The issue of design pressure
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I am currently designing a liquefied hydrocarbon storage area. The liquefied hydrocarbon is unloaded from tank trucks, which are under a pressure of approximately 0.4 MPa. The discharge pump selected is a dedicated pump for liquefied hydrocarbons (a belt pump), with a pressure difference of 0.5 MPA. The liquefied hydrocarbon in question is isobutylene. May I ask how the design pressure for the pump’s outlet pipeline should be determined? Do we also need to take into account the vaporization pressure of the liquefied hydrocarbon? Liquefied hydrocarbon storage tanks and tank trucks are connected by gas piping.
The design pressure is 1.25 times the working pressure; that’s usually the case. You can check this
The design pressure can be taken as 1.25 times the operating pressure; if a higher safety factor is desired, a larger multiple can be used
Regarding the selection of design pressure values, the various codes are generally similar, but there are also differences. Generally, the design pressure must be at least as high as the maximum operating pressure that may occur during operation. :lol
The design pressure can be calculated as at least 1.1 times higher than the maximum pressure that the pipeline might experience; this is still a rather conservative approach
The design pressure should be set at 1.1 times the operating pressure; if a higher safety factor is desired, a larger multiple can be used
According to the specification requirements, when designing projects for liquefied hydrocarbon products, the minimum design pressure should be no less than 2.5 MPa; therefore, the design pressure of the pump outlet pipeline should be 2.5 MPa.
The design pressure must not be lower than the maximum operating pressure that may occur. That’s what the regulations state.
The design pressure is 1.25 times the operating pressure
Which specification exactly mentions this point? I’ve seen this claim, but I’ve never been able to find its source.