Unless I had a very, very good reason I use the design temperature. Why? Because that is the temperature that the system can operate to so my materials in turn should be good for those materials.
Lots of the pipelines in Saudi Arabia were constructed like that. I thought there was a specific term but I can't remember it (it's driving me nuts). All I come up with are berms but I don't think that is correct.
My experience is that there is no standard way how the instrumentation engineer or client wants these shown. Yes, I know ISA likely defines something but the individuals involved all seem to have their own preferences.
As a process engineer, I would just draw two dashed lines from the LIC...
I don't have any experience with grease calculations and a quick look suggests my concern that this material is not a newtonian fluid is correct. Not an area that I have experience in.
1/4" by 5" = 0.13 ft/sec at 0.5 gpm and it's far slower in the main cylinder...
< Unfortunately I do not have the differential head curve but I do have pressure ratio curve which I think will correspond to the head curve. If I understand you correctly you are indirectly saying that the pressure ratio curve is also valid for the increased suction pressure, not just the...
I'm having a hard time following the information. For a given flow, the NPSHR from the pump curve is in feet of liquid and it's the same feet of liquid be it feet of of ethylene or feet of propane or feet of water.
So, assuming with ethylene you need 5.2 ft of NPSHR at 2160 gpm, you need 5.2...
I've seen that done. Strainers for example can be purchased with a code stamp (have to consider fire at a minimum IMO) or non-code in which case most of the clients I've dealt with are willing to treat it as part of the piping and isn't protected against fire.
ASME Section 8, Div 1 has a good...
< how can there be any flow at all in the blocked outlet case? >
The flow goes through the PSV to avoid over-pressuring the system.
Look at the flow curve for the compressor. Calculate the head required to compress the inlet gas from its inlet pressure to the relieving pressure. Use the...
It's a matter of NPSHA versus NPSHR. NPSHR for most centrigal pumps increase with flow and past the BEP, significantly. A fully open discharge valve gives you the maximum flow if there no type of flow control device on the pump such as variable speed or a discharge control valve. So max flow...
Your equation is correct. The issue is what pressure drop do you use for the strainer? Do you use it as an equivalent length of piping per the vendor's charts which is when the strainer is clean? Or do you want to assume a fixed dP representing the pressure drop in a dirty state? If you are...
" whay we say this point in to isulation....isulation dont have any flange>? "
< i talk about insolation joint whith material api 5l grade b and class 600# >
I don't know what you are referring to. Are you talking about an electrical insulation flange? kit?
An approach I've seen used is the errosional equation from API-14E, 100 divided by the square root of the density which for most oils gives a maximum velocity in the mid teens (ft/sec). For short term operation, you can use a value 25% higher.
If it's a clean fluid and you aren't close to the...
What are the units associated with the 263 capacity? I assume it's L/sec at normal conditions.
During the draw down time (240.7 sec), the air used is 157.4 L/sec * 240.7 sec = 37886 L
This is supplied by the decrease in pressure in the receiver from 825 kPa to 700 kPa or a dP = 125 kPa. That...
api 5l grade b is the material as previously said, it's carbon steel.
600# refers to the flange class, look for a copy of B16.5. The class sets the maximum pressure that flange can withstand for a given material of construction and temperature.
What do you mean by "fail"?
If the pump can not overpressure the piping and would basically "stall", then I would accept a calculation note. If by fail you mean a loss of containment due to failure of the pump, then I would want a relief valve sized to prevent that.
< I have seen and read posts that say rule of thumb is to install a thermal relief valve for every 500 liters of liquid >
That makes no sense. I've seen some guidelines about installing thermal relief valves if a section of piping that can be blocked in is greater than a certain distance but...
You might want to check the latest edition, your copy is pretty old.
< it is stated that the minimum relief valve size for 1000 gpm is 4 inch >
The 4"is the body size, I would assume the inlet flange but I haven't looked in the NPFA 20. If there isn't a sizing method in NFPA 20, then I would...
