1) Your licensor say correct but it can not stay for last long, it happen only inteval of the residence time or retention time.
2) After the feed gas stop longer than its retention time , the mass transfer will change ( in flow can not equal to out flow) , then your understanding is correct.
3)...
1) It is normal if your fluid contain lighter component than its design.
2) Can you try with following suggestion
-Trottle pump discharge
-Spray water at your drum to gain sub cool liquid.
-check pump vent line already release before pump start. if in doubt, just stop the pump for a while then...
If your initial pressure is within 300# before depressurization
and your piping downstream depressurization made of carbon steel it can tolerate up to -29 C
all calculation show not below -10 to -20 C minimum temp.
except your upstream system 600# including higher (900#,1500#) your let...
Do not compromize or too optimize in the safety system.....
a) Take maximum level alarm high hieight or any specified for max and calculate wetted area, if you do not have take about 80% is good enough.
b) If you need to cover uncertainty in your operating envelop, should take max F.
Better take experiment, it is much better than trial calculation.
your titration and measure temperature and correlate back we short your evaluation.
hope this help.
You can use if ensure gas field not mix Gas/water/oil
Not recommend if later your well fluid will contain >10 % of liquid.
Not recommend if later well pressure deplete more than 50% of orinal value. That mean its work only narrow range.
Please re-consider, you will end up very narrow of...
1) why licensor say no need;
-Due to that place always last location for monitoring not for control. SRU air requirement alway over size/ & high margin for air flow. especially when run lower S load
- SRU unit always has exessive air/O2 exess by its nature.
-may be SRU design has 1 train spare...
1)If can not avoid, Modify the suction elevation to improve NPSHa, You can not find the good pump for this service, but I think you may wrong calculation in NPSHa, I guess you should have at least 3 FT, Please check again, I also work for oily water pump offshore from open drain drum.
2) This...
negative tolerance provide your risk of flange leak due to not easy to tightening, especially when the pipe OD >6", more stress to your flage if you try to fit it..
1) The best of two phase flow calculation still always 20% error from the real situation in specified operation range. Then if you have so wide operate envelop error could be 40-60%..
2) Many formular is good only for horizontal pipe not vertical pipe
3) Liquid/Gas ratio & its densidty in each...
1) What is the suitable material for vessel service temperature -46/100 C ( Design P 80 barg, high CO2 41% ,H2S 150 ppmv,wet stream)?
2) What is mill certificate require on such vessel?
3) Any special test before accept material?
4) Any cladding require?
5) Welding such as Pre/post welding...
1) Yes, the gas from CO-1 will go to liquid line to CO-2 and similarity from CO-2 to CO-3, if no liquid seal at bottom column.
2) But the gas rate will limit by valve size & system delta P between valve, You should open the Cv-(Liquid valve coffeficient)valve originally size for liquid , you...
1) filtration system will be solution
2) Please test your sytem via your pilot scale before go to real invesment, you must know by collect information of inlet concentration & load vary
3) the full closed loop will have high operation and maintenance cost if bio-growth too high
4) take 60% as...
