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Problem Statement: How does Model Liquid Choking check box affects Cv calculation in HYSYS DYN? | Solution: When Handle multi-phase flows rigorously is checked, HYSYS performs the sizing method with consideration of mixture of vapor and liquid. But this option may be found disabled if the inlet flow has no vapor (i.e. vf=0). You can see 6-162 in HYSYS OPS guide on this topic.
When Model Liquid Choking is checked, HYSYS performs an extra test of liquid chock flow. In the test, if the pressure of the valve outlet falls below the vapor pressure of the liquid, and Frictional Delta P (Pin - Pout) is greater than Frictional Delta P allowable then, Liquid Chocking Status is ON (active!), hence the sizing method will now consider a liquid choking calculatio.
HYSYS OPS guide (HYSYS V7.1) provides general information regarding the valve sizing methods in HYSYS, refer to section 6-146~6-177, Sizing Theory and equations therein.
Keywords: Cv, Liquid choking, choking, sizing, size, valve
References: None |
Problem Statement: How to Obtain Isentropic Expansion Coefficient Using Aspen HYSYS? | Solution: Aspen HYSYS could not directly report Isentropic Expansion Coefficient, k.
Based on the equation Definition: -V/P(dP/dV)T*Cp/Cv, we could get numerical derivative of dP/dV at equal temperature condition.
Actual volume and Cp/Cv are reported in Properties page at actual condition. You can calculate the Isentropic Expansion Coefficient k. A hand calculation is provided in thisSolution for your reference. It uses 1 Pa to get the derivative. You may try to use different value until derivative is not changing too much. Refer to the attach the file, for your reference.
Keywords: Isentropic Expansion Coefficient, Aspen HYSYS
References: None |
Problem Statement: In critical property utility, Zc value is same for all pure components, when I pick Equation of State Model. Why? | Solution: This is the nature of cubic equation of state. Except some special cases, most EOSs have a fixed Zc value, no matter what compound is used because Zc only depends on the formula and some constants of the EOS. If you try different EOS, you will find that for different EOS, they have a different value, but not compound dependent. This information about compressibility factor can be accessed from thermodynamics text books. The text book mentions that many substances have very similar compressibility at critical point.
Keywords: critical, compressibility, Zc
References: None |
Problem Statement: Are there any improvements to the Macro Language Editor in Aspen HYSYS V7.2? | Solution: It is now possible to run up to 10 specific macros directly from the Tools menu.
The macro explorer allows for direct access to the first ten macros in the designated folder. The user can use the session preferences to enter a folder for the macros as shown below:
Keywords: MLE, Enhancement, New, V7.2, Improvement
References: None |
Problem Statement: API-RP-14E Erosion Velocity estimation in Aspen HYSYS | Solution: The API-RP-14E recommends C=100 for Continuous services. However, the empirical constant is not dimensionless and when user uses SI units the C is corrected by a factor of 1.22.
This conversion was not implemented correctly in the older versions (V7.3). The users will require to multiply the erosion velocity by 1.22 if using the Field units. The values are correct for SI units.
The conversion from Field and SI units has been fixed in V8.0 and new versions.
Keywords: Erosion Velocity, API-RP-14E
References: None |
Problem Statement: What is the PR option in the GCEOS fluid package? | Solution: GCEOS model is used to define and implement your own generalized cubic equation of state including mixing rules and volume translation. When you select PR option from within the GCEOS it reduces to the PR EOS.
This is the Standard PR, not HYSYS PR. The main difference between standard PR and HYSYS PR is the alpha function used (HYSYS PR uses a modified alpha function when acentric factor is greater than 0.49). It is recommended to use Hysys PR or PRSV property package, rather than using GCEOS and modifying this to PR. HYSYS PR is more advanced and continuously improved over years.
Keywords: GCEOS, PR
References: None |
Problem Statement: Fluctuation in liquid holdup volume for LNG in Dynamics | Solution: You can get in to this problem if number of zones needed is very less than what you have specified. Depending on the temperature difference between the inlet and outlet streams, you will need zones. Increasing the number of zones helps in stabilizing the LNG dynamics.
You can momentarily get around this problem by changing the parameters of the Auto Prevent Temp. Cross. Change the value of 1e-2 to 1 and the value of 1 to 100 and the lines go more stable.
Although, you still get the occasional upset. The Auto Prevent Temp cross is sort of taking the role of better distributing the duties between the limited number of zones you have, but when it does a change, it immediately results in a significant upset and those are the upsets you still see. As you will see, the upsets are too big, you really need more zones. It just serves to prove the point that you need more zones really.
Notes:
Reach small split steps (0.001-1000): The rate to decrease the heat transfer area of entrance section for convective elements. A small enough value will help preventing the temperature cross.
Reach even split steps (0.1-1000): The rate to reach the even split for the two section areas in the heat zones.
Keywords: LNG
References: None |
Problem Statement: Why do I see a negative pressure drop across the orifice plate in Aspen Hydraulics in certain conditions? | Solution: Normally one would expect a pressure drop across the orifice plate. However, sometimes users may find an increase of pressure instead of decrease.
This can happen when the flow is choked. If this unusual behaviour is observed then check the following:
1. The flow rate across the orifice is reasonable.
2. If the users do not wish to consider choked condition then this option can be unchecked in the steady state in the Hydraulics sub-flowsheet as shown below.
This box is selected by default to control the fluid velocity less than the speed of sound.
Now Go to Orifice Plate | Design | Data | Solver Variables, and change the Compressible Transition from 0.15 to 1.
Run the case again.
3. For convergence issues try to specify the outlet pressure of this Hydraulics sub-flowsheet and let the inlet pressure be calculated, which may help the convergence. Relax the tolerance in Steady State page may also help the file to converge.
Keywords: Choked flow, Hydraulics, Orifice Plate
References: None |
Problem Statement: What effect does a user defined standard temperature have on standard flows? | Solution: This Tech Tip gives a brief description of the standard flow properties in Aspen HYSYS. For full details see section A.6 of the Aspen HYSYS Simulation Basis pdf manual.
Std Ideal Liq Vol Flow
Standard Ideal Liquid Volume Flow is based upon the individual ideal liquid densities of each component at standard conditions and consequently does not include any mixing effects. The ideal liquid densities for each component (found on the Critical tab of each pure component property view) are tabulated at 15C, and are therefore not affected by the standard temperature settings specified in the session preferences.
Liq Vol Flow @ Std Cond
Liquid Volume Flow at Standard Conditions is determined based on a rigorous standard liquid density calculation. This value is obtained by calculating a liquid density using the COSTALD method for each phase at standard conditions, and thus includes mixing effects. The standard temperature here depends upon the settings specified in the session preferences (seeSolution 130604 for more information). Note that the density and flow will be reported as <empty> if the pseudo critical temperature of the stream is below the defined standard temperature (the pseudo critical temperature is the molar sum of the component critical temperatures as described inSolution 109290).
Std Gas Flow
Standard Gas Flow is calculated based on the molar volume of an ideal gas at standard conditions. The standard condition used here depend on the temperature units in use by Aspen HYSYS (if C or K are used, standard temperature is taken as 15C, otherwise 60F is used).
Keywords: Volume Flow, Standard, Ideal, Actual, Gas
References: None |
Problem Statement: How do I copy a PFD table so it can be pasted into MS Excel or MS Word? | Solution: A PFD table is not a valid object for copy and paste functionality. If you press Ctrl+C after selecting a PFD table, you will receive the following error message:
To avoid this problem, double click on the PFD table to open the property view. Hold down the Ctrl key and click individually on every cell you want to copy. Press Ctrl+C to copy the contents of the table to the clipboard; press Ctrl+V to paste into another application.
Keywords: copy, PFD, table
References: None |
Problem Statement: Validation of hydrate formation in hydrocarbon and CO2 rich gas processes | Solution: There are frequently asked questions from users regarding the quality of hydrate predictions using the Hydrate Formation Utility available in Aspen HYSYS. This knowledge basedSolution has been created to present the validation of hydrate formation with experimental data found in the published literature [1, 2]. The validation shown for hydrocarbon stream is shown with and without Ethylene Glycol. Ethylene Glycol is a hydrate inhibition agent. The attached Excel spreadsheet contains the data and hydrate results generated from HYSYS. There are two HYSYS files attached with thisSolution one for hydrocarbon and the other for CO2 rich gas streams.
Figure 1 shows the prediction of hydrate formation temperature in hydrocarbon processes containing methane(CH4), ethane(C2H6), propane(C3H8), butane(C4H10), pentane(C5H12), hexane(C6H14),2-methylpropane(C4H10), benzene(C6H6), cyclohexane(C6H12), methylcyclopentane(C6H12), 2-methylbutane(C5H12) and water(H2O).
Figure 1: Hydrate prediction in hydrocarbon process [1].
Figure 2 shows the hydrate prediction temperature in CO2 rich gas processes containing nitrogen(N2), methane (CH4), ethane (C2H6), carbon dioxide (CO2) and water (H2O).
Figure 2: Hydrate prediction in CO2 rich gas process [2].
Keywords: Ethylene Glycol, Hydrate Formation, Hydrate Validation
References: s:
1. Effect of Ethylene Glycol or Methanol on Hydrate Formation in Systems Containing Ethane, Propane, Carbon Dioxide, Hydrogen Sulfide or a Typical Gas Condensate. Ng, H.-J.[Heng-Joo], Chen, C. J. and Robinson, D. B.[Donald B.]. DB Robinson & Associates Ltd. Research Report 92, Edmonton, Alberta, Canada, 1985.
2. Experimental and modeling studies on the hydrate formation of CO2 and CO2-rich gas mixtures. Fan, S. S., Chen, G.-J.[Guang-Jin], Ma, Q. L. and Guo, T.-M. Chem. Eng. Journal 78, 173-178. 2000. |
Problem Statement: When double click on a Aspen HYSYS .hsc file in Windows Explorer, the file is opened in the default version of Aspen HYSYS. How can I set up the default version of Aspen HYSYS? | Solution: You have to register the version which you want to set up as a default version when you open any file. You can register the default version from the command prompt. Open the Administrator Command Prompt, go to C:\Program Files\AspenTech\Aspen HYSYS 2006.5, and type hysys /regserver. A pop-up window will say that it was successful.
If the above procedure has not worked Open the Administrator Command Prompt and type the following including the quotations:
C:\Program Files\Aspentech\Aspen HYSYS 2006.5\hysys /regserver
For the versions later than 2004.2, i.e., 2006, 2006.5, V7.0, you can restore file association from Start | Program | Aspen engineering Suites | Aspen Hysys, and right-click on the Restore File Associations.
After running Restore File Associations, whenever you double-click to open a HYSYS file, it will be opened in the default version.
There is another way you can set up the default version of HYSYS. The steps are as follows:
-You right click the file | select Open with option | then select Choose program and you will see the window like the snap shot below.
You select any of Aspen HYSYS.Plant simulation software and click on check box of ?Always use the selected program to open this kind of file?. The only problem with this method is that you have to try one by one to get your preferred version as it does not show the version number directly.
The referenceSolutions on the same issue are 119947,123977 and 124669.
Keywords: open file, default, version, restore File Association, administrator, command prompt
References: None |
Problem Statement: Suppose the Define from Other Stream option was used to initialize a new stream. Later the model is developed into a non-trivial sized flowsheet. Given that the source stream ID is not recorded within the Aspen HYSYS simulation, is it possible to find the source stream where the current stream data was copied from? | Solution: Currently this information is not recorded as part of stream data. The idea here is to capture the identical elements between the original and the copy. If the temperature, pressure and compositions are copied, the temperature, pressure and molecular weight must be the same. If only compositions are copied, molecular weight must be the same.
If we can tabulate temperature, pressure and molecular weight of all streams on PFD and sort the values of molecular weight, we can find the matching streams.
The implementation of this idea is carried out using the available HYSYS Stream Reporter (KBSolution 110500 and 121701), an Excel workbook with macros. The user should select correct version of the HSR file and choose Temperature, Pressure and Molecular Weight as stream properties to generate the report table. The data on this table can be transposed so that one property occupies one column on spreadsheet. Lastly, a user can used Data | Sort to sort based on any of the selected properties. Detailed steps and screen shots are given in the attached Word file.
Keywords: sorting, define, source, stream
References: None |
Problem Statement: When using the Fired API521 mode within the Depressuring Utility in HYSYS, if the C3 value is specified to 0, the results are the same as the adiabatic mode. This is inconsistent with the Dynamic Depressuring - A Practical Guide document, which states that if C3=0, the initial wetted area is used during the duty calculations. | Solution: The Dynamic Depressuring - A Practical Guide document corresponds to an earlier version of the Dynamic Depressurization Utility. Even though it is still a useful guide for the many aspects of the utility, some changes have been made to the application. Since v2004, the wetted area is no longer calculated by the stated equation:
Wetted area(t)=Wetted area(0)*(1-C3*(1-LiqVol(t)/LiqVol(0))) [A]
Instead, it is automatically calculated from the level in the vessel within (using the stream conditions and the vessel holdup). Also, the equation stated in the practical guide for the calculation of the Heat Flux in Fired Wetted mode has been replaced with the newer one which includes a different definition of the C3 parameter,
Q=C1*(C3*WettedArea(t))^C2 [B]
The C3 constant above does not correspond to the constant used in equation A and instead works as an Environmental factor used to de-rate the fire calculations due to mitigating circumstances (such as a partially buried vessel, etc.). The equivalence with the Environmental Factor, F, defined in the API521 is,
F=C3^0.82 [C]
Notice that when C3=0, no duty is applied and the Fired API521 reduces to the Adiabatic mode.
Keywords: Depressuring, API521, Fired, Wetted, Equation
References: None |
Problem Statement: When I have different streams connected to a mixer and one of them has zero flow, the outlet stream does not have the same temperature as the feed stream with a flow. | Solution: When there is a material stream without a flow entering a mixer and this stream has a lower pressure that the other material streams entering the mixer, the outlet stream from the mixer shows a different temperature to the one expected.
The reason for this could be that the mixer is using the lowest pressure of all streams entering the mixer to calculate the outlet temperature.
A work-around could be to select the Equalize All option on the Design | Parameters page of the mixer to make all the pressures the same.
Keywords: Pressure, Temperature, Mixer
References: None |
Problem Statement: How does one change the number of stages in a distillation column? | Solution: Two methodologies can be employed; change the total number of stages by supplying a new value in the Num of Stages entry box (on the Design | Connections tab) or click the Edit Trays button on the Design | Connections tab and provide required information.
Changing the total number of stages results in Aspen HYSYS estimating feed locations by attempting to maintain stripping and rectifying stage ratios. This approach typically requires some addition input from the user in order to define the correct feed and draw locations.
Using the Edit Trays button gives the user control over where the specific stages are removed and should not require further manipulation one complete.
Keywords: Top, Bottom, Add, Remove, Tray, Stage, Column
References: None |
Problem Statement: How does one generate a cooling curve for an air cooler? | Solution: Starting with Aspen HYSYS V7.3 you can generate the cooling curve within the Air Cooler unit operation via the Performance tab (selecting the PLOTS page will display the curves in graphical format, whereas the TABLES page will display the results in a tabular form).
For Aspen HYSYS V7.2 and lower versions the air cooler operation does not have the same functionality as the air cooler in V7.3 or heat exchanger unit operation in regards to the plotting of enthalpy curves. The simplest way to achieve a similar result from an air cooler in Aspen HYSYS V7.2 and lower version is to model the same heat transfer using a heat exchanger as in the attached case.
Heating / cooling curves can be obtained for a heat exchanger in Aspen HYSYS via the Performance tab (selecting the PLOTS page will display the curves in graphical format, whereas the TABLES page will display the results in a tabular form).
Note that selecting the Exchanger Design (Weighted) model from the Design | Parameters tab allows one to dictate how many intervals are used when generating the enthalpy curve.
Keywords: Cooling Curve, Performance, Air Cooler
References: None |
Problem Statement: Which fluid package is recommended to predict CO2 solubility in oil and water? | Solution: In general for a system with CO2 dissolved in water, we recommend the Peng-Robinson equation of state. This is valid for temperatures higher than -271 C and pressures lower than 100000 kPa. For a low pressure system (sub atmospheric) you may find that an activity model (like NRTL) may give better results.
Peng-Robinson applies some special functionalities to particular BIPs. H2S, CO2, and H2O are among those receiving special treatment. For example, the BIPs for the pairs of H2S-H2O and CO2-H2O are treated as functions of temperature. This helps the model to better represent the behaviour of systems containing these components.
As an alternative, the PRSV equation of state should also be considered. It can handle the same systems as the PR equation with equivalent, or better accuracy, plus it is more suitable for handling moderately non-ideal systems. PRSV does not use temperature dependent CO2-H2O BIPs like PR does.
Keywords: Fluid package, CO2 solubility
References: None |
Problem Statement: What is REFPROP under fluid package in Aspen HYSYS when I select Aspen Properties radio button? | Solution: REFPROP fluid package is from NIST contains properties of some components (pure components, refrigerants etc). REFPROP models to evaluate thermodynamic and transport properties of a mixture.
The NIST databank in Aspen Properties contains the REFPROP components. However, you have to choose RefProp (REFPROP in Aspen Plus) as the fluid package (property method) to use REFPROP models.
You can access REFPROP components via NIST databank in Aspen Properties but RefProp is not available as a fluid package in Aspen HYSYS V7.0. RefProp is available in Aspen HYSYS V7.1 and up.
Keywords: REFPROP
References: None |
Problem Statement: What is the difference between 'vapour-liquid-liquid' and 'vapour-liquid-free water' and 'vapour-liquid-dirty water' options available in Aspen properties 'Phase handling' options? | Solution: Vapour-liquid-liquid option basically uses rigorous three-phase calculations to determine water in all the phases. The vapour-liquid option with free water or dirty water is usually used in modeling water-hydrocarbon systems. The free water or dirty water calculations are completely rigorous, except for the assumption that the water phase is pure (free water) or has only a trace amount of organic components (dirty water).
For water-hydrocarbon systems, Free water calculations are normally adequate. The hydrocarbon solubility in the water phase is generally negligible. In applications where the hydrocarbon solubility in the water phase is of great concern (such as in an environmental study), use dirty water or rigorous three-phase calculations. For chemical systems such as water-higher alcohols, Free water or dirty water calculations do not apply. Solubility of the organics in the water phase is significant. Rigorous three-phase calculations are required.
Keywords: Aspen Properties, Vapour-Liquid-Liquid, Vapour-Liquid-Free water, Vapour-Liquid-Dirty water
References: None |
Problem Statement: When will Windows 8 be supported? | Solution: Windows 8 is supported in V8.2.
The supported platforms for V8.2 are the same as in V8.0, with the addition of Windows 8 (64 bit only):
Desktop:
Windows 8 Enterprise (64 bit)
Windows 8 Professional (64 bit)
Windows 7 Enterprise SP1 (32 and 64 bit)
Windows 7 Professional SP1 (32 and 64 bit)
Windows XP Professional Edition SP3 (32 bit)
Server:
Windows Server 2003 R2 Standard SP2 (32-bit)
Windows Server 2003 R2 Enterprise SP2 (32-bit)
Windows Server 2008 Standard R2 (64-bit)
Keywords: None
References: None |
Problem Statement: How can I save a report in *.mdi or *.pdf format so that I can print it later? | Solution: You can save the report in *.mdi and *.pdf format to print it later on. Note that you should have acrobat writer if you want to get report in pdf format and you should have Microsoft office if you want report in mdi format. Below are the steps to save a report:
After creating the report, highlight the report and click 'preview'.
While report is open, pick 'print setup' from the top.
From print setup window, pick 'Microsoft office image document writer' (if you have acrobat writer, select option for that )from the printer name drop-down list.
Press 'OK' and after that click on 'print' to save this report in *.mdi ( or *.pdf) format.
In 'save as' dialogue box, give it a name and save it.
Keywords: mdi, pdf, print, report, save.
References: None |
Problem Statement: How do I prevent the warning message when I click on Interactive Size Rigorous Shell & Tube in Heat Exchanger? | Solution: If user is having multiple version of Aspen HYSYS and EDR installed on same machine then below warning message appears when user click on Interactive Size Rigorous Shell & Tube from Size Rigorous Shell & Tube drop down menu
This is due to incorrect version of EDR registered
User can register correct version of EDR from below path
Start/Programs/AspenTech/Exchanger Design and Rating V8/Version Control Utility
User need to select version 27 for EDR V8 version
Keywords: Hysys and EDR warning message, Interactive Size Rigorous Shell & Tube waning, Heat Exchanger warning in HYSYS, HTFSplusDesignObject
References: None |
Problem Statement: Why is the total amount of water fraction in the Light Liquid product stream different from the user specified carry over fraction of Heavy liquid in light liquid? | Solution: When modelling water carry over in a 3 Phase Separator, the overall fraction of water in the light liquid product stream differs from User specified fraction of Heavy liquid in Light liquid product stream.
The light liquid product stream is separated in the 3 phase separator as a saturated stream.
The option for the user to specify the fraction of heavy liquid in the light liquid product stream refers to the fraction of water in the aqueous phase of the light liquid product stream. This means the additional amount of water in the stream excluding the fraction required to saturate the stream.
The screen shot below shows a carryover set up where user has specified 0.005 fraction of water to be carried over in the Light Liquid (hydrocarbon) product stream.
Looking at the composition of the light liquid stream as below, it reports the overall fraction of water in the stream as 0.0062. This is because the stream requires 0.0012 fraction of water to be saturated and an additional 0.005 fraction of water to be carried over in the aqueous phase.
Keywords: Carry Over, 3 Phase Separator, Heavy liquid, Light liquid?
References: None |
Problem Statement: What's New in Aspen HYSYS V7.2 - Rate-Based Distillation | Solution: In V7.2, the full power of the well-established rate-based distillation calculations from Aspen Plus are now available in the Aspen HYSYS simulator. This provides the HYSYS simulation user with the ability to accurately model distillation towers in which mass transfer rates and heat transfer rates play important roles in the performance of the tower. The rate-based distillation unit operation model is applicable to both packed towers and trayed towers, and a large number of options are available for each of these two classes of towers.
The rate-based distillation models use Aspen Properties to model the phase equilibrium in the tower. This allows the use of sophisticated electrolyte thermodynamic packages which rigorously model the chemical reactions between the solvent and the gases to be absorbed. In particular, this enables the accurate modeling of amine systems which are commonly used to absorb CO2 and H2S from gas streams both upstream processing facilities and refineries. A mix of both equilibrium reactions and kinetic reactions can be included in the electrolyte representation of the liquid phase, as appropriate.
In addition to the normal configuration information used to specify distillation tower models (i.e., tray type, tray dimensions, packing manufacturer, packing type, packing characteristics, pressure drop models, etc.), a large number of rate-based configuration options are available in the unit operation model. These configurable options span areas including:
Flow models (vapor / liquid contacting models)
Film resistance options
Mass transfer correlations
Heat transfer correlations
Interfacial area correlations
Liquid holdup correlations
Adjustment factors also available for interfacial area and heat transfer to allow final trim corrections to match observed unit performance
The simulation user can configure the rate-based distillation towers to have different characteristics in different sections of the tower, allowing appropriate selection in each section to match the configuration as accurately as possible. It is also possible to utilize user-supplied correlations instead of the list of selectable built-in correlations for mass transfer, heat transfer, etc., if desired.
Keywords: Rate-Based Distillation, New V7.2
References: None |
Problem Statement: What are the differences between Active, Estimate and Current spec check box options in column in Aspen HYSYS? | Solution: The Active, Estimate and Current checkboxes enable to specify the status of the specification in column.
The active specification is one that the convergence algorithm is trying to meet. An active specification always serves as an initial estimate. An active specification always exhausts one degree of freedom.
An estimate is considered an inactive specification because the convergence algorithm is not trying to satisfy it. The value then serves only as an initial estimate for the convergence algorithm. An estimate does not exhaust an available degree of freedom.
When the Active checkbox is activated, the Current checkbox automatically activates. You cannot alter this checkbox.
When Alternate specs are used and an existing hard to solve spec has been replaced with an Alternate spec, this checkbox makes it clear to you the current specs used to solve the column.
Keywords: Active, Estimate, Current specifications, column
References: None |
Problem Statement: After selecting the PVT launch engine button, the error message appears on the screen Access Violation Address 004cb232 in Module @PVTProPkg.exe' Read of address FFFFFFFF in Windows XP. | Solution: DBR PVT PRO will try to write a file in C:\Program Files\Common Files\hyprotech\DBRPVTProPkg. The file name COMThermoPVTPro.Pro would generate during running PVT Pro environment. If your system folder C:\Program Files folder is write-protected, you will get the following message: Access Violation Address 004cb232 in Module @PVTProPkg.exe' Read of address FFFFFFFF.. In order to work, you need have modify rights to the above folder.
Keywords: PVT environment, PVT Pro, Upstream.
References: None |
Problem Statement: How do I ensure that every time I load the same preference file through automation (OLE)? | Solution: Here is the code that sets the preference file via Automation.
Dim hyApp As HYSYS.Application
Set hyApp = GetObject(, HYSYS.Application)
hyApp.LoadPreferences d:\myprefs.prf
Note: Change the text d:\myprefs.prf to match your preference file, this only works when a case is open.
Keywords: OLE, automation, preference file
References: None |
Problem Statement: How does a user capture maximum percentage opening of a valve in a dynamic scenario where the valve opens and closes? | Solution: It can be easily achieved via using a user variable associated with the valve. The code looks following:
Sub DynPressureFlowPreStep()
Dim Val As Double
Val = ActiveVariableWrapper.Variable.GetValue
If(activeobject.PercentOpenValue > Val) Then
Val = activeobject.PercentOpenValue
End If
ActiveVariableWrapper.Variable.SetValue Val
End Sub
To see an example, run the attached case, notice Reboil Valve's user variable tts, its initial value is 0. Notice also the valve's opening is shown on the Rating's page. Now kick off the solver, notice tts value matches the valve's opening during the opening phase, but tts value remains at maximum value when the valve is closing. So effectively tts actually captures the maximum opening during the time window the model is run.
Keywords: Maximum, opening, track
References: None |
Problem Statement: How is it possible to modify my component list via the Hysys Workbook without removing any component from my simulation? | Solution: In a Hysys simulation, a user can modify the components shown in the Workbook so that not all used in the simulation are visible.
To modify go to Workbook in the Home tab, this will create a Workbook tab in the Hysys ribbon. In Setup|Workbook tab window, select Compositions. In the Variables window select one component and then Delete, however this will clear the entire component list.
The current workaround for modifying variables in Compositions tab is
1. Delete all the variables from this tab.
2. Use Add button to append the desired components individually.
Keywords: Workbook, Modifying Workbook, Workbook tabs
References: None |
Problem Statement: Why different flash point method gives very different results? Which one should I use? | Solution: Different flash point methods are applicable for different type of streams. A wrong method can lead to a very wrong result.
The default method for Flash Point calculations in HYSYS (via the Cold Properties Utility, for example) is calculated by the API 2B7.1 method. The temperature range for the flash point calculation are not the actual process temperature but the ASTM D86 10% point. The accepted range is 65 C (150 F) < ASTM D86 10% point < 621 C (1150 F).
According to ASTM, the TAG method covers the determination of flash point of liquids with a viscosity below 5.5 cST at 40C (104F), or below 9.5 cSt at 25 C (77 F) and a flash point below 93C (200F).
The Pensky-Martens method is used for liquids with a viscosity of 5.5 cSt or above at 40C (104 F), or a viscosity of 9.5 cSt or above at 25 C (77 F), or a liquid that may contain suspended solids or have a tendency to form a surface film under test conditions. It is basically for heavier fluids than the TAG method. The flash point range is 40 C (104 F) - 360 C (572 F).
Keywords: Flash point, methods, applicability
References: None |
Problem Statement: How do I enter the compressor head in kJ/kg in the compressor curves? | Solution: The default unit for compressor head in the curves is in length (e.g., m, ft). If the data from the compressor vendor is in kJ/kg then the data can be converted to meter (m) and then entered in the curve data. An alternative approach would be to create a unit set cloning from the current unit.
curves[m] = curves[kJ/kg^]*1000/g
For HYSYS V7.3 and older versions a unit set can be cloned Tools/ Preferences/Variables/Units. After cloning the unit add kJ/kg to the Length unit with a conversion factor of 9.8103e-3 (1 kJ/kg = 9.8103e-3 m). See the screenshot below.
For HYSYS V8.0 and newer versions the unit set can be accessed File/Options/Units of Measure. Select Display unit for Head and then click Add. Specify the unit name and the conversion factor as below.
The new unit for the compressor head can be selected as below.
Keywords: Compressor Curves, Head, kJ/kg
References: None |
Problem Statement: What methods does Aspen HYSYS use in calculating the phase viscosities? | Solution: Aspen HYSYS uses three different models in calculating the phase viscosities depending on the type of system.
1. Mod Ely & Hanley (modification of the NBS method)
2. Twu's model
3. Mod Letsou-Stiel (modification of the Letsou-Stiel correlation)
The best suited model is automatically selected for predicting the phase viscosities of the system based on the following criteria:
All of the above models are based on corresponding states principles and are modified for more reliable application. Internal validation showed that these models yielded the most reliable results for the chemical systems shown. Viscosity predictions for light hydrocarbon liquid phases and vapour phases were found to be handled more reliably by an in-house modification of the original Ely and Hanley model, heavier hydrocarbon liquids were more effectively handled by Twu's model, and chemical systems were more accurately handled by an in-house modification of the original Letsou-Stiel model.
For more details on the models refer to the Aspen HYSYS Simulation Basis Manual A.5.3 Viscosity section.
Keywords: viscosity, phase, methods, correlation
References: None |
Problem Statement: Why are the Auto Water Draw options disabled? | Solution: The Auto Water Draws (AWD) option available on the Parameters| 2/3 Phase page of the column property view allows for the automatic adding and removing of total aqueous phase draws depending on the conditions in the converged column.
The AWD option is available for HYSIM Inside Out (IO) or Modified HYSIM Inside Out (MIO) solvers only with the 2 Liq Check option selected for the Two Liquids Check in the Parameters tab of the Solver page.
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If any of the other solvers are used and for the IO and MIO solvers if the No 2 Liq check is selected then AWD options will be disabled.
Keywords: Columns, Auto Water Draws, Two Liquids Check
References: None |
Problem Statement: I cannot view the files I downloaded from | Solution: 115343.Solution
These files are videos with extension SWF. SWF stands for Small Web Format. This is a file extension for a Shockwave Flash file owned by Adobe.
Therefore, you require Adobe Shockwave Player to open these files. To install, please refer to the Adobe website http://get.adobe.com/shockwave/
After you install Adobe Shockwave Player, you need to open the object in your browser in order for you to be capable of viewing it.
Keywords: extension swf, video,
References: None |
Problem Statement: How to model a Cold Bed Adsorption process in Aspen HYSYS Sulsim (Sulfur Recovery) | Solution: The conventional Claus sulfur recovery process is limited by reaction equilibrium considerations to sulfur recoveries in the range of 94-97%. For applications requiring an intermediate level (97.5-99.5%) of sulfur recovery, the so-called Sub-Dewpoint Claus Process or Cold Bed Adsorption Process (CBA) can be used. This process extends the capability of the Claus process by operating the Claus reaction at a lower temperature, so that the sulfur produced by the reaction condenses.
To model the CBA process in Aspen HYSYS Sulsim (Sulfur Recovery), we should use the Sub-Dewpoint Catalytic Converter unit operation.
The Sub-Dewpoint Catalytic Converter uses the same correlations as the Catalytic Converter and behaves similarly, except that:
· Allows absorption of sulfur liquid into the catalyst, removing it from further processing.
· Can operate at an outlet temperature lower than the sulfur dewpoint.
· Elemental sulfur remains in the catalyst, which will lead to a mass imbalance in the flowsheet, so it must be recovered by regenerating the catalyst frequently.
Keywords: Cold Bed Adsorption, CBA, Sub-dewpoint Claus Process, Sub-Dewpoint Catalytic Converter, Sulsim
References: None |
Problem Statement: Why did the Dynamic Depressuring Utility give different results in each run when the vessel contains 100% subcooled liquid? | Solution: If you are looking at the phase diagram at initial time conditions of the stream used as a Feed to the Depressuring Unit, you would find that the entire vessel somehow goes from the outside of the vapor-liquid envelope as an all liquid fluid, to the inside of the vapor-liquid envelope when venting material through the valve.
The problem is that the vapor phase density calculation fails when crossing the bubble point as the pressure goes down. This, in turn, affects the valve flow computation and, as a result, a severe numerical failure takes place.
DPUs which are full of liquid will eventually partially vaporize their contents, and have similar problems as above. The workaround here is the following: switch to Peng-Robinson in Aspen Properties.
Also, the user should work with a smaller time step size such as 0.1 seconds instead of 0.5 second to avoid numerical noise at some of the variables, in particular the vapor-phase density. (in the DPU property view, Design tab, Operating Conditions page).
Keywords: Dynamic depressuring utility, 100% liquid, Aspen Properties.
References: None |
Problem Statement: In LNG exchanger, the composite curves for both hot passes and cold passes are calculated. How are the composite curves constructed? | Solution: A composite curve is a temperature - enthalpy plot representing the heat availability or the heat demands in a process. A heat curve is the property of a material stream. If a material stream has constant heat capacity, its heat curve will be a straight line linking inlet and outlet temperature of an exchanger. When there are two or more streams for one side (hot or cold), the construction of the composite curve involves the addition of the enthalpy changes of the streams in the respective temperature intervals, as shown in Figure 1 below:
Figure 1. Temperature-Enthalpy Relations Used to Construct Composite Curves
In this example, there are two streams. If we consider three temperature intervals, 50-100 C, 100-150 C and 150-200 C. The enthalpy changes are tabulated below.
T Interval Enthalpy Change Enthalpy Change Enthalpy Change
Stream 1 Stream 2 Total
Keywords: None
References: None |
Problem Statement: The | Solution: for RVP empty case.Solution
This is JapaneseSolution.
Please see attached pdf file (Japanese).
Keywords: Reid Vapor Pressure
RVP
Cold properties
References: None |
Problem Statement: What is the Tray Sizing Utility? What is the difference between Design and Rating modes in Tray Sizing Utility? | Solution: With the help of Tray Sizing Utility you can perform design mode or rating mode calculations on part or all of a converged 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 column diameter, pressure drop, flooding, tray dimensions, and so forth.
The tray sizing utility has two calculation modes:
Design
Rating
In Design mode, Aspen HYSYS enables you to perform a design sizing based on the vapor and liquid traffic in the tower. Available design specifications for trayed and packed sections include the type of tower internals, maximum allowable pressure drop, and maximum allowable flooding. For trayed sections the maximum allowable downcomer backup, maximum allowable weir loading, and various other tray parameters can also be specified.
In Rating mode, Aspen HYSYS enables you to perform rating calculations based on a specified tower diameter and fixed tray configuration. If desired, some of the tray dimensions can be left unspecified and Aspen HYSYS automatically calculate design values for them. To perform a rating on a packed section, only the tower diameter is required.
Note:
The Tray Sizing Utility is only available for columns with vapour-liquid flows.
This utility cannot be used to size the Liquid-Liquid Extractor.
The Tray Sizing Utility must correspond to a single column flowsheet tray section.
Keywords: Tray Sizing, Design and Rating, Packing etc;
References: None |
Problem Statement: In HYSYS, Reid Vapor Pressure is calculated according to several standards. One of them is ASTM D323 82. For some streams, RVP ASTM D323 82 may be shown as empty. | Solution: ASTM D323-82 is a standard procedure for the measurement of Reid Vapor Pressure. Liquid hydrocarbon is saturated with air at 33?F and 1 atm pressure. Since the lab procedure does not specify that the test chamber is dry, the air used to saturate the hydrocarbon is assumed to be saturated with water.
This air-saturated hydrocarbon is then mixed with dry air in a 4:1 volume ratio, and flashed at the temperature of 100?F such that the total volume is constant (since the experimental procedure uses a sealed bomb). The gauge pressure of the resulting mixture is then reported as the RVP.
For HYSYS to calculate the RVP of a given stream, this stream has to be liquid at 33?F and 1 atm. If the stream has a vapor fraction larger than zero, the program will not continue with the calculation and the property for this stream will be shown as empty.
A user needs to identify the streams with petroleum liquids under the conditions of 33?F and 1 atm for this stream property.
Keywords: RVP, Reid Vapor Pressure
References: None |
Problem Statement: What do the different splits types in a component splitter imply? | Solution: The separation fractions or splits (ranging from 0 to 1) must be specified for each component in the stream exiting the Component Splitter on the Splits page.
You can select either the Mass or Molar Basis for each component and select Fraction Type to either Feed Fraction in Products, Fraction in Products or Flow in Products.
If the FeedFrac to Products option is selected, the molar flows going to the overhead and bottoms are calculated as:
ai = xi fi
bi= (1 -∑xi) fi
Where:
xi = FeedFrac to Products, or fraction of component i going to each overhead
If the Fraction to Products option is selected, the molar flows going to the overhead and bottoms are calculated as:
fi = xi a + yi b
Where:
xi=Fraction in Products, fraction of the ith component in each overhead, ∑xi=1
yi= Fraction in Products, fraction of component in bottom, ∑yi=1
a = molar flow of the overhead
b = molar flow of the bottom
If the Flow in Products option, the following applies:
ai =Flow in Products, molar flow of the ith component in each overhead
bi = Flow in Products, molar flow of the ith component in the bottom
Keywords: Component Splitter, Splits, Fraction Type
References: None |
Problem Statement: Can I use the same curves for any liquid assuming volumetric flow vs. head behavior is the same? | Solution: The head in a pump or compressor curve is in terms of the process fluid.
Vendors generally provide pump curve(s) in terms head of water. We can use the same curves for any liquid assuming volumetric flow vs. head behavior is same. The outlet pressure will be different for different fluid due to density difference.
Keywords: pump curve, compressor curve, head, water, process fluid.
References: None |
Problem Statement: How does Aspen HYSYS report phase properties when the fluid is in dense phase? | Solution: Aspen HYSYS reports a vapor fraction for a stream under supercritical conditions as zero or one. Theoretically, this value does not have a specific physical meaning since there is no distinct liquid and vapor phases in a supercritical region. However, for the purpose of flash calculations, Aspen HYSYS will determine the vapor fraction of a dense-phase stream based on the following criteria:
For Phase Identification in HYSYS the default method is the Poling-Prausnitz method (B.E. Poling and J.M. Prausnitz, “Thermodynamic properties from a cubic equation of state: avoiding trivial roots and spurious derivatives�, Industrial and Engineering Chemistry Process Design and Development, 20(1) (1981) 127-130). This method uses the isothermal compressibility (BETA) to identify phase type for phase equilibria calculations.
Keywords: Dense Phase, Phase Properties
References: None |
Problem Statement: How do I access a Cyclone unit and its inlet and outlets through automation? | Solution: The attached MS Excel workbook and HYSYS file are used to demonstrate the access of Cyclone unit and its materials streams via automation. To use this demonstration, the user has to load up the HYSYS file Cyclone Unit.hsc using HYSYS 2006.5 or later first, and then open the Excel workbook.
Next the user will click on the button Get Cyclone Info. The stream names will be updated for the cyclone unit named on cell C8. In the example, the name for the unit is Cyclone. For any user flowsheet, simply change the name accordingly, and the macro will work.
The VBA code can be viewed from Visual Basic Editor, and a snippet is give below.
'Link to the cyclone
Set hyGasCyclone = hyCase.Flowsheet.Operations.Item(Range(UnitName).value)
' Get attached streams
Set hyGCFeed = hyGasCyclone.FeedStream
Set hyGCVaporProd = hyGasCyclone.VapourProductStream
Set hyGCSolidProd = hyGasCyclone.SolidProductStream
Keywords: Automation, cyclone, VBA, macro.
References: None |
Problem Statement: Can I see the mass/molar/volume concentration in a stream in Hysys? | Solution: The mass/mol/vol fraction cannot be directly presented in PPM using Aspen HYSYS in the stream Conditions tab> Concentration. However, the Spreadsheet operation can be used to achieve this. After importing the fraction into a cell inside de Spreadsheet the user need to calculate the concentration in PPM in another cell by multiplying that cell by 1e+6. After that, use the drop down menu Variable Type to specify it as Mass/molar/volume Concentration PPM.
This variable is available in the Tools menu> Preferences> Variables> Formats because is used in some Unit Operations availables only in Aspen Hysys Petroleum Refining like the Hydrocracker (Reactor Section> Specification>Properties/ Conversion)
Keywords: Concentration, ppm
References: None |
Problem Statement: How do I deactivate Enterprise Databanks to get rid of the message at least one databank should be installed and registered in Aspen Properties configuration tool? | Solution: You need to select Legacy Properties Databanks in Aspen Properties Database Selector. The default path to this option is as follows.
Start || Programs || Aspen Tech || Process Modeling || Aspen Properties || Aspen Properties Database Selector. and select the legacy databanks || click OK. Then open HYSYS.
Keywords: at least one databank
References: None |
Problem Statement: How can I add text to my PFD on the New interface? | Solution: On v8.0, the Add Text option is under the Flowsheet/Modify menu, under the Flowsheet section on the Ribbon
On v8.2 and later, this option shows on the Format tab, which appears when you are working on the PFD. This section also gives the user the options to edit the text.
Keywords: Text, label, PFD
References: None |
Problem Statement: The naming convention for the hypo components created by HYSYS Oil Manager includes starting string NBP and an index in a pair of bracket, followed by a string converted from the integer part of the boiling point value. The name for a crude hypo component is generated by Oil Manager and is also updated each time the Oil Manager calculates the blends.
By design, the names of crude hypo components cannot be edited. If the names of components from a blend have to be changed, this document presents a procedure. | Solution: Before proceeding with this method, please understand that this is a circumvention of the design. As a result, Oil Manager will no longer update the components and their physical properties. If the original components are already linked with Spreadsheet, these links will need to be re-built after making the change.
On this screen shot, we see that the component name is in black and cannot be edited.
Let us take the following steps:
1) Identify the blend in the original fluid package and the stream its compositions are installed to;
2) Make a copy of the material stream the blend is installed to in Simulation environment;
3) Export the fluid package with a given file name, say test name.fpk;
4) Import the fluid package test name.fpk to create a new fluid package;
Now you will have a new hypo group with the copy of the original components. The names of the components in this hypo group can be edited (the names are in red).
4) Switch default to the imported fluid package, and change fluid package associations if necessary.
5) In Oil Environment, uncheck Install check box for the blend;
Now the original compositions of the blend are maintained in the stream created in step 2), and the stream is associated with the copied fluid package. You can edit the names of the hypo components in this fluid package.
Keywords: NBP, hypo component
References: None |
Problem Statement: I would like to convert ASTM 3710 boiling point data into a ASTM D-86 via HYSYS. Is this possible? | Solution: There is an open literature published by the DCG Partnership, which is an expert in manufactured chromatographic reference standards for the petroleum, petrochemical and natural gas industries.
The literature states: DCG has available an N.I.S.T. traceable by weight gravimetrically prepared calibration standard for ASTM Method D 3710. ASTM method D 3710 typically is prepared with the highest carbon
number being nC15. Due to customer request, DCG's 3710 calibration standard also contains n-
Alkanes C16, C17, C18, C19, & C20.
This description suggests that users can treat ASTM 3710 curve as TBP mass curve without a big error.
You can find the full literature at: http://www.dcgpartnership.com/Catalog/Standards/ASTM_3710.pdf
Keywords: ASTM 3710, ASTM D-86
References: None |
Problem Statement: How do I combine unit operations and streams from a section of my simulation flowsheet into a Sub-flowsheet? | Solution: On the simulation PFD, highlight every object you want to include in the sub-flowsheet by clicking and dragging your mouse over them. Alternatively, you can hold down the Shift button while you click on all the objects to select them.
Next, right-click on any of the objects selected, the scroll due to the Cut/Paste Objects option on the menu that pops ups.
Then click on the Combine Into Sub-flowsheet option to create the new sub-flowsheet.
Keywords: Sub-flowsheet, PFD
References: None |
Problem Statement: Is it possible to copy a unit operation into a different case? | Solution: Highlight the desired objects on the PFD, then right click on one of the selected icons. Choose one of the following options from the ensuing menu:
Cut/Paste Objects | Copy Objects to File (Export)
Selecting this option allows you to save the copied objects into a file so that they can be used at a later date. To insert the copied objects into a different case, right click on the PFD and select Cut/Paste Objects | Paste Objects from File (Import). Choose the appropriate path using the File Selection window, then press OK.
Cut/Paste Objects | Cut Selected Objects
The selected objects are removed from the existing file and can then be pasted into a different case either by pressing Ctrl+V or right clicking on the PFD and selecting Cut/Paste Objects | Paste Objects.
Cut/Paste Objects | Copy Selected Objects
This option will allow you to create a virtual copy of the existing objects which can then be pasted into a different case either by pressing Ctrl+V or right clicking on the PFD and selecting Cut/Paste Objects | Paste Objects.
Keywords: copy, paste, import, export, stream, unit, operation, flowsheet
References: None |
Problem Statement: Why is the combined/mixed liquid viscosity value generated by the HYSYS Stream Reporter (HSR) different than that reported by Aspen HYSYS? | Solution: In the HSR, the flash calculation for combined liquid is obtained by mixing the aqueous and liquid phases. Unlike the HSR, Aspen HYSYS does not internally flash the mixture of aqueous and liquid phases, but instead directly obtains the combined liquid phase viscosity from the stream object. The same approach can be used in the HSR (instead of using the current method of extracting both liquid and aqueous phases and then mixing and flashing them) by making a minor modification of the existing code.
Set a backdoor variable bd as StreamObj and then access viscosity using the following moniker:
Case Viscosity
Set bd = StreamObj
Set bdVar = bd.BackDoorVariable(:Viscosity.522.5).Variable
Syntax can be found in the module modWriteTable, Line 3989.
Note: If you have multiple versions of Hysys in your PC, you may get error when reporting this property. Please seeSolution 125548 for work around.
Keywords: HSR, combined liquid, mixed liquid, viscosity
References: None |
Problem Statement: What sizing equations are used in Fisher valve of Depressuring Utility or valve? | Solution: In Depressuring utility, Fisher valve use the Universal Sizing equation instead of fisher equation in Fisher Manual. This equation model is very similar to the Fisher equation. The difference between the two is the backwards compatibility when the valve has both vapour and liquid flowing through. The Universal Sizing model uses the overall density.
Universal Sizing method:
For the gas flow through the valve, the equations are as follows:
f = vfracfac 1.06 Cg (rho*P1)0.5 sin(arg)
Where:
arg = 59.64/C1 (1-P2/P1)0.5 *Cpfac
With upper and lower limits: 0<Arg< p/2
C1=Cg/Cv
Km=0.001434C1
Cpfac=(0.4839/(1-(2/(1+g))g/(g-1)))0.5
g=Cp/Cv
f = flowrate, lb/hr
rho = fluid density, lb/ft3
P1 = pressure of the inlet stream
P2 = pressure of the exit stream without static head contributions
vfracfac = 1, when outlet molar vapor fraction vfrac >0.1
= 0, when outlet molar vapor fraction vfrac =0
= vfrac/0.1, otherwise
For the liquid flow through the valve, the equations are as follows:
f = (1- vfracfac) 63.338 Cv (rho)0.5 (P1-P2)
Keywords: Fisher valve, sizing equation, depressuring utility, valve
References: None |
Problem Statement: When linking Excel to Aspen HYSYS, there might be issues referencing the Aspen HYSYS type library. This | Solution: provides the steps to fix this problem.Solution
To correct Aspen HYSYS type library reference in Excel you need the Administrator rights to the PC you are working. You also will need to make sure that the reference in the macros are referencing the correct version of Aspen HYSYS.
That can be done following the steps given below:
Open in excel the Macro view editor by hitting Alt+F11.
From the VBA debugger navigate to Tools |
Keywords: Restore File Association, HYSYS Type Library
References: s and make sure that the Aspen HYSYS type library is the same as the version you are using.
If the Aspen HYSYS type library is not the same as Aspen HYSYS version, then de-select the reference, click OK to close the references window, reopen it and select the correct reference. The Aspen HYSYS Type library is located on the Root Aspen HYSYS folder ussually under C:\Program Files\Aspentech\HYSYS version. See screenshot below for HYSYS 2006 type library.
If this still doesn't help either run the attached script (choose the one that matches your version and change the extension from txt to bat)
Otherwise, create a text file with the following code and change the line highlighted bit in yellow with the path to your version.
C:\Program Files\AspenTech\Aspen HYSYS V7.2\hysys.exe /unregserverquietly
C:\Program Files\AspenTech\Aspen HYSYS V7.1\hysys.exe /unregserverquietly
C:\Program Files\AspenTech\Aspen HYSYS V7.0\hysys.exe /unregserverquietly
C:\Program Files\AspenTech\Aspen HYSYS 2006.5\hysys.exe /unregserverquietly
C:\Program Files\AspenTech\Aspen HYSYS 2006\hysys.exe /unregserverquietly
C:\Program Files\AspenTech\Aspen HYSYS 2004.2\hysys.exe /unregserverquietly
C:\Program Files\AspenTech\Aspen HYSYS 2004.1\hysys.exe /unregserverquietly
C:\Program Files\AspenTech\Aspen HYSYS 2004\hysys.exe /unregserverquietly
C:\Program Files\AspenTech\Hyprotech\HYSYS 3.2\hysys.exe /unregserverquietly
set myVersion=C:\Program Files\AspenTech\Aspen HYSYS V7.1
%myVersion%\Hysys.exe /regserverquietly
pause |
Problem Statement: Can I specify the Watson K Factor in Aspen HYSYS? | Solution: The user can directly specify the Watson K Factor in Aspen HYSYS. This is the default option in the program. If this value is not specified by the user, then the program automatically calculates the Watson K Factor.
The Watson K Factor is used to characterize crude oils and crude oil fractions and it is defined as,
Where;
K = Watson K factor
TB = normal average boiling point for the crude oil or crude oil fraction, ?R
SGo = specific gravity of the crude oil or crude oil fraction
Example; A particular kerosene cut, obtained over the boiling point range 284 - 482 ?F, has a specific gravity of 0.7966. Values of K typically range from about 11.5 to 12.4, although both lower and higher values are observed. In the absence of a known value, K = 11.9 represents a reasonable estimate.
Keywords: Watson K Factor
References: None |
Problem Statement: How are the liquid levels defined in a separator with a boot for carry-over calculations? | Solution: For a separator with a boot, the liquid levels are defined based on the bottom of boot as datum.
If heavy liquid is in the boot only, then the height of heavy liquid is height in the liquid in boot.
For light liquid it will be Height of Boot+liquid level in vessel.
When entered these into carryover calculations, HYSYS treats these levels in the following manner.
heavy liquid level = heavy liquid level entered - boot height
light liquid level = light liquid level entered - boot height
Keywords: real separator, liquid height, heavy liquid, light liquid, boot.
References: None |
Problem Statement: Why are there drastic changes in outlet liquid streams after I add water in a three phase separator? | Solution: Addition of water can change the three phase separator's behavior significantly. For example you have light hydrocarbon and heavy hydrocarbon in liquid outlet streams of a three phase separator. If you add water, the aqueous phase will become the second liquid phase. The light and heavy hydrocarbon phases will combine to form one liquid phase. There will be some component distribution between the aqueous and liquid phase of course.
If you want separate the two liquid phases you observed before adding water you need another three phase separator in series. Please use a a component separator to deduct enough water from the liquid phase of the first three phase separator so that an aqueous phase does not form or predicted and then feed it to the second three phase separator. As long as HYSYS detects aqueous phase as one liquid phase you will not see the other two liquid phases.
There is a file attached with this document. If you make flow rate of Water 0 in one case and 100 kmol/h in the second you can observe the behavior in question.
In the file the first separator observes an aqueous phase as one of the two liquid phases. The component splitter is removing water so that no aqueous phase is detected. The second separator finds two liquid phases (no aqueous phase).
Keywords: Three phase separator, water
References: None |
Problem Statement: While using activity models such as NRTL or UNIQUAC from the Aspen Properties databank in Aspen HYSYS, my three phase separator only solves for one liquid phase. | Solution: The reason it does not solve normally is because the default valid phases in these fluid packages are Vapor-Liquid, thus making the 3-phase separator behave as a simple separator.
To modify this behavior, you must go to the properties environment and select the package in question. There, go to the Phase Handling tab.
Once in the Phase Handling tab, select Vapor –Liquid –Liquid from the Valid Phases dropdown menu.
Finally, return to the simulation environment and your three-phase separator will converge normally.
Keywords: 3 phase separator, activity models, aspen properties, valid phases.
References: None |
Problem Statement: The extension was registered successfully, however it does not show up on the list of registered dlls in the HYSYS list of extensions. The Error message below is displayed:
The extension Name###.3C extension is not available on this machine. This type of Unit Operation is removed from PFDs | Solution: The ProgID which is exposed in the edf is not the same as the ProgID for the class in the dll. So, while the extension is registered with HYSYS successfully and the class in the dll is registered with Regasm.exe successfully, the two are not linked correctly.
To resolve this error message, copy and paste the ProgID as the edf to ensure both have the same name.
The same ProgID needs to be used in the edf as in the code for the class definition.
Keywords: Extension, edf, dll
References: None |
Problem Statement: When the user enters the Safety Analysis environment to design relief valves, the datasheets of the corresponding valves are accessible through the Documentation Builder.
However, when the functionality is used in the same file, after being saved and reopened, an error message is displayed:
The database file dow not have an entry for this valve or scenario. This is most likely caused by opening the HYSYS case with a missing or inconsistent database file. It is recommended to re-open this case with the correct database file. To continue using this open case, then then the valve or scenario should be deleted. | Solution: One of the reasons of this error message can be related to the Microsoft Access version if the user, who created the file, accessed the Documentation Builder through the Safety Analysis environment.
The COM call to open the *.mdb file is selected when the user clicks the Documentation Builder button. This step might fail with MS Office 2007 because Aspen HYSYS uses a 2012 version of the file Microsoft.Office.Interop.dll and backwards compatibility is not guaranteed by Microsoft.
So, if the user wants to use the Documentation Builder, it is necessary to install the 2010 runtime version of MS Access.
Keywords: Documentation Builder, Safety Analysis
References: None |
Problem Statement: I have found two components in HYSYS’ databank with the same CAS Number. Shouldn’t CAS Number be unique per component? | Solution: The reason why there are two components with the same CAS Number is because they are the same component with a different common name.
You might find that using each of these components in a simulation show slightly different results in their flash and/or thermodynamical properties. This is because they have different critical properties, since they are built according to different editions of the DIPPR (Design Institute for Physical Properties).
Since HYSYS only has one component database (unlike Aspen Plus) these components with different properties are found on the same databank.
Components with a low ID number are components that are in the databank since the software was known as Hyprotech (2Propanthiol ID 695). Components with high ID numbers were added later on, when the software became Aspen HYSYS and the databank was updated to a newer version of the DIPPR (2C3Mercaptan ID 3162).
You might find components with duplicated CAS Numbers, but the one with the high ID number (3xxx) is the updated one.
Keywords: CAS Number, Critical Properties, ID Number
References: None |
Problem Statement: Why do the binary interation parameters (BIP's) change for certain components in Aspen HYSYS? | Solution: The Peng-Robinson package in Aspen HYSYS updates BIP's based on temperature.
For example, the BIP's for the pairs of H2S-H2O and CO2-H2O are treated as functions of temperature. The purpose is to improve its prediction for polar and associating fluids such as water, alcohols, glycols and acid gases.
The complete list of systems that HYSYS will overwrite the BIP's is given below.
DEG-CO2
TEG- Benzene
H2O-TEG
DEG-H2S
TEG- Toluene
H2O-DEG
DEG-CH4
TEG- Ethyl-Benzene
H2O-N2
DEG-HC (all hydrocarbons)
TEG- o-Xylene
H2O-CO2
DEG-Benzene
TEG- m-Xylene
H2O-H2S
DEG-Toluene
TEG- p-Xylene
H2O-HC
DEG- Ethyl-Benzene
DEG- o-Xylene
DEG- m-Xylene
DEG- p-Xylene
Note: H2O-HC pair is modified only if the original value on the form is zero or 0.5. The overwrite will occur if the ?Estimate HC/HC? radio button is selected on the Binary Coeffs form. If you wish to input values for the above pairs, please set the option to ?Set All to 0.0?.
Keywords: binary, interaction, parameters, Peng, Robinson, PR, temperature, dependent, BIP's, BIP
References: None |
Problem Statement: What is the definition of Boilup Ratio and what is the default basis?
Reboiled absorber requires Boilup Ratio in its last page of input expert. What is the definition and basis of it? | Solution: Boilup ratio = Vapor leaving a reboiler divided by liquid leaving the reboiler.
= Vr/Lr, with reference to the picture below.
Molar basis is the default basis of boilup ratio. You can choose a different basis (mass or volume). To do so double click on Boilup Ratio spec or select it and then click on View button in Monitor or Specs Page. Then choose a different basis from the dropdown list. The picture below shows the interface if you do it via Specs page.
Keywords: Boilup, boil-up, boilup ratio, ratio, definition, define, basis, molar, mass, volume, reboiled absorber
References: None |
Problem Statement: Why does Aspen HYSYS generate the error message 'Not Licensed for Crude Distillation' when I have not created an assay in the case file via the oil manager? | Solution: If any of the conditions below are true, the user will receive a crude license error:
1) Using Oil environment or
2) Case file contains a hypo component with a normal boiling temperature > 533.1 K AND a column has been created in the simulation case.
Note that the second scenario requires the column solver to have been run at least once. If the user doesn't have the crude license an error message will be displayed (if a crude license exists, it will be displayed under Help | About HYSYS | License Information).
Keywords: Crude, License
References: None |
Problem Statement: How do I set base elevation of vessel used in the depressurization utility? | Solution: According to the API521 standard (API RECOMMENDED PRACTICE 521 1997) only the portion of the vessel that is wetted by its internal liquid and is equal to or less than 25 feet (7.6 m) above the source of flame needs to be recognized. If the vessel bottom is above 25 feet then the fire will not have any effect i.e. Q=0.
By default the vessel elevation is set zero. For the actual calculation it is necessary to enter the correct elevation of the vessel. This can be done via the Rating tab and Nozzles page in the vessel. The vessel is located in the depressurizing sub-flowsheet. See screenshots below showing the depressurizing vessel.
The base elevation can be entered via the Rating -> Nozzles tab. See below.
Keywords: Depressurizing Utility, Fire API521, Base Elevation
References: None |
Problem Statement: How can I get vessel orientation via OLE Automation? | Solution: Since the separator orientation properties are not available within the HYSYS type library (they are not yet 'wrapped' for standard Automation access), it is necessary to use a 'Backdoor' method.
This can be achieved by using the code provided below.
1. Open up HYSYS with any case that contains a separator.
2. Paste the code into the VBA editor in Excel
3. Set the code to reference the separator name
4. Make a reference to the HYSYS type library (Tools ...
Keywords: None
References: s menu option in the VBA editor)
5. Run the procedure.
Sub GetSeparatorOrientation()
'
'Description: Get Orientation of separator
'
'Declare Variables |
Problem Statement: Which are the reactors available in Aspen Hysys and what are the requirements? | Solution: Reactor Types
Yield: Set product yields from reactor; no stoichiometry required
Gibbs: Minimize Gibbs free energy to determine outlet equilibrium composition; no stoichiometry required
Conversion: Specify stoichiometry and conversion; outlet composition calculated
Equilibrium: Specify stoichiometry and define equilibrium constant; outlet composition calculated
CSTR: Specify stoichiometry and define kinetic rate constant. Contents assumed to be completely mixed; outlet conditions calculated
PFR: Specify stoichiometry and define kinetic rate constant. Assumes stream passes through reactor in plug flow; outlet composition calculated
Keywords: Yield, Gibbs, Conversio, Equilibrium, CSTR, PFR, Reactor
References: None |
Problem Statement: Adiabatic cooling is the operation whereby a liquid stream (typically water) is injected directly (and mixed) into a superheated gas/vapour stream. The cooling effect (or temperature decrease) is brought about by vaporisation of the liquid as energy is absorbed by the water molecules in converting them from liquid to vapour phase. This results in partial saturation the gas stream. The liquid stream is usually at a lower temperature than the that of the gas (though this is not the key feature).
There is currently no single unit operation in Aspen HYSYS that can model an adiabatic cooler. | Solution: ThisSolution seeks to provide the user with a flowsheet (and methodology) that can be used to model the heat and mass balance around this type of equipment. Typically, adiabatic coolers can be specified either on desired product outlet temperature or relative saturation/humidity.
See the attached simulation file.
Keywords: Adiabatic cooler, humidity, saturation
References: None |
Problem Statement: I get a consistency error when I add a pumparound and specify the pressure drop, however, there is no overspecification. How do I solve this problem? | Solution: This particular issue is addressed in the error message window. Here is copy of the message in this scenario.
The lines in red box indicate the cause and aSolution. The cause: Draw stream's enthalpy is calculated by the column subflowsheet and the pumaround and there a difference exist that is not acceptable by flash tolerance. The difference came through the gap of heat / spec tolerance of the column. The difference is small but was enough to cause the error. It can be resolved by either one or combination of the following two actions:
1. Tighten the Heat / Spec Error Tolerance. The option is under Parameters | Solver. The default value of 5e-4 should be reduced to 1e-4 or lower. Please note that tightening the tolerance may require additional iterations for the column to converge.
2. Close the error message. Turn the solver on (click the green traffic light button in toolbar). You may have to repeat this step several times until the column converges.
Keywords: pump around, pumparound, consistency error, pressure drop
References: None |
Problem Statement: Is it possible to create tab file from Hysys which can be used for Olga? | Solution: Hysys needs following support files to run OLGA
*.inp; *.tab; *.snp
HYSYS does not generate the *.inp and *.tab files. These are what the user has to provide to set-up the case.
The *.inp file is the OLGA input file that defines the problem, ie geometry, boundary conditions, etc.
A *.tab file is not necessary but it can be used to specify the fluid conditions and loaded through the *.inp file.
An *.snp file is a snapshot file that saves all the OLGA results at a given time to a file. HYSYS can generate *.snp file if the user requests one. It can then be loaded later so the simulation does not have to start at time 0.
Keywords: Olga, tab, inp, snp, *.inp, *.tab, *.snp
References: None |
Problem Statement: How can the data from the column stage be transferred to an internal stream within the column subflowsheet environment? What is the transfer basis for this internal stream? | Solution: To export the stage data into an internal stream within the column subflowsheet the user has to navigate to the flowsheet internal streams option within the column specification window. After selecting the add button, the user will then have to input an internal stream name, the stage, type, Net/Total and unselect the export tick box. A screenshot of this option is shown in the image below:
The internal stream will now be located within the column subflowsheet environment and the internal stream will be populated with the corresponding stage data after the column has solved. The transfer basis for this internal stream is a P-H flash.
Keywords: HYSYS, Column, Internal Streams
References: None |
Problem Statement: When using the depressuring utility, how is the wetted area calculated for a horizontal vessel? | Solution: Refer to the attached HYSYS file created in v 2006.5.
Variables:
L = cylinder height
h = height of liquid
W = height of head (cone/ellipsoid/hemispherical/dished)
R = cylinder radius
V = Volume of liquid
A = Surface in contact with liquid
Horizontal vessels
Cylindrical part
In the discussion below, the result of an inverse trigonometric function (i.e. arccos) is in radians.
A = L*R * 2 * arccos((R-h)/R)
Ellipsoidal heads (V& A account for both heads)
V = Pi() * h2*W*(1-h/3R)
A= W / R*(2*PI()*R*h)+(1-W/R)*(V/L)
Hemispherical heads (V & A account for both heads)
V = PI()*h2*(R-h/3)
A = 2*Pi()*R*h
Hysys calculates WettedArea as below for Flat Horizontal Vessel
HoldupLiqVolume = 18.1227 m3
Height, h = liqLevel/100.0*diam = 27.22/100.0*1.3106 = 0.3567
rad = diam/2=1.3106/2=0.6553
cylinderArea = L*R*2*acos((R-h)/R)=60.9485*0.6553*2*acos(0.4555)=87.6923
wettedSideArea = HoldupLiqVolume/L=18.1227/60.9485=0.2973
wettedArea = 2 * wettedSideArea + cylinderArea=2*0.2973+87.6923=88.2870
Sample: Try the following:
1. Open the attached case;
2. At Design/Config. Strip Charts click Add Variable button
3. Add Tank Wetted Area;
4. Run the utility;
5. See the results by clicking the View Historical Data button. At time 0 (sec), the WettedArea=88.2870 (m2).
Notes:
1. The wetted area in the Duty spreadsheet, cell D8 is in m2 and it is the current time of the integrator.
2. Initial liquid Percent(%) = Initial holdup volume / Total liquid volume. Please note that it is not initial level %, it is initial liquid volume %
3. When the liquid volume is more than the actual liquid volume, the vapor volume will be less than the actual vapor volume since we keep the total volume constant or the same.
The total volume will always sum up to the liquid and vapor volume. The pressure of the vessel will be adjusted accordingly. In depressuring utility it should not calculate negative volume or negative mass. The dynamic integrator does a material and energy balance at specific time steps, and will maintain the balance across the separator.
4. The Duty, VaporFlowRate and LiquidFlowRate spreadsheets all list the information in metric. If desired, users can have the information displayed in Field units as the main simulation uses this unit set.
Users can change the unit set on the Parameter tab of the spread sheet, however caution should be exercised when doing this. Certain formulas used to calculate spreadsheet cell values are entered considering a particular unit set. It is better to add another spread sheet and link the value to the new spread sheet. Change the unit set for new spreadsheet to Field units. As shown below in the attached image file. The wetted area is 84.80 m2 in SI units and 912.8 in ft2 in Field units.
Keywords: wetted, area, depressuring, utility, volume
References: None |
Problem Statement: What is the latest version of the Aspen HYSYS-OLGA link extension? | Solution: The latest version of the Aspen HYSYS-OLGA Link extension is V6.2. This is included with the installation of Aspen HYSYS (V7.2-V8.6).
This can be seen on the unit operation name as shown below.
Keywords: version, OLGA, HYSYS_OLGA
References: None |
Problem Statement: How do I save a preference set and have it load automatically every time I open my model? | Solution: You can do it only by replacing the original preference file. Make a copy of the original file (in case you need it in future). Then make the changes in preference and save the preference set as the default preference file.
Here are the detail steps.
1. Find the location of the preference (.PRF) file: Open HYSYS. Go to Tools || Preference || click on Save Preference Set or Load Preference Set button. You should see one more more files with .PRF extension.
2. Select the appropriate .PRF file (for example, for version 2006.5 it is Aspen HYSYS 2006 5.PRF. For V7.0 version it is Aspen HYSYS V7.PRF).
3. Press Ctrl+C (or right click and Copy).
4. Click on an empty space (to un-select the file name), then press Ctrl+V (or right click and paste). Now you have a copy of the original preference file. If you want to bring the back the originial preference file, please use this copied file.
5. Go ahead and make the changes in preference (such as clone unit set, change unit etc.).
6. Click on Save Preference File button. Select the original preference file (Aspen HYSYS V7.PRF, for example).
7. A message will ask whether you want to overwrite the file or not. Choose Yes.
With these steps, you have changed the original preference file with your new preference file. HYSYS will load it automatically everytime you open HYSYS.
Please note that if you want to use the same preference file in a different computer, you need to take the copy of this preference file and replace it in the other computer.
Keywords: Preference, everytime, every time, load
References: None |
Problem Statement: Why are the Aspen HYSYS files I save, not showing .hsc extension on the computer? | Solution: If you have selected the Hide extensions for known file types in the Folder options on the computer HYSYS files are shown without the .hsc extension. To restore the extension open the folder where HYSYS files are saved and select Tools menu | Folder options... In the View tab unselect the Hide extensions for known file types
Keywords: extension, missing, folder,options
References: None |
Problem Statement: How can I clone a component from the database and modify its properties? | Solution: 1. Go to the Simulation Basis Manager by pressing Ctrl+B or selecting Simulation | Enter Basis Environment from the main menu.
2. Open the Hypotheticals Tab.
3. Click the Clone Comps button.
The Convert Library Comps to Hypothetical Comps window appears:
4. Select the component to clone on the Available Library Comps List.
5. Unclick the Replace ALL Instances checkbox, otherwise all instances of the original component everywhere in the flowsheet will be replaced.
6. Click the Convert to Hypo(s) button. The new component is created as (name)* in the default HypoGroup1 hypo group.
7. Close this window.
8. Select HypoGroup 1 from left hand side Hypothetical Groups and press the View button. It will show the new hypo component. By double clicking on the component, the pure component window appears where you can change the name and the properties.
Keywords: Clone component
Modify properties
References: None |
Problem Statement: Can Aspen HYSYS predict oil product's TAN (Total Acid Number)? | Solution: There is no built-in feature in Aspen HYSYS to simulate TAN number however you can use User Property in oil characterization environment, which allow you to supply a property and have Aspen HYSYS characterize it with an assay.
Following are the brief steps to add user property using oil manager:
1. In the basis environment go to oil manager tab and enter oil environment.
2. Under Oil Characterization view select User Property then Press Add
3. In the user property view you can select mixing basis as well as mixing rule from the drop down list
4. Next select edit component user property value in the bottom to enter the property value for the components. If you do not have data for light components, enter 0. The purpose of this property view is to instruct Aspen HYSYS how the user property should be initialized throughout the case. Whenever the value of a user property is requested by the user property utility or by the column specification, Aspen HYSYS uses the composition in the specified basis and calculate the user property value using your mixing rules and parameter. Finally, press submit.You can name the property as TAN
7. Go to Assay property view and select user curve tab.
8. Select the Edit button and enter your assay data you have and press calculate.
Keywords: TAN, total acid number
References: None |
Problem Statement: How to switch from scientific notation to normal notation when displaying numbers in Aspen HYSYS? | Solution: In Aspen HYSYS you have select the options tab.
Now select unit of measures and go to Variable formats and say format and select Format under format select Significant Figure and change the value to 6.
Keywords: Unit of Measures, scientific Notation, Significant Figures
References: None |
Problem Statement: I am converting a file from PROII to HYSYS. Where is the Stream Data 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 stream data is specified under the section entitled the Property Stream. An example from the PROII input file is found below:
PROPERTY STREAM=002, TEMPERATURE=230.7, PRESSURE=2, &
RATE(WT)=92090.9, ASSAY=LV
The stream data that will be imported into HYSYS will be labelled directly after the property stream. In the PROII code above the rate refers to the mass flow rate, assay refers to the input assay which will be imported within the oil manager in HYSYS.
Keywords: HYSYS, PROII, Converter
References: None |
Problem Statement: What are the capabilities of Fidelity option in Aspen HYSYS Dynamics? | Solution: Aspen HYSYS Dynamics contains Fidelity (an extension of Aspen HYSYS) that provides advanced dynamic features to your simulation. It allows users to supply levels of detail that would only be available after detailed equipment drawings and general arrangement drawings have been developed for detailed dynamic studies. Specifically, this option include the following capabilities:
Detailed heat loss model to take into account heat transfer from equipment with holdup to the environment. Users supply information such as insulation thickness and heat transfer coefficients.
Static head to account for pressures as function of equipment elevations, and liquid levels.
Nozzle elevations to account for vapor exiting in the liquid stream or vice versa as a function of the actual nozzle location on the vessel. Nozzle locations also affect the static head calculations.
Actuator dynamics to account for time lags between the desired actuator position and the actual position. Related options also included are 'sticky' and 'leaky' valves, and fail positions.
Details on rotating equipment. Inertia terms account for the starting up and shutdown of rotating equipment.
The value being emphasized here is not on dynamic simulation, but the merits of detailed models. If the answer to some of the following questions is yes, then HYSYS Fidelity option will be useful:
1. Is the process very sensitive to ambient temperature? For example, does a column produce off-spec product for a period of time if ambient temperature changes?
2. Is the process very sensitive to small pressure fluctuations? For example is the static head due to tank liquid levels important? Does the plant have problems with pumps cavitating because of insufficient NPSH?
3. Is there a problem with passing vapor to the liquid lines or vice versa? Are the nozzle locations affecting this?
4. Are there controller tuning challenges where the actuator dynamics will affect the proper tuning? Do you need to model safety scenarios where the speed at which a valve opens or closes will be critical to properly assessing the outcome?
To use Aspen HYSYS Dynamics features, you must have a valid Aspen HYSYS Dynamics license. If you do not have a Aspen HYSYS Dynamics license, or it is not activated, you will not able to see or access these features.
Keywords: Fidelity, Aspen HYSYS Dynamics, Cavitation, Nozzle, Heat Loss, Actuator Dynamics, NPSH, Static Head
References: None |
Problem Statement: When you hyStdFlowVar.StdLiqVolFlow.Erase, you will get the error message. The function is not working. | Solution: Some of Standard condition properties' objectives are not fully exposed from hysys automation. You may want to try to use the backdoor variables:
Set hyStdFlowVar = hyBD.BackDoorVariable(:StdLiqVolFlow.501.0).Variable
If hyStdFlowVar.CanModify And hyStdFlowVar.IsKnown = True Then
hyStdFlowVar.Erase
End if
Keywords: Automation, Hysys, Backdoor Variables, Standard condition properties
References: None |
Problem Statement: How to configure a Remote SQL Express 2005 server to be used by remote Aspen Clients | Solution: Install a component from Process Modeling V7.1 on the SQL server and follow the steps outlined on a SQL Express 2005 server to be used by remote clients.
Launch the SQL Server Configuration Manager from Start | Programs | Microsoft SQL Server 2005 | Configuration Tools | SQL Server Configuration Manager.
1. Under SQL Server Configuration Manager (Local) | SQL Server 2005 Network Configuration | Protocols for <instance name such as SQLEXPRESS>, enable the TCP/IP and Named Pipes protocols by right-clicking and selecting Enable on each one.
2. Under SQL Server Configuration Manager (Local) |SQL Native Client Configuration | Client Protocols.
3. Launch SQL Server Surface Area Configuration from Start | Programs | Microsoft SQL Server 2005 | Configuration Tools | SQL Server Surface Area Configuration.
4. Click the link for Surface Area Configuration for Services and Connections.
5. Under <instance name> | Database Engine | Remote Connections, select Local and remote connections, then select Using both TCP/IP and named pipes.
6. Under <instance name> | Database Engine | Service, click Stop (if enabled), then click Start to restart the database engine service.
7. Under SQL Server Browser | Service, ensure the Startup type is Automatic. Click Apply and OK after changing this setting. Then click Stop (if enabled), then click Start to restart the server browser service.
8. Make sure that sqlservr.exe and sqlbrowser.exe are in the exception list of the firewall.
9. Make sure that the Remote Connections is enabled on the server.
Keywords: APED
Remote
SQL Server
References: None |
Problem Statement: How can I open and view multiple utilities at the same time? | Solution: You can view the utilities from Utilities option under Tools menu. Select the multiple utilities(both control and shift key works for selection), and select View Utility button.
Note: Shortcut key to view the Utilities is: control + U
Keywords: open, view, multiple, utilities.
References: None |
Problem Statement: What is Damping Factor (under column Parameter | Solver page | Damping settings) and when should I modify this number. | Solution: Damping factor is used to control the step size for the solver. It helps in faster convergence of a column solver.
The Damping Factor is a multiplication factor that controls the step size used in the outer loop when updating the thermodynamic models in the inner loop. A Damping Factor of 0.4 -0.6 may provide a faster, more stable convergence for most of the column simulations.
Use the following guidelines for specifying damping factor.
Type of Column
Damping Factor
All hydrocarbon columns from demethanizers to debutanizers to crude distillation units.
1.0
Non-hydrocarbon columns including air separation, nitrogen rejection.
1.0
Most petrochemical columns including C2= and C3= splitters, BTX columns.
1.0
Amines absorber
1.0
Amines regenerator, TEG strippers, sour water strippers
0.25 to 0.50
Highly non-ideal chemical columns without azeotropes.
0.25 to 0.50
Highly non-ideal chemical columns with azeotropes.
0.50 to -1.0
Keywords: Damping Factor, Amines, Dehydration, Regenerator
References: None |
Problem Statement: How can I report scenarios results with labels? | Solution: To copy the results and labels of scenarios created in Databook (Table or Transposed Table) and paste into Excel or other program, highlight the results, go to Edit in the main menu and click on Copy with Labels. You can also use the keyboard shortcut <CTRL>+<SHIFT>+C.
Keywords: Copy, paste, Databook, table
References: None |
Problem Statement: The Masoneilan equation is presented in the depressurization utility without units. | Solution: Attached document explains the derivation in SI units
Key Words
Masoneilan Equation - SI Units
Keywords: None
References: None |
Problem Statement: When creating a new correlation set, the Save correlation set to file option is selected. But when loading the saved set, the program shows that the file was not created: | Solution: This problem is solved by modifying the Stream Correlation Sets File path. Click on the Tools menu and the Preferences submenu. The Session Preferences window is now open. On the Files tab, select the Locations page and scroll down to select the Stream Correlation Sets File path. The default is 'Support\StreamCorrSet.xml' as shown below:
Change the path to 'Support' as presented in the following figure:
Keywords: Stream Correlation Set
References: None |
Problem Statement: How to model Divided wall column in Aspen HYSYS? | Solution: There are different ways to model Divided wall columns in Aspen HYSYS. An informal presentation about modeling DWCs and a sample simulation case with 2 conventional columns and the equivalent DWC is attached alongwith.
Keywords: divided wall column
References: None |
Problem Statement: What needs to be referenced for ASW automation? | Solution: On Excel you will need to add all the related references. To add them,
Step 1. Open Excel, and then go to ribbon bar Developer, and then click “Visual Basic” to open the VBA.
Step 2. Select “
Keywords:
References: s…” from Tools bar. If you have problem to open the reference, close Excel and reopen it “Run as administrator”.
Step 3. Make sure you have checked the following references.
Aspen Simulation Workbook - V7.3 or the other versions.
HYSYS Vx.xx Type Library
AspenOSEWorkbookXLA
AspenSimulationWorkbookXLA
If you don't see those references from the available references list, you can use Browser to add them to the list.
C:\Program Files (x86)\AspenTech\Aspen Simulation Workbook V7.3\AspenOSEWorkbook.tlb
C:\Program Files (x86)\AspenTech\Aspen Simulation Workbook V7.3\AspenOSEWorkbook.xla
C:\Program Files (x86)\AspenTech\Aspen Simulation Workbook V7.3\AspenSimulationWorkbook.xla |
Problem Statement: How does the percent of maximum flooding change? | Solution: The % of maximum flooding changes depending on the correlation used to calculate the maximum gas velocity before there is flooding (Flood gas velocity). With a larger Flood gas velocity, the % of Max flooding will be greater.
When the packing size is increased, the cross sectional area for the gas flow decreases as expected. The values do not change with the correlation since they depend on the geometry and size of the packing.
With this area, the gas velocity is being calculated (gas velocity = volumetric flow / cross-sectional area).
The maximum flooding velocity is being calculated by the correlations available ( Robbins & SLE)
On the Design\Specs tab you will be able to select the correlation to calculate the Flooding (Robbins or SLE)
Note: The % of Max Flooding is calculated by dividing the gas velocity over the Flood Gas Velocity.
Keywords: Flooding Velocity, Packing Correlation, Gas velocity, Robbins, SLE
References: None |
Problem Statement: I am converting a file from PROII to HYSYS. How is the column 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 column is specified under the section entitled Column UID. An example from the PROII input file is found below:
COLUMN UID=T1, NAME= COLUMN EXAMPLE
PARAMETER TRAY=13, IO=75
FEED D29,7/S70,14/D73,6/D72,14,
PRODUCT OVHD(WT)=WG,62400, LDRAW(WT)=D76,8,32380, &
LDRAW(WT)=LN,1,71237.4, LDRAW(WT)=D79,7,21230, &
LDRAW(WT)=HLCO,11,7123.99, WATER(M)=D81,1, & 10AS8.31, BTMS(WT)=CLO,15664, SUPERSEDE=ON
CONDENSER TYPE=MIX, PRESSURE=0.707, TEST=40
PA NAME=BPPTL, FROM=7, TO=7, PHASE=L, DNAME=2, RATE(WT)=243000
PA NAME=HCO, FROM=11, TO=10, PHASE=L, DNAME=3, & RATE(WT)=413339
METHOD SET=SRK01,14
The section for the Feed is specified after the line Feed. The Products are specified in the next lines where the code states how the mass flow rate exiting from each section of the column. The method set signifies the different property packages used in the column. Finally the PA signifies the pump around. The Pump around also provide the exit stages and re-entry stage to the column.
Keywords: HYSYS, PROII, Converter
References: None |
Problem Statement: Is there a way to have a Degree of Freedom (DOF) analysis for my whole simulation? | Solution: In modeling operations, Aspen HYSYS uses a Degrees of Freedom approach, which increases the flexibility with whichSolutions are obtained. For most operations, you are not constrained to provide information in a specific order, or even to provide a specific set of information. As you provide information to the operation, Aspen HYSYS calculates any unknowns that can be determined based on what you have entered.
In Aspen HYSYS you cannot obtain a general DOF analysis; this is reported only for Distillation columns and heat exchangers. If you want to monitor the status of the simulation, you won't see DOF analysis but if you access to the Flowsheet summary from Simulation menu> Flowsheet summary (For V8.X you need to go to Home tab> Summaries ribbon> Flowsheet summary) and in there you can track all the items in certain status, for example: Not solved items, then you can take a look to them and manually determine why the item is not solved.
Keywords: DOF analysis, flowsheet summary
References: None |
Problem Statement: I don’t have administrator privileges, how can I select the version of Aspen HYSYS to be launched through automation? | Solution: Administrator privileges are required to register and unregister COM components for Aspen HYSYS, and therefore to set the default version of the program. However, there is an alternative method to specify through VB code the version to be launched when creating a new instance of the program.
For both starting objects, HYSYS.Application and HYSYS.SimulationCase, you can use a ProgID containing the application version as follows:
Set hyApp = CreateObject(HYSYS.Application.Vx.x”)
Set hyCase = GetObject(lv_FilePathName, HYSYS.SimulationCase.Vx.x)
Where “x.x” is the version you want to launch.
In order to make it easier to reuse your work, you can set a public string variable with the version of the program and refer to that in the rest of your code. For instance:
Public myVersion as string: myVersion = “8.4”
Set hyApp = CreateObject(HYSYS.Application.V” & myVersion)
Set hyCase = GetObject(lv_FilePathName, HYSYS.SimulationCase.V & myVersion)
Keywords: Automation, register, ProgID, VB, VBA, Visual Basic, getting started, default version.
References: None |
Problem Statement: Let us consider the following data are available for creating a hypo:
MWÂ Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â 500
Ideal Liq Density (kg/m³)           1189
Tc (°C)                                     630
Pc (bara)Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â Â 13.05
Volume (m³/kgmole)                 2.45
Accentricity                              0.95
Using these data the hypo was created as shown in the figure (1):
When the “estimate the missing properties� is clicked, Aspen HYSYS estimates NBP of 651.5 °C but then this hypo cannot be added to the simulation. The error message that the component could not be estimated is displayed (see figure 2) | Solution: The problem with the generated Hypo is that the estimated NBP is higher than the specified critical temperature and this causes problem for HYSYS. If you delete the critical temperature and let Aspen HYSYS estimate then you can use the hypo in your case.
One of the following would be the minimum information required for defining a hypothetical component:
1.        Normal boiling point (NBP), if NBP < 371 0C
2.        NBP AND Ideal Liquid Density, if NBP > 371 0C
3.        Molecular Weight AND Liquid Density
4.        UNIFAC structure
Keywords: hypo component, estimation failed
References: None |
Problem Statement: How do I find the Developer menu in the Microsoft Excel Ribbon? | Solution: The Developer menu on the Microsoft Excel Ribbon is not active by default. Here are the steps to enable it.
Open File | Options
Then go to Customize Ribbon, and make sure the Developer checkbox is checked. By default, it is not checked. After that, the Developer ribbon bar would show in the Ribbon.
Keywords: extension, VBA
References: None |
Problem Statement: What is Adiabatic mode in the Depressuring Utility? | Solution: Adiabatic Mode – Gas blowdown
1. Models a normal gas blowdown of pressure vessels and/or piping.
2. No external heat to the system.
3. Heat flux between fluid and the vessel is modeled as fluid temperature drops.
4. When estimated by Aspen HYSYS, the Heat Transfer coefficient estimated from wetted area and vessel volume specified by the user. The wetted area specified should be equal to the total surface area of vessel not the area in contact with liquid.
Keywords: Adiabatic Mode, Gas blowdown, Depressuring Utility, No external heat
References: None |
Problem Statement: Can I run a Case Study when I am in the Sub-Flowsheet Environment? | Solution: When in the Sub-Flowsheet Environment, you can add the variables for the Case Study Set up but when you want to run it the warning message Case study can run only in the main environment will show up.
Please move to the main flowsheet and run the case study.
Keywords: Sub-Flowsheet, Case Study
References: None |
Problem Statement: How do I export a Material Stream from one simulation to another? | Solution: The first step is to copy and paste the stream from one simulation to another (press control in order to copy the stream) and then paste it in the other simulation, once you have done that a new Fluid Package and Component list will be created. Also you need to be aware that the composition and properties are only going to be exported if the stream is user-defined in the original simulation. If you want to copy a stream that is being calculated by Hysys the only way to copy all his properties will be to create a new stream in the original simulation, then in the new stream press the button Define from Other Stream this action will make the new stream as user-defined and you will be able to copying it.
Another way to do it is exporting the Fluid Package form the first simulation and importing into the new one, this will carry the component list related. Then you can copy the composition and the properties manually from the other stream.
Keywords: Material Stream, Export, Import
References: None |
Problem Statement: What is difference between Wax Deposition temperature and Critical Wax Deposition temperature (located in the Flow Assurance tab of the Pipe Segment unit operation)? | Solution: Deposition temperature - the temperature at the pipe wall where the wax is forming.
Critical deposition temperature - the wax formation temperature at the given pressure and composition of the pipe cell.
Keywords: Wax Deposition, Pipe Segment, Flow Assurance
References: None |
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