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Hi LittleInch, Thank you. We have considered the options suggested and ruled them out for various reasons as listed below. Lowering the pump - Creates a pocket where hydrocarbons/H2S can accumulate making it potentially unsafe Using a submersible/Can pump - These pumps are ruled out due to...

Hi, We are designing an atmospheric crude storage tank of 3000 m3 volume, 17 m dia with pumping facility. We have to provide NPSH for the crude export pumps ( centrifugal , 100 m3/hr, 50 bar g discharge pressure ) which pump crude out from the tank. We have two options to provide the NPSH...

I have reduced the time step to the least possible on my machine i.e 0.001 sec. However the peak surge pressure keeps going up. The event is the main pump trip initiated at 10 sec. The trend is attached for various time steps...

I generally go by the piping class as it is easier to specify and gives a conservative value, quickly. regards, Benoy

Hi, I have been modelling a pumping station ( Booster + Main pumps) and pipeline (68 km 10" long) for analysing the transient conditions like pump trips and shutdown valve closures using TLNET software (Pipelinestudio). I have observed that the peak surge pressure during any case is dependent...

Pikadoh, Liquid formation with drop in pressure can be good or bad based on the end use of the fluid. In the case of fuel gas to gas turbine, the liquid droplets in the fuel can cause improper combustion , uneven temperature profile in the combustion chamber leading to mechanical damages. For...

Hi ziptron, I did some quick calculations with the assumption that the tank can withstand a vacuum of 0.25 kPA which is the case for API 650 tanks generally. The vent line equivalent length was calculated considering two elbows and a metre of straight length. (assuming a goose neck vent)...

Hi, What are the typical design codes applicable for mechanical design of double pipe heat exchangers? Are they built to confirm to ASME Sec VIII? Thanks, Benoy