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liquid is NGL and Pump A is pumping from Storage tank.

JRLAKE I am trying to calculate NPSHa for Pump B. Inlet temperature of Pump A is 80 F. And discharge of 'A' is appx. 90 F. both pumps 'A' and 'B' are closest and there is negligible elevation change between these two pumps. How do I get vapor pressure at suction of pump B at 90F. From...

How do I calculate NPSHa for the pump where suction of the pump is discharge of other pump? Pump 'A' is pumping liquid at 90F with discharge pressure 220 Psig. Pump 'B' has suction pressure of 220 psig, which is discharge of Pump 'A'. Pump 'A' has suction from the storage tank, and storage tank...

For orifice plate, how can I find at what length/distance pressure will recover almost same(considering friction losses) as upstream of orifice plate?

MortenA, dcasto is right, you required Drizo process to dehydrate the gas and to recover 99.99% TEG purity. We have drizo process and able to achieve -70 F dewpoint measured at std condition condition.

Abd74 , i am agree with tylang06 that wireline is good option in both avenue of getting good money and career. But it's hardworking sometimes as you never know about working time. mostly DST works during day time, but being wireline operator you have to be ready for 24*7. good luck,

thank you dcasto, We are facing second issue also. We have started adding corrosion inhibitor solution six months ago in to our amine-DEA system. since then corrosion rate is coming down but at a same time HSS(&bicine,oxalate,format) is coming up. Do you know the reason behind this ? I know...

Montemayor & dCasto, I understand you guys have designed so many amine plants, you can asnwer my question. I am trying to simulate DEA-35wt% system for absorption of acid gas. But to understand basic, how can I calculate(without simulator) how much flash gas will liberate in flash tank from...

ivegotgas, Thanks for your quick reply. You are right, I am working on to put filter on rich side to remove Fes/other particulates. I asked the question on carbon filter because I saw your answer for reena1957's question. gosooners

ivegotgas Can you elaborate term : '10-20% of the circulating lean amine' you mentioned on 21st Feb reply. Don't you think superficial velocity 2-4 gpm/ft2 is too conservative ? gosooners

ivegotgas, thanks for your valuable thoughts. We are facing high fouling problem in L/R exchanger purticular in rich side of the stream. We did our Iron analysis and it is found 25 mg/l, Sulfate analysis is also very high. Now, we are thinking to put filter that can catch iron/sulfide particle...

dcasto & SJones, Yes, feed enter on tray 3. as i mentioned we don't have corrosion issue on bottom part of stripping column and reboiler. First 15 trays have significant corrosion issue and nozzle that enter to column. We have SS304L pipeline not 316L. Do you think this problem is because of...

CKruger, Thank you for suggestions. But what do you think about high velocity just after control valve. Flashing of gas occur after control valve and it is appx 2%. Before the control valve velocity is only 5 ft/sec and there is no significant corrosion issue on that part. gosooners

Greg, I used Promax software to calculate velocity. Yes, it's two phase flow with intermittent regime. We have already place corrosion coupon before we started our corrosion inhibitor circulation last week. we will wait for results of inhibitor success for 3 months & then i am thinking of...

Hi all experts, Here is the situation in my gas processing plant : MDEA of 50.5% is used to absorb CO2 and H2S with loading 0.37 m/m. I have corrosion problem in exit of lean/rich exchanger pipe to entry of the stripper(first 4 trays) and bottom of the tower. I have checked following analysis...