Suggest you spend some time researching pump NPSHr, what, when, where,and why.
NPSHa is a fixed condition set by the installation, whereas NPSHr is set pump by design.

It is a capital mistake to theorise before one has data. Insensibly one begins to twist facts to suit theories, instead of theories to suit facts. (Sherlock Holmes - A Scandal in Bohemia.)

NPSHa is measured at the inlet flange to the pump. If the fluid is going to move from this point into the suction eye of the impeller, the pressure must drop lower. Flow only goes from higher pressure to lower pressure. The amount of pressure needed to move the fluid from the inlet flange to the impeller eye is dependent on the design and operating conditions of the pump. It depends on flow rate and pump speed. This is generally determined experimentally. If a higher flow rate is required, more pressure drop is required. NPSHr must be tested at different flow rates to generate an NPSHr curve for the individual pump.

NPSHr is not the point where cavitation starts. Research "Incipient Cavitation". In order to be measured and documented, NPSHr is the point where the cavitation is sufficient to reduce the pump developed head by 3% (for most pumps) or 1% (for some high energy pumps, or if specified by purchaser). In either case, if NPSHr = NPSHa then there is already a significant amount of cavitation occurring. Thus, a margin is required in order to reduce the amount of caviation to an acceptable level.

Johnny Pellin

Thank you I understand now. I had totally forgotten that there is some space between the inlet of the pump (where the gauge is) and the eye of the impeller, hence there is a pressure drop from the inlet to the impeller. So since we can't really measure the pressure directly at the impeller, we just have to test to see what inlet pressure initiates cavitation at the impeller; then that inlet pressure minus the vapor pressure is the NPSHr at that pump speed.

Cray.

Read what JJ is telling you.

NPSH is NOT cavitation point. It is simply the point at which differential pressure dec re ases by 3% because onset of cavitation is very difficult to measure but differential pressure is easy.

You could be spot on NPSHA = NPSHR and be busy cavitating like mad.

Always best to add at least 1m and 2 if you can

Remember - More details = better answers
Also: If you get a response it's polite to respond to it.

Ok I think I finally get it. NSPHr marks the point when the inlet pressure gets low enough relative to the vapor pressure to cause about a 3% decrease in pump TDH. Cavitation had started at something slightly higher than NPSHr. So basically, you want to stay above NPSHr by a reasonable amount; you don't want to see NPSHr as the lowest safe bound. The lowest safe bound is actually like 10% above NPSHr. Sorry I wasn't really listening, but I think I've got it straight now. Thanks for the help.

Thats basically it.

It's always interesting asking a vendor if they have a cavitation curve as well as an npsh curve.

Sometimes it is close sometimes further away depending on flow.

Remember - More details = better answers
Also: If you get a response it's polite to respond to it.

Hi, does any of you know of a tool that helps with NPSH calculation? I found this one, but it is only available in Spanish:
https://herramientasdeingenieros.com/calculadora-d...
Thanks!

Cray25,

It should be:

NPSHa ≥ NPSHr
Where,
NPSHA = Psuction – Psaturation

NPSHa comes from the system while NPSHr comes from the pump. Note that you are comparing the differences of two pressures not the saturation pressure and suction pressure.

Matt1309.

You really need to start your own thread and not hijack someone elses dead thread.

Mech eng - the thread ended 5 months ago....

Remember - More details = better answers
Also: If you get a response it's polite to respond to it.

LittleInch:

Thank you for letting me know that.
I didn't notice the date of the post itself and just replied since it was on top of the posts. I wonder why Matt1309 didn't create a new post. I will let the Admins decide on what to do with last few responses.

Sorry, my mistake! I really didn't mean to hijack somebody else's thread...
MechEng, thanks a lot for your answer

Pump NPSHr is not just dependent on pump speed and flow. A lesser known fact is that it is also related to the density of the fluid being pumped. Pump manufacturers publish standard NPSHr curves based on water, and many users tend to incorrectly use these for other fluids also. If you cannot get the manufacturer to give you NPSHr plots for your service fluid, see Perry Chem Engg Handbook 7th ed for approximate corrections.

i have prepared a formulated excel sheet for calculating the NPSHA. add the value on yellow marked box.

• https://files.engineering.com/getfile.aspx?folder=652d985a-474e-41ce-be81-9

NPSHA= Hstatic+ H atm + H velocity -H vapour pressure- Hfriction losses
As you see from the above equation that NPSHA is dependent on vapour pressure.
SUppose, the fluid is boiling the Hatm will be equal to H vapour pressure and both cancels out each other, as in case of boiler feed pump.
Hence BFP application the static head should be high and the velocity shall be more in order to acheive the the difference between NPSHA and NPSHR.
ALso note that in case of suction lift H static is negative.


Hope the above clarifies.

A well phrased question has answers in itself!!!