Sir, I've performed the entire simulation as per tutorial but the conversion of Ethanol and Acetic acid is showing 0.395404 and 0.379588 respectively. I've run the simulation many times by watching the tutorial but the results doesn't match.
I am using DWSIM version 8. I have followed the exact steps as mentioned in the tutorial. The CSTR gets simulated successfully but the results are totally different. In Compound conversions, only the acetic acid conversion is being displayed and its value is 1.86E-14 % as opposed to >90 % in the tutorial. Also the heat load is not being displayed.
When the simulating the CSTR, error is generated in calculation mode so that i cannot obtain the desired conversion through this CSTR simulation. CSTR.dwxmz
When i am calculate for CSTR i given value of isothermic in calculation mode and i have facing the error in calculation and i did not getting the conversion and i have follow every steps as you tough me in tutorial and my DWSIM version is 8 in windows 11.
The residence time obtained match with that of tutorial whereas the conversion percentage attained is 65.8% and 63.2% for ethanol and acetic acid respectively (that too by changing the velocity units to kmol/m3s.(version installed is 6.4.3).Kindly help
Drive link:https://drive.google.com/file/d/117US25tw_eUSA0rlgzCYXkUX8oPYabal/view?usp=sharingThis error was raised during the calculation of a Unit Operation or Material Stream.System.NullReferenceException: Object reference not set to an instance of an object. at DWSIM.SharedClasses.SystemsOfUnits.Converter.ConvertToSI(String units, Double value) in C:\Users\Daniel\source\repos\DanWBR\dwsim\DWSIM.SharedClasses\UnitsOfMeasure\SystemsOfUnits.vb:line 1184 at DWSIM.UnitOperations.Reactors.Reactor_CSTR.NewCalculate(Object args) in C:\Users\Daniel\source\repos\DanWBR\dwsim\DWSIM.UnitOperations\Reactors\CSTR.vb:line 701 at DWSIM.SharedClasses.UnitOperations.BaseClass.Solve() in C:\Users\Daniel\source\repos\DanWBR\dwsim\DWSIM.SharedClasses\BaseClass\SimulationObjectBaseClasses.vb:line 442 at DWSIM.FlowsheetSolver.FlowsheetSolver.CalculateObjectAsync(Object fobj, CalculationArgs objArgs, CancellationToken ct) in C:\Users\Daniel\source\repos\DanWBR\dwsim\DWSIM.FlowsheetSolver\FlowsheetSolver.vb:line 223 at DWSIM.FlowsheetSolver.FlowsheetSolver.ProcessQueueInternalAsync(Object fobj, CancellationToken ct) in C:\Users\Daniel\source\repos\DanWBR\dwsim\DWSIM.FlowsheetSolver\FlowsheetSolver.vb:line 520Location:Code Location: ConvertToSI (file 'C:\Users\Daniel\source\repos\DanWBR\dwsim\DWSIM.SharedClasses\UnitsOfMeasure\SystemsOfUnits.vb', line 1184)Calling Method: NewCalculate (file 'C:\Users\Daniel\source\repos\DanWBR\dwsim\DWSIM.UnitOperations\Reactors\CSTR.vb', line 701)Check input parameters. If this error keeps occurring, try another Property Package and/or Flash Algorithm.
I use DWSIM version 6: The conversion value I got for synthesis of Ethyl Acetate in a CSTR are Ethanol - 0.395 & Acetic acid - 0.379. i checked every value and steps shown in the tutorial and everything is the same. Every time the value has some difference than the value in tutorial, I understand it is because of versions. But, this low conversion is not accepted. Kindly help me with this.
When i run the simulation it shows error, no reactor headspace defined. Their is no data about headspace in problem statement.
Material stream status shows "not calculated".
After selecting the units and when I add feed it shows NRTL Error: Missing interaction parameters for binary pair acetic acid/ethanol.
I am getting the heat load of the CSTR ( in results) as -5.68434E-13.and outlet temperature in the CSTR property editor as 70 C while here in spoken tutorials it is showing as 25C.
The conversion is way off. Attaching the simulation file. https://drive.google.com/file/d/16DSJ-Ps7f5_kmq5gc6eyVhutsj2erBvH/view?usp=sharing
Hello,I'm not getting heat load correctly in result section as per the tutorial results,i try so many times but getting heat load -32.0258KW
I followed the same procedure and the heat load estimation is different in my simulation. Do you know why it is happened? Thanks
I am following the exact same steps as shown in tutorial but when I solve flowsheet, I am getting 2 errors Maximum number of iterations reachedErrors occurred during the calculation of the flowsheet, please read the following messages for more details.
I am using NRTL package with nested loop for the calculation of molar flow and residence time of reaction between CaO and HNO3. I have added the materials using pubchem data in form of joson file. When I am preparing the flowsheet, no error is indicating in error panel but when I am solving the flowsheet it is showing kinetics of reaction not found. What I can do to solve this issue?*While making the compound, no data related to kinetics have been asked*
I am following the exact same steps as shown in tutorial but when I solve flowsheet, I am getting 2 errors Maximum number of iterations reachedErrors occurred during the calculation of the flowsheet, please read the following messages for more details.I am using DWSIM version 6.2
I am unable to find "New Steady-state simulation" option under File Menu as displayed in the tutorial. I am using DWSIM Version 6.1 Update 1.
In Video: Volumetric Flow rate is 4.16 m3/hOn my interface, it is 4.1095 m3/h. I am using DWSIM Version 6.1 Update 1
I am unable to locate the Continuous Stirred Tank Reactor under Unit Operations. I am using DWSIM Version 6.1 Update 1
In the Direct Reaction, there are two options as Arrehenius and User-Defined. For which should A=0.004 be entered?. I am using DWSIM Version 6.1 Update 1
I am unable to find any green tick button to Accept changes. I am using DWSIM Version 6.1 Update 1
I am unable to locate the Composition option to enter the Basis as Mole Fraction. I am using DWSIM Version 6.1 Update 1
I am unable to locate Object Pallete to add the material stream. I am using DWSIM Version 6.1 Update 1
while checking the conversion after solving the flow sheet..I saw the conversion of water as 2390.06%..is there any error while solving flowswheet
how to know the Tmin And Tmax range vaild for the define rate constant ?1) Repeat this simulation with different compounds and thermodynamics Compounds: Methyl Acetate, 1-Butanol, Methanol, N-Butyl Acetate Property Package: Raoult's Law 2) Repeat this simulation with different feed conditions Inlet stream: Mass Flow: 3600kg/h Mole Fraction(CH3OH): 0.1 Mole Fraction(C4H9OH): 0.45 Mole Fraction(CH3COOCH3): 0.45 Temperature: 75 degree C Pressure: 5 bar 3) Repeat this simulation with different CSTR dimensions and reaction kinetics CSTR Dimensions: Volume: 4 m3 Reaction rate: rA = KCACB K = 0.01 , n = 2
How to set up the range for Tmin and Tmax? Are there any rules upon selecting the range?
Dear Sir /Madam,I) How can I specify the reaction order to be 2 . Should I just specify the DO of the reactants i.e.Ethanol and Acetic acid to be 2 ?ii) The question specified only the value of 'rate constant' and how can we enter it as 'frequency factor' In the Arrhenius equation
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Outline:കെമിക്കൽ കമ്പോണന്റ്സ് ചേർക്കുന്നു പ്രോപ്പർട്ടി പാക്കേജുകളും ഫ്ളാഷ് അൽഗോരിതംയും ചേർക്കുന്നു യൂണിറ്റുകളുടെ സിസ്റ്റം ചേർക്കുന്നു ഫ്ളോസ്ഷീറ്റിലേക്ക് മെറ്റീരിയലും ഊർജ്ജവും ചേർക്കുന്നു പ്രതികരണങ്ങൾ മാനേജർ ഉപയോഗിക്കുന്നു ഫ്ളോസ്ഫീറ്റിലേക്ക് CSTR ചേർക്കുന്നു കണക്ട് ഫീഡ്, പ്രൊഡക്ട്, എനർജി സ്ട്രീമുകൾ റിയാക്ടറിലേക്ക് കണക്കുകൂട്ടൽ രീതിയും റിയാക്റ്റർ പരാമീറ്ററുകളും നിർവ്വചിക്കുന്നു മാസ്റ്റർ പ്രോപ്പർട്ടി ടേബിൾ ഉപയോഗിച്ച്
കെമിക്കൽ കമ്പോണന്റ്സ് ചേർക്കുന്നു പ്രോപ്പർട്ടി പാക്കേജുകളും ഫ്ളാഷ് അൽഗോരിതംയും ചേർക്കുന്നു യൂണിറ്റുകളുടെ സിസ്റ്റം ചേർക്കുന്നു ഫ്ളോസ്ഷീറ്റിലേക്ക് മെറ്റീരിയലും ഊർജ്ജവും ചേർക്കുന്നു പ്രതികരണങ്ങൾ മാനേജർ ഉപയോഗിക്കുന്നു ഫ്ളോസ്ഫീറ്റിലേക്ക് CSTR ചേർക്കുന്നു കണക്ട് ഫീഡ്, പ്രൊഡക്ട്, എനർജി സ്ട്രീമുകൾ റിയാക്ടറിലേക്ക് കണക്കുകൂട്ടൽ രീതിയും റിയാക്റ്റർ പരാമീറ്ററുകളും നിർവ്വചിക്കുന്നു മാസ്റ്റർ പ്രോപ്പർട്ടി ടേബിൾ ഉപയോഗിച്ച്
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