In real life the rupture disk should be fully open when the relief valve activates. If the disk partially opens and the differential is not great enough the safety valve may chatter. My recommendation is to set the rupture disk at 15-psig and decrease the safety valve setting to say 13-psig...
I am evaluating a Revamp project.It requires a 4"x P x 6" safety valve.
The inlet line loss is between 12% to 16% of set at actual valve capacity.
The Client says the next opportunity to increase inlet pipe size will be in the year 2030.
The outlet pipe friction slightly exceeds 50$ of set.
The...
I am looking at a turbine installed in the field.
The inlet flange is 250# ASA
The outlet flange is 125# ASA
It appears the inlet pressure rating is different than outlet.
I'm not clear how I should evaluate the turbine mechanical pressure limit
Most Turbine documents have inlet Design Pressure and Outlet design pressure.
I don't understand the need for an Outlet Design rating.
Is this an actual mechanical casing rating?
Is this a pressure at which turbine fails to deliver power?
Is this a pressure for bearing loads.
Given 120-psig...
I believe this standard comes from API 520
In flammable vapor service, the minimum exit velocity should be 100 ft/s (30 m/s) at 25% of the rated capacity of
the PR valve (i.e., calculated flow using 25% of the installed PR valve’s effective orifice area). For modulating type
POPRVs the minimum...
Most everyone is familiar with safety valve chatter due to excessive friction losses in inlet pipe.
But given a liquid filled system with long piping and the pressure source liquid near (but below) safety valve set,
Is it possible to have repeated activation due to hydraulic surge (not friction...
Can someone advise if there is an ASHRAE standard for sizing compressor discharge safety valve.
I am evaluating a R-134a compressor purchased in 1999.
The safety valve rated flow is sized for about 25% of compressor rated capacity.
I'm wondering if this is an ASHRAE standard.
My current client...
I'm looking at a set of PID's for a turbine driven pump.
The Client has no record files for either pump or turbine.
Using 150-psig steam and exhaust to atmosphere, is it reasonable to estimate 150-psig maximum possible pump discharge pressure?
I have a client that operates a rail car facility with 17 folding gangways.
Normally the gangways are operated using 80-psig nitrogen from header.
For nitrogen outages, the client wishes to use a small portable air compressor.
The vision is for the compressor and driver (gasoline) to be mounted...
I am a 30+ engineer and am a little embarrased to ask.
But how does one handle Q = U*A*LMTD for a Steam Heated Reboiler?
The main issue seem to be LMTD determination
The process side is a constant boiling temperature.
Neglecting steam superheat & steam subcooling, the steam is a constant...
I am currently working with a Client that needs two 2" V-notched gate valves.
The devices will be used in in Slurry service to maintain min flow at a centrifugal pump.
The required flow is betewwn 60-120 gpm. The process fluid is oil at 580-F and 220-psig.
I have two problems
1) What sizing...
I disagree that API-2000 is the correct sizing method.
The correlations were made years ago based on a sudden rain storm outside a hot tank. I believe the contents was hexane.
The tank is assumed to cool at 300F per hour.
API-2000 could apply if your water spray is outside the tank.
For inside...
Well, external Fire with internal Chemical reaction - in today's world a dynamic simulation is almost a requirement.
I used to normally calculate both steady state and unsteady state.
The unsteady state calc was used to only report time duration required for the external fire to activate the...
