Search results for query: *

Good advice has been given by previous posters. As to standard, if you check Shell DEP 80.45.10.10 on pressure relief, it states clearly that PSV should be located u/s of demister...and the reasoning can be inferred from next line that allows PSV to be located d/s of demister if the PSV flow...

Thanks Snorgy Separators are 2 phase. That indeed is the scheme. The liquid flows are measured and compared and then the control logic attempts to reduce gas flow by throttling the vapour outlet of the vessel where the liquid flow is higher (while keeping the other vapour outlet fully open)...

Thanks David. It gives me comfort to hear that this phenomenon is not uncommon and do agree that unless it hurts, no action need be taken. Whats the worst that could happen (beyond this imbalance - slugging, internals damage ?) While running at about 70% of design capacity, the level is...

We have 2 separators operating in parallel - with symmetrical piping etc. However, we experience a 1 : 2 liquid flow distribution at approximately same gas rates, despite the u/s symmetrical piping arrangement. The control system aims to control the vapour outlet flow from the vessel seeing...

Hi Is there any publication / guideline / industry practise for purge rates to be maintained in Horizontal flares (always lit)? Are any provisions made to address change in direction of wind /gusts in such conditions ? Thanks Bala

Hi Maybe I'm missing something..do u have a problem with the motor current(pump operating at end of curve without resistance...)? Lizking has the solution for you...this route is often followed to "match" pump to required system head...This would be inefficient though (as u'd kill a lot of...

Hi I have a problem with power not being available at the GT's during hot summer days. Fogging has been suggested to improve the situation. The required water quality is the (traditional !) DMW with < 10 ppm of TDS, <3 SiO2, pH bet 6.5 to 7.5, conductance < 11x10^(-6) mho/cm. I have the...

Hi I have a problem with power not being available at the GT's during hot summer days. Fogging has been suggested to improve the situation. The required water quality is the (traditional !) DMW with < 10 ppm of TDS, <3 SiO2, pH bet 6.5 to 7.5, conductance < 11x10^(-6) mho/cm. I have the...

Flareman You mention : the lower purge rate is irrelevant in situations where the flare is on - the lower rate being useful only if the flare is idle and waiting to come on. This is readily understood. Can we hence conclude that in cases where flare is continuously on (or on for a...

Hi A very interesting thread....thanks to all in the chain. Montemeyor : Is the low temperature event irreversible? You mention "personally burned a 24” hole on its shell to clearly put it “out of its misery” --- "...is there nothing that can be done (depending on materials employed of...

Hi I believe you are agonising about having two independently connected parallel PSVs protecting same vessel. If so, provided you have taken care of keeping one PSV always available, there should be no problem. How is this different from parallel PSV's mounted on same header (consider the...

Hi From the originator's response on conditions prevailing, it is clear that the gas is compressed, cooled and sent for re-injection. He does mention cooler performance. Under the circumstances, it would be logical to assume the gas to be water saturated (is the KOD having water after the...

In a (Hydrocarbon gas) Dehydration column using TEG as absorbant, generally a 5 deg C superheat is maintained on TEG over the inlet gas temperature to prevent Hydrocarbon condensation. We have a higher differential (gas temp is still practically just a deg C up on its inlet...so not much TEG...

Does any operator have direct experience with degradation of TEG in Sour gas dehydration - dark non-settling colour that is not filterable / adsorbable in charcoal filters ? H2S is in <0.1% range, CO2 upto 6%, Contactor operating at 27 bar / 18 deg C; REgen at 204 deg C max. Please also give...

Hi There have been excellent responses to this query from pump point of view. I also understand that the motor also has an efficiency which peaks at about 85% or so of the load. This the manufacturer of motor will be able t confirm. Hence, when switching to 3 pumps, you may be increaseing...

Hi You can &quot;estimate&quot; the losses as follows : Losses are due to 2 accounts - A : Carryover & B : Evaporation (or vapour pressure related) A. With a proper demister in place you can have a typical liquid carryover loss of 0.1 USG/mmscf from a column - Use this to estimate...

Hi Just a word of caution... While usage of water would be a nice way to clear Ammonia, besides the heating mentioned by dimitris, also be aware that the high solubility can cause vacuums. Your mention about the N2 purge makes me wonder if the same is located on the dosign tank. If so...

I remember these two grades as generally used for flanges and other applications like tube sheet etc., On the former, there is a max limit in weight of 10000 lbs (this is old, rusty recollection of mine, I am not sure what the current code says...) Sorry if I have mislead anyone with this...

We have a client who has given us a 50 bara / 80 deg C design pressure, which unfortunately is pushing the entire plant into 600# category from 300#, and hence the costs. A typical consultant (vs) engineer confusion ! Can some one advise what to do ? I know as an engineer( ...!!) that I can...