# TUTORIAL. NPSHA for those who hate that stuffy word. by Jacques Chaurette p. eng. copyright 2006

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1 TUTORIAL NPSHA for those who hate that stuffy word by Jacques Chaurette p. eng. copyright 2006

3 page.3 Figure 1 Variation of atmospheric pressure with elevation. To measure suction pressure two units are typically used, the psia or the inch of mercury. Pressure gauges can be purchased that have scales with either one of these two units in North America. The following figure shows how these two scales can be used.

4 page.4 Figure 2 Relationship between pressure measurements in psig, psia and inch of mercury. Most pumps can operate with a suction pressure that is below atmospheric pressure. A pressure that is below atmospheric pressure is referred to as a vacuum. That is why a value of 20 feet for NPSHA can be quite acceptable. This is also how it is possible for a normal centrifugal pump to lift fluid from an elevation that is below the suction. Figure 3 A pump can operate with low pressure or vacuum at the suction. A pump that operates in this fashion will require a foot valve to keep the liquid in the suction pipe to avoid having to re-prime the pump when it is stopped.

5 page.5 We can calculate or we can measure NPSHA, let s start with measuring NPSHA. The main measurement we need is the pressure close to the pump suction. But first a digression on what the pressure measurement we take will mean. What happens to the flow and pressure within the pump past the point of measurement. Figure 4 shows that the pressure drops considerably as the fluid enters the eye of the pump. This happens for two main reasons: the velocity as the fluid approaches the eye increases which decreases pressure also friction and turbulence further decreases pressure. The pressure can be low enough that the liquid will start to boil at this low pressure. What do you mean the liquid will boil at low pressure? Figure 4 Pressure profile at the pump entrance. There are two ways to boil a liquid. One way is to increase the temperature while keeping the pressure constant until the temperature is high enough to produce vapor bubbles. In Figure 5 this is what happens if you take one point in the liquid phase and you move horizontally (that is at constant pressure) by increasing the temperature. Eventually you hit the vaporization line of the particular fluid and the fluid starts to boil or produce vapor bubbles. We do the same thing every day when we boil water in a pot.

6 page.6 Figure 5 Vapor pressure vs. temperature. The other way to boil a liquid is to lower the pressure. If you keep the temperature constant and lower the pressure the liquid will also boil. In Figure 5 this is what happens if you take one point in the liquid phase and you move vertically (that is at constant temperature) by decreasing the pressure. Again you hit the vaporization line of the particular fluid and the fluid starts to boil or produce vapor bubbles. If the pot were covered and you had a source of vacuum (see Figure 6) by lowering the pressure in the pot you would be able to make the water boil at a lower temperature. When the pressure is 7.5 psia or ( = 7.2) or 7.2 psi less than the atmospheric pressure the water will boil at a temperature of 180 F and when the pressure is 1.5 psia the water will boil at 120 F. This is what happens at the pump suction when the pressure is low enough to make the fluid boil or vaporize. It is not unusual for industrial processes to operate at temperatures that are close or higher than 120 F. Therefore if the temperature is high and the pressure drops as the fluid enters the pump, it will be easier to produce cavitation because the pressure drop produced by the pump will have to be smaller to match a higher vapor pressure. If cavitation is occurring or suspected, two possible solutions are: to increase the pressure at the pump inlet or decrease the fluid temperature. Figure 6 Making a liquid boil under low pressure.

7 page.7 The pressure at which the liquid vaporizes is known as the vapor pressure and is always specified for a given temperature. If the temperature changes, the vapor pressure changes. Why is vapor pressure an issue? If the pressure in the pump eye drops below the vapor pressure, cavitation will occur. Cavitation begins as the formation of vapor bubbles at the impeller eye due to low pressure. The bubbles form at the position of lowest pressure at the pump inlet (see Figure 4), which is just prior to the fluid being acted upon by the impeller vanes, they are then rapidly compressed. The compression of the vapor bubbles produces a small shock wave that impacts the impeller surface and pits away at the metal creating over time large eroded areas and subsequent failure. Figure 7 Vapor bubble implosion. The sound of cavitation is very characteristic and resembles the sound of gravel in a concrete mixer. You can hear this sound at this web address

8 page.8 Figure 8 Impeller damaged by cavitation. The formula for NPSHA based on a pressure measurement at the pump suction is: NPSH p ft fluid absol. ) = 2.31 ( psi) SG 2 v ( ft / s) S + + z 2g( ft / s ) GS avail ( 2 GS ( p ( psia) p A ( ft) SG va ( psia)) [1] Figure 10 Typical pump suction pressure measurement for NPSHA.

9 page.9 where p GS : pressure in psig at the pump suction (this pressure can be negative z GS : is the difference between the gauge height and the pump suction, this is necessary to correct for an erroneous reading due to the gauge height. v S : the velocity of the liquid at the suction in ft/s p A : atmospheric pressure in the local environment p va : vapor pressure of the liquid at the operating temperature. g: the acceleration due to gravity equal to ft/s 2 SG: specific gravity of the liquid. If we are designing a system then it is not possible to measure the pump suction pressure and therefore we have to calculate it. The pressure head at the pump suction is given by: where H S : z : H F : vs HS ( ft fluid ) = HF + 2g 2 [2] pressure head corresponding to the pressure measurement p GS the height between the free surface of the suction tank and the pump suction centerline. the friction head loss in the suction line. z H S is related to P GS by the static head relationship seen in the pump tutorial. H 2.31 ( ft fluid ) = p GS ( psia ) SG S [3] If we replace the value of p GS in equation [3] into equation [1] and considering that there is no correction for pressure gauge height required then the term z GS disappears, we obtain: NPSH avail ( ft fluid absol. ) = H F ( p ( psia) p A ( ft) + z( ft) SG va ( psia)) [4]

10 page.10 Figure 11 Typical pump suction variables. Therefore to calculate NPSHA, we use equation[1] when we have an existing system and we can measure the pressure at the pump suction. And we use equation [4] when we are designing a pump system. Let s try an example. The pump system used in the pump tutorial is a good start. We will use equation [4] to calculate the NPSHA. The value of z which is the suction static head is 15 feet. In the pump tutorial we calculated the friction loss in the suction to be 3.1 feet. The velocity head or term v s 2 /2g is often quite small, of the order of 1 foot or less and this is no exception so we will therefore neglect it. The atmospheric pressure is 14.7 psia. The vapor pressure for water at 60F is 0.5 psia. Values for vapor pressure of other fluids at various temperatures is available in the pump glossary. The specific gravity of water is 1.0. Figure 12 Typical domestic water system.

11 page.11 The value of NPSHA is then: NPSH avail ( ) ( ft fluid absol. ) = = [4] This value is a bit on the low side and I would normally check the pump curves to ensure that I have sufficient NPSHA at the required flow rate. However in this case, we know we are using a jet pump which is specifically designed for this type of application so I wouldn t worry about it.

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