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Folks. Is there any available spreadsheet for the calculation of the sulfur recovery in a SRU , i am asking this because different results has been used from engineering compared to operation

Folks, Any idea from previous experience, how many time it took to change the trim of an 8 inch valve with simple accessibility

Folks; I am designing in aspen flare analyzer the flare network. when setting the parameters of the Blowdown valves, I am supposed to set the back pressure @the valve. Any idea how to calculated it? is it based on the Maximum pressure of the system?

Folks; While running aspen flare analyser, I am getting this mesage: nhv calculation failed because phase properties are not saved! any thoughts to resolve?

Dear Sir; thanks for the reply! May I was not clear enough in the post, I know the sdt, I should wrote if we have a leak in a flange ( which is not a normal operation ) what ever the leak rate or duration then should the surrounding area be considered in HAC or since it is not a normal...

Folks; did we consider in stds like API 505, IP 15 that flange connections are within class 0, 1 or 2?

Was the flowrate used in the radiation and vapour cloud disposal report equal to the design capacity or not. Yes equal We can't see the report and I'm struggling to believe updating the report is either a costly or time consuming thing to do and then no one can ever question the design. Cost...

if the gas composition has been changed slightly (same HHV), flow capacity not exceeding design , ambient cd are the same, is it worth to update the Flare Radiation and Vapor Cloud Dispersion report?

@LittleInch we have a brownfield project,we have requested the contractor to update the flare radiation report, the flare capacity is not exceeded, I need to know even if the flare capacity still within capacity , if the flare radiation can be affected?

Folks does flare capacity if not exceeded by an additional equipment can be taken as a credit to not update the flare radiation ? cheers

Folks; our current design on site we have a chemical injection pump operating at high pressure. we are intend to add a second train operating at low pressure, same pumps will be used. on this low P, a PVC (with PIT) is being presented in the design, OPs team has challenged the design , under...

Folks; the plant is optimally manned, no manual operation forseen as long as we need operator on place just in case I am thinking about override the ESDVs for this particular case and monitor the presence of liquids very closely and consider the gas blow by scenario during hazop of downstream...

Folks; in the design of a plant, the compressor in equipped with suction scubber,at LL liquid level the ESD will close, however there is no liquid in the suction in normal operation. how to fix this? thx

Folks, which comes first , the preparation of the plot plan or Hazardous area classification? thx

@LittleInch this is due to electrical availability. the compressors are reciprocating not centrifugal! rgds

Folks; our engineering companie is proposing 2x 50% compressors configuration. one is electrically driven and the second is through gas engine working in parallel. from technical perspective anyone has an experience with this configuration and especially any expected drawbacks, potential...

@dik what is the reference of the 3.6.4.4? thx

1503-44 thx for more precision any std that stipulate that any building shall be equiped with ledder and cages? thx

Folks! is any standards that mention the access ladders with cages to the roof top of buildings? rgds

Floks, Our plant is designed with electrical and back up diesel pump. According to NFPA 20 should we Connect the electrical one to UPS in addition to a national grid (reliable source) or only to the latest one (no need to UPS connection) Regards