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minimum design temperature of piping is -30 deg C and it has been tested for -50 deg C. bleeder is 3/4''.Main pipe is 8''.The pipe is not insulated. I talked to our third party inspector and he confirmed that we do not need to consider leakage of bleeder. It will be considered as permanently...

system is in operation. I understand what you say but then all high pressure Ethylene piping should be stainless steel. But normally it is Carbon steel. The pipeline from which we receive Ethylene is also carbon steel.

we have a high pressure ethylene piping. Pressure is about 80 barg. Material is carbon steel. There is two possibilities which we may face auto refrigeration/brittle fracture: 1- There are some bleeders on piping which in case of leaking may cause auto refrigeration ( pressure drops from 80barg...

Hi all, For high pressure Ethylene piping, how you solve problem of auto refrigeration if bleeder leaks?

Thanks every body. My problem is that we have a lot of piping which theoretically can be blocked in between two manual valves or one manual and one automatic block valve . The pipes have different length and sizes.If we decide to install a TRV, I am sure 3/4'' x 1 '' will be enough. The only...

Hi Everybody, do you know any criteria for a minimum pipe Length/Volume, for that Thermal expansion relief valve shall be considered? I have seen in some company's Design practice that they consider 0.5 m3 for LPG and for all other medium 1m3 or 30 meter. It is not always possible to size the...

yes exactly I am doing Lopa but I doubt if the consequence analysis of HAZOP was correct in first place.The assumption was that both tube and shell side crack and LPG will escape to Atm. As you said it depends to system. Therefore I described design temperature for both side of exchanger. Since...

yes you are right. But I need to know what exactly can happen and need to add safegaurd with certain probability depends to the risk. Exchanger has been designed for the operation range but we still need to know what happens in case of failure and define safegaurd for it. Even if the design...

hello everybody, we have some shell and tube heat exchangers for cooling of LPG with different inlet temperature ( min 4deg C, Max 150 deg C).As cooling medium we use Ammonia. Ammonia flow to shell side and LPG in tube side. Design temperature of shell side is -28/50 deg C. The question is that...

Hi every body, Can somebody tell me what happens if we increase level of water in seal drum (1m app.) integrated to an elevated flare? consider there are two flare systems one ground flare with low capacity which has a water seal drum and one elevated flare with much higher capacity which has a...

Thanks all for your help.

thakas all. Unfortunately it is not possible to replace flame arrestor. It is a regulatory requirement to install it when we have even EX-Zone 2 in tank. last inspection shows no accumulation of liquid and no plugging in pv vent. But actually it does not prove anything because we have heat...

Hi all, Can somebody tell me what can happen if Liquid collects in a pipe with deflageration flame arrestor ? or if liquid condenses in a tank breathing valve with flame arrestor? Can we say it will not be effective anymore? we are a polymer plant and most of our storage tank breathing valves...

Thanks for the fast reply. Unfortunately the statement is correct. We receive Superheat steam at our interface and the pipe is designed for temperatue up to 250 deg C. The plant is big and till the pipe reaches to each single equipment , the steam is saturated and not Superheat anymore ( this...

hi, I am working in a chemical plant which receives steam from a supplier. We receive super heat steam with temperature between 180 deg C to 250 deg C and pressure between 10 to 11 barg. There is a safety valve with set pressure of 11.4 barg at interface point and also some temperature...