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Thanks a lot George… I think with a fixed suction pressure (hence a fixed density), a fixed discharge volume (a compressor casing subject to test) and a fixed strokes per minute (fixed RPM) we would have a fixed mass flow rate hence a constant timely increase in discharge pressure (corresponding...

Largest volume of the casing to be tested is 400 Litres… Should the recip compressor in such test stand be equipped with VFD system or having the constant pressure increasing rate (5 bar/min) during pressurizing steps and having no flow during no pressurization steps (in ramp-up diagram) can be...

Thanks George for your response… But there are another questions: -Do you mean the compressor should be operated in whole time of the test and just to be full recycled at intermediate constant pressures steps within ramp-up plan? -Can this He compressor be also applied for Gas Leak Test by N2...

Hello guys, We are designing a test stand for Helium and Gas Leak Tests such that to be able to do the tests on manufactured Compressor Casings up to test pressure of 400 barg and want to know about the type, characteristics and specifications of the compressor included in mentioned test stand...

@HTURKAK, Ok, i am involving the process design of the storage tanks for many years and agree with what you mentioned about the rules for storage tanks sizing based on API 650... But the matter around which i did open a discussions, might different than what the OP initiated, was a basic concept...

@HTURKAK Thanks for sharing a good example for clarification... This example approves what i was saying about the pressure variation inside the tank due to temperature variation... In fact, in third and fourth stages of your example the pressure inside the flask is higher than atmospheric due...

Please think about the thermal out-breathing in a sealed fixed roof tanks and suppose the relevant facility for pressure relief, say pressure breather valve haven't been considered. Doesn't the fluid temperature increase due to ambient temperature change, hence the vapor pressure increase...

@IFR

@Sawsan, Don't you think considering the desalter vessel(s) is full of liquid and the level of the connection point of outgoing line from desalter to stab column is normally well above the desalter level, basically no need to control the pressure at desalter outlet to avoid the desalter to be...

@Sawsan But i mentioned cascade control based on separator level and pressure at the inlet of column...your opinion on this scheme?

Thanks George, In option 1 considering the desalter is full of liquid,don't the FV and PV fight against each other? For option 2 please clarify about the flow surge...

Attached there can be seen three options; which one is applicable and logical?https://files.engineering.com/getfile.aspx?folder=9100d10d-1c66-4a05-bb1b-15dda788df42&file=Desalter_system_control_configuration.pdf

@george I think the PV has been applied on the exit line to maintain the desalter pressure above the bubble point; but will fight against the FCV on the same line...right?. FCV is modulated by LIC on the upstream separator. @Sawsan I do fully agree with you for avoiding to apply the control...

Dear All, In an existing crude oil desalter there is a control configuration as follows: A level/flow cascade control will maintain the liquid level in upstream separator while the LT/LIC is in the separator and FT/FIC is at pump discharge. A pressure control valve (PV) is controlling the...

Dear All, Referring to the thread378-351722 (titled: 3 phase flow in pressurized pipeline) there is discrepancy between the two declarations included in mentioned thread as follows: Post by BigInch on 13 Sep 13 14:11 "Generally the more gas you have in the pipelines, flowing, the friction loss...

Hello gerhardl, It's the subject of our challenge with client; they want the ESDVs equipped with handwheel for maintenance cases but we say an emergency valve shouldn't be equipped with handwheel to avoid the risk potential due to inadvertent opening/closing by operator.

Thanks gerhardl Please let's know if there is any standard/practice mentions no handwheel needed to be mounted in ESDV?

Dear All, Is there an standard/practice mentions that the ESDVs should be equipped with no handwheel due to safety matters?

Thanks rotw, I'm thinking to consider three anti surge loops for three compressors each one starting from tapping at downstream of each compressor's discharge cooler and terminated to upstream of same compressor suction drum. What's your opinion on these anti surge loops configurations?

Dear Latexman, Thanks a lot...