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Hi LittleInch and georgeverghese, Thanks for your help. The compressor suction system contains a suction scrubber, without any isolation from the compressor casing. And yes the suction scrubber has a fire PSV. The suction system design pressure of 20 barg is based on worst case settle out...

Hi, I would appreciate if someone could help me with the following question: I have a compressor with suction system designed for 20 barg. The seal gas supply pressure is at 22 barg, which has taken into account of normal suction pressure and worst case settle out pressure (around 19 barg). My...

Hi, I would like to ask if it is possible to have a filter (particle removal) for two phase flow? one of our clients said this is not going to work but I remember we have it in a previous project. Thanks.

Hi, I would like to ask the following question: When we determine the PSV minimum design temperature, do we consider the low temperature when relief fluid flashes across the PSV? In my previous project, we took the lead line minimum design temperature as the PSV min design temperature and did...

Hi, I would like to know if we should consider sand in a conventional separator vapour outlet for a typical offshore oil&gas platform? Can sand be separated out in a conventional separator due to gravity? Otherwise does it mean we have to design the separator vapour outlet lines suitable for...

Hi, I would like to know what is the effects of inlet gas temperature on TEG Glycol Contactor performance? I understand that the TEG should be circulated at a range of 15 - 50 degC as per GPSA, but is there a limitation on inlet gas temperature and, what is the effects? Thanks.

Hi Katmar, Could you explain on why if the line is not liquid full, then Bernoulli equation does not apply? Also, what would be the theory to be used for this situation in order to understand it? Thank you.

Hi georgeverghese, Thank you for your response. Can I not consider atmospheric pressure at point 1 if I have a properly sized vent line on top of it? I thought this is the purpose of the vent line to avoid vacuum / sub-atmospheric?

Hi bimr, In my current situation, we have an existing firewater overboard dump line which has flowrate of 4300 m3/h and the Froude number is 4, so if I assume that flooding would occur and therefore line would be liquid filled, am I correct to say that then the pressure at P2 (i.e. at exit)...

Hi, If I have a vertical firewater overboard line with a vent on top of this vertical line, by applying Bernoulli equation between point 1 (on top) and point 2 (on exit at bottom): P1 + rho.g.h + 0.5rho.v1^2 - friction = P2 + 0 (reference height) + 0.5rho.v2^2 suppose the height is long and...

With the answers collected here, I would expect the piping segment downstream of the orifice will not experience supersonic flow. Is this correct? More specifically, downstream of a blowdown (or depressuring) orifice used in offshore gas processing or onshore gas plant, it is not possible to...

Hi, I would like to ask if it is possible to generate supersonic flow across a restriction orifice? I know that supersonic flow can be generated by passing subsonic flow through a converging and then diverging nozzle, but I am not sure if the same will happen for an orifice. Thanks.

Hi georgeverghese, Thanks for your reply. In this brownfield project, it seems not feasible to relocate the CM drum to highest point. Do you have any opinion if installing an automatic venting for the new aftercooler would help solving the issue? Thanks.

Hi, I need to design a submerged seawater lift pump. Can anyone tell me what should be a general "margins" for the lift pump bottom? I have the following design steps as below: a. Find the lowest sea trough (in this case it is -9m) b. Find the SW Lift Pump length (estimated 2m in this case) c...

Hi, I am working on one offshore brownfield modification where a new module has to be placed on existing platform topsides. It requires cooling medium on the new module but that means the new compressor aftercooler will be located higher than the existing Cooling Medium Expansion Drum. I...

Hi, I would like to know if API Std 521 (Year 2007) Mach number formula (27) and (28) can also be used for PSV lead line / BDV inlet line etc, and not only limited to PSV outlet line. Is there any limitation in the mach number formula derivation for the above? Thanks.

Hi, I am a process engineer and I would like to know when a centrifugal compressor suction is blocked, will the compressor pulls vacuum at its suction? I have heard that a reciprocating compressor will create vacuum at its suction, is this true? Please help. Thanks.

Hi, I would like to know what is the lowest water dew point (in ppm) that can be achieved using typical TEG gas dehydration design for offshore, without going into those proprietory licensing design (e.g. Coldfinger)? Is 1ppm the lowest? And what is the lowest whe stripping gas (e.g. fuel gas)...

Hi, in one of my previous project, I have an offshore facility which includes 3 stage separation and condensate heater in between to achieve the TVP / RVP spec of the condensate. Our client states that the maximum condensate heater outlet temperature should not be greater than 100 degC due to...

Hi, I have gas treating plant with dehydration and mercury removal units. So fa r I only see the mercury removal unit located at the downstream of the Dehydration Unit. Does anyone know the reason? Is it because the Hg Removal Unit can receive "less" gas after dehydration? Thanks.