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Oh I am really sorry. It was unintentional and I cant delete it. :(

Hello experts, I am now involved in a project to design a distillation column for PF5 generator. This project is a scale up of existing plant. Existing design of distillation column is: Bottom part of the column is a reactor and there is a re-circulation pump. There is only 1 outlet from the...

Hello experts, I am now involved in a project to design a distillation column for PF5 generator. This project is a scale up of existing plant. Existing design of distillation column is: Bottom part of the column is a reactor and there is a re-circulation pump. There is only 1 outlet from the...

Thank you Mortena and Pierreick for the suggestions. I will do the calculations :) Both comments are really helpful

Hello experts!! Is it possible to obtain overall heat transfer coefficient value (roughly) without experiment for a reactor with cooling jacket? My approach to estimate U value by designing shell and tube heat exchanger using process simulator but the value was quite high than our expectation...

We can use stream calculator.

Thanks, MJCronin I found the answer in the forum you mentioned.

Dear experts, I am still in the learning phase. Bear with me. (My main task is process simulation but slowly trying to develop myself into a process engineer) While preparing a datasheet for pressure vessels, what would be sound engineering practices to specify the design pressure and...

Thankyou Strong and EdStainless :)

Can anyone suggest a vendor that manufactures a 2 KW capacity turbo-expander? It is for laboratory purposes. The least I found was 25 KW by Turbogaz.

Thankyou TugboatEng for the suggestion. However, I contacted LEWA as suggested by DMHCE and already sent the datasheet for quotation.

Thankyou DMHCE, I will write an email to them.

I am looking for a pump vendor which meets my design specification: Process fluid: Liquid CO2 Temp: -50oC suction prsesure: 7 barg discharge pressure: 70 barg volumetric flowrate (at T and P): 60 L/hr. I tried to find local vendors in South Korea but no luck with this low temperature and small...

To make my point understandable without confusion..... I am getting liquid phase even below the bubble point pressure. And the vapor phase is produced only at vacuum pressure. I cannot plot the phase envelope due to some required changes to be made on thermodynamic model.

Dear experts, This query is based on simulation results (aspen hysys). What I thought was scrubber or column bottom pressure would be at bubble point which corresponds to bubble point pressure. However, the vapor pressure at the scrubber bottom temperature (with the same composition) is...

To me it is not okay..... usually such results are not reliable. What is the error msg?

I did some projects regarding CO2 capture but used aspen hysys as suggested by the client (and using a different solvent). We don't need to change the chemistry as it is very difficult to obtain our own reaction kinetics. Aspen plus has a very useful tool "design spec". Therefore, after fixing...

"But when I try to increase BOTH (the lean solvent flowrates and K2CO3 concentration)" What is the ratio of Flue gas CO2 flow rate and solvent flowrate?

There is no straightforward equation to estimate the minimum no of trays/reflux ratio for extractive distillation. Take a good initial guess for number of trays and observe its effect (vary the tray no.) on duty of reboiler and condenser. You might get a curved line. Higher duty-more operating...

If you want to proceed to really build the scrubber on the basis of simulation, the appropriate thermodynamic model should be elecNRTL (you can change the vapor phase to RK model). You are not supposed to use UNIFAC model (it is my recommendation). you can estimate missing interaction parameters...