Accounting for N2 solubility in water at 655 barg, Google tells me H = 6e-5 / MPa, where solubility of N2, the Henry's Law constant, is expressed as mole fraction of N2 / kgmole of water. Simplifying, this works out to 6.2kg of N2 dissolved / m3 of water. Add the corresponding mass dissolved in...
Compressibility factor z is roughly 1.61 for N2 at this high pressure from T-S diagram of N2 in Perry Chapter 3
Find n
n=P.V/z.R.T
n= kgmoles of N2 gas
V= actual volume of gas space in m3
P=pressure = 656e2 kpa abs
R=8.314kJ/kgmole/degK
T= 300degK
Actual mass of N2 required, kg = n x 28...
You're off to a good start, this gas is probably not at or below water or hydrocarbon dewpoint.
Pistons with labyrinth type piston rings last much longer than those with conventional piston rings, but such machines carry a CAPEX premium, but these payoff very well in the long run with increased...
I set up flow control loops on hot high viscosity bitumen lines running 180-220degC with ultrasonic clamp on FT some 10years ago - cant remember the brand name , but it was some German company - worked as intended. They offered onsite troubleshooting assistance, which was re assuring.
Reverse siphon flow will not be possible as long as the discharge point is above the level at the inlet. Besides, you still got the check valve on pump discharge.
In my experience, gravity flow lines in down flow should have this air valve at the top of the high point - this is to let air INTO...
Can you describe this discharge ?
"The pipe will be discharging into the gravity network."
If this discharge is into a liquid flooded pipe or tank, then I see the justification for this air valve.
Pls ask a process engineer familiar with hydraulics in this flare network - there are many variables that will affect choice of location where this tie in should be made. You wont find this guidance in B31.3.
By the way, how many levels of flare do you have in your plant - LLP, LP, HP etc?
Maybe a side tap off the suction header to the lateral leading to pump A, instead of a bottom tap?
With pump sets in HT fluid service, where autostart of the standby pump is enabled, there is usually a warming line in operation on the discharge side of each pump that bypasses the discharge...
Since you plan to move from oil seals to dry gas seals on K303, and given the low mol weight gas service requirement, it is most likely new compressors will be required to operate with the existing GTs' for these machines.
Compressor rotor fouling may require changeout of demisting devices on...
See the footnotes on that F factor table in API 521- will your foam glass insulation remain intact with high velocity fire hose jet stream ?
If not, go for this insulation which is typically used in the oil/ gas business to enable taking full credit for its insulation during a pool fire ...
Agreed, at max flow, P2 may be 36barg, while P1 may be 36+x barg, where x is the dp relevant for this max Cv case.
Note that in some services, for the max Cv case, it would be acceptable for calculated Cv to be < say 0.75x wide open Cv, while in other operating cases, it may be acceptable for...
Those values are probably the range of pressures for P1 and P2. This info you've presented is clearly not the sizing info. There should be 2 design cases for control valves:
a) Flow with P1/T1 and P2 /T2 which leads to max Cv
b) Min flow with P1 / T1 and P2 / T2 which leads to min operable Cv...
Think there is an error in that writeup - the inner glass liner of 72mm dia is not 1000mm height. It is the outer 90mm glass liner, which forms the base of the cylindrical insulation, which is 1000mm. Height of the 72mm inner liner is not stated, but is shown to be much less than 1000mm looking...
This document may be useful as a checklist
https://www.eiga.eu/uploads/documents/DOC211.pdf
This std also recommends a min design pressure of 40barg (class 300 ) for the vent pipe to withstand detonation, and this would include the PSV also. Note it doesnt suggest the use of this toroidal...
Valves installed at the bottom of the suction pipe for pumps are not a good idea - they tend to bung up with debris/ corrosion products over time, and the valve will not close. Preferred orientation is vertical downward movement to close.
You may most likely have to purge this PSV exit line with N2 to prevent flashback / detonation for this highly flammable H2. Purging this line with N2 is much preferred to installing a flame arrestor / detonation arrestor which is often prone to blockage. N2 flowrate should enable a line...
