Pipe stress analyses can be fairly intensive and often requires specialized software.
I'd start with defining your system:
1) What fluid are you pumping?
2) What is your suction pressure? What is your desired pressure at the end of your new pipeline? From these, you can define your total...
chemebabak, thanks for your reply. Now that your example is working with a bubble-point fluid, the resulting NPSHA (-2 ft) is in-line with what I was expecting. Unfortunately, "higher safety margins" usually result in "more $$$$," which is why a 3 ft NPSH margin hasn't been feasible in the...
The problem with chemebabak's response to my question is that water is not a bubble point fluid at 60 psig and 300 deg F. My analysis was for bubble point fluids. As I'm typically working with NGLs and even LNGs, I'm often working with bubble point fluids.
All I'm saying is that putting your...
I agree with chemebabak - the bottom tangent line is what I'd recommend using. However, the 3' safety margin for NPSH seems excessive.
For example, a 6' high bottom tangent line would give you, at most, 6' of NPSHa for a bubble point fluid. Say the centerline of your pump is at 12" (fairly low...
