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Found Thank you very much, Pierre. That is exactly what I need. for info, not for reply Actually my concerns are related to LL densities. Densities difference is small ~20 kg/m3 or 2% and those are variable/unstable. I would not post such issue if this was similar to a hydrocarbon-water...

If U-pipe is not connected to the separator then U-pipe elevation will have nothing to deal with L-L interface in the vessel. Am I correct? The highest point of U-pipe can be 1 meter higher or 1 meter lower and this won't affect L-L level. Or I do not catch something? @LittleInch This is the...

Disconnect from light liquid (green) and connect to vapor space (white). The same as for G-L level control? Am I correct? What if the horizontal run of U-pipe will be oversized so velocity is almost 0? Will it help to avoid carryover?

Dear forummembers Is here anybody familiar with such L-L level control scheme? Is this method workable or not?

Start with process model and properties grid in Hysys or Aspen+. Aspen EDR is not intended for phase equilibrium modelling

Could you please share some related to the liquids having viscosity less than water?

flashing CV is indesired but stiil a normal option for the process industry as those are sensitive to a control loop adjustments and actuall Cv rangebility make sure that existing CV inlet conditions are total liquid accounting the flow acceleration due to CV's DN is smaller than upstream piping...

1/ i-butane or n-butane? 2/ Is pressure at the tank constant? 3/ Is pressure at the injection point variable? 4/ Is flowrate variable? 5/ Are total liquid conditions at CV inlet nozzle guaranteed?

This community has no policy, no ethics, rules, or codes. This leads to it is gradually corrupting. Note that the issue concerns to the comunnity, not the forum platform. A community is much harder to built&manage.

thank you, it helped

Please somebody explain how to manage "My forums" ribbon to the right of the forums list.

The logic is corrupted Second tank is uncovered. Second tank has neither a cover nor a hole lid. How do the gases get into tank if there is no a barrier between the tank vapor space and atmosphere?

Where has the forum policy been moved to? How will the newcomers know what is ok and what is not?

1/ Assumed suction ID is 6", hydraulic pressure drop @150gpm is 0.5m - see file attached. You can reiterate results by yourself - https://www.pressure-drop.online/ 2/ Assumed water temp is 120°F water vapor pressure is 1.2m 3/ Atm pressure head is 10.5m 4/ Suction velocity head is negligble -...

1/ Is this pump properly vented? I do not see any vent valve on P&ID you have shared. Where is the air going to go to? 2/ Delete strainer. You have no enough NPSH for such features. If this type of pumps can't tolerate the liquid you are going to pump out you should get back to submersible...

Is pump capacity controlled? What exactly do you mean "self-priming"? Can you describe? How are you going to fill suction piping with liquid for self-priming? Why do you need a booth valve? Can you describe? Does this liquid contain any amount of a dissolved gas? What is suction intake design...

to add to mentioned above Tank roof is the highest point while control valves shall assure free draining. If you locate valves below tank how are you going to route CV downstream piping downward to a vapor space nozzle?

Please share statistics how much the community activity has been lost since the new forum was launched. % of posted / watched / commented

I have limited experience with "stans" region. Below is what I have learned. Sorry for language, I have rare practice in english. 1/ Local compliance codes are written not to ensure compliance but rather to maintane some level of justification for bribing local officials. This means it is not...

Complaints above are definetly good but anyway is there a way to get this forum back as a new one is unable to navigate? I don not have free time to waste on reading through 90% threads I have nothing to do with.