COMPONENT 1: PUMPING AND PUMP SELECTION
1. INTRODUCTION
Transportation of solids through a pipeline using fluids dates back to the early application of
dredging in the mining industry. Now that transport costs are becoming a significant
component of total production costs, the use of slurry pipelines is beginning to receive
attention once more. Factors favouring slurry applications include economies of scale (low
unit capital costs and power requirements) and relatively high reliability. In addition, slurry
pipeline systems have very low operating costs, low labour requirements, relatively immune
from the effects of escalation, safe and low impact on the environment relative to
alternative modes of transportation.
Unlike all other forms of transportation, slurry pipelining is a static system, i.e. material
move in relation to carriage medium. For example in trucks, rail, and belt systems, carriage
medium moves while payload is motionless except at transitional points.
The numerous solids such as coal, copper, iron and phosphate concentrates as well as
limestone are being transported by pipe network in slurry form in many operations around
the globe. Long distance transportation includes pumping of gold, lead, zinc, nickel, bauxite
and oil sands slurries.
The purpose of this lecture is to describe components of a slurry transportation system and
special design considerations for each component.
Figure 1. Pipe installation for transporting slurry
2. ECONOMIC FEASIBILITY
Slurry transport has proven to be technically and economically viable in transportation of
coal, iron ore concentrates, sulphide concentrates, limestone (for Portland cement
1
manufacture) and phosphate minerals. Economically feasible slurry pipeline projects tend to
have large point-to-point volumes and capacity to maintain such volume in rugged and
inhospitable terrains.
Slurry pipelines have significant initial capital costs but low operating costs and therefore
have relatively low exposure to cost escalation. However it is always prudent to compare all
possible modes of transport before settling on a particular choice based on the prevailing
needs.
The economic benefit in selecting a slurry pipeline as a mode of solids transportation has
proven itself in many applications. Some of the main factors, which affect the economics of
a slurry transport system, are the tonnage and distance transported, existing infrastructure,
physical characteristics of the solids and terrain conditions along the pipeline.
Slurry pipelines have an aesthetic advantage in addition to commercial advantages over
other modes of transport. In most case pipes are buried below surface with only few
structures or facilities exposed, even then structures are far apart. Land where pipes are
buried can be used for agricultural purpose compared to, for example, belt conveyors where
their installation affects movement of livestock. This makes pipelines are more
environmentally friendly due to low levels of noise, almost zero liberation of dust and less
negative visual impacts. Furthermore, efficient use of energy results in lower greenhouse
gas emissions compared to alternate options.
Figure 2. Pipeline traversing through mountainous terrain
3. PIPELINE HYDRAULIC CONSIDERATIONS
The design of a slurry pipeline is determined largely by hydraulic considerations. The solid
particle size distribution selected for the slurry will have a major impact on the whole
transportation system (including pumps, slurry preparation and the infrastructure). Particle
2
size distribution selected should be manageable and lead to minimization of preparation
costs, pumping costs and dewatering costs (on the other end of the pipeline) while at the
same time maintains favourable hydraulic characteristics during transportation.
Once the solid particle size distribution has been defined, ratio of liquid to solid (slurry
composition) must be determined, bearing in mind geological and hydraulic properties of
the conveyed solids. Normally solids concentrations in the slurry are between 40% and 65%
by weight.
Hydraulic design involves determination of critical velocity or the lowest permissible mean
flow velocity which ensures deposit-free (settlement) transportation. If the average flow
velocity is below critical velocity, particles will begin to deposit and creep at the bottom of
the pipe. As deposited particles creep along the bottom pipe wall, wear is induced especially
if material is abrasive in nature. In addition, creeping material can result in frictional
pressure losses which lead to further reduction of flow velocity. Because of these adverse
effects, it is prudent to operate slurry pipelines at flows above critical velocity.
Pipe friction pressure loss, particle attrition, pipeline plugging, transient flow, slack line flow
and cavitation (the rapid formation and collapse of vapour pockets in flowing liquids in
regions of very low pressure, a frequent cause of structural damage to propellers and
pumps) are among hydraulic characteristics that must be considered when designing a
slurry pipeline.
3.1.
Pump Station Design
Slurry pipelines will have one or more pump stations at appropriate locations along its
length. The size and location of stations will be determined by a steady state hydraulic
analysis. Both centrifugal and positive displacement pumps can be used to pass slurries. The
required discharge pressure dictates the choice.
Centrifugal pumps are low-head, high-volume devices and are often used for in-plant
pumping and providing suction for the mainline pumps. Pulsation dampeners, accumulators
and/or signal biasing circuits should be used to reduce flow-induced pressure pulsations.
Standpipes can be a very effective method of reducing pulsations on the suction side of
positive displacement pumps. Slurry pipeline systems need not to operate as “tight-line”
systems. Each pump station may well have an agitated storage tank on its suction side.
Centrifugal pumps are the most widely used type of pump in the chemical industry. A
centrifugal pump, in its simplest form, consists of an impeller rotating inside a casing. The
impeller imparts kinetic energy into the fluid. The velocity head, which is created by moving
3
fluid from the low-velocity at the centre to high-velocity on the edge of the impeller, is
converted into a pressure head when the fluid leaves the pump.
3.1.1. Advantages of centrifugal pumps
 Simple to construct
 Low cost operation
 Fluid is delivered at uniform pressure without shocks or pulsations provided there is a
constant intake
 The discharge line may be throttled (partly shut off) or completely closed without
damaging the pump
 They are able to handle liquids with large amounts of solids
 They can be coupled directly to motor drives
 There are no valves involved in the pump operation
 They have lower maintenance costs than other types of pumps
 They are available in a wide range of sizes
3.1.2. Disadvantages of centrifugal pumps
 They cannot be operated at high heads
 They must be primed
 They are prone to air binding which normally leads to heating up of the shaft and
impeller
 Maximum efficiency ranges over a fairly narrow range of conditions
 They do not handle highly viscous fluids efficiently
4
Figure 3. Pump station
4. SLURRY PREPARATION AND UTILISATION
The solid portion of the slurry must be crushed to the specified size distribution before
entering the system. Crushing and/or grinding may be necessary. Several slurrification
techniques use devices such as gravity feed chutes and hopper-shaped sumps.
In order to build flexibility into a slurry transport system, storage facilities will be required at
the terminal locations. Storage facilities enable the system to be operated at steady state
conditions i.e. fluctuations in volume can either be taken up by storage tanks or stored
material can be fed back into the system.
Various techniques are available for dewatering mineral slurry. Vacuum and pressure filters,
centrifuges, hydro cyclones and thermal drying are examples of such techniques. In practice
combination of techniques are used.
4.1.
Instrumentation and Controls
The control of a slurry pipeline system is similar to that of regular crude oil pipelines in many
respects. A Supervisory Control and Data Acquisition (SCADA) system is used to monitor and
control process variables at various locations from a central control point. Some pump
stations may be fully or partially automated and require few if any operating personnel. The
initial or primary pump station should use rate of flow of material as the principal control
parameter with override systems providing for flow, suction and discharge pressure
controls. Booster or secondary pump stations should be installed on the suction pressure
side with override systems being on the discharge side. Control valves should be used
sparingly and limited to start-up, shutdown and bypass-type situations.
5
The initial pump station area is a critical location for process monitoring and control. The
slurry must be inspected to assure the solid-liquid mixture has the required properties
before it is passed into the pipeline. Injection of incorrect slurry mixture into the hydraulic
system could cause problems. Density of the slurry must be monitored because improper
density can lead to formation of slurry plugs or create undesirable friction pressure drops.
A section of pipe before the first mainline pump station should be earmarked for
determining friction pressure drop that can be expected in the pipeline system. Slurry
particle size distribution should be checked periodically. Finally, slurry acidity or alkalinity
should be maintained at a level that will reduce erosion and/or corrosion of pipeline.
4.2.
Overall System Optimization
The construction of a slurry transportation system can be an expensive undertaking. Thus,
for a particular project, there is a considerable economic benefit to optimise the total
system. This optimisation can be achieved by selecting the slurry preparation, pipeline
pumping, slurry utilisation system with minimum cost. However, this selection process is no
small task. A pilot plant study may be required for the various elements of the system to
determine a cost equation that is a function of several variables. Crushing-grindingpreparation costs must be determined for slurries of different particle size distribution,
concentration and quality.
Test loop studies are necessary to estimate the pressure loss in pipelines of various
diameters carrying slurries at different velocities, concentrations and particle size
distributions.
An overland slurry transportation facility is a system of pipelines, pump stations and
associated process facilities working together to move a water-crushed mineral mixture. At
the head of the system is the slurry preparation facility. Grinding and slurrification
equipment produce a controlled solid-water mixture for injection into the pipeline system.
The pipeline is sized and designed by considering the hydraulic characteristics of the solidliquid two-phase flow. Pump stations are positioned at appropriate locations along the
pipeline to energise the system.
Several types of pumps may be utilised, but again consideration must be made for the twophase nature of the flow. The terminal point of slurry system will have facilities and
equipment for storing, thickening and dewatering the slurry. With growing environmental
concerns, the water from the liquid-solid separation step may require clarification or other
treatment prior to discharge. However it is a good idea to consider recycling of water
especially in South Africa where there is critical shortage of water. Throughout the
transportation facility, instrumentation and controls will be used to measure critical
variables such as flow rate, pressure and density.
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5. TAILINGS DISPOSAL SYSTEMS
Due to greater demands on tailings pipeline systems, recent designs reflect increased
sophistication and use of new construction materials. Mineral processing plant tailings, coal
washing refuse, scrubber sludges, fly ash, smelter slag, tar sands, and other industrial
wastes are frequently transported to their disposal sites by slurry pipeline.
There is a shift towards better tailings disposal systems. Forces behind the shift are longer
distances to be traversed in order to dispose material, higher concentrations with view of
conserving water, environmental concerns and longer tailing dam lives. Pragmatic, costeffectiveness and pumping systems which provide reliability and flexibility, are essential for
efficient tailings disposal systems.
A slurry transport system design incorporates the following activities:
 Site and route selection
 Slurry preparation
 Laboratory testing
 Dynamic modelling and computer simulation
 Pressure analysis
 Pipeline material specification
 Slurry pipeline design
 Construction management
 Pump, choke, valve and cyclone station design
 De-watering
 Product storage and reclaim water system
 System controls
 Leak detection system design
 Plant start-up and operations
 On site loop testing
Some specific applications include sub-sea tailings placement (STP), thickened (or paste)
tailings transport and backfill systems. Expertise in slurry systems includes laboratory
testing, computer modelling/simulation, overall system design, slurry preparation, process
control, de-watering, and product utilization.
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Backfilled area
Figure 4. Tailings used for backfilling in cut-and-fill mining method.
6. LABORATORY TESTING
Although a great deal of commercial experience is available for a wide range of materials, each new mineral
deposit must be analysed so that its slurry pipeline characteristics can be correlated.
A slurry laboratory provides important input data for the computerized design models. The laboratory should
have the capability of performing all bench-scale tests that are required for slurry systems design using only
small samples, thus eliminating the need for costly large scale loop testing.
The testing procedures include rheological analyses for defining hydraulic parameters and corrosion properties
of material for purposes of selecting pipe wall corrosion allowances and chemical corrosion inhibitors. There
are also tests to determine the abrasivity of the slurry on mechanical equipment such as pump parts. There are
also tests to define the pipeline operating conditions, including restart after system shutdown.
7. CARRYING CAPACITY OF CONTINUOUS FLOW FLUID TRANSPORT
The carrying capacity of any hydraulic transport system can be expressed as:
𝑇 = 𝑎𝑠𝑣
Where a is average cross-sectional area of solids; s is solids density; v is fluid velocity.
If the volumetric concentration of solids is c, and the full area of the pipe flume is A, then:
8
𝑐=
𝑎
𝐴
Strictly speaking c is the actual concentration and not the delivered concentration, but
unless the speed is very low and closer to the speed that may cause settlement, the two
concentrations can be considered as equal.
The velocity required for fluid transportation must be greater than the velocity required to
cause the solids to “float” in an upward stream of fluid and a useful practical guide is:
𝑠−𝑟
)
𝑟
𝑣 = 𝐾√𝑑 (
Where K is a constant related to particle size; d is the pipe diameter; s is the solids density; r
is the fluid density. For pipe sizes above about 20in. (0.5m), the value of d can be considered
as 20in. (0.5m).
For suction and pressure systems, pressure difference of p = pi – po must be overcome in
order to induce motion inside the pipe, where pi is inlet pressure and po is the outlet
pressure. The pressure difference may be due to fluid friction on the conduit walls, sliding
friction of the solids is on the conduit walls, increase in potential energy of both fluid and
solids and/or conditions at inlet or outlet of the pipe.
The power required to induce motion inside the pipe is given by:
𝑊 = 𝑝𝐴𝑣 = 𝑝𝑄
Where 𝑄 = 𝐴𝑣 is the total volumetric flow
If the pressure is generated by a pump or a fan (compressor), the power of the driving
motor will also depend on the pump or fan efficiency, which is often about 75%. So a typical
value of overall efficiency of pump and motor is about 67.5%, assuming 90% motor
efficiency.
The four main components of the pressure differences are:
 Pressure due to fluid friction on walls.
 Pressure due to sliding friction of solids.
 Pressure required to overcome potential energy of fluid and solids.
 Pressure required to increase kinetic energy of fluid and solids.
Some of these pressure difference components may be neglected in particular
circumstances, but they may be important in other cases. Energy is also involved when
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temperature changes are considered, particularly with pneumatic transport, but in most
cases temperature can be ignored.
The pressure difference to be overcome by the fluid is thus:
𝑝 = 𝑝𝑓 + 𝑝𝑠 + 𝑝𝑝 + 𝑝𝑘
These pressures are determined in the following way:

Pressure due to fluid friction:
𝑓𝑙 𝑟𝑣 2
𝑝𝑓 = ×
𝑚
2
Where f is friction coefficient; l is conduit equivalent length; m is hydraulic mean radius.

Pressure due to sliding friction:
𝑝𝑠 = 𝜇𝑘𝑐𝑙ℎ 𝑔(𝑠 − 𝑟)
Where μ is coefficient of friction of the solids on the conduit; k is portion of weight
actually touching the walls (0.1 ≤ k ≤ 1.0); lh = l cos q (q is a pipe slope angle).

Pressure due to increase in potential energy:
𝑝𝑝 = 𝑔ℎ[𝑟 + 𝑐(𝑠 − 𝑟)]
Where h is an increase in elevation over l.

Pressure due to increase kinetic energy:
𝑣2
[𝑟 + 𝑐(𝑠 − 𝑟)]
𝑝𝑘 =
2

Overall pressure difference:
Where pi is intake pressure and p0 is discharge pressure.
𝑝 = 𝑝𝑖 − 𝑝0
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8. CONVEYING SLURRY ICE AT MPONENG MINE
Due to the ultra-deep level mining that most gold mines are involved in. The need to fight
the high virgin rock temperatures is at the top of the agenda of most mining houses. Ice and
its transport underground play a crucial role. In 1992 Mponeng Mine commissioned its
underground ice slurry plants for cooling purposes. The 1520kWh vacuum ice plant was
designed to produce 4 200t of ice slurry daily. The ice slurry and service water help the mine
to maintain the underground temperature at 27.5° wet bulb.
Generation and transportation of ice slurry underground came with the advantage water
and electricity savings.
It is recommended that students should familiarised themselves with the transportation of
ice slurry at Mponeng Mine and backfilling at Black Mountain Mine.
9. PUMP SELECTION
To move fluid from one point to another in a pipe, it is necessary to supply a driving force. In
some cases, gravity can be used to supply the driving force (i.e. when there is a difference in
elevations). In most cases, however, pumps or blowers must be used to supply the driving
force that is required to move the fluid.
Different types of pumps can be used to accomplish different tasks. For example,
mechanical-energy transferred from a pump to the fluid may be used to increase velocity,
pressure, or elevation of the fluid. As an engineer, you must become familiar with the
various types of pumps that you will encounter in the mining industry. You must also
become familiar with the types of calculations that must be performed in order to decide on
the size of the pumps that you will need to accomplish a given task.
9.1.
Pump Performance Curves/Characteristic Curves
There are many different factors, which determine the actual performance characteristics of
a pump. For this reason, it is best to use the actual experimental performance of the pump
for determining the size that is required. The performance characteristics of a pump can be
measured in-house or obtained from the pump manufacturer.
The performance curves which are supplied by the pump manufacturer will typically show
plots of developed head (pressure) vs. discharge (flow rate); efficiency vs. discharge, and
11
brake horsepower vs. discharge for various pump speeds. These plots are typically given for
water but for low viscosity fluids the plots will not change much.
Pump performance curves can be used to determine to the operating characteristics of a
pump under various process conditions.
9.2.
Sizing a Pump
This section provides an outline of the calculations that you will need to complete in order
to specify the pump sizes, which are required for a particular application.
Before you begin, you will need to determine the following:

Pump performance curves for one or more pumps. If you cannot obtain the
manufacturer specifications for a pump you can probably use data for centrifugal pump
specifications.

A detailed piping system. You need to decide whether your design will require storage
tanks, reactors, columns, etc. In addition, you may need to specify pipe dimensions,
column dimensions, etc.

Flow rates that will be required. Use the information that you have to determine the
flow rates through your process (e.g., annual production rates, specified feed rates,
etc.).

Calculate the fluid velocity from the pipe dimensions (inlet and outlet) and the
volumetric flow rate.

Estimate the friction losses in the piping system envisaged.
9.3.
Estimating Friction Losses in a Pipe
Fluid flow is always accompanied by friction and energy loss. This results in a pressure drop
in the direction of flow (the pressure downstream will be lower than the pressure
upstream). The pressure drop, hf (J/kg), is proportional to the square of the velocity, v (m/s),
the length of the pipe, L (m) and inversely proportional to the pipe diameter, D (m) and it is
determined by the following equation:
𝟒𝒇𝑳𝒗𝟐
𝒉𝒇 =
𝟐𝑫
12
In the laminar flow regime, the friction factor, f, can be found from the following equation:
𝒇=
𝟏𝟔
𝑵𝑹𝒆
Where the Reynold's Number, NRe < 2 100, for laminar flow. In the turbulent region, the
friction factor, f, is a function of the Reynold's Number, NRe, and the Relative Roughness
(𝑒⁄𝐷). The relative roughness parameter is dimensionless ratio of the absolute pipe
roughness e and the pipe diameter D. The value of f for a given set of conditions is generally
found from a Moody Friction Chart.
The friction losses that result from turbulent flow through various types of valves and fitting
are summarized below:
Type of Fitting
Friction
Loss,
Equivalent
Friction Loss, Number of
Length of Straight Pipe in Pipe
Velocity Heads, Kf
Diameters, Le/D
Elbow 45º
0.35
17
Elbow 90º
0.75
35
Tee
1
50
Return Bend
1.5
75
Coupling
0.04
2
Union
0.04
2
Gate Valve, wide open
0.17
9
Gate Valve, 1/2 open
4.5
225
Globe Valve, wide open
6.0
300
Globe Valve, 1/2 open
9.5
475
Angle Valve, wide open
2.0
100
Check Valve, Ball
70.0
3500
Check Valve, Swing
2.0
100
Water Meter, Disk
7.0
350
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The friction losses that occur for laminar flow through various types of valves and fittings
are summarized below.
Friction Loss, Number of Velocity Heads, Kf vs. NRe
Type of Fitting
50
100
200
400
1000
Turbulent
Elbow 90°
17
7
2.5
1.2
0.85
0.75
Tee
9
4.8
3.0
2.0
1.4
1.0
Globe Valve
28
22
17
14
10
6
Check Valve, Swing 55
17
9
5.8
3.2
2.0
You should also estimate the friction losses that occur due to sudden expansion and
contractions. Be sure to have a globe or gate value for each piece of equipment such as a
pump, tank, etc.
NOTE: Many students calculate pump sizes that are too small for their design project. This is
because students rarely account for the pressure losses, which occur because of valves. A
control valve, for example, requires a pressure drop of at least 5 to 10 psi to maintain good
control for a pump. These types of losses will affect your design calculations!"
The total friction loss that will result from the pipes, fittings, etc., in your process can now
be obtained by summing all of these contributions. This result will be used as the frictional
loss term, ∑ 𝐹, in the mechanical-energy balance equation.

Use the Mechanical Energy Balance equation (2.7-28, Geankoplis, p. 103) to determine
the actual or theoretical mechanical energy, Ws (J/kg), which must be added to the fluid
by the pump:
Mechanical Energy Balance (Incompressible Fluids)
(𝑝2 − 𝑝1 )
𝑎
( ) (𝑣2𝑎𝑣 2 − 𝑣1𝑎𝑣 2 ) + 𝑔(𝑧2 − 𝑧1 ) +
+ ∑ 𝐹 + 𝑊𝑠 = 0
2
𝜌
Where
a
= correction factor: 1.0 (turbulent), 0.5 (laminar)
v1av = average velocity (m/s)
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v2av = average velocity (m/s)
g
= gravitational acceleration (9.80665 m/s )
z1 = height (m)
z2 = height (m)
p1 = pressure (N/m )
p2 = pressure (N/m )
ρ
= density (kg/m )
ΣF = Sum of frictional forces (J/kg)
Ws = mechanical energy supplied by pump (J/kg)

Use the pump performance curves to eliminate pumps that cannot supply the necessary
total head. Select the most efficient pump from those that can supply the required head.

Use the values from manufacturers’ tables to obtain the fractional efficiency, n, of the
pump at the specified flow rate.

Calculate the shaft work delivered to the pump, Wp (J/kg):
𝑾𝒑 = −

𝑾𝒔
𝒏
Calculate the actual or brake power of the pump:
𝑩𝒓𝒆𝒂𝒌 𝒌𝑾 =

𝑾𝒑 𝒎
𝑾𝒔 𝒎
=−
𝟏𝟎𝟎𝟎
𝟏𝟎𝟎𝟎𝒏
Calculate the developed head of the pump, H (m):
𝑯=−

𝑾𝒔
𝒈
Calculate the total electric power input (kW):
𝑻𝒐𝒕𝒂𝒍 𝑬𝒍𝒆𝒄𝒓𝒊𝒄𝒂𝒍 𝑷𝒐𝒘𝒆𝒓 𝑰𝒏𝒑𝒖𝒕 (𝒌𝑾) =
𝑩𝒓𝒆𝒂𝒌 𝒌𝑾
𝑾𝒔 𝒎
= −
𝒏𝒆
𝟏𝟎𝟎𝟎𝒏𝒏𝒆
15
Typical Electric Motor Efficiencies (ne)
Power (kW)
Efficiency (%)
1/2
77
2
82
5
85
20
88
50
90
100
91
500
93
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SLURRY PUMP SELECTION
Calculate the Clean Water Pump Head [HCW] and Total Discharge Head [Hsl] for the
requirements of a work listed below and Select a suitable pump from the provided
manufacturer's chart.
Concentrations of Solid by Volume
CV
20%
Density of Solids
SGs
2.5 t/m
Requested flow
Q
150 l/s
Geodetic head
H
20 m
Pipe diameter
D
200 mm
Pipe length
L
300 m
Size of solids
d85
3
3 mm
17
Graphs and Formulae
STEP 1:
SG of slurry ?
SG conversion Chart A
read here
2.5
20
Calculate by using the formula aboe or use Cv and SGs points on the Chart A
3
SGsl=
1.30 t/m
or 1.28
18
STEP 2:
Critical velocity?
Table B: Critical Velocity V cr (m/s) for d85 and SG=3
Solid Size d85 (mm)
Pipe D (mm)
25
50
75
100
150
0.2
1.3
1.3
1.6
1.7
1.7
0.3
1.4
1.7
1.8
1.9
2.0
0.5
1.4
1.8
1.9
2.0
2.1
0.7
1.4
1.8
1.9
2.1
2.4
1.0
1.4
1.8
1.9
2.1
2.4
2.0
1.4
1.8
1.9
2.1
2.4
>5
1.4
1.8
1.9
2.1
2.4
200
300
400
1.8
1.8
1.8
2.0
2.1
2.1
2.3
2.4
2.5
2.5
2.7
2.8
2.5
2.8
2.9
2.5
3.0
3.1
2.5
3.0
3.6
SG correction graph C [ since the table above is for SG=3]
V cr=
2.5 m/s
Correction Factor=
V cr=
read from Table B
0.87
2.175 m/s
read from Graph C
Critical velocity
Q=
Actual velocity=
Vactual=
V=Q/A
4.78 m/s
A=
V cr *correction factor
0.15 m3/s
0.0314 m2
Actual velocity
Compare & Comment:
Actual velocity is higher than the critical velocity, OK!
If other way around, solids will settle inside the pipe and block the pipe.
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STEP 3:
Total Discharge Head?
Frictional Loss correction factor Chart D
40
30
Cv
20
10
1.0
1.1
1.2
1.3
1.4
1.5
1.6
1.7
1.8
Correction Factor
Correction Factor=
1.17
read from Chart D
Frictional Loss= Hfrsl= Frictional Loss x Correction Factor
Frictional Loss Chart E
100
[Requested Flow]
frictional loss factor
100
Frictional Loss=
30 m
Frictional Loss correction factor
Include Correction Factor= Hfrsl=
read from Chart E
(frictional loss factor/1000m)xPipe length
1.17 read from Chart D
35.1 m
frictional loss * Frictional loss correction factor
Total discharge Head=Hsl
Hsl=H+Hfrsl
H=
Hsl=
55.1 m
20
20 m
STEP 4:
Clean Water Pump Head?
Head Reduction DR factor Diagram F
0.045
2.5
3
HR factor K=
0.013 read from Diagram F
HR= 1-K(Cv/20)
HR=
0.987
Hcw= Hsl /HR
Hcw=
55.8 m
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STEP 5:
Choose a pump from the manufacturer's chart G
Hcw=
Q=
55.8 m
Q=
150 l/s
3
540 m /hr
Flow Rate scale is Logarithmic
Conclusion:
Pump Code No:150 is suitable for the work (read from the Chart G)
If the range is not available in the Chart G, check higher capacity pump charts from manufacturers.
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