HHV basis etc;
References: None |
Problem Statement: The internal stream inside my column subflowsheet environment does not report the same values as the column stage data? | Solution: Inside the column environment it is possible to export stage data from inside the column into a stream located within subflowsheet environment. The steps for this process are documented inside knowledge baseSolution 144437. After the column has converged, the internal streams in the column subflowsheet will be flashed as a PH Flash. If there is an aqueous phase present within the column, the temperature of the internal stream might be different to the properties provided for the column stage. This discrepancy is expected since the liquid phases in the column might not be checked during the column convergence sequence.
This discrepancy between the column stage and the internal stream is due to the column not checking for two liquid phases. This can be resolved by choosing the 'Sparse Continuation Solver' option of the available solving methods and also selecting the 'Two Liquids Check' box to handle two liquid phases in the column. As the column will now be using a different solver algorithm, the user is recommended to review the column specifications which are found in the Design|Monitor section of the column environment.
Keywords: HYSYS, Column, Internal Streams
References: None |
Problem Statement: How do I setup a feedforward controller in Aspen HYSYS through the PID controller? | Solution: The setup of the feed forward controller in Aspen HYSYS can be configured within the PID controller. The option to select a feedforward controller is within the parameters tab within the PID controller. The user must select to enable the feedforward controller:
The feedforward controller consists of a lead-lag function with an adjustable gain. A dead time function can be added if the effect of the disturbance has a long time delay. The time constants are the lead and lag constants which are set to get the correct timing for the control action. The transfer function for when feed forward function is selected inside the controller is provided in the Aspen help guide and it is also shown below:
Where Kp is gain, Tp1 and Tp2 is the time constant and d is the delay. It is also possible to setup a feedforward controller using an alternative design. Knowledge baseSolution 143950 highlights an alternative method to setup a feed forward controller using a function generator.
Keywords: HYSYS, HYSYS Dynamics,
References: None |
Problem Statement: When using the tray sizing utility, what are the results of the Trayed tab in the Performance section? | Solution: The columns that are displayed are the following:
Delta P This is the total pressure drop considering the sum of dry pressure drop, clear liquid height on the tray, and any residual pressure drop terms that might apply to the column. The units are the pressure units the current unit set has in your simulation.
Delta P (ht of liq) This is the total pressure but in liquid height units; this is defined by the following relation:
Pressure drop in conventional units/(Density of liquid exiting the tray*Gravity).
The result should be in length units.
Dry Delta P (ht of liq) -This is the average pressure drop when the liquid flow is zero so no liquid height is considered on trays. The same relation as in total Delta P is used to determine the liquid height.
Keywords: Tray Sizing utility, column pressure drop, HYSYS.
References: None |
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