Does anyone have a general rule to specify control valves either "flow to open" or "flow to close"?
I have seen control valve specs requiring both "flow to close" and fail "closed" or "flow to open" and fail "closed".
Is there a major advantage to specify one or the other?
Thanks for all your...
Is there a general rule to determine what is the relief temperature for blocked outlet, thermal expansion, loss of liquid seal, thermal expansion at suction of pump, pump discharge blocked in, etc.?
Is it safe to use Relief temperature = (oper. temp./op. press.) x relief pressure for these...
I have an upstream vessel (A) that has a letdown valve at the bottom outlet which connects to another downstream vessel (B). I have to size a PSV for the downstream vessel (B) for loss of liquid seal from the upstream vessel (A).
How do I determine the required flow capacity for the PSV...
I am trying to size some PSV's that have properties (hydrocarbons) with MW < 40 and Relief Pressure above 2000 psig. The API curve has a minimum of MW = 40 and a max pressure at 1000 psig.
For Fire case, how do I obtain the Latent Heat of Vaporization and Relief Temperature at the conditions...
I am trying to size some PSV's that have properties (hydrocarbons) with MW < 40 and Relief Pressure above 2000 psig. The API curve has a minimum of MW = 40 and a max pressure at 1000 psig.
For Fire case, how do I obtain the Latent Heat of Vaporization and Relief Temperature at the conditions...
