Recent content by skoutso

Its perfectly normal. Your system obeys the hydraulic balance law. The available pressure balances exactly the friction losses including the pressure drop at outlets. Friction losses are a function of flow. The flow and pressure at the outlets obey the following formula Flow = k *...

Thanks again BigInch. I'm not running acid pipelines either. That's why I'm looking for best practices and BATs. I would not just rely on intuition and experience alone when it comes to safety.

Many thanks donf.

Hi BigInch, I'm a petroleum guy too, and I've built quite a few oil and gas pipelines with ANSI and other oil standars/practices. The "specific issues" I'm trying to get a reply are: 1. Should the PL be burried or installed aboveground (for better inspection etc.)? 2. What kind of leak...

Hi you all, I'm currently involved in the design of a 5 km 6" pipeline that transports 98-99% wt. sulfuric acid. I'm interesting to know what codes/standards are applicable to the design of such a system and what are the best practices to follow for specific issues related to operation...

Thanks for your info BigInch. 1. What's the meaning of "D PUMPSTRT F(T) 5"? 2. RPM are in thousands?

Surge analysis (water hammer) of liquid pumping systems requires knowledge of pump startup and stop time. In old existing systems such information is not generally available from pump manufacturer. I wonder if there is some rule of thumb for quick estimation of those parameters for centrifugal...

SeanB, I agree. I always use two of them.

Thank you all. EGT01. I refer to API-598 that defines the leakage rates for metal-to-metal seated "healthy" check valves. I'll try to get a copy of the 7th RP-521 Ed. Thanks for the info. SeanB-Latexman. Check valves by construction "fail" in the closed position. "Fail" condition refers in...

Your calculation for the pressure rise is correct. But you need a TSV only if the line can be shut-in. You can get rid of the TSV by carefully evaluating the chances of blocking-in the line. If the line is not isolated there is no need for TSV. If the line operates constinuously and it is...

Hi you all. Currently there is a check valve in our plant that separates a low (600#) and a high pressure (900#) system. The LP side must be protected for check valve leakage, failure to close etc. The API leakage rates (for valve rating purposes) are too low and to my consideration do not...

chemieingineour The total hold-up is the sum of the two hold-up times. Hold-up times provided refer to an unbuffled bottom.

Hi bloem. It sounds like a “vapor binding” of “film boiling” problem. As the steam flow increases, the duty increases as does the heat flux up to a point (11 tph steam) that a film of vapor is formed on the outer surface of the tubes. This film reduces heat transfer and the steam flow into...

Aerodynamic and hydrodynamic noise depends on the mass flow. The higher is the quantity of flashed steam, the greater is the velocity at vena contracta, the higher is the resulting noise. Try intial slow and gradual depressuring through an 1" globe valve. If the condesate goes to the boiler...

chemieigineur The RVP specification is customary in condensate stabilizers. Follow the 25362 lead for the design of such systems. The reboiler duty is fixed for a certain separation. In your case assume that the RVP spec stands for the bottom tray liquid. The bottoms product will be of lower...