For heat exchangers in simulations, I have often seen that sometimes the UA value is often held constant. Like its taken from a max/design case and kept constant for other cases like turndown. However, is this truly the correct approach? Given that the overall heat transfer coefficient (U) is...
In a typical propane refrigeration loop (e.g. in photo), there is always an accumulator or surge vessel. There is no level control on this vessel...so how does the level in the vessel get maintained. The expansion valve usually a level control valve maintains level in chiller. Does that valve...
In a typical fractionation column with a total condenser, does the liquid going to the reflux drum remain fully in the saturated liquid phase? Is any vapor formed in the reflux drum? Is the reflux drum usually just an accumulator or does it also act as a separator? If the reflux drum has a boot...
I am trying to understand if I can send a hydrocarbon product to an API 650 tank which has max internal design of 2.5 psig.
Product is from Inlet Separator at 50 psig. Now when I model it I see that the vapor pressure of liquid from Separator is 50 psig. When I take it across LCV to the tank...
Hi,
I am trying to understand use of high and low selector in process control
For e.g. in the attach photo, can we use high selector for pressure and flow controller to control min. flow recycle control valve?
Should we use high or low selector?
Should PC and FC be direct acting or reverse...
How does VFD speed control actually work in Reciprocating/Positive Displacement Compressor?
In case of reciprocating compressor, how does capacity control work with speed control. Since we don’t really measure capacity / flow, is the speed control done based on pressure?
For example lets...
I have a pump that is pumping stable product to a tank. There is no blanketing on the tank and it is not vented to the atmosphere. What will be the pressure in the tank? Will it be due to vapor pressure of the liquid. Since vapor pressure is below atmospheric..will there be vapor in the tank at...
I have a oil water separator operating at 50 psig with a level control for interface. Water flows out of the level control valve to a pressure vessel. The level control valve is sized for p inlet = 50 psig and p outlet = 15 psig. The water pressure vessel has no blanketing or any positive...
How flow change with pressure drop? If P1 at the inlet of pipe=50 psig &P2 at end of pipe is based on pr. drop and flow is x for e.g. Now if i put orifice in pipe due to more delta P should flow increase to > x since flow is proportional to delta P? Why by putting orifice then flow decrease???
In a low pr. flare system can a the flare ko operating pr. be kept at atmospheric?
Since pr. at flare tip is atmospheric then how flare ko can be atmospheric? would it not be always higher than atmospheric due to backpressure?
attachd...
I am simulating a well with GOR at standard condition as 2000 standard cubic feet / barrel (SCF per barrel)
The well stream go through separation in high , medium and low pressure separator follow by a tower for stabilizing
the pressures are 500 psig, 300 psig, 90 psig and 55 psig
i have 2000...
hlo,
im trying to calculate the pr. drop in vertical piping for gas.
i have a vertical section where gas goes down in elevation 5 ft
the pressure at starting point is 85 psig
since there is fall of 5 ft i assume pr. gain can be calculate as = rho x g x h2-h1 where h2 is 5ft , h1 is 0 ft...
Gas is being sent from Equipment 1 (Separator) to Equipment 2 (Compressor)
I have a pressure control valve in b/w Eqpment 1 and 2
For line sizing, I have straight line length as 50 feet
I have two ball valves and a control valve (globe valve)
Eqment 1 pressure is 50 psig and control valve is...
hello all, i am trying to convert a gas flowrate of propane to equivalent liquid volume and mass.
My consumption of propane is at 0.5 mmscfd. I have tried to do following calculation by converting gas propane to mass and then using that mass and liquid density to convert to liquid volume...
Is the Flow Tubing Head Pressure (FTHP) downstream or upstream of the well head choke valve?
What is the pressure downstream of the well head choke valve called?
For a three phase separator turndown, would level settings have any consequence?
Lets say vessel is designed for 1000 BOPD and 200 BWPD and 2 MMSCFD gas
But we are operating at 50% i.e. 500 BOPD, 100 BWPD and 1 MMSCFD
if the LLL-LLLL time was 2 minutes for design...would not it increase now...
Evaluating whether this process scheme (attachd pdf) is ok or not. I have high pr. Scrub which is operating at 15 barg and low pr. Scrub at 1.9 barg. On low pr. Scrub I have pressure control valve with split range which maintain pr. At 1.9 barg in scrub. Down strm of the compressor I am mixing...
How does one interpret CGR ration. If there is a reservoir fluid composition and a flash CGR ratio of 165 STB/MMSCF...does that mean if gas flow is 200 MMSCFD then condensate will be 200*165 = 33000 bpd??
i have two sample from bottom hole which provide flashed liq and flash gas and reservoir fluid composition. Now the sample is flashed from reservoir conditions to std conditions to get these composition. I have CGR ration as 28.88 stb/mmscf and the gas flow reqd is 60 mmscfd. How i get the...
i have a gas vessel operating ayt 25 psig and psv set pressure at 55 psig.
during psv inlet line sizing for blocked flow, should i take properties of gas at 55 psig? or 25 psig? for line sizing?
what should be the temperature for line sizing ...will it be operating temp / ambient temp?
