Q. I have been told that centrifugal pump impellers may still cavitate when operating with NPSH Available greater than NPSH Required. Is this true? If so, why do pump suppliers show NPSHR values when they know that cavitation may occur?
The standard procedure for the determination of NPSHR has been used for many years and was formally approved as an American National Standard in 1994 with the designation ANSI/HI 1.6 Centrifugal Pump Tests.
To determine the values of NPSHR, the pump is run at constant rate of flow and constant speed with the suction condition varied to produce cavitation. Plots of head shall be made for various NPSH values at a series of constant rates of flow (see Figure 1.122).
Figure 1.122. NPSH test with rate of flow held constant.
As NPSHA is reduced, a point is reached where the curves break away from a straight-line trend, indicating a condition under which the performance of the pump may be impaired. The 3 percent drop in head is the standard to determine NPSHR. Reference ANSI/HI 1.6 for more detail on this test
Although pumps may be cavitating when operating with NPSHA values greater than NPSHR, the impeller is not necessarily damaged. Actual damage to the impeller also depends on a number of other factors as follows:
- Liquid thermodynamic properties. As the amount of vapor bubbles increase under operating conditions, they do more damage when they collapse. This is also related to the liquid vapor pressure. For example, cold water does more damage that hot water, while hydrocarbons do less damage than hot or cold water.
- Corrosive liquids. Intergranular corrosion and crevice corrosion not only cause direct damage, but also weaken the structure and make it more susceptible to pounding from collapsing vapor bubbles.
- Impeller material. Steel, cast iron and brass are more susceptible to cavitation damage while stainless steel, titanium, and aluminum bronze are more resistant.
- Higher speed. More energy concentrated in smaller volumes results in more metal removal from higher speed impellers.
- Operation away from best efficiency rate of flow. Mismatch between the actual flow angles and the impeller geometry also aggravates cavitation damage.
- High suction specific speed design. Special impeller designs for low NPSHR values will suffer more due to larger impeller eye diameters and some mismatch with the flow which is necessary to achieve low NPSHR values.
- Duty cycle. Obviously, the longer a pump is operated, the more it may be damaged by cavitation.
Q. What is pump critical speed and how is it determined? I understand that operation at critical speed could damage the pump.
A. Critical speed is the natural frequency of vibration of a pump. All centrifugal and vertical turbine pumps have rotors and structures that can vibrate in response to excitation forces. When the frequency of the excitation forces is close to the natural frequencies of the structures, resonance can occur and excessive and damaging vibration levels can be reached. These natural frequencies of vibration usually occur in one or more of the following modes:
- Rotor lateral vibration
- Rotor torsional vibration
- Structure lateral vibration
Computational methods using application-specific programs or finite element analysis (FEA) programs may be required to produce accurate results. Even so, the actual distribution of the structure mass and stiffness can be difficult to determine, affecting the accuracy of the calculation.