PUMPS for Process Industries Ranjeet Kumar M.Tech - Chemical
Equation of Energy A pump converts Electrical energy to Pressure Energy via Kinetic Energy. Electric energy K.E. K.E Pressure Energy Impeller Rotating Part Volute Static Part
A pump converts Electrical energy to Pressure Energy via Kinetic Energy.
Electric energy K.E.
K.E Pressure Energy
Types of Pumps Centrifugal - Impeller & Volute Reciprocating - Piston / Plunger Rotary - Screw, Gear, Lobe, Progressive Cavity, Sliding Vane Vertical - Peristaltic - Series of rollers to push through tubing
Centrifugal - Impeller & Volute
Reciprocating - Piston / Plunger
Rotary - Screw, Gear, Lobe, Progressive Cavity, Sliding Vane
Vertical -
Peristaltic - Series of rollers to push through tubing
Basis for selection of Pump Capacity – No. of pumps in parallel Total Head – No. of stages Physical, Chemical properties of Liquids Viscosity @ Frictional Loss @ Power Required Corrosive Fluid @ MOC Site conditions Source of Power >>>Capacity & Head required are most important selection criteria and define size of the pump.
Capacity – No. of pumps in parallel
Total Head – No. of stages
Physical, Chemical properties of Liquids
Viscosity @ Frictional Loss @ Power Required
Corrosive Fluid @ MOC
Site conditions
Source of Power
Capacity Volume of liquid to be pumped in unit time May vary as per Max, Min & Normal requirement – design should be for Max capacity. Its function of Impeller size and rotational speed for Centrifugal pump Q = V * A : V = ω * r
Volume of liquid to be pumped in unit time
May vary as per Max, Min & Normal requirement
– design should be for Max capacity.
Its function of Impeller size and rotational speed for Centrifugal pump
Q = V * A : V = ω * r
Centrifugal Pump Design Problem Inability to deliver the desired flow & head Seal problems (leakages, loss of flushing, cooling, quenching system, etc) Pump & Motor bearings related problems (loss of lubrication, cooling, contamination of oil, abnormal noise, etc) Leakages from pump casing, very high noise & vibration levels. Benefits of Centrifugal Pumps – low cost, easy maintenance, wide selection, & simple design.
Inability to deliver the desired flow & head
Seal problems (leakages, loss of flushing, cooling, quenching system, etc)
Pump & Motor bearings related problems (loss of lubrication, cooling, contamination of oil, abnormal noise, etc)
Leakages from pump casing, very high noise & vibration levels.
Head of Pump Total Head = P discharge – P suction Normal head test by vendor was done for water at 20°C. Advantages of using Head--
Total Head = P discharge – P suction
Normal head test by vendor was done for water at 20°C.
Advantages of using Head--
Physical Properties Consideration Specific Gravity 1) Increases Power consumed directly. 2) Max suction lift inversely. Viscosity Pump efficiency decrease directly so Power required directly Open or semi open impeller are better for highly viscose liquid. Volatile liquid at boiling points require high NPSH. Abrasive property of liquid or solid entrainment causes erosion and need specific MOC. Corrosive liquid require specific MOC.
Specific Gravity
1) Increases Power consumed directly.
2) Max suction lift inversely.
Viscosity Pump efficiency decrease directly so Power required directly
Open or semi open impeller are better for highly viscose liquid.
Volatile liquid at boiling points require high NPSH.
Abrasive property of liquid or solid entrainment causes erosion and need specific MOC.
Corrosive liquid require specific MOC.
Solid content Centrifugal pump operation is most difficult when liquid handled contains solid particles. Special attention required for selecting a centrifugal pump Open Impeller for solids > 2% Large cross section in Impeller & Volute Min No. of Vanes Inspection holes in tha casing & suction passage Abrasion resistant MOC Smooth corners & edges in lines Stuffing boxes sealed with clear fluid
Centrifugal pump operation is most difficult when liquid handled contains solid particles.
Special attention required for selecting a centrifugal pump
Open Impeller for solids > 2%
Large cross section in Impeller & Volute
Min No. of Vanes
Inspection holes in tha casing & suction passage
Abrasion resistant MOC
Smooth corners & edges in lines
Stuffing boxes sealed with clear fluid
Fig – Types of Impeller
Temperature of liquid Direct Impact on physical properties of liquid & Vapor Pressure and MOC.
Temperature of liquid Direct Impact on physical properties of liquid & Vapor Pressure and MOC.
Site Conditions Altitude – P atm decreases with altitude & P atm has direct effect on NPSHa Gas Dust Hazard – if the surrounding atmosphere is hazardous/inflammable Flame proof & Dust proof MOC of Motor. Stand by unit for vital application.
Altitude – P atm decreases with altitude & P atm has direct effect on NPSHa
Gas Dust Hazard – if the surrounding atmosphere is hazardous/inflammable Flame proof & Dust proof MOC of Motor.
Stand by unit for vital application.
Selection of Pump – Capacity & Head < 200 cSt < 25 m Upto 1 m 3 /h Peristaltic > 2% < 25% < 600 cSt 10500 m < 300 m 3 /h Positive Displacement > 2% < 5% Max 1050 m < 350 m 3 /h Rotary < 2% Upto 20% < 200 cSt Upto 105 m Upto 7500 m 3 /h Centrifugal % Gas Solid Viscosity Head Capacity Type
Flow Rate Design Margins for rated/maximum capacity PFD indicates normal flow rate without any margin & the Maximum flow is Considered for sizing of the pump with margin 30% Waste Heat Boiler pump 25% Boiler Feed water pump 0% Recirculation pump 3-5% Large cooling water pump 0-5% Transfer pumps 0% Intermittent pumps 20-25% Reflux pumps 10% Continuous process pumps Margin Service
Margins for rated/maximum capacity
Minimum flow rate ???? Under development………….
Minimum flow rate ????
Under development………….
Static Head Pump centre line as datum for Hydraulic calculation Pump centre Line from ground (estimated) Minimum level in Suction & Maximum level in Discharge tank. 1.0 Above 200 0.9 100 – 200 0.7 0 – 100 Pump centre line above ground Flow Rate (m 3 /h)
Pump centre line as datum for Hydraulic calculation
Pump centre Line from ground (estimated)
Minimum level in Suction & Maximum level in Discharge tank.
Line Pressure Drop ? Under development
Under development
Pressure Drop for Control Valve The following criteria can be used for sizing the control valve 15~25% of the variable system drop is typically allowed. On recycle and reflux pumps allow 1/3 of the variable system pressure with minimum of 0.7 bar. For liquid system 0.7 bar For system with large variable pressure drop ( >10 bar) ~15% of the variable pressure drop exclusive of control valve
The following criteria can be used for sizing the control valve
15~25% of the variable system drop is typically allowed.
On recycle and reflux pumps allow 1/3 of the variable system pressure with minimum of 0.7 bar.
For liquid system 0.7 bar
For system with large variable pressure drop ( >10 bar) ~15% of the variable pressure drop exclusive of control valve
Pressure Drop for Devices 0 Ultrasonic & electromagnetic Flow Meter 0.2 – 0.4 Corilolis Flow Meter 0.2 – 0.4 Vortex 0.02 – 0.05 Venturi Flow Meter 0.25 Orifice Flow meter 0.07 bar (continuous strainer) Y, T or Bucket type Strainer 1.0 bar Air cooler 0.35 – 0.5 bar per shell 0.7 bar per pass in tube side Shell & Tube type Heat Exchanger Press Drop (in bar) Devices in Flow Line
NPSH NPSHA = Suction Pressure – Vapor Pressure NPSHA should be 2 – 3 ft more than NPSHR. It is the pressure enough to prevent formation of vapor bubbles due to vaporization or release of dissolved gases in the Impeller. Pressure increases along the impeller on collapse of vapors – Cavitation. Cavitation – Noise, Vibration, Drop in performance curve, high wear & tear loss.
NPSHA = Suction Pressure – Vapor Pressure
NPSHA should be 2 – 3 ft more than NPSHR.
It is the pressure enough to prevent formation of vapor bubbles due to vaporization or release of dissolved gases in the Impeller.
Pressure increases along the impeller on collapse of vapors – Cavitation.
Cavitation – Noise, Vibration, Drop in performance curve, high wear & tear loss.
NPSHA optimization NPSHA can be increased by – Raise the liquid level Lower the pump Reduce the friction losses in the suction line Use a booster pump Sub cool the liquid NPSHR can be reduced by – Slower speed Double-suction impeller Large impeller area Oversize pump Inducers ahead of conventional pump at suction side Several smaller pumps NPSHR Rotary < NPSHR Centrifuge < NPSHR Reciprocating
NPSHA can be increased by –
Raise the liquid level
Lower the pump
Reduce the friction losses in the suction line
Use a booster pump
Sub cool the liquid
NPSHR can be reduced by –
Slower speed
Double-suction impeller
Large impeller area
Oversize pump
Inducers ahead of conventional pump at suction side
Several smaller pumps
Efficiency Efficiency = WHP/BHP Overall efficiency reflects hydraulic, leakage & mechanical losses of pump. η centrifugal < η reciprocating < η rotary (50 – 80%) (50 – 90%) (70 – 90%)
Efficiency = WHP/BHP
Overall efficiency reflects hydraulic, leakage & mechanical losses of pump.
η centrifugal < η reciprocating < η rotary
(50 – 80%) (50 – 90%) (70 – 90%)
Seals, pumps curves Under Development……..
Under Development……..
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