Guide to the_selection_of_rotodynamic_pumps_final

EUROPEAN ASSOCIATION OF PUMP MANUFACTURERS
ASSOCIATION EUROPEENNE DES CONSTRUCTEURS DE POMPES
EUROPAISCHE VEREINIGUNG DER PUMPENHERSTELLER
ASSOCIAZIONE EUROPEA DEI PRODUTTORI DI POMPE

GUIDE TO THE SELECTION OF
ROTODYNAMIC PUMPS

Contents
1. Purpose of this Guide to pump procurement 2
2. Method of classifying pumps 2
3. Industries and applications 3
4. Pump characteristic curves 4
5. Details of pump types 5
6. Selecting a pump 20
6.1 Choosing the pump duty point 20
6.2 Impeller modifications to match the duty 21
6.3 The selection process 21
6.4 Worked example 24
6.5 Importance of pump operating speed 24
7. Optimising the pump efficiency 25
7.1 Allowing for the effect of Specific Speed 25
7.2 Attainable efficiency levels 27
7.3 Worked example 29
8. Useful Pump information 29
8.1 Total Head “H” 29
8.2 Speed of Rotation 31
8.3 Pump Power input calculation 31
8.4 Motor Power Input 32
8.5 Net Positive Suction Head (NPSH) 32
8.5.1 NPSH Calculations 32
8.5.2 NPSH at positive pumping mode 33
9. Life Cycle Costs (LCC) 33
10. Useful references 33
11. Acknowledgments 34
12. Further Information 34

Tables
1. Categorisation of pump types 2
2. Principal industries and their applications 3
Pump Types: 3. Single entry volute – conventional 6
4. Single entry volute – solids handling 7
5. Single entry volute – non clogging 8
6. Single entry volute – in-line 9
7. Double entry volute 10
8. Two stage volute 11
9. Multistage radial split 12
10. Multistage axial split 13
11. Multistage barrel casing 14
12. Single stage well 15
13. Multistage well 16
14. Mixed flow volute 17
15. Mixed flow bowl 18
16. Axial flow well 19

Figures
1. Pump characteristics 4
2. Onset of possible adverse effects when operating away from BEP 5
3. Illustration of the effect on efficiency of throttling a pump 20
4. Pump characteristics showing various impeller diameters 21
5. Indication of head and flow coverage of basic pump types 22
6. ‘Tombstone’ curves for the selection of pumps by duty 23
7. Effect of speed reduction on pump characteristics 25
8. Plot to determine value of K 26
9. Plot to determine value of C 27
10. Mean Best Efficiencies of Volute pumps 28
11. Mean Best Efficiencies of Multistage and Well pumps 28

1

1. Purpose of this Guide to pump procurement
This Guide provides an introduction to the very complex subject of the selection of pumps. It is
aimed at anyone who wishes to purchase or select a pump and, at the same time, wishes to save
money on their energy bill. Almost invariably, this saving will be far more than the first cost of the
pump. The reader may be the end user, a contractor or a consultant. This Guide provides the reader
with the basic principles of pump procurement, giving pointers to the pump type and performance
they should consider. Pumps are divided into their main types, then their basic construction and
performance are considered, their principal applications are described, the basic principles of pump
selection are explained and, last but not least, target efficiencies are set to help minimise energy
usage. The hope is that both pump users and the environment will benefit.

2. Method of classifying pumps
Table 1 shows pump types listed under two main categories, Rotodynamic and Positive
Displacement, each of which has three sub-categories. It excludes many types of specialist pumps
(e.g. Jet, Liquid Ring, Regenerative), but these only account for a relatively small amount of
absorbed energy. Since around 90% of pumping energy in the UK is absorbed by rotodynamic
pumps, this Guide concentrates only on this category.

Pump Type Table

Single Entry Volute - Conventional 3
Single Entry Volute – Solids Handling 4
Single Entry Volute – Non-Clogging 5
Single Entry Volute – In-Line 6
ROTODYNAMIC

Double Entry Volute 7
Centrifugal
Two Stage Volute 8
Multistage Radial Split 9
Multistage Axial Split 10
Multistage Barrel Casing 11
Single Stage Well 12
Multistage Well 13
Volute 14
Mixed Flow
Bowl 15
Axial Flow Well 16

Progressing Cavity
Sliding Vane
DISPLACEMENT

Rotary Peristaltic
POSITIVE

Screw
Lobe
Gear
Diaphragm
Reciprocating Plunger
Piston
Open Archimedean Screw

Table 1.
Categorisation of pump types

2

3. Industries and applications
Table 2 shows the major industries which use rotodynamic pumps, together with the main
applications on which the pumps are used. It also guides you to the exact table numbers, within
section 5, where further descriptions of the pump types that can be used for each of the applications
can be found.

Typical Applications
Principal Industries (+ Table nos. detailing
pump types used)

General Services Cooling water(3)(7), Service water(3), Fire-fighting
(3)(7)(8)(12)(13), Drainage (16)
Agriculture Irrigation (3)(7)(9)(15)(16), Borehole (3)(13), Land drainage
(15)(16)
Chemical / Transfer (3)
Petrochemical
Construction / Pressure boosting (3)(8), Drainage (4), Hot water circulation
Building Services (6), Air conditioning (6), Boiler feed (9)
Dairy / Brewery Transfer (3), ‘Wort’ (4), ‘Wash’ to fermentation (7)
Domestic Hot water (6)
Metal Manufacture Mill scale (4), Furnace gas scrubbing (7)(12)(13), Descaling
(9)
Mining / Quarrying Coal washery (4), Ore washing (4), Solids transport (4),
Dewatering (4)(9)(10)(13), Water jetting (8)
Oil / Gas Production Main oil line (7)(10)(11), Tanker loading (7), Water injection
(10)(11), Seawater lift (13)
Oil / Gas Refining Hydrocarbon transfer (3)(6)(7)(9)(10), Crude oil supply (7),
Tanker loading (7), Product pipeline (9)(10), Reactor charge
(11)(13)
Paper / Pulp Medium / low consistency stock (3), Wood chips (4), Liquors /
Condensate (4), Stock to head box (7)
Power Generation Large cooling water (3)(7)(14), Ash handling (4), Flue gas
desulphurisation process (4), Condensate extraction (7)(8)(13),
Boiler feed (9)(10)(11)
Sugar Manufacture Milk of lime / syrup (3), Beet tailings (4), Juices (4), Whole
beets (5)
Wastewater Raw and settled sewage (5), Grit-laden flows (5), Stormwater
(5)(15)(16)
Water Supply Raw water extraction (7)(12)(13)(14)(15), Supply distribution
(7)(8)(9), Boosting (7)(8)

Table 2.
Principal industries and their applications

3

4. Rotodynamic Pump characteristic curves
Pumps are always defined by the basic pump characteristic curves (Fig 1). These show the
relationship between head, power and efficiency against flow. It is important to note just how
‘peaky’ the efficiency curve is, showing that running at a flow above or below Best Efficiency Point
(BEP) is likely to lead to a significant reduction in pump efficiency.

Fig 1.
Pump characteristics

The curves shown in Fig 1 are fairly typical of a Centrifugal pump. A Mixed Flow pump would
have a much steeper head curve, a power curve which would probably fall continuously from zero
to maximum flow, and an efficiency curve which would be more ‘peaky’. An Axial Flow pump
would have even steeper head and power curves than a Mixed Flow pump, and an efficiency curve
which would be even more ‘peaky’. These variations are important in that they affect maximum
pipe pressures, motor sizes and off-peak operating efficiencies. (The definitions of Mixed and
Axial Flow types are covered in section 7.)

Also shown on Fig 1 is the Net Positive Suction Head required by the pump (NPSHR). The NPSH
is defined as the total head at the pump inlet above vapour pressure (corrected to the level of the
first stage impeller inlet, if different). The NPSHR is usually (but not always) the NPSH at which
the pump (or the first stage impeller if a multistage pump) loses 3% head due to cavitation. The Net
Positive Suction Head available to the pump on site (NPSHA) must exceed the NPSHR by a safety
margin. This would rarely be less than 0.5m but will usually be greater because of many factors,
including pump speed, size, liquid pumped and operating range. More information on this safety
margin is given in Ref 1, which provides a useful coverage of the subject of NPSH.

The importance of selecting a pump to operate as closely as possible to its BEP cannot be over-
emphasised. Not only should this save on energy costs, it will have several other benefits. The
pump should run smoothly with minimum internal disturbing forces, thereby saving on maintenance
costs due to premature failure of components such as bearings, wear rings, bushes, couplings and
seals. The risk of damage to pump components due to cavitation should be reduced. Vibration
should be minimised, benefiting other equipment. Noise should be minimised, improving the
environment. Pressure pulsations should also be minimised, reducing the risk of problems in the
pumping system as a whole. Fig 2 indicates some of the problems which can result from operating
away from BEP. Some of these problems may not be serious in small pumps, but they increase in
severity as pump power increases, and should therefore be discussed with the pump supplier.

4

Fig 2.
Onset of possible adverse effects when operating away from BEP

5. Details of pump types
The following Tables 3 to 16 give details of the rotodynamic pump types listed in Table 1.

In practice there are dozens of variations on the basic pump themes, each one taking on the
attributes dictated by its particular market. Branch positions can change, the shaft can be horizontal
or vertical or even inclined, there are many options in shaft sealing, the drive may be by fixed or
variable speed motor or diesel engine or belt, etc., etc..

The tables show drawings of the most common arrangements of each of the 14 types, together with
brief descriptions. They also show typical characteristic curves. However, the actual curve shapes
can vary considerably, so the curves produced by the maker of a pump being considered must be
checked to make sure they suit the application. Comments on performance are made on the sheets
which should help in this respect.

Finally, the main applications of each pump type are listed to help with the choice of pump.
Obviously, this can only be a general guide, the suitability of each selection for an application must
be judged on its merits.

5

Pump Type / Performance Description / Applications

Single Entry Volute - Conventional Description
Impeller may be mounted on motor shaft, or
pump may have its own shaft and bearings
with pump driven via a coupling. Standard
pumps to ISO 2858 (EN 22858, ex Din
24256) and EN 733, ex DIN 24255, enable
back pull-out of rotating element without
disturbing pipework, if using spacer
coupling, without disturbing motor. Some
pumps have special inlet casings for self-
priming.
Typical Performance
Shaft is sometimes vertical with pump
120
suspended in a sump by a column pipe, with
Power no pump gland, and discharging to surface
% of Best-Efficiency Head,

Head
100
through a separate pipe between casing
Power & Efficiency

Efficiency
80 discharge flange and column/motor
60 support/mounting plate.
40
Applications
20 General: Cooling water, Service water, Fire-
0 fighting (special characteristics required).
0 20 40 60 80 100 120 Agriculture: Irrigation (usually with priming
% of Best-Efficiency Flow device), Borehole (small flows and depths
using ejector in borehole).
Smaller pumps tend to be relatively low cost with Chemical/Petrochemical: Transfer (superior
efficiency on the low side. Back wear rings with construction and special materials, often
impeller balance holes (to reduce thrust and gland glandless using magnetic drive or canned
pressure) cause some efficiency loss. Efficiency motor, sometimes vertical sump type).
falls relatively slowly as flow moves away from Building Services: Pressure boosting in tall
best-efficiency. buildings.
On some pumps of this type , head may fall with Dairy/Brewery: Transfer (special stainless
reducing flow (as shown). If so, at reduced flow steel fabricated construction with crevices
surging may occur and pumps will not run in avoided to permit ‘Clean in place’).
parallel at low flows. Oil/Gas Refining: Fuel oil, Gas oil,
Lubricating oil, Kerosene, Petrol (‘Process’
Power may increase considerably beyond best- type, centre-line supported, special shaft
efficiency flow. To cover this, larger motors may seals, complying with API 610)
be needed. Paper/Pulp: Medium/low consistency stock
(special designs with single shrouded
Some small pumps are fitted with integral speed impellers, often stainless steel).
controllers which can be used for energy saving. Power Generation: Large cooling water,
(vertical shaft, largest have concrete
volutes).
Sugar: Milk of lime and syrup.

Table 3.
Details of Single Entry Volute – Conventional Pumps

6


Single Entry Volute – Solids Handling Description
Very robust construction. Usually horizontal
shaft but some pumps have vertical shaft,
using either cantilevered shaft suspended in
sump with no gland, or driven by
submersible motors. Impellers and casings
usually in hard nickel or chrome iron for
larger solids, and rubber or polyurethane
lined for small solids. Impeller usually
screwed on to shaft to protect it. Gland
packing flushed with clean water or expeller
used to keep gland dry while running.
Typical Performance Bearings and front cover axially adjustable
140
to take up wear on radial wear faces. Speed
Head and head are limited to minimise wear.

120
Higher heads achieved by running pumps in
Power and Efficiency

100
Efficiency series.
80 Power

60 Applications
40 Brewery: Brewed barley mash (‘wort’).
20 Construction: Drainage (diesel engine driven
0
and self priming by vacuum pump, or
0 20 40 60 80 100 120 vertical submersible motor driven).
% of Best-Efficiency Flow Metal Manufacture: Mill scale.
Mining/Quarrying: Coal washery, Ore
Efficiency generally low, because of low number of washing, Solids transport, Dewatering open
thick impeller vanes, ‘pump-out’ vanes on impeller cast mines (cantilevered shaft).
shrouds and concentric casings. Paper/Pulp: Wood chips, Liquors,
Condensate.
Head usually rises to zero flow. Power Generation: Ash handling, Flue gas
desulphurisation process.
Power usually rises beyond best-efficiency flow, Sugar: Beet tailings, Sugar juices.
although pumps do not normally operate here.

Head/flow/power adjusted by speed (belt drive or
variable speed motor) since impellers cannot be
cut.

Table 4.
Details of Single Entry Volute – Solids Handling Pumps

7


Single Entry Volute – Non-Clogging Description
Usually vertical pump shaft.

Normally, pump will be in wet well using
integral submersible internally dry motor,
with oil reservoir with two seals between
pump and motor to avoid contamination
from pumped fluid. Units are usually
mounted on rails to guide them down into
well, making a self-sealing joint at discharge
pipe and allowing simple installation and
Typical Performance removal.

175 Submersible motors may require cooling,
depending on size of unit and whether they

150
Head need to operate un-submerged. Cooling may

125
be by enclosed circuit using oil or glycol , or
Power
100 by jacket using pumped liquid where
75
Efficiency
suitable. These units are also used in dry
50 wells, inherently protected against flooding.
25
Sometimes, pumps in dry wells are driven
0
0 20 40 60 80 100 120
through intermediate shafting by
% of Best-Efficiency Flow conventional motor on higher floor to avoid
flooding.
Efficiency can be on the low side, particularly for
small pumps. Requirement for ‘non-clogging’ or
‘unchokability’ necessitates use of one or two vane Applications
impellers (except in large sizes). Back vanes on Sugar: Whole beets (horizontal shaft).
impellers to reduce axial thrust and protect seal also Wastewater: Raw sewage, Grit-laden flows
absorb power and reduce efficiency. Pumps (‘vortex’ impeller), Settled sewage,
handling material heavy in grit use multi-vane Stormwater.
‘vortex’ impellers, set back from main flow and
having low efficiency.

Head will usually rise continuously to zero flow,
allowing parallel operation.

Power will usually peak reasonably close to best-
efficiency flow.

Pump is usually required to pass a sphere of
between 75 and 150mm diameter. However,
‘sphere size’ is only a crude guide to solids
handling performance.

Table 5.
Details of Single Entry Volute – Non-Clogging Pumps

8


Single Entry Volute – In-Line Description
Larger pumps have vertical shafts and are
usually located (and often supported) by
pipework. Motor is fitted above pump, so
that forces on pump flanges do not affect
pump/motor alignment. Motor and impeller
can be removed without disturbing
pipework.

Smaller pumps have horizontal shafts and
are usually supported by pipework. Canned
rotors are used to avoid shaft seals, and
Typical Performance bearings are lubricated by pumped liquid.
140 Smaller pumps (up to about 200 mm
Head branches) are often built with two pumps

120
combined, sometimes known as

100
Efficiency
Power
‘twinpumps’ or ‘twinsets’. These can be
80
used as duty/standby and sometimes in
60 parallel.
40

20 Applications
0 Building Services: Hot water circulation, Air
0 20 40 60 80 100 120 conditioning.
% of Best-Efficiency Flow Domestic: Hot water circulation.
Oil/Gas Refining: Fuel oil, Gas oil,
Efficiency is reduced a little by cramped Kerosene, Petrol.
arrangement of suction and discharge passages.
Back wear rings with impeller balance holes (to
reduce thrust and gland pressure) cause some
efficiency loss.

Head usually rises continuously with reducing
flow, except on some of the smaller pumps.

Power will sometimes rise at higher flows, may
require larger motors to cover this.

Smaller pumps will often have integral speed
control, enabling automatic head control to suit
demand.

Table 6.
Details of Single Entry Volute – In-Line Pumps

9


Double Entry Volute Description
Usually horizontal shaft, axially split.
Lifting cover gains access to rotating
element without disturbing pipework or
motor. Shaft may be vertical if space is
limited or flooding is possible (in which
case motor will be on higher floor). Axial
hydraulic balance minimises axial thrust.
Larger high head pumps have double volutes
to reduce radial thrust. In-line branches
simplify pipework.
Typical Performance
140 Applications
Head General: Cooling water, Fire-fighting

120
(special characteristics required).

100 Power Agriculture: Irrigation (usually with priming
80
Efficiency device).
60 Brewery: ‘Wash’ to fermentation tanks.
40 Metal Manufacture: Furnace gas scrubbing.
20 Oil/Gas Production: Main oil line (radially-
0 split for higher heads), Tanker loading.
0 20 40 60 80 100 120 Oil/Gas Refining: Crude oil supply
% of Best-Efficiency Flow (radially-split for higher heads, API 610),
Fuel oil, Gas oil, Kerosene, Petrol (‘Process’
Efficiency good and usually falls away fairly type, centre-line supported, special shaft
slowly as flow moves away from best-efficiency. seals, API 610), Tanker loading.
Paper/Pulp: Low consistency stock to head
Head usually rises continuously with reducing box (impeller vanes offset to minimise
flow, allowing parallel operation. pulsations).
Power Generation: Condensate extraction
Power often rises at higher flows, so motor powers (vented back to condenser), Large cooling
may need to be increased to suit. water.
Water Supply: River and reservoir
Suction performance benefits from two impeller extraction, Supply distribution, Boosting.
inlets.

Table 7.
Details of Double Entry Volute Pumps

10


Two Stage Volute Description
Two impellers are usually mounted back-to-
back on shaft with pressure breakdown bush
in between. Integral cross-over passage from
outlet of first stage impeller to inlet of
second stage impeller. Second stage gland
under first stage discharge pressure, so
sealing must suit. Inherent axial balance, so
low axial thrust.

Applications
Typical Performance General: Fire-fighting (special
140 characteristics required).
Head Building Services: Pressure boosting in tall

120
buildings.

100
Efficiency
Power
Mining/Quarrying: Jetting water monitors.
80
Power Generation: Condensate extraction
60 (vented back to condenser).
40 Water Supply: Supply distribution,
20 Boosting.
0
0 20 40 60 80 100 120
% of Best-Efficiency Flow

Efficiency reduced a little by losses in crossover
passage and inter-stage bush. However, probably
more efficient than equivalent single-stage Double
Entry Volute pump for same duty.

flow, allowing parallel operation. Two impellers in
series produce relatively high head (without
expense of using two pumps).

Power likely to increase at higher flows, so motor
powers may need to be increased to suit.

Table 8.
Two Stage Volute Pumps

11


Multistage Radial Split Description
Usually three or more stages. Each impeller
discharges into a multi-vaned diffuser
leading to return guide vanes which feed
flow to inlet of next impeller. Stages are
held together by long through-bolts.

Larger pumps have horizontal shafts and
may be driven through step-up gearboxes to
increase speed and pressure. All impellers
face same direction and rarely have back
wear rings, so a balance disc or drum is
Typical Performance usually fitted at discharge end with leakage
140 returned to suction. On abrasive duties, a
Head heavy thrust bearing may also be required.

120
On hot duties, may be centre-line supported

100
Efficiency
Power
and use balance drum and thrust bearing.
80

60 Smaller pumps usually have vertical shafts
40 with motor mounted on top. Hydraulic
20 components may be sheet metal or plastic
0 composite.
0 20 40 60 80 100 120

Applications
Agriculture: Small scale irrigation.
Used for relatively high head duties where single or Building Services: Boiler feed (fabricated
two stage pumps are unsuitable. stainless steel components in smaller
pumps).
Efficiency suffers somewhat from tight hydraulic Metal Manufacture: Descaling (with
passages and relatively large shaft diameter at external thrust bearing).
impellers. Also from larger wear ring clearances on Mining: Dewatering.
hot pumps. Efficiencies of smaller pumps can Oil/Gas Refining: Fuel oil, Gas oil,
benefit from use of thin sheet metal hydraulic Kerosene, Petrol (‘Process’ type, Centre-line
components. Efficiency will be better than 1 or 2 supported, special shaft seals, complying
stage pumps for high head applications. with API 610), Product pipeline.
Power Generation: Boiler feed.
Head usually rises continuously with reducing Water Supply: Supply distribution (high
flow, allowing parallel operation, but rise to zero pressure).
flow is minimised to limit maximum pressure on
pipework.

Power increases at higher flows, so motor powers
may need to be increased to suit.

Table 9.
Details of Multistage Radial Split Pumps
12


Multistage Axial Split Description
Each impeller discharges into a double
volute which feeds flow back to next
impeller. Impellers are split into two sets,
mounted back-to-back. First set fed by
suction at one end of pump and discharges
into crossover passage from middle of pump
to other end, where it feeds second set of
impellers which discharge at centre of
pump. A pressure breakdown bush is fitted
between last impeller of first set and final
Typical Performance impeller. Another breakdown bush is
140 necessary before first impeller of second set,
Head with leakage returned to suction. Axial

120
thrust is basically balanced, so a large thrust

100
Efficiency
Power
bearing is not needed. Axial split of casing
80
involves difficult sealing to atmosphere and
60 between stages. Hot pumps are centre-line
40 supported.
20

0 Applications
0 20 40Mining: Dewatering.
60 80 100 120
% of Best-Efficiency Flow Oil/Gas Production: Water injection, Main
oil line.
Used for relatively high head duties where single or Oil/Gas Refining: Fuel oil, Gas oil,
two stage pumps are unsuitable. Kerosene, Petrol (‘Process’ type, centre-line
supported, special shaft seals, complying
Efficiency suffers somewhat from tight hydraulic with API 610), Product pipeline.
passages and relatively large shaft diameter at Power Generation: Boiler feed.
impellers. Also from larger wear ring clearances on
hot pumps.

flow, allowing parallel operation, but rise to zero
flow is minimised to limit maximum pressure on
pipework.

Power increases at higher flows, so motor powers
may need to be increased to suit.

Table 10.
Details of Multistage Axial Split Pumps

13


Multistage Barrel Casing Description
Stages are built up much as for Multistage
Radial Split pump, then inserted into a
forged steel barrel casing which provides
full pressure containment, which is then
closed by a heavy cover. Suction end of
barrel is only subjected to suction pressure.
Axial thrust is usually accommodated by a
balance drum with a thrust bearing to take
residual thrust.
Hot pumps are centre-line supported.
Typical Performance
140 Applications
Head Oil/Gas Production: Water injection, Main

120
oil line.

100
Efficiency
Power
Oil/Gas Refining: Reactor charge (anti-
80
corrosive materials and allowance for high
60 differential expansion).
40 Power Generation: Boiler feed.
20

0
0 20 40 60 80 100 120

Used for relatively high head duties where single or
two stage pumps are unsuitable.

Efficiency suffers somewhat from tight hydraulic
passages and a large shaft diameter at impellers.
Also from larger wear ring clearances on hot
pumps.

Head rises continuously with reducing flow,
allowing parallel operation, but rise to zero flow is
minimised to limit maximum pressure on pipework.

Power increases at higher flows, but pumps rarely
run beyond best-efficiency flow.

Table 11.
Details of Multistage Barrel Casing Pumps

14


Single Stage Well Description
Pump is suspended from floor level. Flow
enters through a bellmouth to give well
distributed flow to impeller (provided intake
arrangement feeding pump has been well
designed). Impeller discharges to a multi-
vane axial/inward diffuser and thence to
column pipe and discharge bend. Discharge
flange can be above or below floor. Axial
thrust is taken by a thrust bearing below
motor, or the motor bearings . The pump can
also be driven by a submersible motor.

Applications
Typical Performance General: Fire-fighting (special
175
characteristics required).
Metal Manufacture: Scrubber circulation.

150
Head Water Supply: River and reservoir

125 extraction.
Power
100

75
Efficiency
50

25

0
0 20 40 60 80 100 120

Pump efficiency is reasonably good if losses in
column pipe, discharge bend and thrust bearing are
deducted from motor output.

Head is suitable for parallel operation.

Power usually peaks at or near best-efficiency flow.

Table 12.
Details of Single Stage Well Pumps

15


Multistage Well Description
Above-ground motor version is basically
similar to Single Stage Well pump, except
that several impeller/diffuser stages are
connected in series. For high heads or small
diameters, radial impellers and diffusers are
used (similar to Multistage Radial Split
pump arrangement).

Shaft drive may be used in wells up to 30m
deep, although use in deeper wells may still
be economical.

Submersible motor version is used in deep
Typical Performance wells, with motor mounted below pump to
175
aid cooling. Motor usually water-filled with
integral thrust bearing.

150
Head

125 Applications
100
Power
General: Fire-fighting (special
75 characteristics required).
Efficiency
50
Agriculture: Borehole (driven by shafting or
submersible motor).
25
Metal Manufacture: Scrubber circulation.
0 Mining: Dewatering underground mines
0 20 40 60 80 100 120
% of Best-Efficiency Flow with submersible motor drive.
Oil/Gas Production: Seawater lift.
Pump efficiency reasonably good but submersible Oil/Gas Refining: Reactor charge
motor less efficient than conventional motor. (suspended in canister).
Column pipe losses may be significant in deep Power Generation: Condensate extraction
well. (special first stage impellers, suspended in
canister).
Head is suitable for parallel operation. Water Supply: Borehole extraction (driven
by submersible motor or shafting in shallow
Power usually peaks at or near best-efficiency flow. wells).

Table 13.
Details of Multistage Well Pumps

16


Mixed Flow Volute Description
Generally used for higher flows and lower
heads. Usually vertical shaft with bottom
entry. Rotating element can be removed
without disturbing pipework. Impeller
sensitive to inlet conditions so inlet pipe
(usually a bend) needs careful design. Motor
may be supported from ground level or on a
higher floor.

Applications
Power Generation: Condensate cooling
Typical Performance water (largest flows have concrete volutes).
200
Water Supply: Reservoir extraction (very
large flows only).

Head

150

Power
100

Efficiency
50

0
0 20 40 60 80 100 120

Efficiency reasonably good but falls fairly quickly
above and below best-efficiency flow.

Head rises fairly steeply with reducing flow. Best-
efficiency head is relatively low. Instability is
possible at around 60% flow.

Power rises with reducing flow, so a larger motor
may be required to cover this.

Table 14.
Details of Mixed Flow Volute Pumps

17


Mixed Flow Bowl Description
Conventional pump is suspended from floor
level. Flow enters through a bellmouth to
give well distributed flow to impeller
(provided intake arrangement feeding pump
has been well designed). Impeller discharges
to a multi-vane axial/inward diffuser and
thence to column pipe and discharge bend.
Discharge flange can be above or below
floor. Axial thrust is taken by a thrust
bearing either below the motor or by the
motor bearings.

Submersible motor version is usually
Typical Performance lowered into a canister below floor. Motors
are dry internally, having oil reservoir with
200
two seals between pump and motor to avoid

Head
contamination from pumped fluid.

150

100
Power Applications
Agriculture: Irrigation (often with
Efficiency
50
submersible motor), Land drainage (usually
with submersible motor).
0
Wastewater: Stormwater (surface water
0 20 40 60 80 100 120 only).
% of Best-Efficiency Flow Water Supply: River and reservoir
extraction.
Efficiency falls fairly quickly above and below
best-efficiency flow. Efficiency of conventional
version is reasonably good if losses in column pipe,
discharge bend and thrust bearing are deducted
from motor output. Submersible motor version
loses some efficiency due to losses in canister.

Head rises fairly steeply with reducing flow. Best-
efficiency head is relatively low. Instability is
possible at around 60% flow, limiting the operating
range.

Power rises with reducing flow, so a larger motor
may be required to cover this.

Table 15.
Details of Mixed Flow Bowl Pumps
18


Axial Flow Well Description
Conventional pump is suspended from floor
level. Flow enters through a bellmouth to
give well distributed flow to impeller
(provided intake arrangement feeding pump
has been well designed, very important for
this pump type). Impeller discharges to a
multi-vane axial diffuser and thence to
column pipe and discharge bend. Discharge
flange can be above or below floor. Axial
thrust is taken either by a thrust bearing
below motor or by the motor bearings.

Submersible motor version is usually
Typical Performance lowered into a canister below floor. Motors
are dry internally, having oil reservoir with
250
two seals between pump and motor to avoid

contamination from pumped fluid.

200
Head

150 Power Applications
100 Efficiency
General: Drainage.
Agriculture: Irrigation (often with
50 submersible motor), Land drainage (usually
0
with submersible motor).
0 20 40 60 80 100 120 Wastewater: Stormwater (surface water
% of Best-Efficiency Flow only).

Efficiency falls quickly above and below best-
efficiency flow. Efficiency of conventional version
is on the low side, even after losses in column pipe,
discharge bend and thrust bearing are deducted
from motor output. Submersible motor version
loses some efficiency due to losses in canister.

Head rises rapidly with reducing flow. Instability is
very likely around 60% flow limiting the operating
range. Best-efficiency head is low.

Power rises rapidly with reducing flow. It is
unlikely that motor will be sized to cover power at
low flow.

Performance is very dependent upon providing
good inlet flow to bellmouth. Intake model tests are
advisable.

Table 16.
Details of Axial Flow Well Pumps
19

6. Selecting a pump
This section gives a quick overview of the fundamentals of choosing and using a pump for best
efficiency. This is not an exhaustive guide, but is designed to be just sufficient for non-technical
personnel to get a better understanding of the technical background to this work. The following
applies to most types of rotodynamic pumps.

6.1 Choosing the pump duty point
The first step in pump selection is to determine the principal duty point, i.e. the required flow and
head. The cheapest pump for the duty will probably be that which runs at the highest available
speed, whilst still being able to cope with the suction conditions on site over its full operating range.
However, it should be remembered that just one additional point of efficiency may be sufficient to
pay for the pump over its lifetime, through savings in energy costs. Thus, a lower speed pump, if it
is more efficient, may prove to be more economical in the long term. Another option which should
be considered is to split the flow, i.e. to have two or more pumps running in parallel (or even, very
occasionally, in series). This can also give flexibility if covering wide flow ranges. For more detail
of the efficiency implications of this, see section 7.1 below.

The chosen duty of the pump should not be over-estimated. This frequently happens when
allowance is made for a possible future increase in demand, and/or the system designer has been
prudent and over-sized the system, and/or the purchaser has added his own ‘safety’ margin.
Certainly the problem can be overcome by throttling the flow with a valve. However, deliberately
restricting the system flow is far inferior to better matching of the pump to the actual system
requirements in the first place. All throttling results in an unnecessary increase in energy costs, and
can lead to other operational problems as explained earlier in section 4 and Fig 2.

Fig 3.
Illustration of the effect of throttling a pump

20

Fig 3 shows what happens if a pump is over-sized. QB represents the flow required at the chosen
duty. The curve passing through points A and C is the normal system curve, i.e. the variation of
head across the pump if flow increases from zero to QB, QA and beyond. The pump head/flow
curve (passing through A and B) meets the normal system curve at point A, so that the pump
operates at head HA delivering flow QA. Since QA is greater than the flow required (QB), the pump
is over-sized.
In order to reduce the flow from QA to QB, the discharge valve must be partially closed to throttle
the flow. This produces a new system curve passing through point B, so that the pump now
produces the required flow QB, but is working at the higher head HB. If the pump had not been
over-sized, flow QB would have been obtained by a pump head/flow curve passing through point C,
so that the pump would only be working at head HC. Thus, the difference between HC and HB is
purely head lost in the throttle valve, and therefore wasted energy. (For this illustration, the small
variations shown in power and efficiency should be ignored.)

6.2 Impeller modifications to match the duty
The need for throttling can be avoided by reducing the diameter of the impeller and thereby
eliminating this unnecessary energy loss. Just looking at best-efficiency points (black dots), Fig 4
shows that the power absorbed by a reduced diameter impeller D2 is considerably less than that
absorbed by a maximum diameter impeller D1, whilst that absorbed by the minimum diameter D3
is less again. Usually manufacturers offer the same pump casing with a range of impeller diameters
because of this. Manufacturers may also offer different designs of impellers for one casing, to cope
with higher or lower flows at better efficiencies than are given by the ‘standard’ impeller.

Fig 4.
Pump characteristics showing various impeller diameters

In the case of axial flow pumps, reducing the impeller diameter is not practical. In this case the
pump performance can be changed by altering the angle setting of the blades. This is usually a
permanent alteration but some pumps do have blades which can be reset after manufacture or even
during operation.

Pumps are not usually made to standard duties. This makes comparing efficiencies less simple than
with products that are made to standard duties (such as motors).

21

6.3 The selection process
Fig 5 gives a very rough indication of the head/flow coverage of basic pump types when running at
speeds of up to 3000 rev/min. (Some pump types will always run slower than this.) This plot will
help when deciding which pump type is most likely to suit the chosen duty. Pumps can be provided
to work beyond these ranges but will mostly be special designs.

10000

Multistage

1000
Head (m)

100 Single Entry Double Entry
Single Stage Volute Single Stage Volute

Mixed Flow
10
Axial Flow

1
10 100 1000 10000
Flow (m3/h)

Fig 5.
Indication of head and flow coverage of basic pump types

When selecting a pump from an existing range, a manufacturer will use “tombstone” curves, which
show their ranges of pumps to cover a range of duties (Fig 6). The ideal duty will be towards the
right of the top of a tombstone, at the point which corresponds to the BEP of the selected pump.
(Each tombstone is built up from the individual pump curves such as that shown in Fig 4).
However, for economic reasons manufacturers have to restrict the number of pumps that they offer.
This means that even a manufacturer of particularly efficient pumps may lose out when quoting an
efficiency in competition with a less efficient pump, whose BEP just happens to be nearer the
requested performance. The worked example in section 6.4 below makes this clearer.

22

Fig 6.
‘Tombstone’ curves for the selection of pumps by duty

23

6.4 Worked example

BEP (B)

BEP (A) = 86%
= 82% 83%
84 80%

Desired (Quoted) 82 Pump B
Duty Point
80%

Actual (Installed) 77%
Duty Point Pump A
Head

Pump Efficiency Pump A Pump B
Flow
Peak (BEP) 82% 86%
At desired (quoted) duty point 81.5% 80%
At actual (installed) duty point 79% <77%

A user requests quotes for a pump at a particular desired duty. Manufacturers A and B offer the
pumps shown, which are the best that they can offer from the ranges that they have. (These two
pumps are excerpts from two manufacturers’ ranges of the type shown in Fig 6).

There are two important points to note:

While pump B has a higher BEP, pump A actually has a higher efficiency than pump B at the
desired duty.

Over-specifying the duty means that at the actual installed duty, the efficiency of the pump will be
considerably less than quoted. (In this particular case it would be better to reduce the diameter of
the impeller further, to suit the installed duty without throttling, or perhaps to use a quite different
pump to either of those quoted for.)

6.5 Importance of pump operating speed
Often a manufacturer will offer the same pump at different motor speeds to allow the one pump to
be used over a much wider range of duties. For instance, changing from the most common 4-pole
motor to a faster 2-pole motor will enable the same pump to deliver twice as much peak flow at 4
times the head. Of course, using a relatively high speed pump will not be possible if suction
conditions are not adequate. (The effect of running a pump with 4 and 2 pole motors is the same as
what happens when running at 50% and 100% speeds as shown in Fig 7 below).

Variable Speed Drives allow a pump to operate efficiently over a wide range of speeds and hence
duties, and so are very good for saving energy (Fig 7). They are particularly useful in systems
where there is a wide variation in demanded flow.

24

Fig 7.
Effect of speed reduction on pump characteristics

What this all means is that the same basic pump can serve different duties depending on both the
diameter and design of impeller fitted and the speed of the motor chosen. The power consumption
will vary with these parameters and with other factors such as liquid specific gravity and viscosity.
The size of motor required therefore needs to be determined for each application.

7. Optimising the pump efficiency
It is not possible to decide whether the efficiency of a pump being quoted is high or low without
some sort of benchmark. This section is intended to provide some assistance in this respect.

7.1 Allowing for the effect of Specific Speed
The Specific Speed (Ns) of a pump is a number which tends to define its shape and performance. It
may be given in any units of speed, flow and head. The most common units for these variables in
the UK are speed in revolutions per minute (rev/min), flow in cubic metres per hour (m3/h) and
head in metres (m).

To determine the Specific Speed (Ns) of a pump, enter Fig 8 at the best-efficiency head and flow
and read off ‘K’.

Then: Ns = K x (rev/min) ………… (1)
1000

25

100000 20,000
40,000
10,000
5000
2000 Based on formula:
1000
500
10000 200
Ns = (rev/min) x (m3/h)0.5
100 m0.75
50
20
10

1000
K

100

10

Flow
(m3/h)

1
1 10 100 1000 10000
Head (m)

Fig 8.
Plot to determine value of K

Roughly speaking, at Specific Speeds below about 3500 the impeller can be considered to be of the
‘Radial Flow’ type. Above about 11000 Specific Speed, the impeller can be considered to be of the
‘Axial Flow’ type. Between these approximate values, the impeller can generally be considered to
be of the ‘Mixed Flow’ type. (Note that there is no universal standard for deriving Specific Speed.
Speed, flow and head may be used in a wide variety of units, so great care must be taken to
ascertain which units are being used when a Specific Speed is quoted.)

These designations are reflected in the shapes of the impellers, as shown below:

Radial Mixed Axial

Optimum Specific Speed occurs at about 2650. At Specific Speeds higher and lower than this, for a
given family of pumps of similar size (basically the same flow and speed), efficiency falls away at
an ever increasing rate. As mentioned in section 6.1 above, the pump speed can be selected to
improve efficiency by moving the pump Specific Speed closer to optimum. Also, the required duty
flow can be split by using two or more pumps running in parallel, again moving the Specific Speed
of the individual pumps closer to optimum and thus improving pump efficiency.

26

A guide to the number of points of efficiency (C) to be added to a quoted efficiency figure in order
to bring it to around the value of a pump of the same flow but of Optimum Specific Speed is
provided by Fig 9. (Note that ‘one point of efficiency’ is defined as the difference between, say,
66% and 67%.)

Thus: ‘Equivalent efficiency’ at Optimum Specific Speed = Quoted efficiency + C …….. (2)

This ‘Equivalent efficiency’ at Optimum Specific Speed can then be compared with other pumps
using plots such as Figs 10 and 11 below.

16

14

12
Points of efficiency = C

10

8

6

4

2

0
0 1000 2000 3000 4000 5000 6000 7000 8000 9000 10000 11000 12000 13000 14000 15000
Specific Speed of pump stage = Ns

Fig 9.
Plot to determine value of C
7.2 Attainable efficiency levels
The plots on Figs 10 and 11 below give a rough guide to the mean Best Efficiency levels of
rotodynamic pumps at Optimum Specific Speed. These should not be taken too literally, since they
are based on fairly small samples and efficiency variation can be very wide for some pump types
(e.g. in the case of Single Entry Volute - Solids Handling pumps, the pump geometry (and therefore
efficiency) depends on the solids size, shape, concentration and hardness, on the pump material
chosen, on the impeller design and on the method of shaft sealing).

To use the plots, the Specific Speed (Ns) at a pump’s chosen duty should first be calculated using
formula (1) in section 7.1 above. Then its quoted efficiency should be converted to Optimum
Specific Speed, using formula (2) in section 7.1, before comparing with Figs 10 and 11. In most
cases this derived efficiency at Optimum Specific Speed is unlikely to come very close to the
plotted efficiencies, since the pump’s chosen flow will probably lie above or below Best Efficiency
flow and/or the impeller diameter may be reduced. However, the curves do provide a rough
benchmark, by indicating the sort of efficiency that can be obtained if it is possible to find a pump
which is close to Best Efficiency at the chosen duty. For illustration of the procedure, see the
worked example below (section 7.3).

27

90 90
Double Entry Volute
Pump Best Efficiency at Optimum Specific Speed

85 Single Entry Volute - Conventional 85

80 80
(%)

75 75
Single Entry Volute - Conventional
Double Entry Volute
Mixed Flow Volute
70 70

Single Entry Volute - In-Line Single Entry Volute - Non-Clogging
Two Stage Volute
65 65

Single Entry Volute - Solids Handling

60 60
10 100 1000 10000

Pump Flow (m3/h)

Fig 10.
Mean Best Efficiencies of Volute pumps

90 90
Pump Best Efficiency at Optimum Specific Speed

Axial Flow Well

85 85

Single Stage Well
Multistage Well
80 Mixed Flow Bowl 80
Multistage Radial Split
Multistage Axial Split
(%)

75 75

Multistage Barrel Casing

70 70

65 65

60 60
10 100 1000 10000
3
Pump Flow (m /h)

Fig 11.
Mean Best Efficiencies of Multistage and Well pumps

28

7.3 Worked example

Chosen duty: 1000 m3/h at 120m.
Chosen pump type (Fig 5): Double Entry Volute.
Quoted pump performance: 78% efficiency at 1460 rev/min.
Value of K from Fig 8: 870.
Ns from section 7.1, formula (1): 870 x 1460 = 1270.
1000
Value of C from Fig 9: 5.
‘Equivalent efficiency’ from
section 7.1, formula (2): 78 + 5 = 83%.
Mean Best Efficiency from Fig 10: 87%.
Action: Seek further quotes.

In this example, if the quoted pump performance had been at 2900 rev/min, K would be the same
but Ns would nearly double to 2520. Since this is practically Optimum Specific Speed, the quoted
efficiency would probably have been several points better. It is therefore assumed that in this case
the Net Positive Suction Head available to the pump was too low to permit the higher running
speed.

8. Useful Pump information

8.1 Total Head “H”
In the pumping technique there are more alternatives of mutual positions of a pump and a tank
when pumping through a simple piping system. This arrangement is described in detail on Figures
8.1 and 8.2).

Figure 8.1
Pumping system with various arrangement in negative NPSH operation

29

Figure 8.2
Pumping system with various arrangement in positive NPSH operation

A open discharge tank with piping mouthing under free water surface
B closed discharge tank with free outlet from pipeline
C closed discharge tank with mouthing of piping under level
D open tank in negative/positive NPSH arrangement
E closed tank in negative/positive NPSH arrangement
Hgs geodetic NPSH (difference of levels with discharge branch centre line for the case of the pump
situated above suction tank)
Hgn geodetic positive NPSH (difference of levels with discharge branch centre line for the case of
the pump situated below suction tank)
z difference in elevation of discharge branch above suction branch
p’m atmospheric pressure in suction tank with negative/positive NPSH
p’’m atmospheric pressure in discharge tank
pb barometric pressure (in open tank)
ps pressure in pump suction nozzle
pv Pressure in pump discharge nozzle
vs liquid velocity in pump suction nozzle
vv liquid velocity in pump discharge nozzle

H = Hg + ( p" - p' ) /ρ.g + ( v"2 - v'2) / 2.g + Σ Hz [m]

1 2 3 4
static part dynamic part

The value H is called total head. The total head (relation 1.2) has its static share expressed by terms
1 and 2 and the dynamic part (depending on v2 by terms 3 and 4) on the right hand side of the
equation.

Hg elevation head – difference of liquid level in suction and discharge tanks
(if the discharge piping is mouthing above the liquid level in the discharge tank, see
the alternative B in the figs. 1.7 and 1.8, the elevation head Hg refers to the
centerline of the discharge cross section).

( p" - p' ) /ρ.g gauge head – pressure difference above levels in suction and discharge tanks.

30

(In case of two vented tanks with atmospheric pressure p’’ = p’ = po the gauge head
equals to 0).

( v"2 - v'2) / 2.g velocity head – difference of velocity heads in the tanks

(Very often this term is negligible as velocities of level differences in the tanks are
usually very small.)

Σ Hz friction head loss. At flowing of some actual (viscous) liquid the equation hydraulic
friction losses (local and longitudinal) ∑Hz should be involved and added to the
single enumerated heads as well as inlet and outlet head losses of the piping system.

All components of the head H are in [m]; pressure p [Pa], velocity v [m/s],density ρ [m3.kg-1],
gravitational constant g in [m.s-2].

Practically we can often neglect the term of velocity heads. In case the tanks B, C and E (figs. 1.7
and 1.8) are closed, the equation (1.2) is simplified to the formula:

H = Hg + ( p" - p' ) /ρ.g + Σ Hz [m]

For open tanks A as well as D other simplification occurs (p’’ = p’ = pb). The total head is then
calculated as follows:

H = Hg + ∑ Hz [m]

This simplified formula is very often used in practical applications.

8.2 Speed of Rotation

If the pump is driven by an electric motor (squirrel cage asynchronous motor), the following basic
rates of speed are available that are calculated from mean values of pump asynchronous electric
motors:

Pole 2 4 6 8 10 12 14
number
50 Hz 2900 1450 960 725 580 480 415
60 Hz 3500 1750 1160 876 700 580 500

8.3 Pump power input calculation

Centrifugal pump power input is the mechanical power input consumed at the pump coupling or
shaft from the drive and is calculated acc. the following formula:

P = ρ.g.Q.H / 1000.η [kW]

where density ρ is in kg/dm3
gravity g is in m/sec2
pump flow Q is in l/sec
pump head H is in m
pump efficiency η is in %/100

31

8.4 Motor power output

Drivers used for driving pumps must perform the required power output corresponding with
requirements of any operation conditions ( see power input in the whole working area on pump
performance curve).

In practice there is used reserve for motor output acc. to figure 8.3 ( from standard ISO 9908):

Figure 8.3
Required driver power output as percentage of pump power input for range of
application from 1 to 100 kW

8.5 Net Positive Suction Head NPSH

NPSHR – “net positive suction head required” characterize suction ability of pump and is
determined by pump supplier.

NPSHA – “net positive suction head available” is done by pumping system on suction side.

It is necessary for correct pumping: NPSHA > NPSHR

8.5.1 NPSHA calculations

Figure 8.4
NPSHA examination in suction mode for horizontally and vertically installed pump

32

NPSHA is calculated in this case according to the following formula:

NPSHA = ( p' - pt ) / ρ.g + c'2 / 2.g - Hzs - Hgs ± s' [m]

where c’ – velocity of decrease of suction tank free surface
s’ – vertical distance of suction nozzle to impeller inlet centerline
pt - vapour presure

If pumping cold water from the open tank (fig. 1.15) at zero altitude the previous formula is
simplified to the formula that is sufficiently precise for practical application:

NPSHA = 10 - Hzs - Hgs ± s' [m]

8.5.2 NPSHA - at positive NPSH pumping mode (pump below inlet tank)

Figure 8.5
NPSHA examination in positive NPSHA mode for horizontally and vertically installed pump

At positive NPSHA operating mode (fig. 1.16) the pump is installed conversely below the inlet
tank free liquid level. In the preceding formulas –Hgs is changed to +Hgn:

NPSHA = ( p' - pt ) / ρ.g + c'2 / 2.g - Hzs + Hgn ± s' [m]

If pumping cool water from the open tank (fig. 1.16 in the left) at zero altitude the preceding
formula is simplified to the formula sufficiently precise for practical application:

NPSHA = 10 - Hzs + Hgn ± s' [m]

9. Life Cycle Cost (LCC)
It is likely that the design of the pumping system and the way the pump is operated will have a
greater impact on the energy consumption than the pump efficiency alone. An LCC analysis should
always be carried out to compare different technical alternatives of designing, operating and
maintaining a pumping system. The LCC represents the total expenses to purchase, install, operate,
maintain and repair a pumping system during its projected life. Down-time and environmental costs
are also considered.

A well-documented guide has been published by Hydraulic Institute and Europump (Ref 6). The
guide explains how the operating costs of a pumping system are influenced by system design, and
shows in detail how to use an LCC analysis to estimate these costs. Using the recommendations of
that guide, not only the initial investment cost should be taken into account, but also all the others
costs and expenses to operate the system during its projected life.
33

10. Useful References
o ‘NPSH for Rotodynamic Pumps’, Europump Guide No. 1, 1999.
o ‘Efficiency prediction method for centrifugal pumps’, Hydraulic Institute, 1994.
o ‘Centrifugal pumps and allied machinery’, Anderson, H.H., Elsevier Advanced Technology,
1994.
o ‘Theoretically attainable efficiency of centrifugal pumps’, Stoffel, B. and Lauer, J., Summary
of the final report on the research project for VDMA, Technical University of Darmstadt, 1994.
o ‘Attainable efficiencies of volute casing pumps’, Europump Guide No. 2, 1999.
o ‘Pump life cycle costs: A guide to LCC analysis for pumping systems’, Europump and
Hydraulic Institute, 2000. (ISBN 1-880952-58-0)
o ‘Study on improving the efficiency of pumps’, Report produced for the European Commission
– SAVE, 2001.
o ‘European Guide to Pump Efficiency for Single Stage Centrifugal Pumps’, SAVE Project Team
and EUROPUMP, 2003.
o Variable Speed Pumping : A Guide to Successful Applications’, Europump and Hydraulic
Institute , 2004 .(ISBN 1-85617-449-2)
o System Efficiency : A Guide For Energy Efficient Rotodynamic Pumping Systems – Written
and Published by Europump.

11. Acknowledgement

This Guide was originally written by David T Reeves, Pump Engineering Consultant.
Members of the Europump Technical Commission in particular;
John Bower – Flowserve
Jan Nevěřil –SIGMA Group a.s.
Aldo Janigro – Assopompe
Steve Schofield – BPMA
Have subsequently modified the guide to suit a European marketplace in doing so they wish to give
reference and thanks for David’s original work.

12. Further information
For further information please contact :

Europump General Secretariat
Diamant Building, Blvd. A.
Reyers 80 B-1030 Brussels
Belgium
Tel: +32 2 706 82 30
Fax: +32 2 706 82 53
E-mail: secretariat@europump.org
Web: www.europump.org

.

34

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