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I can't see any reason why this would not work. I would have a self regulating PCV on the upstream which would open when the header pressure falls and another downstream to open when header pressure rises. In my mind this arrangement (assuming sizing has been carried out correctly) would...

See if you can get hold of the Mad Dog Gas Release HIPO (28 Feb 2007) report. This will show you bursting discs can fail in reverse. This particular incident had almost catastrophic consequences.

Latexman - As most PSVs have an outlet larger than the inlet pipework, they could be thought of as a very crude converging-diverging nozzle. As hfgnick pointed out: "However since the pipe is an imperfect diverging nozzle there will be tremendous loss of energy due to internal fluid friction...

If we consider a PSV as a converging diverging nozzle with sonic velocity in the throat and the outlet pressure being lower than the throat pressure, is it possible to experience supersonic velocities in the outlet line? I.e. in the same way as a Laval Nozzle. This question has been bugging me...

I would consider LV1 failing open 100% and LV2 staying in normal position. If the backpressure of the flare line was less than the operating pressure of COL3 plus the losses in the inlet line and contol valve wouldn't all the gas flow though the PSV on COL2 anyway?

It well could be the control valves gives a constant pressure upstream of the RO. Thus, a constant flow will be maintained though the orifice assuming the downstream pressure is fixed. I’ve seen this arrangement before on purge gas supply lines, not that I think it’s a particularly good way of...

Hi all I’ve been asked by my company to research methods of predicting pressure drop for non Newtonian fluids (Bingham-Plastic Model in particular). I’ve found quite a lot of information on pressure drop in the laminar flow regime but as yet very little on turbulent flow. Can anyone give me a...

I’ve been following this thread with some interest. The equations for pressure drop are all for the laminar flow regime. How is pressure drop calculated for turbulent flow??

I’ve just been asked the question if supersonic flow could occur at any point in the plant we are currently designing. I explained at no point the speed of fluid could exceed Mach 1 (chocked flow) unless flow passes though a convergent-divergent nozzle with sonic flow at the throat and the...

Thanks for all your answers. I'll run a few calc's later today

The “acid gas” stream mostly consists of the reject streams from Glycol and Amine units. This will be sent to a dedicated Acid Gas Flare. I’m interested in making a very rough estimate of the amount of fuel gas need to be blended into the stream without having to go to flare tip vendors.

Hi A post from the UK. I’ve been asked to calculate the amount of Fuel Gas that would nee to be added to an acid gas stream to create a flammable mixture. I have a full Hysys simulation to hand so physical properties are readily available. Any suggestions??

CJKruger is correct, the downstream equipment will be protected from over pressure by the downstream vessel PSV. When calculating the size of the PSV on the downstream vessel the amount of gas that can pass through the failed open valve must first be calculated (from the valve Cv). Then this...