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Pennpiper thank you for your replies. I am so familiar with LDT. My main point is, from piping engineer point of view, if process define different commodity code is it a concern/ for you? For example, considering “steam" commodity code for a line number instead of "steam condensate" or another...

Hi ALL, As I know people used to separate or categorize the lines in the line list (LDT) based on their commodity (fluid which is flowing in the line) code. Is there any firm reason(s) for this separation or what’s going to happen if a person doesn’t follow this rule? I have seen a lot of fluids...

Thanks zdas04

Thank you TD2K & zdas04 for your answers. zdas04, why do you choose the 0.6 Mach as a criteria? How do you find choked flow condition? (Choked Pressure/Flow Rate) Could you please give me a clear example from that you are refering to?

Hi all, I am using the RO (Restriction Orifice) to let-down the pressure from 900# (ANSI Class) to 300#. The steam is flowing through the pipe and sends to some consumers. I have manual valve downstream of the RO. These are my questions: 1. Do I need any PSV (Pressure Safety Valve) for...

Thank you don1980. So for the thermal expansion relief scenario, there is no concern about pressure drop across the PSV's inlet line (max 3% of set pressure) and you can always ignore it. (No need to calculate)

don1980 / Cahnce17 /OilToil Do you think the thermal expansion and control valve failure (as I mentioned above) will have the same issue (chatteing) regardless of the rated flow technically is NOT available?

Sorry guys I was busy with other stuff during the past few days. Thank you Chance17 , OilToil, don1980 for your answers. Then selected orifice size, upstream and downstream pressure are only three factors which you should consider for PSV’s inlet/outlet sizing regardless of how much flow is...

Chance17, thank you for your answer but let me be more clear: I believe for PSV sizing in control valve failure case, considering the rated flow for PSV’s inlet/outlet pressure drop calculation, is not necessary because we have already considered it. Kia

Please give me your idea: In case of PSV’s sizing for "control valve failure" you have to calculate PSV’s required relieving rate based on maximum flow can be passed through the control valve which it is calculated from maximum cv of the control valve. As everybody knows, the orifice’s selected...

Thank you guys for your replies.

Hi everybody, Does anybody know which items, in new edition of API 520 part 1 (Edition 8th Dec. 2008) have changed / modified and how it could be affected to PSVs’ design / selection? Thanks.