Atmospheric Pressure

 Atmospheric Pressure @ Sea Level

Absolute Pressure

The sum of the available atmospheric pressure and the gage pressure in the pumping system

Absolute Pressure (PSIA) = Gauge Pressure + Atmospheric Pressure

Absolute P. = 150 PSIG (Gauge P.) + 14.7 PSI (Atmospheric P.) = 164.7 PSIA

Vacuum

The full or partial elimination of Atmospheric Pressure

Atmospheric Pressure on the Moon = 0 = Full Vacuum

1 Inch Hg Vacuum = 1.13 Ft of Water

Specific Gravity

Specific Gravity is the ratio of the weight of anything to the weight of water.

Specific Gravity of HCl = (Weight of HCl)/(Weight of Water) = (10.0)/(8.34) = 1.2

Pressure and Liquid Height Relationship (Head)

1 PSI = 2.31 Ft of Water

Pressure, Liquid Height, & Specific Gravity Relationship

Pressure (PSI) = Head (FT) x Specific Gravity (SG) / 2.31

Example - Water - 231Ft x 1.0 / 2.31 = 100 PSI

Example - HCL - 231 Ft x 1.2 / 2.31 = 120 PSI

Example - Gas - 231 Ft x .80 / 2.31 = 80 PSI

Vapor Pressure

The pressure pushing against atmospheric pressure on liquids at elevated temperatures.

A Suction Head exists when the liquid is taken from an open to atmosphere tank where the liquid level is above the centerline of the pump suction, commonly known as a Flooded Suction.

Total Dynamic Head (TDH) = Elevation(ft) + Friction(ft)

Centrifugal Pump Components

The two main components of a centrifugal pump are the impeller and the volute. The impeller produces liquid velocity and the volute forces the liquid to discharge from the pump converting velocity to pressure. This is accomplished by offsetting the impeller in the volute and by maintaining a close clearance between the impeller and the volute at the cut-water. Please note the impeller rotation. A centrifugal pump impeller slings the liquid out of the volute. It does not cup the liquid.

Pump Performance Curve

A Pump Performance Curve is produced by a pump manufacturer from actual tests performed and shows the relationship between Flow and Total Dynamic Head, the Efficiency, the NPSH Required, and the BHP Required.

Lower Flow = Lower Horsepower                 Higher Flow = Higher Horsepower

Based on Water SG 1.0

Capacity

A Centrifugal Pump is a variable displacement pump. The actual flow rate achieved is directly dependent on the Total Dynamic Head it must work against.

The flow capacity of a centrifugal pump also depends on three (3) other factors:

1        Pump Design

2        Impeller Diameter

3       Pump Speed

Affinity Laws

The performance of a centrifugal pump is affected by a change in speed or impeller diameter.

Q = Capacity (GPM)           D = Impeller Diameter                      N= Speed(RPM)

H = Total Dynamic Head(Feet)                                BHP = Brake Horsepower

The affinity law for a centrifugal pump with the impeller diameter held constant and the speed changed:

Flow:   Q1 / Q2 = N1 / N2

Example:   100 / Q2 = 1750/3500      Q2 = 200 GPM

Head:  H1/H2 = (N1) x (N1) / (N2) x (N2)

Example:    100 /H2 = 1750 x 1750 / 3500 x 3500    H2 = 400 Ft

Horsepower (BHP):

BHP1 / BHP2 = (N1) x (N1) x (N1) / (N2) x (N2) x (N2)

Example:   5/BHP2 = 1750 x 1750 x 1750 / 3500 x 3500 x 3500     BHP2 = 40

The affinity law for a centrifugal pump with the speed held constant and the impeller diameter changed:

Flow:   Q1 / Q2 = D1 / D2

Example: 100 / Q2 = 8/6        Q2 = 75 GPM

Head:  H1/H2 = (D1) x (D1) / (D2) x (D2)

Example: 100 /H2 = 8 x 8 / 6 x 6       H2 = 56.25 Ft

Horsepower (BHP):

BHP1 / BHP2 = (D1) x (D1) x (D1) / (D2) x (D2) x (D2)

Example: 5/BHP2 = 8 x 8 x 8 / 6 x 6 x 6       BHP2 = 2.1

Brake Horsepower

BHP = Flow(GPM) X TDH(FT) x SG /3960xEFFICIENCY(%)

Example: BHP = (100 GPM) x (95 Ft) x (1.0) / 3960 x .6                BHP = 4.0

Flooded Suction Application

Total Suction Head = Static - Friction

Total Discharge Head = Static + Friction

Suction Lift Application

TDH = Total Discharge Head + Total Suction Lift

Total Suction Lift= Static + Friction

Total Discharge Head = Static + Friction

To Calculate a System Head Curve several points must be chosen to calculate friction losses on both the suction and discharge sides of the pump at various flow rates. The static suction head/lift and the static discharge head remain constant.

Net Positive Suction Head Required (NPSHR)

The net positive suction head required is a function of the pump design at the operating point on the pump performance curve.

Net Positive Suction Head Available (NPSHA)

The net positive suction head available is a function of the pump suction system.

The Net Positive Suction Head is the absolute total suction head in feet.

The NPSH available in a flooded suction system is:

Atmospheric Pressure (-) Vapor Pressure (+) Liquid Height (-) Friction in the Suction Line.

The NPSH available in a suction lift system is:

Atmospheric Pressure (-) Vapor Pressure (-) Liquid Ht. (-) Friction in the Suction Line.

If the NPSHA < NPSHR the Pump will cavitate

Cavitation

Cavitation may occur in two different forms:

Suction Cavitation

Suction Cavitation occurs when the pump suction is under a low pressure/high vacuum condition where the liquid turns into a vapor at the eye of the pump impeller. This vapor is carried over to the discharge side of the pump where it no longer sees vacuum and is compressed back into a liquid by the discharge pressure. This imploding action occurs violently and attacks the face of the impeller. An impeller that has been operating under a suction cavitation condition has large chunks of material removed from its face causing premature failure of the pump.

Discharge Cavitation

Discharge Cavitation occurs when the pump discharge is extremely high. It normally occurs in a pump that is running at less than 10% of its best efficiency point. The high discharge pressure causes the majority of the fluid to circulate inside the pump instead of being allowed to flow out the discharge. As the liquid flows around the impeller it must pass through the small clearance between the impeller and the pump cutwater at extremely high velocity. This velocity causes a vacuum to develop at the cutwater similar to what occurs in a venturi and turns the liquid into a vapor. A pump that has been operating under these conditions shows premature wear of the impeller vane tips and the pump cutwater. In addition due to the high pressure condition premature failure of the pump mechanical seal and bearings can be expected and under extreme conditions will break the impeller shaft.

Suction Cavitation & Discharge Cavitation are extremely damaging to pump components.