Cent Pumps Presentation

Centrifugal Pumps Selection A technical presentation by

Jyoti Swarup Tripatra Engineering & Construction On

29th T:\Pumps\Cent Pumps presentation

April 2010 1

Centrifugal Pumps Selection Contents 1. 2. 3. 4. 5. 6. 7. 8.

Definitions & Classifications Performance Curve Affinity Laws Specific speed NPSHA, NPSHR and Cavitation Suction Energy Viscosity and multi-pump operation Selections & Example

Positive Displacement Pumps are "constant flow machines". Centrifugal Pumps are "constant head machines". 2 of 69

Selection – various types of pumps

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Types of pumps  

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Centrifugal Pumps - Use centrifugal force to push the fluid through the outlet. Metering Pumps - Bellows, diaphragm, peristaltic, piston, and syringe pumps that pull the fluid through the inlet valve into a chamber, close the inlet valve, and then push the fluid through the outlet valve. Positive Displacement Pumps - Bellows, doublediaphragm, gear, piston, progressing cavity, rotary lobe, rotary vane, and peristaltic pumps - fixed cavity that the fluid is pushed through by rollers, gears, or impeller. It leaves a void or vacuum which pulls in more fluid. 4 of 69

Centrifugal Pumps Most commonly used machine (next to electric motors) Consist of a set of rotating vanes, enclosed within a housing or casing, used to impart energy to a fluid through centrifugal force Two main parts: a rotating element which includes an impeller and a shaft, and a stationary element made up of a casing (volute or solid), stuffing box, and bearings. Classified by API Std 610-10th edition as Overhung OH1 to OH6 Between bearings BB1 to BB5 Vertically suspended VS1 to VS7 API Standard 610- Tenth edition 2004 (ISO 13709: 2003 identical) Centrifugal Pumps for petroleum, petrochemical and natural gas industries

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Characteristics of Centrifugal pump 

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Pumps offer high flow rates, low pressures, and pulseless flow at a low price—ideal for general transfer applications. Simple design means quick installation, low maintenance, and easy repair. Most centrifugal pumps must be gravity fed or utilized with a priming chamber; some are self-priming. Can control the flow rate by restricting the flow at the outlet with a nozzle or valve, (H vs Q is drooping) In smaller pumps, can restrict the outlet indefinitely without damaging the pump. Centrifugal pumps should not be run dry. 6 of 69

API Std 610, Oct 2004 (1/2) Centrifugal Pumps for Petroleum, Petrochemical and Natural Gas Industries - Tenth Edition; ISO 13709 Adoption Introduction .........................................................................................vi 1 Scope ...............................................................................................1

2 Normative references ...................................................................... 1 3 Terms and definitions ...................................................................... 4 4 Classification and designation .......................................................... 9 5 Basic design .................................................................................. 16

6 Accessories ................................................................................... 55 7 Inspection, testing, and preparation for shipment .......................... 64 8 Specific pump types ...................................................................... 71 9 Vendor's data ................................................................................ 84 Annexures Bibliography........................................................................................181 7 of 69

API Std 610, Oct 2004 (2/2) Centrifugal Pumps for Petroleum, Petrochemical and Natural Gas Industries - Tenth Edition; ISO 13709 Adoption Annex A (informative) Specific speed and suction-specific speed ............... 90 Annex B (normative) Cooling water and lubrication system schematics ...... 91

Annex C (normative) Hydraulic power recovery turbines ........................... 102 Annex D (normative) Standard baseplates .................................................106 Annex E (informative) Inspector's checklist .................................................108 Annex F (normative) Criteria for piping design ............................................110

Annex G (informative) Materials class selection guidance ..........................124 Annex H (normative) Materials and material specifications for pump parts..126 Annex I (normative) Lateral analysis ............................................................136 Annex J (normative) Determination of residual unbalance............................142 Annex K (normative) Seal chamber runout illustrations ................................148 Annex L (informative) Vendor drawing and data requirements .....................149 Annex M (informative) Test data summary....................................................158 Annex N (informative) Pump datasheets.......................................................162 8 of 69

Centrifugal Pumps

Overhung

Horizontal Flexibly coupled

Rigidly-coupled Close-coupled

Vertical in-line with bearing bracket Vertical in-line Vertical in-line High-speed integrally-geared

Foot-mounted OH1 Centre-line OH2 supported OH3 OH4 OH5 OH6

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FLOWSERVE Model ERPN Overhung, Single stage, Process pump per API 610 Centerline supported casing (OH2); Double Volute Renewable Wear ring for casing and impeller

IN-LINE FIRE PUMP OH4

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Centrifugal Pumps

Between Bearing

1- and 2- stage Multistage

Axially-split Radially-split Axially-split Radially-split

BB1 BB2 BB3 Single-casing BB4 Double-casing BB5

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DMX API 610 (BB3) 10th Edition, Between Bearing Axially Split Multistage, Double Volute, Opposed impeller

API 610 (BB1) Between Bearing Axially Split

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Centrifugal Pumps

Vertically Suspended

Vertically Suspended

Singlecasing Doublecasing

Discharge through column Separate discharge Diffuser Volute

Diffuser Volute Axial-flow Line-shaft Cantilever

VS1 VS2 VS3 VS4 VS5 VS6 VS7

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FLOWSERVE

FLOWSERVE

VPC (VTP-Can) Vertical Turbine, Double Casing Pump

QL, Vertical, wet pit

Open or Enclosed line shaft construction Option: Solid shaft or hollow shaft motor Pressure upto 150 bar Flow upto 160,000 m3/hr VS6

Enclosed line shaft construction Twin volute casing Double suction impeller Option: Solid shaft or hollow shaft motor Pressure upto 70 bar Column size 100 to 1200 mm VS2

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A CENTRIFUGAL PUMP ANIMATION •

This animation shows fluid particles (represented by gray balls) enter the eye of the impeller and after they turn 90 degrees.

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At this point they are at the entrance of the volume formed by two adjacent impeller vanes.

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The rapid rotation of the vanes displaces the fluid particles by moving them in a radial direction into the pump volute and are decelerated and pressurized.

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Check out the direction of rotation. 15 of 69

Positive Displacement Pumps (1/2)

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Positive Displacement Pumps (2/2)

Progressive cavity pump Multiplex pump Lobe pump

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Applications general purpose fluids, pure water, sludge and sewage, slurry, high viscosity fluids, power generation, the paper industry, the petroleum industry, chemicals and corrosives, gravel and solid materials, high temperature materials, and marine applications. 18 of 69

Fluid Properties (1/4) The properties of the fluids being pumped can significantly affect the choice of pump. Key considerations include: 1. Acidity/alkalinity (pH) and chemical composition: Corrosive and acidic fluids can degrade pumps, and should be considered when selecting pump materials. 2. Operating temperature: Pump materials and expansion, mechanical seal components, and packing materials need to be considered with pumped fluids that are hotter than 200°F (93°C). 19 of 69

Fluid Properties (2/4) 3. Solids concentrations/particle sizes: When pumping abrasive liquids such as industrial slurries, selecting a pump that will not clog or fail prematurely depends on particle size, hardness, and the volumetric percentage of solids. 4. Specific gravity: The fluid specific gravity is the ratio of the fluid density to that of water under specified conditions. Specific gravity affects the energy required to lift and move the fluid, and must be considered when determining pump power requirements. 20 of 69

Fluid Properties (3/4) 5. Vapor Pressure: A fluid’s vapor pressure is the force per unit area that a fluid exerts in an effort to change phase from a liquid to a vapor, and depends upon the fluid’s chemical and physical properties. Proper Consideration of the fluid’s vapor pressure will help minimize the risk of cavitation.

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Fluid Properties (4/4) 6. Viscosity: The viscosity of a fluid is a measure of its resistance to motion. Since kinematic viscosity normally varies directly with temperature, the pumping system designer must know the viscosity of the fluid at the lowest anticipated pumping temperature. High viscosity fluids result in reduced centrifugal pump performance and increased power requirements. It is particularly important to consider pump suction-side line losses when pumping viscous fluids 22 of 69

PUMP COMPONENTS

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Electric Motors - RPM Description

Singapore

USA

50 Hz

60 Hz

2 Pole Motor speed, RPM

3000 / 2950

3600 / 3550

4 Pole Motor speed, RPM

1500 / 1460

1800 / 1750

6 Pole Motor speed, RPM

1000 / 970

1200 / 1160

Electric Supply Frequency, Hz

n poles, RPM

Supply Freq x 2 x 60 / n Poles

For 3-phase AC motor, HP (output) = 1.73 x Current x Voltage x Eff. x P.F. / 746 Power Factor (P.F.) = KW / KVA

Torque in lb-ft = HP x 5250 / RPM 24 of 69

Head Energy content of liquid per unit weight

Relationship with pressure Head in ft = psi x 144 / w, w Sp. weight lbf/ft3 (for Water Sp. Wt. w = 62.3 lbf/ft3) Hence Head in ft = psi x 2.31 / Sp. Gr.

[Head in m = kPa / (9.81 x Sp. Gr.) ] Velocity Head ft = V2/2g, g = 32.17 ft/s2, V in ft/s [Velocity Head m = V2/2g, g = 9.81 m/s2, V in m/s ] 25 of 69

Pressure, Liquid Height (Head) and Specific Gravity Relationship - FPS units

231 ft

Water s.g. 1.0

HCl s.g. 1.2

100 psi

Crude s.g. 0.8

120 psi

80 psi

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Why use Head ? The main reason for using head instead of pressure to measure a centrifugal pump's energy is that the pressure from a pump will change if the specific gravity (weight) of the liquid changes but the head will not change.

Many Different Types of Pump Head Total Static Head - Total head when the pump is off Total Dynamic Head (Tot System Head) - Total head when the pump is on Static Suction Head - Head on the suction side, with pump off, if the head is higher than the pump impeller Static Suction Lift - Head on the suction side, with pump off, if the head is lower than the pump impeller Static Discharge Head - Head on discharge side of pump with the pump off Dynamic Suction Head/Lift - Head on suction side of pump with pump on Dynamic Discharge Head - Head on discharge side of pump with pump on The definitions of Pump Head vary in literature !

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Pump Performance Curves

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Performance Curves Shut off head – for parallel operation to be > 110% of rated head. Min. continuous stable flow (% of BEP) Rated operating point flow to be 80% to 110% of BEP (preferred range 70% to 120% of BEP) Best Efficiency point (BEP) – flow rate at which highest efficiency is achieved End of curve Minimum continuous stable flow % increases as Suction Specific speed increases.

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Typical performance curves – centrifugal pumps Relationship at a 

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given RPM between Flow Dynamic Head Efficiency NPSH required BHP required BHP = Flow (GPM) X TDH (FT) x SG / 3960 x EFF. (%) [BKW = Flow (m3/hr) x TDH (m) x SG / 367 x EFF. (%) ] 30 of 69

Characteristics Curves Figures are non-dimensional curves which indicate the general shape of the characteristic curves for the various types of pumps – radial, mixed and axial flow. They show the head, brake horsepower, and efficiency plotted as a percent of their values at the design or best efficiency point of the pump.

MIXED FLOW

AXIAL FLOW

RADIAL FLOW

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Affinity Laws The generated pump head depends upon the exit fluid velocity at impeller periphery, which is V = p x D X N, where D = Imp. diameter, N = RPM. Head a V² , Head a D² or Head a N² For given D, H1/H2 = N1² / N2² For given N, H1/H2 = D1² / D2² Capacity Q a D or Capacity Q a N For given D, Q1/Q2 = N1 / N2 For given N, Q1/Q2 = D1 / D2 Power a D³ or Power a N³ Affinity Laws

140 120

H1

Diff Head

100

80

N1

H2

N2

60 40 20

Q2 Q1

0 0

20

40

60

80

100

120

140

Capacity

Affinity laws also may be loosely applied to NPSHR & Pump shaft deflections (square law) and pump wear rates (cubic law)

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Affinity Laws - Example A pump operating in Singapore at 2950 RPM (2 pole motor, 50 Hz) generates 100 m3/hr at 100m differential head. Same pump in USA operating at 3540 RPM (60 Hz) will generate approximately Flow 100 x 3540 / 2950 = 120 m3/hr and Head 100 x (3540/2950) ² = 144 m Power ratio P2/P1 = N2³/ N1³ = 1.728

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Variable speed operation 

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For varying flow or pressure, a variable speed drive may be used. Using affinity laws, one can calculate the flow rate & head at any given operating speed. The drives may be using hydraulic couplings, variable frequency drive, or a steam/ gas turbine for variable speed operation.

System head requirement (no valve)

RPM1 RPM2 H (ft) Pump curve for Di

q (gpm) q* (desired) q produced by pump with no flow control

Advantage: Lower operating Cost 34 of 69

Specific Speed (API 610, 10th ed., Annex A) At Best Efficiency Point, Max. Impeller diameter

Ns = N (Q)0.5 / (g H)0.75 Ns Specific Speed, dimensionless N Rotative speed RPM Q total pump flow m3/sec (Alternate Q m3/sec per impeller eye)

H Head per stage, m Example: Q = 100 m3/hr (0.0278 m3/sec) H = 100m, RPM 2950, Ns=15.55 SI units Conversion to US units x 51.64 = 802.9

Specific speed vs. Efficiency Even though Specific Speed is dimensionless, ignoring “g” in above equation had made it 35 of 51 dimensioned quantity

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Specific Speed Calculation Check (for FPS units) Flow 100 m3/hr (Q = 440.3 USGPM) Head 100m (H = 328.08 ft) Pump RPM N = 2950 Ns = N (Q)0.5 / (H)0.75 = 2950 (440.3)0.5 / (328.08)0.75 = 802.9 (US units) Specific Speed of impellers is indicative of its shape and characteristics as shown in next slide. 36 of 69

Comparison of pump profiles Radial flow – low specific speed Mixed flow – intermediate specific speed Axial flow – high specific speed

N Q Ns  3 / 4 H

D2

D1

D2/D1 > 2

D2/D1 = 1.5 to 2

Specific speeds in US units

D2/D1 < 1.5

D2/D1 = 1 37 of 69

Specific Speed 

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High Ns pump impellers have inlet diameters (D1) that approach or equal the outlet diameter (D2), and relatively large open flow passages. Low Ns pump impellers have outlet diameters (D2) that are much larger than the inlet diameters (D1) and relatively narrow flow passages.

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Net Positive Suction Head NPSHA: Net Positive Suction Head available is the total suction head available from pump centerline less the vapor pressure of the liquid in ft (m) absolute – determined by purchaser at rated flow. NPSHR: Net Positive Suction Head required is a performance characteristics of the pump, determined by the vendor by testing with water (3% loss of head, first stage head in a multi stage pump) NPSHA > NPSHR through the range of operation to prevent detrimental cavitation. 39 of 69

NPSHA Calculations Calculation of system Net Positive Suction Head Available for typical suction conditions.

a b

NPSHA = a) PB- (VP+Ls+hf) b) PB+ LH - (VP+hf) c) p - (VP+Ls+hf) d) p + LH - (VP+hf)

c d Note: Enclosed sheet is a sample NPSH and DH calculations 40 of 69

Suction Specific Speed (API 610) At Best Efficiency Point, Maximum Impeller Diameter.

Nss = N (Q)0.5 / (NPSHR)0.75 Nss Suction Specific Speed, dimensionless N Rotative speed RPM Q pump flow per impeller eye m3/sec NPSHR Net Positive Suction Head required at best eff. Point, max. impeller diameter, m Example Q = 100 m3/hr (0.0278 m3/sec) NPSHR = 5m, RPM 2950, Single suction impeller Nss=147.0 (SI units) Conversion to US units x 51.64 = 7593 41 of 69

NPSHR and margins 

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NPSHR of a pump is the NPSH that cause the total head (Ist stg head of multistage pumps) to be reduced by 3%, due to flow blockage from cavitation vapor in the impeller vanes. NPSHR is not the point at which cavitation starts. (that level is referred to as incipient cavitation). The NPSH at incipient cavitation can be from 2 to 20 times the 3% NPSHR value, depending on pump design.

The higher ratios are associated with high suction energy pumps or pumps with large impeller inlet areas.

a pump running at an NPSHA equal to the NPSHR is already cavitating! 42 of 69

Cavitation Cutaway view of a pump volute shows the passage of flow through the impeller. Top curve System pressure (Ps) > fluid vapor pressure; cavitation cannot occur. Bottom curve Ps < the vapor pressure as it enters the impeller eye. This will cause cavitation.

One cubic foot of water at room temperature becomes 1700 cu. Ft . of vapor at the same temperature.

Cavitation exists in high percentage of pumps, however acceptable life can be achieved.

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Cavitation types 1. 2. 3. 4.

Low NPSHA: Fluid Vaporizes at impeller inlet Low Flow (suction recirculation and discharge recirculation) Air Injection (air leaks or entrained gases) Turbulence (Excessive, due to high velocity, bends, TEE at inlet)

Symptoms of Cavitation: 1. "Pumping gravel" cavitation noise 2. Failure history: repeated seal or bearing failures 3. Rapid decrease in discharge pressure when attempting to increase rates 4. High vibrations 5. Lower than expected discharge pressure 6. Repeated impeller replacements 44 of 69

Suction Cavitation 

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Suction Cavitation: The pump suction is under a low pressure condition where the liquid turns into a vapor at the eye of the pump impeller. This vapor carried to the discharge side of the pump 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 which will remove large chunks of material from its face causing premature failure of the pump. 45 of 69

Suction Energy (Old) Prediction, when cavitation may cause problems can be based on ―Suction Energy‖. Following formula approximates the Graph in Hydraulic Institute Standard on NPSH Margin (ANSI/HI 9.6.1- 1998):

Suction Energy (SE) ≈ (De x N x NSS x s.g.)   

De = Impeller Eye Diameter (inches) N = Pump Speed (RPM) NSS = Suct. Sp. Speed ...RPM x (GPM)0.5/(NPSHR)0.75 s.g. = Specific Gravity of Liquid

De = Suction Nozzle Diameter x 0.9 (is a good approximation for End Suction Pumps) De = Suction Nozzle Diameter x 0.75 (is a good approximation for Side/Double Suction Pumps)

(This HIS code 9.6.1 has since been withdrawn now, and thus some slides are now removed from this presentation. A description of various terms of suction energy are as in next three slides.) http://www.gouldspumps.com/cat_technews.ihtml?pid=9&lastcatid=41&step=4

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Suction Energy (1/3) Pumps with high suction energy level are generally more likely to suffer from cavitation damage. However, there are many factors that contribute to this and no precise definition has been established. These factors typically include: 1. The peripheral velocity at the outside diameter of the impeller eye. Values above approximately 120-ft/sec are considered high suction energy. 2. The suction speed S of the pump. S = nQ0.5/(NPSH)0.75 where n = rpm, Q = gpm and NPSH = feet. Values above about 12,000 are considered high energy. 3. The specific gravity of the liquid pumped. The higher the level, the higher the suction energy. 47 of 69

Suction Energy (2/3) 4. Thermodynamic properties of the liquid. Cold water is one of the highest energy liquids, followed by high temperature water and hydrocarbons. 5. The geometry of the pump inlet. Side suction pumps are considered higher suction energy than end suction. 6. The overlap of the impeller vanes. Impellers with two or three vanes have higher suction energy than four or more vanes. 7. The incidence angle between the inlet impeller vanes and the approaching liquid. The greater the angle, the greater the turbulence and suction energy level. This value may have to be obtained from the pump manufacturer.

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Suction Energy (3/3) 8. 9.

The geometry of the inlet piping to the pump. Piping turns and pipe size changes add to the suction energy of the pump. Operation away from the best efficiency point (BEP) of the pump. At reduced rate of flow, the pump may operate in its suction recirculation region, which considerably increases suction energy. This is a complex situation and a single equation or relationship has not been developed which will accurately tie all of these factors together. Manufacturers can often provide installation lists of pumps that are operating successfully.

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Viscosity correction for Centrifugal Pumps Example: Pump at 750 GPM, 100 ft diff head, Viscosity 1000 SSU, Sp. Gr. 0.90 CQ = 0.95, CH = 0.92 for 1.0 QNW, Ch = 0.635 QW = 750 / 0.95 = 790 GPM

HW= 100 / 0.92 = 109 ft Select pump for water capacity 790 GPM @ 109 ft head. If selected pump eff. 81%, than viscous eff. = 81% x 0.635 = 51.5% Pump BHP = (750 x 100 x 0.90) / (3960 x 0.515) = 33.1 HP 50 of 69

Pumps in Series and Parallel (1/2) Pumps in Series Flow rate Q is same for both Total Head = HA + HB

Pumps in Parallel Head H is same for both Total Flow = QA + QB

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Pumps in Series and Parallel (2/2) When two or more pumps are arranged in parallel their resulting performance curve is obtained by adding their flowrates at the same head as indicated in the figure below.

When two (or more) pumps are arranged in serial, their resulting pump performance curve is obtained by adding their heads at same flow rate as indicated in the figure below.

Composite Performance Curves – 3600 RPM

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Composite Performance Curves – 1800 RPM

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Composite Performance Curves – 1200 RPM

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Pump 3X2X10 operating characteristics at variable speed Pump RPM

BEP Flow, BEP Head, GPM ft

3600

490

400

1800

256

100

1200

170

43

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Pump Performance parameters at various speeds For a given Centrifugal Pump Model 3 x 2 x 10, performance at BEP @ Max Impeller diameter:

Selected Centrifugal pump model for flow capacity 200 GPM @ 80 ft diff head:

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3600 RPM, 68 HP, Q= 490 GPM @ DH = 400 ft

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1800 RPM, 8.4 HP, Q= 258 GPM @ DH = 100 ft

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1200 RPM, 2.4 HP, Q= 170 GPM @ DH = 44 ft

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3600 RPM, 3 x 2 x 6, h  70%, NPSHR = 6.2 ft, Imp. diam 5.3‖ 1800 RPM, 3 x 2 x 10, h  78%, NPSHR = 5.5 ft, Imp. diam. 9.0‖ 1200 RPM, 4 x 3 x 13, h  63%, NPSHR = 4.8 ft, Imp. diam 13‖ 57 of 69

Goulds 3196 Pump Curves Manufacturers provide series of pumps to cover broad ranges of capacities, heads, and suction and discharge piping diameters. Most pumps can be equipped with different diameter impellers and can be operated at different speeds to change capacities. The 60 Hz curves provided (T:\PUMPS) are for a few variations of the Goulds pump model 3196 process pump, at 1180, 1750 and 3550 RPM. Pump sizes are denoted with 3 numbers.

3x4-7 Discharge Diameter Inches

Suction Diameter Inches

Casing Diameter Inches 59 of 69

Pump Selection Goal is to find a pump whose curve matches the piping system head vs. flow rate curve. We can fit our process conditions on the manufacturers pump curves. To select a specific pump from a product line, find the pump with the highest efficiency that does not require the use of the largest impeller diameter. This will allow for future production expansions. Suppose that we have a process that requires a flow rate of 300 GPM and has a head requirement of 60 ft. at that flow rate. Can a 3x4-10 model 3196 Goulds pumps be used?

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Examples Example 1: Please select centrifugal pumps for following duties 1. Capacity 250 USGPM, Diff Head 200 ft, Sea Water Sp Gr 1.03, 50 Hz Electric Supply, NPSHA 15 ft. 2. Capacity 36 m3/hr, 41.5m Dhead, Crude Oil Sp Gr 0.80, 60 Hz electric supply, NPSHA 2.5m 2a The best efficiency point of above pump at 50 Hz operation.

Example 2 Please select suitable centrifugal pumps for following duties 1. Capacity 6000 USGPM, Ps 20 psig, Diff head 200 ft, Hydrocarbon Sp. Gr. 0.9, NPSHA 18 ft 60 Hz Electric Supply 2. Capacity 500 m3/hr, Ps 150 kPa, Diff head 20m, Diesel Oil Sp. Gr. 0.85, NPSHA 3.5 m, 50 Hz 2a. The best efficiency point of above selected pump at 60 Hz operation.

Show Pump Model, RPM, Eff., Rated BKW, Driver rating, NPSHR, Impeller Diameter, Shut Off Head, Specific Speed, Suction Specific Speed, Nozzle sizes and ratings, in the given format.

Show Pump Model, RPM, Eff., Rated BKW, Driver rating, NPSHR, Impeller Diameter, Shut Off HeadSpecific Speed at BEP,Suction Specific Speed at BEP, Nozzle sizes and ratings, BKW @ End of Curve

Please note Model Goulds 3196 is taken as an example only, it is not a suitable model for service.

(Please note Model Bell & Gosset series VSX is taken for example only, it is not a suitable model for service)

Refer Goulds Model 3196 / Bell & Gossett curves available in T:\pumps directory

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Codes and Standards (1/2) 

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API Std 610, 10th ed., 2004 Centrifugal Pumps for Petroleum, Petrochemical and Natural Gas Industries-Tenth Edition; ISO 13709 Adoption API Std 682, 3rd ed. 2004, Pumps Shaft Sealing Systems for Centrifugal and Rotary Pumps-Third Edition; ISO 21049 Adoption; Errata: November 10, 2006 API Std 685, Ist ed., 2000 Sealless Centrifugal Pumps for Petroleum, Heavy Duty Chemical, and Gas Industry Services Downstream Segment, Errata 10/2007 ASME B 73.1, 2001 Specification for Horizontal End Suction Centrifugal Pumps for Chemical ProcessReplaces B73.1M (R2007) ASME B 73.2, 2003, Specification for Vertical InLine Centrifugal Pumps for Chemical Process (R2008) ASME B 73.3, 2003, Specification for Sealless Horizontal End Suction Metallic Centrifugal Pumps for Chemical Process (R2008) ASME PTC 8.2, 1990, Centrifugal Pumps 63 of 69

Codes and Standards (2/2) 

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BSI BS EN 22858, 1993 End-Suction Centrifugal Pumps (Rating 16 Bar) Designation, Nominal Duty Point and Dimensions Second Edition; (CEN EN 22858: 1993) NFPA 20, 2010, Standard for the Installation of Stationary Fire Pumps for fire protection : NFPA 20H, 2010 Stationary Fire Pumps Handbook - Third Edition

There are many other codes available for Centrifugal pumps from various international organizations as       

BSI, EN DIN, JIS, AWWA, ISO, GOST, ASHRAE etc. 64 of 69

Hydraulic Institute Standards (1/3)

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Hydraulic Institute Standards (2/3)

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Hydraulic Institute Standards (3/3)

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Unit Conversions Some unit conversions (for ready Some formulas (for ready reference) reference)  USGPM = 449 x CFS  Flow m3/hr = 4.403 USGPM  Pipe Vel. ft/sec = GPM x 0.321/ (ID in)2 3  Flow m /hr = 0.2778 liter/sec  BHP = GPM x H x Sp Gr / 3960 / Eff.  Flow m3/hr = 0.5886 ft3/min  BKW = m3/hr x H,m x Sp Gr/ 367 / Eff.  Head 1 m = 3.2808 ft  Head H = V2/2g  Head 10.19m WC = 1 bar  Ns = N Q ½ H ¾ pressure  Nss = N Q ½ NPSHR ¾  Power 1 KW = 1.341 HP 2 2  Accel. due to gr. g = 9.806m/s2 =  Q1/Q2 = N1/N2, H1/H2 = N1 /N2  psi = head in ft x Sp Gr / 2.31 32.17 ft/s2  Sp. speed in US units = 51.64 x SI kPa = head in m x Sp Gr / 0.102 units (API 610) 68 of 69

Books on Centrifugal Pumps

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Thank YOU

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Composite rating charts for the ―Goulds 3196‖ family of pumps

Bell & Gossett VSX 1780 RPM

Base Mounted – Double Suction

Bell & Gossett VSX 1180 RPM

Base Mounted – Double Suction

Manufacturer’s pump characteristics

Index of pumps from Goulds Pumps Inc

Affinity law - NPSHR 1/ 5

1  h 2  D1     1  h1  D2 