Product Information
Slurry Pumps
2.0 PRODUCT INFORMATION
Page
2.1 Pump sizing ………………………………………………………....................2
- Slurry Formulas …………………………………………………………...4
- The Pipe system ………………………………………………………....6
- Laws for fixed impeller diameter ………………………………………15
- Laws for fixed Impeller speed ……………………………………….….16
2.2 Material options ……………………………………………………………….26
2.3 Pump testing …………………………………………………………………..34
2.4 Application guide ……………………………………………………………..34
2.4.1 General …………………………………………………….......……34
1. Selection of a Slurry Pump - by duty …………………........................….35
2. Selection of a Slurry Pump - by industrial
Application …………………………………………………………………...35
2.4.2 Selection of a Slurry Pump - by duty ……………………......……36
2.4.3 Selection of a Slurry Pump - by industrial
Application ……………………………………………………………41
2.5 Conversions and Equations …………………………………………………49
2.5.1 Table of useful conversions ……………………………………….49
2.5.2 Table of useful equations ………………………………………….50
2.6 Maximum possible vibration level …………………………………………...51
2.7 Sound level…………………………………………………………………….51
2.8 Standard allowable flange forces and moments for
Metso Minerals pumps ………………………………………………………52
2.9 Pressure ratings ………………………………………………………………53
2.0
BSR
10-W21
Edition 8
1/56
Product Information
Slurry Pumps
2.0
PRODUCT INFORMATION
2.1
Pump sizing
Modern sizing procedures for slurry pumps are computerised and easy to handle, as in
Metso’s”PumpDim™ for Windows”. It is important to know the steps for sizing slurry pumps and
the relationship between them, to ensure that these procedures are correctly understood.
The following manual procedure is approximate and gives reasonable accuracy, except in extreme
applications. For froth pumping, also see Section 9.0.
Installed in a piping system a Slurry Pump must be rated against the static head, any delivery
pressure requirement and all friction losses to be able to provide the required flow rate.
The duty point is where the pump performance curve crosses the system curve.
Note!
Never overestimate the system resistance. If over estimated, the Slurry Pump will:
Give a greater flow than required
Absorb more power than expected
Run the risk of overloading the motor (and in worst cases suffer
damage)
Poor suction conditions may cause Cavitation.
Suffer from a higher wear rate than expected
Always use the best estimate of system head. Add safety margins to the calculated power only.
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Slurry Pumps
The sizing steps
Step 1.
Establish if the slurry/liquid is a:
Clear liquid
Non-settling (viscous) slurry (Particle size < 50 micron)
Settling slurry
Step 2.
Set up the duty details. These vary depending on the type of liquid according to Step 1. Common
details are:
Slurry Flow or Solids Tonnage
Static lift (head)
Friction losses given or pipe system known/selected
Chemical properties like pH value, content of chlorides, oil, etc.
Other liquid/slurry details as below.
Clear liquids
When clear water - no further liquid details are required. For other clear liquids the following is
needed.
- Liquid S.G.
- Liquid dynamic viscosity. If kinematic viscosity is given, convert using this formula :
Dynamic viscosity = (Kinematic viscosity) x (Specific gravity)
Slurries
For slurries a number of details are required. According to the following formulas certain combinations
of these data are required to be able to calculate all of them.
Sm = Slurry S.G.
Cv = Concentration by Volume %
Cw = Concentration by Weight %
S = Solids S.G.
Q = Flow rate in m3/hour
tph = Tonnes per hour (solids)
QUS = Flow rate in US gallons per minute.
stph = Short tons per hour (solids)
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Slurry Pumps
Slurry Formulas:
Sm
CV =
CV =
=
C V (S - 1)
+1
100
(S m - 1) x 1 0 0
(S - 1)
1 0 0 x CW
[S(1 0 0 - C W ) + C W ]
CW =
1 0 0x S
100
+ (S - 1)
CV
Q = t ph x [
CW = 1 0 0 -[
1 100
+
- 1] m3/hr
s CW
Q US = 4 x st p h x [
1 0 0 - CV
]
Sm
1 100
+
- 1] USgpm
s CW
For non-settling (viscous) slurries also the plastic dynamic viscosity and max. particle size is
required.
For settling slurries max. and average particle sizes (d50 or d85) are required. Also, during the piping
system analyses check that the actual velocity in the pipe is higher than the critical velocity for
stationary deposition. Using particle size, solids S.G. and pipe diameter, determine this velocity from
the nomographic chart on Page 9.
If a pipe diameter has not been specified, the best way to arrive at one is to select the first pipe size
giving a velocity above 3 m/s (10 ft/s). This pipe size should be checked to ensure that the actual
velocity is greater than the critical velocity. The diagram on Page 10 can be used to find the velocity
and friction loss coefficient for a given pipe diameter and flow.
If the actual velocity is less than, or much greater than, the critical velocity, repeat the calculation for a
size of pipe smaller, or bigger, to check that the largest possible pipe is used to ensure that settling
does not take place, as well as to minimise friction losses.
NOTE:!! Always use minimum anticipated flow value to calculate the pipe velocity to avoid
settling problems.
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Edition 8
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Slurry Pumps
Solids tonnage or slurry flow ?
It is very important to understand the difference between”percent solids by weight” and”percent
solids by volume”.
Percent solids by weight are the normal way of describing a slurry.
Magnetite slurry, 40 % solids by weight (solids S.G.= 4.7).
Limestone slurry, 40 % solids by weight (solids S.G.= 2.6).
This is due to the practice that production in general is measured in solids tons/hour (or short
tons/hour), assume that for the above slurries:
Magnetite and Limestone feed to the circuits are both 300 tonnes/hour (331 stph).
These are not directly useful figures for a Slurry Pump man as pumps are volumetric machines and
must be sized on flow.
If we calculate the flow conditions of the above slurries, we will find that:
The magnetite slurry gives a slurry flow of 515 m3/hour (2267 USgpm).
The limestone slurry gives a slurry flow of 566 m3/hour (2493 USgpm).
As tonnage, these capacities are equal; but hydraulically they are not!
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Slurry Pumps
Step 3. The Pipe System
The total head in a liquid is the sum of the static head (gravitational energy), pressure head (strain
energy) and velocity head (kinetic energy). The head (energy), the pump has to supply to the liquid for
the required flow rate, is the difference between the total head at the outlet and inlet flanges
respectively.
As we do not know the conditions at the pump flanges, we must select a point on each side of the
pump where we do, and then allow for pipe work losses between these points and the flanges to
determine the total head at the flanges.
In the diagram above the total head is known at the liquid surface in the feed tank (Point 1) and the
outlet pipe exit (Point 2).
At point 1
Static Inlet Head
= H1
Pressure Head
= 0 (atmospheric pressure)
Velocity Head
= 0 (practically no velocity)
Therefore,
Pump Inlet Head
= H1 – inlet pipe losses
At point 2
Static Head
= H2
Pressure Head
= 0 (atmospheric pressure)
Velocity Head
= V22 / 2g
Therefore,
V2
= Flow velocity at Point 2 in m/s.
g
= Gravitational constant = 9.81 m/s2
Pump Outlet Head
= H2 + V22 / 2g + outlet pipe losses
Pump Total Head, H
= (Outlet head – inlet head)
H = (H2 + V2 2 / 2g + outlet pipe losses) – (H1 – Inlet pipe losses)
In practice is the pump suction bigger than the discharge, which makes the inlet velocity head small
and is therefore often ignored. A 3.0 m/s (10 ft/s) flow velocity does only generate a velocity head of
0.46 m (1.5 ft.).
Then
H = H2 – H1 + (V22 / 2 g) +outlet losses + inlet losses
The effect of pressurised inlet and/or outlet, e.g. pressurised tank or hydro cyclone feed, is allowed for
by adding the pressure value, in meters (feet) of liquid, to H1 or H2 as appropriate.
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Slurry Pumps
SLURRY EFFECTS ON FRICTION LOSSES
As for pump performance, slurries also affect friction losses since they behave differently to clear
water. The slurry has to be treated either as settling or non-settling (viscous).
Generally, slurries with particle size < 50 micron are treated as non-settling.
Friction losses for settling slurries
The assessment of friction losses for settling slurries is very involved, and best accomplished on
computer software such as Metso PumpDim6TM for Windows.
However, for short runs of pipe at higher velocities, head loss can be taken as equal to the water
losses. For approximate estimations the correction factor on the bottom of Page 10 can be used.
At low velocities, head loss is difficult to predict, and there is a real risk of solids settling out and
blocking the pipe.
The nomogram on Page 9 will provide a safe minimum velocity.
Friction loss calculations
Straight pipes
Similar to voltage drop in a power cable, there are friction losses in a pipe system.
The friction loss in a straight pipe varies with:
•
Diameter
•
Length
•
Material (roughness)
•
Flow rate (velocity)
The friction loss can either be:
2.0
1.
Looked up in a table
2.
Extracted from a Moody diagram.
3.
Calculated from semi-empirical formula, such as the
William & Hazen Formula.
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Slurry Pumps
Fittings
When a system includes valves and fittings, an allowance for additional friction is needed.
The most common method is called the ”Equivalent pipe length” method. The fittings are treated as a
length of straight pipe giving equivalent resistance to flow. See Table on Page 11.
TEL - Total Equivalent Length
TEL = Straight pipe length + equivalent length of all pipe fittings.
TEL is used to calculate the total friction losses in the system.
If software such as Metso’s "PumpDimTM for Windows" is not used then we recommend that you use
the table on Page 10 to calculate the friction losses.
Friction losses for non-settling slurries
Friction loss calculations for non-settling slurries are best accomplished with the aid of computer
software. However, there are numerous methods of making calculations manually, although these can
prove difficult with all the variables involved.
Whatever method is used, a full rheology of the viscous solution is necessary for any accurate
assessment.
Assumptions can be made but these can prove very inaccurate.
Summary:
It is very important that all the losses in a slurry system are calculated in the best way possible,
enabling the pump to balance the total system resistance, operate at the correct duty point, giving
correct head and capacity!
Use computer software PumpDimTM for Windows.
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Slurry Pumps
Nomograph chart for minimum velocity. (Adapted from Wilson, 1976).
Example :
2.0
Pipe dia. 250 mm
= 0,250 m
Particle size
= 0,5 mm (Worst case)
Particle S.G.
=3,8
Minimum velocity
= 4,5 m/s
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Edition 8
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2.0
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Edition 8
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Slurry Pumps
HEAD LOSSES IN VALVES, FITTINGS, ETC.
Resistance of Valves and Fittings frequently used on slurry pipelines.
Stated as approx. length in metres of straight pipe giving equivalent resistance to flow.
Pipe
Size
N.B
25
R>3xN.B.
Long
Radius
Bend
0,52
R=2xN.B
Short
Radius
Bend
Elbow
0,70
0,82
Tee
1,77
R>10xN.B.
Rubber
Hose
0,30
Plug Lub
Valve
Rect.
Way
Dia-phr.
Full
Open
Full
Bore
Valve
2,60
-
0,37
32
0,73
0,91
1,13
2,40
0,40
3,30
-
0,49
38
0,85
1,09
1,31
2,70
0,49
3,50
1,19
0,58
50
1,07
1,40
1,67
3,40
0,55
3,70
1,43
0,73
63
1,28
1,65
1,98
4,30
0,70
4,60
1,52
0,85
75
1,55
2,10
2,50
5,20
0,85
4,90
1,92
1,03
88
1,83
2,40
2,90
5,80
1,01
-
-
1,22
100
2,10
2,80
3,40
6,70
1,16
7,60
2,20
1,40
113
2,40
3,10
3,70
7,30
1,28
-
-1,58
125
2,70
3,70
4,30
8,20
1,43
13,10
3,00
1,77
150
3,40
4,30
4,90
10,10
1,55
18,30
3,10
2,10
200
4,30
5,50
6,40
13,10
2,40
19,80
7,90
2,70
250
5,20
6,70
7,90
17,10
3,00
21,00
10,70
3,50
300
6,10
7,90
9,80
20,00
3,40
29,00
15,80
4,10
350
7,00
9,50
11,00
23,00
4,30
29,00
-
4,90
400
8,20
10,70
13,00
27,00
4,90
-
-
5,50
450
9,10
12,00
14,00
30,00
5,50
-
-
6,20
500
10,30
13,00
16,00
33,00
6,10
-
-
7,30
Step 4. The next step is to select wet end wear part material.
Select material from the max. particle size according to the Table 1 in Section 2.2.
For clear liquids, metal pumps are the primary choice. Check chemical resistance of the selected
material by referring to Tables 2 and 3 in Section 2.2.
Step 5.Now we have to select the right type of pump by considering the operating costs, taking
into account wear, maintenance and energy usage.
Depending on the application, it can be a horizontal or vertical Slurry Pump.
It could also be a pump for extreme, heavy or normal wear conditions.
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Slurry Pumps
You can see which type of pump we recommend for various industrial applications by referring to
the Application Guide in Section 2.4. From this information, together with the wet-end material
choice, you can select a suitable pump.
From previous steps above, we know the slurry flow rate and pump total head.
By referring to the appropriate tombstone charts under each pump range you can find the suitable
pump size for this duty.
To establish the operating pump speed and installed driver power go to the performance curve for
the selected pump.
Since performance curves are for clear water, corrections may be required if other liquids or
slurries are to be pumped.
Step 6.
Clear water and Slurries with concentrations < 15% by Volume.
Mark the intersection point of the duty flow and pump total head on the upper section of the
performance curve, see example in figure below.
From this, you can determine the required pump speed.
The pump power input (P) required at this speed and duty flow is read from the lower curve.
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Slurries with high concentrations.
For settling slurries, consult the diagram below using average particle size d50 , solids S.G. and
concentration by weight, to obtain the de-rating factors of Head Ratio (HR) and Efficiency Ratio
(ER). HR and ER have the same value.
Divide the pump total head, H by the HR factor. Since the factor is <1, the corrected total head will
be of a higher value.
Mark the intersection point of the duty flow and corrected total head on the upper section of the
performance curve to establish the required pump speed.
Alternatively, read the speed from the curve for the duty flow at the pump total head, H, and then
use the formulae for fixed diameter impellers, see below, to calculate the operating speed for the
corrected total head.
From the lower section of the clear water performance curve, read the power at the intersection
point of the duty flow for this speed. The Efficiency Ratio (ER) is accounted for in this power value.
Now, Relative density = Slurry density / Clear water density.
Multiply the power by the relative density.
This result gives the slurry power required at the pump shaft.
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Slurry Pumps
Laws for fixed impeller diameter:
For change in speed with a fixed impeller diameter the following laws apply where: H = Head
Q = Capacity N = Speed P = Power
With Q1 , H1 & P1 at a given speed N1 and Q2 , H2 & P2 at the new speed
N2, the new speed is calculated:
Q1 / Q2 =
N1/ N2
or Q2 = Q1 x ( N2 / N1 )
H1 / H2 = ( N1 / N2 )2
or H2 = H1 x ( N2 / N1 )2
P1 / P2 = ( N1 / N2 )3
or P2 = P1 x ( N2 / N1 )3
Efficiency remains approximately the same.
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Slurry Pumps
Laws for fixed impeller speed
For a change in impeller diameter with a fixed speed the following laws apply where: H = Head,
Q = Capacity, N = Speed, P = Power
With Q1 , H1 & P1 at a given diameter D1 and Q2 , H2 & P2 at the new diameter D2, the new diameter
is calculated:
Q1 / Q2 =
2.0
D1 / D2
or
Q2 = Q1 x ( D2 /D1 )
H1 / H2 = ( D1 /D2 )2
or
H2 = H1 x ( D2 /D1 )2
P1 / P2 = ( D1 /D2 )3
or
P2 = P1 x ( D2 /D1 )3
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Non-settling slurries.
For non-settling slurries or viscous liquids the diagram below, from Hydraulic Institute Handbook, is
used to correct the pump performance. For non-settling slurries the true plastic dynamic viscosity is
needed, which can be found from a rheogram established by test work.
For Newtonian liquids other than clear water, the viscosity can be in either kinematic or dynamic
terms. See Step 2 for the equation to convert from dynamic to kinematic viscosity.
From the chart above, the correction factors for efficiency (CE), flow (CQ) and head (CH) can be read for
the required viscous flow and total discharge head at the known kinematic viscosity. The head correction
factor CH is taken from the curve marked 1.0 x QN.
Divide the duty flow and head by their respective correction factors and mark these values on the clear
water curve as explained earlier.
From this you can estimate the required pump speed, or calculate it from the formulae given earlier in
Step 6 (Laws for fixed diameter impellers).
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Slurry Pumps
From the lower performance curve, read the power at the above speed and flow. Multiply this by CH and
CQ, and divide by CE. Then, multiply the result by the relative density.
The resultant is the power required at the shaft to pump the liquid.
Step 7.
Check for cavitation.
We need to check the hydraulic conditions at the inlet (suction) side of the pump to prevent cavitation
from taking place.
Hydraulic conditions at the inlet.
To ensure that a Slurry Pump performs satisfactorily, the liquid must at all times be above the vapour
pressure inside the pump.
This is achieved by having sufficient pressure on the inlet side of the pump.
This pressure is called: Net Positive Suction Head, referred to as NPSH*, and is usually expressed in
meter (feet) of liquid column absolute.
Should NPSH be too low, the pressure in the impeller eye would decrease down to the lowest possible
pressure of the pumped liquid, the vapour pressure.
*The name NPSH is an international nomenclature and is used in most languages.
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Vapour pressure and cavitation
When the pressure in the impeller eye, near the vane edge, drops down to or below the liquid vapour
pressure, vapour bubbles start to form. These are carried by the liquid to locations under higher
pressure, where they collapse (implode) creating extremely high local pressures (up to 10,000 bar),
which can erode the pump surfaces.
These mini implosions are called cavitation.
Cavitation is not, as is sometimes stated, due to air in the liquid, but is the liquid boiling at ambient
temperature, due to the reduction in pressure. At sea level, atmospheric pressure is 1 bar (14.5 psi.),
and water boils at 100oC (212oF). At an altitude of 2800 m (9180 ft.), atmospheric pressure reduces
to 0,72 bar (10.44 psi.) and water boils at 92oC (198oF).
See table and diagram under heading ”NPSHa-calculations”.
A major effect of cavitation is a marked drop in efficiency, caused by a drop-off in capacity and head.
Vibrations and mechanical damage can also occur.
Cavitation is mainly a concern when:
• The site is at high altitude.
• When inlet losses are high, as can occur under suction lift conditions.
• When pumping liquids at a high temperature.
• When the pump is used at exceptionally high flow rates.
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Too low NPSH will cause cavitation!!
It’s important to check the NPSH during the sizing process and at start up.
How to calculate NPSH?
How do we know what NPSH (inlet head) we are looking for?
For all pumps, there is a required value for the NPSH known as NPSHr. This is not a calculated value
but is a property of the pump obtained by testing.
On pump curves, NPSHr is usually shown for various flows and speeds.
The inlet conditions of a given system control the available NPSH, known as NPSHa.
Note! The value of NPSHa must always exceed the value of NPSHr.
NPSH - calculations
We have to sum all positive pressure heads and deduct all losses in the piping system on the inlet side.
Centrifugal pumps on suction lift applications will require some kind of priming at start-up though NPSHa
may be adequate.
Some useful figures:
Atmospheric pressure, meters of water head, at different altitudes above sea level.
Altitude (m)
2.0
H2O Head (m)
0
10,3
1 000
9,2
2 000
8,1
3 000
7,1
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(m)
Vapour Pressure
10
8
6
4
2
20
40
60
80
100
o
Temperature (C )
Curve showing vapour pressure for water at different temperatures (oC.)
Formula for NPSHa calculation:
NPSHa = Hatm + H1 - Hf - Hvp.
Where:
Hatm =Atmospheric pressure in meters of liquid column.
H1 = Static Inlet Head (m). Suction lift gives negative value.
Hf = System losses on inlet side (m)
Hvp = Vapour Pressure (m) at operating temperature.
Example:
Metso HM 150 Slurry Pump at high altitude, e.g. Chuquicamata, Chile.
Duty: 65 m head at 440 m3/hour
Slurry S.G.: 1.0
Plant location: 2,800 m altitude: atm.pressure = 7.3 m
Feed point location: lift 2.0 m (2.0 m below pump inlet)
Friction losses in inlet pipes: 0.5 m
Average operating temp.: 22 oC, giving a vapour pressure 0.3 m
NPSHa is 7.3 - 2.0- 0.5- 0.3 = 4.5 m
NPSHr from the pump performance curve is 6.0 m
Therefore, NPSHa is 1.5m too low!!
The same installation in northern Europe at sea level would have given a value for
NPSHA of 7.5 m.
Therefore, at this location NPSHa would be OK!
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Step 8.
Next, we have to size a motor. Common practice is to have at least 15% margin above the calculated
absorbed power. The next larger available motor is then selected.
This margin generally compensates for under sizing that may occur because of calculations and
provides reserve power for future duty changes.
The most common driver is the squirrel cage induction motor because it is economical, reliable and
produced world-wide. Belt drive configurations typically use four pole motors as these provide the
most economical arrangement.
Step 9.
Select a drive configuration to meet installation requirements.
Drives for slurry pumps.
There are two basic drive designs for Slurry Pumps:
Indirect drives used for horizontal and vertical pumps, consisting of a motor, mounted in various
drive arrangements, and a transmission (V-belt/Poly-belt or gearbox).
This approach gives freedom to select low cost (4-pole) motors and drive components according to
local industry standards. Good flexibility is also provided for altering the pump performance by a
simple speed change.
The V-belt drive makes it possible to utilize the full impeller diameter, which maximizes the wear life.
Direct drives are always used on submersible pumps. If required, horizontal and vertical slurry pumps
can be supplied this way too but it is not a recommended configuration because ease of maintenance is
affected and pump speed is not easily altered to meet a change in duty.
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Drive arrangements.
There are several drive arrangements available for electric motors with belt drive:
Overhead
Reverse Overhead
and
Side Mounted.
Comments on drive arrangements.
The most common drive arrangements are the side and overhead mounted motors. Overhead mounting
is generally the most economical and lifts the motor off the floor away from spillage.
If the pump is of ”back pull out” design and assembled on a ”sliding maintenance base”, servicing can be
significantly simplified.
Limitations of overhead mounted arrangements:
The size of the motor is limited by the size of the pump frame.
If overhead mounting cannot be used, use side mounted motors (with slide rails for belt tensioning).
V-belt transmissions (fixed speed drives).
Slurry Pump impeller diameters (hard metal or elastomer) can not easily be altered so for a change in
performance a speed change is necessary. With a V-belt drive configuration, the pump speed can be
”fine tuned” by changing one or both pulleys to operate close to the desired duty point.
Provided belts and pulleys are installed and maintained correctly, modern V-belt drives are extremely
reliable with a life expectancy of 40 000 hours and a power loss of less then 2%.
Maximum speed ratio for V-belt drives is 5:1.
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Slurry Pumps
V-belt transmissions – limitations.
V-belts are not suitable when pump speed is too low, or when the power is too high. In these cases
gearboxes or gear (toothed) belts are used.
Gear belt drives are becoming more popular because they have the dynamic flexibility of V-belt drives in
conjunction with lower tension.
Variable speed drives.
For certain applications, varying flow conditions, long pipelines, etc., variable speed drives should be
used.
With variable speed drives, tying the speed to a flow meter can closely control the flow of a centrifugal
pump. Changes in concentration or particle size then have a minimal effect on flow rate.
Should a pipeline start to block, the speed will increase to keep flow velocity constant and help prevent
blockage.
Modern electronic drives, particularly variable frequency drives, have many advantages (may be used
with standard motors) and are widely used.
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Slurry Pumps
Variable speed drives – limitations.
Only price, which is considerable, prevents wider use!!
Something about ”combustion engines”.
In remote areas, or green field construction sites, temporary or emergency pumping equipment is often
powered by industrial diesel engines. Mounted on unitised bed frames and supplied ready to run, a
diesel powered set provides variable pump performance in response to varying engine speed.
Summary of sizing.
The day-to-day tool for sizing slurry pumps is the”PumpDim™” software mentioned earlier. This follows
the basic sizing process but is simple and quick to use, and automatically carries out many mechanical
checks such as bearing life, shaft deflection and critical speeds.
2.0
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Product Information
Slurry Pumps
2.2 Material options.
Metso offers a wide range of material options. These are the very best available, providing both
excellent wear properties and corrosion resistance. They are:
The family of elastomers, a range of natural rubbers, are by far, the major material used in slurry
pumping. Natural rubber is most cost effective for fine solids with a maximum particle size of 5 to
8mm, depending on the sharpness and density of the particles.
The family comprises:
Natural rubber 110 - a soft liner material.
Natural rubber 168 - a high strength impeller material.
NOTE!!!
Oversize scrap and sharp particles can destroy natural rubber parts very
quickly, particularly the impeller.
The family of synthetic rubbers and polyurethanes are mainly used when it is not possible to use a
natural rubber. The major types are:

Chloroprene type of synthetic rubber.

Polyurethane specially prepared for Metso. It is only available for some pump ranges
and not all sizes. For availability check the Price List. The Polyurethane offers excellent
wear resistance for finer particles (<0,15mm) but it is, at the same time, less sensitive
to oversized scrap than rubber.
There are more types of Polyurethane than there are types of steel. The comparison between
Polyurethanes should be done with great care.
See Table below for Overview properties of elastomers.
See Table 1 for general guidance for wear material selection.
See Table 2 for detail chemical resistance for elastomers.
2.0
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Edition 8
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Product Information
Slurry Pumps
Physical
properties
Material
Chemical
properties
Thermal
properties
Highest service temp.
Oils hydro
C
carbons Contin- Occasi-uously
onally
Max.
Impeller tip
speed m/s
Wear
resistanc
e
Hot water,
diluted acids
Strong and
oxidising
acids
Natural rubber
27
Very
good
Excellent
Fair
Bad
(-50) 50-65
100
Chloroprene
27
Good
Excellent
Fair
Good
90
120
Polyurethane
30
Very
good
Fair
Bad
Good
(-15) 45-50
65
The family of hard metals are generally more tolerant to abuse than rubber and are the best choice for
coarse slurries.
The family comprises:
High Chrome - a wear resistant white iron with a nominal hardness of 600 - 650 BHN. It can
be used on acidic slurries down to pH 2,5.
30% Chrome -
a wear resistant material specifically designed for FGD applications with a
hardness exceeding 500 BHN. Mainly used for applications with chloride ion
contents between 20- and 40-thousand ppm.
See Table 1 for general guidance on material selection.
Table 3 lists the corrosion resistance properties of High Chrome.
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Edition 8
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Product Information
Slurry Pumps
Table 1 - Effect of particle size on material selection
Classification of pumps according to solid particle size (sand hardness particles).
2.0
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10-W21
Edition 8
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Product Information
Slurry Pumps
Table 2 – Natural and Synthetic Rubber Materials
Natural
Butyl
EPDM
Medium
Rubber
Rubber
Rubber
A
A
C
U
A
U
A
A
A
B
A
A
A
A
A
B
A
A
A
Aluminium Chloride
Aluminium Phosphate
Ammonium Nitrate
Animal fats
Beet Sugar Liquors
Bleach Solution
Brine
Bunker Oil
Calcium Hydroxide
A
U
U
U
A
A
B
U
B
U
C
A
A
A
U
U
U
A
A
U
U
B
U
U
U
U
U
U
Calcium Hypochlorite
Chlorine (wet)
Chrome Plating Solutions
Copper Chloride
Copper Cyanide
Copper Sulphate
Creosote
Detergent Solutions
Diesel Oil
Fatty Acids
Ferric Chloride
Ferric Nitrate
Ferric Sulphate
Fluorosilic Acid
Fuel Oil
Gasoline
Glycerine
Glycols
Hydraulic Oil (Petroleum)
Hydrochloric Acid (Hot 37%)
Hydrochloric Acid (Cold 37%)
Hydrofluoric Acid(Conc.)Cold
Hydrofluoric Acid(Anhydrous)
Hydrogen Peroxide (90%)
Kerosene
Lacquers
Lacquer Solvents
Lead Acetate
Lubrication Oils (Petroleum)
U
B
A
U
U
A
Lye
Magnesium Chloride
Mineral Oil
Naphta
Nickel Chloride
2.0
BSR
A
A
C
U
A
A
A
U
A
U
U
A
A
A
A
A
C
U
A
A
A
U
A
U
U
A
A
A
U
U
A
A
U
C
A
B
B
C
U
U
U
A
U
A
A
U
U
A
U
U
A
A
U
C
A
B
B
C
U
U
U
A
U
A
A
U
U
A
Nitrile
Rubber
Chloroprene
Rubber
Hypalon
Rubber
A
A
A
A
A
A
A
B
B
A
C
A
A
A
A
B
A
A
A
A
C
U
U
A
A
A
C
A
B
B
A
A
A
A
B
B
A
A
B
U
B
B
A
A
C
C
A
A
A
C
A
B
B
A
A
A
A
B
B
A
A
B
C
A
A
A
A
A
A
C
U
A
A
A
B
A
A
B
A
A
A
A
A
A
A
A
A
U
B
U
U
A
U
U
B
A
B
A
A
C
A
10-W21
C
C
U
U
B
B
B
A
B
C
Poly Urethane
A
A
U
A
B
A
U
A
A
A
B
U
B
A
B
A
A
B
A
U
U
U
C
U
U
B
U
U
B
A
A
B
U
A
B
B
A
A
C
A
Edition 8
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Product Information
Slurry Pumps
Medium
Nitric Acid (Conc.)
Nitric Acid (Dilute)
Olive Oil
Phosphoric Acid (20%)
Natural
Rubber
Butyl
Rubber
EPDM
Rubber
Nitrile
Rubber
Chloroprene
Rubber
Hypalon
Rubber
U
U
U
C
C
B
B
A
C
U
B
A
B
A
A
A
A
B
B
B
U
U
U
U
C
B
B
A
C
U
B
A
B
A
A
A
A
B
B
B
U
U
U
U
U
U
A
B
C
A
B
B
B
B
A
A
A
A
A
A
B
U
U
B
A
A
C
U
B
A
A
A
A
A
A
B
B
U
C
B
B
U
B
A
B
A
C
U
B
A
A
A
A
A
A
B
A
B
C
B
B
U
Pickling Solution
Pine Oil
Potassium Carbonate
Salt Water
Sewage
Silicone Greases
Silicone Oils
Soda Ash
Sodium Bislufite
Sulphite Liquors
Sulphuric Acid (Dilute)
Sulphuric Acid (Conc.)
Tar, Bituminous
Transformer Oil
Transmission Fluid (Type A)
Trichloroethylene
U
B
A
B
A
A
A
B
B
C
U
U
U
U
U
Poly Urethane
U
C
A
A
U
A
A
B
U
A
U
A = Recommended - little or no effect
B = Minor to moderate effect
C = Moderate to severe effect
U = Not recommended
Table 3 High Chrome materials.
Centigrade
20o
60o
100o
Aluminium sulphite
U
U
U
Ammonia, anhydrous
A
A
A
Ammonia, aqueous
A
A
A
Ammonium chloride
A
Aqua regia
U
U
U
Aromatic solvents
A
A
A
2.0
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Edition 8
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Product Information
Slurry Pumps
Centigrade
20o
60o
100o
Brines, saturated
U
U
U
Bromide (K) soin.
U
U
U
Calcium chloride
U
U
U
Carton disulphide
A
A
A
Caroonic acid
A
A
A
Caustic soda & potash
A
A
A
Chlorine wet
U
U
U
Chlorides oif Na, K, Mg
U
U
U
Copper sulphate
U
U
U
Emulsifiers (all conc.)
U
U
U
Ether
A
A
A
Fatty acids (<Cb)
A
A
A
Ferrous sulphate
A
A
A
Fluorine, wet
U
U
U
Fluorosilic acid
U
U
U
Hydrochloric acid (10%)
U
U
U
Hydrochloric acid (conc.)
U
U
U
Hydrofluoric acid (40%)
U
U
U
Hydrofluoric acid (75%)
U
U
U
Hydrogen sulphide
A
A
A
Hypo chlorites
A
B
C
Hypochlorite (Na 12-14%)
R
ND
ND
Lead acetate
A
A
C
Lime (CaO)
A
A
A
Methanol
A
A
A
Milk and its products
A
B
B
Molasses
A
A
A
Naphta
A
A
A
2.0
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10-W21
Edition 8
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Product Information
Slurry Pumps
Centigrade
20o
60o
100o
Naphtalene
A
A
A
Nickel salts
U
U
U
Nitrates of Na, K, NH3
A
A
A
Nitric acid (<25%)
A
A
C
Nitric acid (50%)
A
A
C
Nitric acid (90%)
A
A
C
Nitric acid, fuming
A
B
C
Nitrite (Na)
A
A
A
Oil, diesel
A
A
A
Oils, essential
A
A
A
Oils, lube + aromatic ads.
A
A
A
Oils, mineral
A
A
A
Oils, vegetable & animal
A
A
A
Petroleum spirits
A
A
A
Phenol
A
A
A
Phosphoric acid (20%)
U
U
U
Phosphorous chlorides
U
U
U
Pieric acid
A
B
C
Sea water
A
A
B
Sodium carbonate
A
A
A
Sodium silicate
A
A
A
Sodium sulphide
U
U
U
Stannic chloride
U
U
U
Starch
A
A
A
Sugar spin, syrups, jams
A
A
A
Sulphates (Na, K, Mg, Ca)
A
A
A
Sulphites
A
A
A
Sulphur
A
A
A
Sulphur dioxide, dry
A
A
A
Sulphur dioxide, wet
A
B
C
Sulphur dioxide (96%)
U
U
U
Sulphur trioxide
U
U
U
Sulphuric acid (<50%)
U
U
U
2.0
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Edition 8
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Slurry Pumps
20o
60o
100o
Sulphur chlorides
U
U
U
Tallow
A
A
A
Tannic acid (10%)
A
A
A
Wetting agents (to 5%)
A
A
A
Zinc chloride
U
U
U
Centigrade
2.0
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Edition 8
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Slurry Pumps
2.3
Pump testing.
All Metso pumps are hydrostatically tested at final assembly to a test pressure of 5 bar.
Tests can be carried out at higher pressures up to the maximum working pressure for an additional
cost if required by the client at time of order.
All bearing assemblies have been mechanically run for min. 20 minutes.
Metso pump manufacturing facilities have the capability of hydro dynamically testing pumps to ISO
9906 grade 2, if required by the client at time of order for an additional cost. The parameters tested
are Head and Efficiency against Flow Rate for five test points. For an additional cost, NPSH tests
can be done.
This International Standard recommends a code for acceptance testing of pumps, defining the terms
and quantities that are used, establishing the methods of testing and the ways of measuring the
quantities involved according to Class C so as to ascertain the performance of the pump and to
compare them with the manufacturer’s guarantee.
In general, this code applies to any sizes of pumps tested with clean cold water and other liquids
behaving as clean cold water such as defined in Section 8 of the Standard.
This code is not concerned with the structural details of the pumps nor with the mechanical properties
of their components.
2.4 APPLICATION GUIDE.
2.4.1
General
This section is a guide to the selection of the correct Slurry Pump range for various
applications. It is equally important to choose the right type of Slurry Pump for the
process application in question.
The sizing of the Slurry Pump and its system is very important!
Remember!
The use of Slurry Pumps for hydraulic transportation of solids is limited mainly
by your imagination!
The Metso Slurry Pump ranges in this manual represent a broad coverage of
applications for hydraulic transportation of solids.
2.0
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Edition 8
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Product Information
Slurry Pumps
To be as practical as possible this application guide is divided in two parts :
1. Selection of a Slurry Pump - by duty
In this section we are selecting the optimal Slurry Pump simply against the
Specified pump duty.
Selecting against duty means selecting pumps considering parameters like:
Solids
(size, shape, density etc.)
Head
(maximum, high or low)
Capacity
(maximum and minimum )
Liquid
(corrosive, thixotropic, frothy)
This guide is strictly based on technical performance reflecting various Solid/Liquid parameters.
2. Selection of a Slurry Pump - by industrial application
This section is more of a practical guide, based on experience with our customers day to day
applications, working in very different industrial environments.
How to pump
•
How to feed
Wood chips
•
Mill scales
•
Mineral tailings
•
Leaching residue
•
Industrial waste
•
a hydro cyclone
•
a pressure filter
•
a tube press
•
a flotation machine
The guide is structured according to practical experience from hydraulic transportation of solids
in the following industrial segments:
•
Minerals (Metallic & Industrial)
•
2.0
Construction
•
Coal
•
Waste & Recycling
•
Power & FGD
•
Pulp & Paper
•
Metallurgy
•
Chemical
•
Mining & tunnelling
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Edition 8
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Product Information
Slurry Pumps
2.4.2
Selection of a Slurry Pump - by duty
 By Solids
Duty: Coarse particles
Comments: Everything larger than 5 mm is considered to be coarse. Use metal pumps
only. Do not use rubber pumps.
Upper practical limit in particle size is normally 50 mm.
Limitation is the impact on the impeller.
Note! Particle size must not exceed 1/3 of the pipe
Recommendation:
diameter.
XM and HM ranges
Duty: Fine particles
Comments: If the particles are sharp - use rubber.
If particles are not sharp - use rubber or metal.
Recommendation:
H and M ranges
Duty: Sharp (abrasive) particles
Comments: If sizes are below 5 mm - use rubber lined pumps.
If particles are above 5 mm - use metal lined pumps.
Recommendation:
X, H, M and VASA HD ranges
Duty: High percent solids
Comments: You have to be careful if the percent solids are getting close to 40%
by volume. Above 50% the slurry is impossible to handle with centrifugal
pumps. Only vertical tank pumps are able to handle applications with really
high percent solids.
Recommendation:
VT and VF ranges
Duty: Low percent solids
Comments: Choose the lightest and most cost effective pumps.
Recommendation:
M and H ranges
2.0
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Edition 8
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Product Information
Slurry Pumps
Duty: Fibrous particles
Comments: The problem is blocking of particles and air blocking. Use induced
flow impellers (Vortex).
Recommendation:
H , M and VS ranges
Duty: Slurry with no fine size particles
Comments: When all fine particles are removed from the slurry the solid settling
rate can be critical and can call for severe derating of the pump performance.
Pumping efficiency goes down for all pump types when used for this duty.
Recommendation:
All pump ranges
Duty: Mixing
Comments: Tank pumps are excellent as mixers for liquid and fine, dry solids.
When mixing water and solids look up the correct ratio between liquid and solids.
Recommendation:
VT and VF ranges
 By Head
Duty: High head
Comments: Normally metal pump applications are due to the high peripheral
speed on the impeller. If your application requires rubber lined pumps,”in series”
pumping may be needed.
Maximum head on hard metal pump 125 m.
Maximum head on rubber impeller 45 m.
Note!
High rates of wear occur at high speeds on centrifugal pumps.
Recommendation:
ranges
XM, XR and HM, or staged (in series) HR and VASA HD
Duty: Varying head at constant flow
Comments: Use a multi-speed drive or a variable (frequency control) drive.
Recommendation:
All ranges
Duty: Varying flow at constant head
Comments: Use variable (frequency control) drives.
Recommendation:
All ranges
Duty: High suction lift
2.0
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10-W21
Edition 8
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Product Information
Slurry Pumps
Comments: Metal pumps are preferred due to risk of rubber lining collapse on
high suction lifts.
Maximum practical suction lift 5 - 8 m depending on
Slurry S.G.
Pumps are not self-priming, i.e. you need a priming
device.
The pump and suction pipe must be filled with liquid
before starting.
Recommendation:
XM, HM and MM ranges
Duty: High flow
Comments: Use parallel pump installations.
Risk of Cavitation.
Recommendation:
All ranges
Duty: Low flow
Comments: Compare to Best Efficiency Point.
At low flows rubber linings can overheat. Use
metal.
Be careful with VS pumps if heads are high and flow
is low.
Open vertical pumps have no problems.
Recommendation: Try to use VS, VT and VF ranges
Duty: Fluctuating flow
Comments: Use horizontal pumps with variable speed drive or fixed speed
vertical pumps.
Recommendation:
speed drives.
*
VT, VF or VS. Horizontals; all
types with variable
By liquid type
Duty: Fragile slurries
Comments: Use induced flow impellers (fully recessed).
Both metal and rubber pumps can be used.
Both horizontal and vertical pumps can be used.
Recommendation:
All ranges
Duty: Hydrocarbon slurries (oil and reagents contaminated)
2.0
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Edition 8
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Product Information
Slurry Pumps
Comments: Natural rubber must not be used. Synthetic
Use metallic pumps or wear parts in polyurethane.
Recommendation:
rubber can be used.
All metal ranges
Duty: High temperature (greater than 100o C) slurries
Comments: Temperature limit for natural rubber is
60° C.
Check with your Pump Sales Support Group for pumps available with
Synthetic rubber parts.
Practical limit for operating temperature is 135 oC.
temperature the bearings can be over-heated!
Recommendation:
Above this
All horizontal ranges
Duty: Frothy slurries
Comments: Use a froth pump of vertical design.
Recommendation:
VF range
Duty: Hazardous slurries
Comments: Warning ! This case must be referred back to your Pump Sales
Support Group.
Shaft sealing is critical from an explosion point of view. Normally closed pump
systems are used.
Recommendation:
Duty:
All Horizontal ranges
Corrosive slurries (low pH)
Comments: For acidic duties use rubber or elastomers.
For metal pumps with chrome iron parts the acid limit is pH 2,5.
Seawater slurries (containing chlorides) must have a rubber pump.
Note!
CuSO4 (used in flotation circuits) is extremely corrosive, use rubber pumps.
Recommendation:
2.0
BSR
All ranges
10-W21
Edition 8
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Product Information
Slurry Pumps
Duty: High viscosity fluids (Newtonian)
Comments: When viscosity increases up to 5 x viscosity of water, the
pumping gets critical.
With this restriction basically any pump in our range can be used, if properly
sized.
Recommendation:
All sizes
Duty: High viscosity fluids (non-Newtonian)
Comments/Recommendation: These applications are very tricky and should
be referred back to your Pump Sales Support Group.
2.0
BSR
10-W21
Edition 8
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Product Information
Slurry Pumps
2.4.3 Selection of a Slurry Pump - by industrial application
This selection guide is based on practical experience from various Slurry Pump
applications within the following industrial segments:
•
Metallic and industrial minerals
•
Construction
•
Coal
•
Waste & recycling
Industrial Segment: Metallic & industrial minerals
Application: Pumps for grinding circuits
Comments: Our X, H and VASA HD ranges are specially designed for grinding
circuits (incl. cyclone feed).
•
Power & FGD
•
Paper coating material (Calcium carbonate etc.)
•
Metallurgy
•
Chemical
•
Mining & tunnelling
For particles sizes below 5 mm use rubber. If possible mix flows containing
coarse and fine particles together for better slurry stability.
Recommendation:
XR and XM, HR and HM and VASA HD
ranges.
Application: Pumps for froth
Comments: The VF range is specially designed for froth pumping.
Be cautious when heads are greater than 15 m.
Recommendation:
VF range
Application: Pumps for floor sumps
Comments: Use VS Sump Pumps with metallic wear parts, since there is
often a risk of oversize waste material coming into floor sumps. The VS
pumps can also be equipped with agitator.
If rubber must be used, put a strainer in front of the suction or around the
pump.
Recommendation:
VS, VSHM and VSMM ranges.
Application: Pumps for tailing
2.0
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Edition 8
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Product Information
Slurry Pumps
Comments: Depending on particle size either rubber or metal pumps can
be used.
For installations with long distance pumping requirements use pumps in
series.
Recommendation: X, H and VASA HD ranges, either rubber or metal.
Application: Pumps for hydro cyclone feed
Comments: For sharp classification use horizontal pumps of the X or H or
VASA HD ranges.
For dewatering cyclones use VT Tank Pumps.
Recommendation:
X, H, VASA HD and VT ranges.
Application: Pumps for pressure filter feed
Comments: High head needed with variable speed control (alternatively
two-speed drive).
Avoid rubber due to low flow heat build up.
Recommendation: HM range with double bearings assembly
Application: Pumps for tube press feed
Comments: Small flow and high head, use metal pumps of the HM range.
One pump can feed many tubes from a slurry distribution ring.
Recommendation:
HM range.
Application: Pumps for leaching
Comments: For acidic duties use rubber or elastomer.
For metal pumps with chrome iron parts the acid limit is pH 2,5.
Recommendation: All ranges
Application: Pumps for dense media (heavy media)
Comments: High inlet head and high percent solids in combination with low
discharge head can cause expeller seal leakage problems.
Recommendation:
HM range.
Application: Pumps for general purpose (mineral)
Comments: Horizontal pumps of the MM and MR ranges are ideal for
normal duty in mineral process circuits. If the wear is extreme, use the X
and H ranges.
Rubber is normally preferred in “hard rock" concentrators.
For special applications use the vertical pumps.
Recommendation:
2.0
BSR
All ranges
10-W21
Edition 8
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Product Information
Slurry Pumps
Industrial Segment: Construction
Application: Pumps for wash water (sand and gravel)
Comments: Normally, vertical pumps of the VS and VT ranges are used.
The M range horizontal pump is also suitable.
Recommendation:
VS,VT and M range
Application: Pumps for sand transportation
Comments: Horizontal pumps with rubber lining are preferred.
Recommendation:
2.0
BSR
MR range
10-W21
Edition 8
43/56
Product Information
Slurry Pumps
Application: Pumps for tunnel dewatering
Comments: Do not use rubber due to oil in slurry.
As front pumps use drainage pumps.
For the first transportation stage the VS Vertical
used.
Sump Pump is normally
For horizontal distant pumping use HM range.
For cuttings from full face boring use HM and MM ranges.
For small tunnels (micro bore) use small HM range.
Recommendation:
HM, MM and VS ranges
Application: Drainage pumps
Comments: For lighter duties use the M range of horizontal pumps. Diesel
driven pump can be practical but these are not our standard version?
Recommendation:
M range.
Industrial Segment: Coal
Application: Pumps for coal washing
Comments: Generally metal pumps are used because of risk for oversized
tramp material.
Recommendation:
HM and MM ranges
Application: Pumps for froth (coal)
Comments: Use the VF Vertical Froth Pump.
Recommendation:
VF range
Application: Pumps for dense media (coal)
Comments: High inlet head and high percent solids in combination with low
discharge head can cause expeller seal leakage problems.
Recommendation: HM range, often with differential impeller to increase the
expeller sealing capability.
2.0
BSR
10-W21
Edition 8
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Product Information
Slurry Pumps
Application: Pumps for coal/water mixtures
Comments: Use horizontal pumps of the M and H ranges.
Recommendation:
MM ranges ( HM for low flow rates )
Industrial Segment: Waste & recycling
Application: Pumps for effluent handling
Comments: Light-duty application.
Use either horizontal or vertical pumps.
Metal pumps are the first selection.
Recommendation:
HM, MM and V ranges
Application: Hydraulic transportation of light waste
Comments: Use horizontal pumps with Vortex induced flow impellers.
Recommendation:
HM and MM ranges
Application: Pumps for soil treatment
Comments: The VT Vertical Tank Pumps are recommended for mobile and
semi-mobile plants (no leaking seal and easy to transport and install).
Recommendation: All ranges
Application: Pumps for general purpose (coal)
Comments: The coal industry does not normally use rubber pumps.
Recommendation:
HM and MM ranges
Industrial Segment: Power & FGD
Application: Pumps for FGD reactor feed (lime)
Comments: Normally mineral applications use X, H and M ranges, all with
rubber and/or metal parts. For slurry with more than 20000 ppm chloride
iron use 30% CR.
Rubber for high chloride concentrations.
Recommendation:
2.0
BSR
X, H and M ranges
10-W21
Edition 8
45/56
Product Information
Slurry Pumps
Application: Pumps for FGD reactor discharge (gypsum)
Comments: See lime pumps above for wear parts selection.
Recommendation:
X, H and M ranges
Application: Bottom ash pumping
Comments: Metal pumps are preferred due to temperature and particle
size.
Recommendation:
XM and HM ranges
Application: Fly ash pumping
Comments: Metal is normally used due to risk of oil contamination.
If pH is so low that rubber has to be used, look out for any oil or other
chemicals or temperature too high, then natural rubber cannot be used.
Recommendation:
X, H, M and VS ranges.
Industrial Segments: Pulp & Paper
Application: Pumps for liquors
Comments: Rubber is not to be recommended on black liquors due to risk
of turpentine.
Recommendation:
HM and MM ranges
Application: Pumps for lime and caustic mud
Comments: These applications are normally of high temperature, therefore
metal parts are recommended.
Recommendation:
HM and MM ranges
Application: Pumps for reject pulp (containing sand)
Comments: Normally light duty, but metal parts are recommended. Normally we
are competing with stainless steel pumps.
Recommendation:
2.0
BSR
MM range
10-W21
Edition 8
46/56
Product Information
Slurry Pumps
Application: Pumps for solids from debarking
Comments: An extra long VS Vertical Sump Pump has been developed for sand
and bark.
Use metal parts and induced flow impeller (Vortex).
Recommendation:
VS range
Application: Pumps for hydraulic transportation of wood chips
Comments: Use horizontal pumps of the H and M ranges with induced flow
(Vortex) impellers.
Recommendation: VASA, HM and MM ranges
Application: Pumps for paper filler and coating slurries
Comments: No rubber allowed due to colour contamination.
Recommendation: HM, MM, VS, VT &VF ranges only metal parts
Application: Floor spillage pumps
Comments: Use a VS Vertical Sump Pump.
Sometimes stainless steel parts are required due to low pH.
Recommendation:
VS range
Industrial Segments: Metallurgy
Application: Pumps for Mill Scale transportation
Comments: First choice is a VS Vertical Sump Pump with induced flow impeller
and metal wear parts. For heavy mill scale handling can VS with agitator be
useful.
Recommendation: HM horizontals and VS sump pumps.
Application: Pumps for slag transportation
Comments: Same considerations as for “Mill Scale” above.
Application: Pumps for wet scrubber effluents
Comments: Normally we recommend horizontal pumps of the M range or
vertical pumps of the VS range. If pH is very low, use rubber. If pH is very
low and temperature is very high, use stainless steel or synthetic rubber
parts.
Recommendation:
2.0
BSR
MR and VS ranges
10-W21
Edition 8
47/56
Product Information
Slurry Pumps
Application: Pumps for iron powder transportation
Comments: See dense media pumps above.
Application: Pumps for machine tool cuttings
Comments: No rubber parts can be used due to oil.
Use vertical pumps of the VS range or horizontal pumps of the M range.
Recommendation:
VS and MM ranges
Industrial Segment: Chemical
Application: Pumps for acid slurries
Comments: First recommendation is horizontal pumps with rubber or
stainless parts. For extremely abrasive slurries use horizontal pumps of the
HR range.
Recommendation:
MR and HR ranges
Application: Pumps for brines
Comments: Very corrosive applications. Can also be abrasive (crystals).
Polyurethane can be used to avoid crystallization on pump parts.
Recommendation: HR, HM, MR, MM and VS (polyurethane parts).
Application: Pumps for caustics
Comments: Easy application.
Both rubber and metal pumps can be used.
Recommendation:
MR, MM, PM and VS ranges
Industrial Segments: Mining
Application: Pumps for hydraulic tailings back filling (with or without cement)
Comments: Watch out for deslimed tailings since that increases the derating factor!
Recommendation: HM or HR and MM or MR ranges
Application: Pumps for mine water (with solids)
Comments: Normal recommendation is horizontal pumps of the HM range (in
series if required).
Watch out for corrosion with low pH mine drainage water!
Recommendation: HM range. For low pH use 30%CR wear parts.
2.5 Conversions and Equations
2.5.1 Table of Useful Conversions
2.0
BSR
10-W21
Edition 8
48/56
Product Information
Slurry Pumps
PHYSICAL TERMS
Area
Capacity
Density
Gravitational Constant
Length
Power
Pressure
CONVERSION VALUES
Metric units
U.S. units
1 m2
6.4516x10 m2
1 m2
0.0929 m2
1 m3/hr
0.2271 m3/hr
1 kg/m3
16.02 kg/m3
9.81 m/s2
1m
0.3048 m
0.0254 m
1 kW
0.745 kW
1 N/m2
6895 N/m2
1 bar = 105 N/m2
1.0132 bar
Velocity
Volume
Weight
2.0
1 m/s
0.3048 m/s
1m3
0.003785 m3
1 kg
0.4536 kg
BSR
1550 in2
1 in2
10.76 ft2
1 ft2
4.4028 US gpm
1 USgpm
0.06243 lbf/ft3
1 lbf/ ft3
32.2 ft/s2
3.281 ft.
1 ft.
1 in.
1.341 hp
1 hp
0.00145 lbf/in2
1 lbf/in2
14.5 lbf/in2
1 atmosphere = 14.7 lbf/in2
3.281 ft/s
1 ft/s
264.17 US gallons
1 US gallon
2.205 lbf
1 lbf
10-W21
Edition 8
49/56
Product Information
Slurry Pumps
2.5.2 Table of Useful Equations
PARAMETER
METRIC
EQUATION
Flow Velocity
Q
()D 
QH(sg)
(Eff)
Pressure
H(sg)
 × 
Specific Gravity
(Relative Density)
Temperature
sg =

DL
Dw
C =( F - )


Tip Speed
DN

Viscosity
{for values
Velocity, V
UNIT
ft/s
m
Pipe inside diameter, D
in
U.S.
EQUATION
(- )
D
Horsepower
(Brake)
TERM AND SYMBOL
UNIT
m/s
cST = (×)SSU
m3/hr
kW
Flow rate, Q
USgpm
Horsepower
hp
m3/hr
Flow rate, Q
USgpm
m
Head, H
ft
none
Specific Gravity, sg
none
none
Efficiency, Eff
none
bar
Pressure, P
lbf/in^2
m
Liquid Head, H
ft
none
Specific Gravity, sg
none
none
Specific Gravity, sg
none
kg/m3
Density of Liquid, Dl
lbf/ft^3
kg/m3
lbf/ft^3
deg C
Density of Clear Water,
Dw
Celsius (Centigrade)
deg C
deg F
Fahrenheit
deg F
m/s
Tip Speed, v
ft/s
m
Impeller diameter, D
in
N
Speed, rev/mt
N
cSt
Centistoke
cSt
Seconds Saybolt
Universal
SSU
QH(sg)
(Eff)
H(sg)
 × 
sg =


F =  + ( )  C

DN

SSU = (x)cSt
>15cSt(70SSU)}
2.0
BSR
10-W21
Edition 8
DL
Dw
50/56
Product Information
Slurry Pumps
2.6
Maximum Permissible Vibration Levels
Heavy-duty slurry pumps properly bolted to rigid foundations are classified as Class III of ISO2372,
Annex A, and pumps not bolted to rigid foundations as Class IV.
Vibration limits in mm/s are as follows:
Newly installed, up to:
In definite operation, up to:
Limited period operation, up to:
Stop operation immediately, above:
Class III
1,8
4,5
11,0
11,0
Class IV
2,8
7,1
18,0
18,0
It should be noted that, particularly for overhead mounted motors, motor manufacturers may specify
lower limits.
Rigid frames are defined as those having a fundamental vibration frequency of at least ten times the
pump’s fundamental frequency.
2.7
Sound Level
Under certain installation conditions, and at operating points outside the pump’s optimum operating
range, the equipment may generate sound levels above 70dB(A). The motor generates most of the
noise, and in general, the pump noise level for properly designed installations will be about 2 dB (A)
above that of the motor.
2.0
BSR
10-W21
Edition 8
51/56
Product Information
Slurry Pumps
2.8 Standard Allowable Flange Forces and Moments for Metso Pumps
FLANGE
mm
inches
32
50
80
100
150
200
250
300
350
400
1¼
2
3
4
6
8
10
12
14
16
2.0
FX and FY
kN
0,35
0,51
0,80
1,10
2,00
2,90
4,35
5,80
7,60
9,70
lbf.
80
115
180
250
440
650
975
1 300
1 700
2 175
BSR
FZ
kN
0,70
1,00
1,60
2,20
4,00
5,80
8,70
11,60
15,20
19,40
MX and MY
lbf.
160
230
360
500
880
1 300
1 950
2 600
3 400
4 350
MZ
Nm
lb.ft.
Nm
165
240
370
510
895
1 325
2 000
2 650
3 460
4 440
120
175
270
375
660
975
1 475
1 950
2 550
3 275
325
475
750
1 000
1 790
2 650
4 000
5 300
6 900
8 880
10-W21
Edition 8
lb.ft.
240
350
540
750
1 320
1 950
2 950
3 900
5 100
6 550
52/56
Product Information
Slurry Pumps
2.9 Pressure ratings
Pressure ratings:
Centrifugal pump performance is usually shown in “Head, Capacity and Efficiency” units. Head is in
length units such as “metres or feet of liquid”, Capacity in ‘volume/time’ units such as m³/h or US gpm,
and Efficiency in “percent” (%).
Head refers to the differential head (pressure rise) across the pump and is called Total Dynamic Head
(TDH). The pump discharge pressure is related to the TDH times the Slurry Density (SG).
Head values can be converted to pressure units by:
Pressure (lbf/in2) = (Feet of liquid x Slurry SG)
(2.31)
OR
Pressure (bar) = (Metres of liquid x Slurry SG)
(10.21)
Operating pressure that can be measured at the pump discharge can be calculated using the
following:
Max. Discharge Pressure = (Pump Inlet pressure + Pressure generated by the pump).
On a single stage pump, tank open to the atmosphere, estimate the “Pump Inlet Pressure” by
converting the Static Inlet Head (liquid level above the pump centreline). In a closed tank, the
pressure above the liquid adds to that calculated from the Static Inlet Head.
On multi-stage pumping, treat the first stage as described above. Subsequent stages are evaluated
based on their installation. For example, if all the stages are in one location then consider the
discharge pressure from one pump to be the inlet pressure of the next. However, if the pumps are
situated along a pipeline then the head losses in the line between each stage and the different
elevation need to be accounted for.
2.0
BSR
10-W21
Edition 8
53/56
Product Information
Slurry Pumps
Permissible Operating Pressures:
Depending on the bolting configuration and Casing type, pumps are rated for the maximum
operating pressures shown in the tables below.
Hydrostatic tests:
Hydrostatic tests can be done, at an additional cost, if specifications require it.

The test pressure typically is 1.5 x (maximum permissible operating pressure).

Obtain factory approval for hydrostatic tests on pumps using High Pressure Casings.
Flange Ratings:
International Standards such as ANSI B16.5 for inch dimensions and EN1092 for metric contain
dimensional and pressure rating data. Flange material and operating temperature affect the pressure
ratings.
Carbon Steel flanges and operating temperatures below 100 0F (38 0C):
Operating Pressure: lbf/in2 ; (bar)
Up to 230 ;
(16)
Flange type
ANSI Class 150
EN1092 NP16
231 to 435 ; (16.1-30)
Class 300
NP25
436 to 1000 ; (30.1-70)
Class 600
NP40
Consult factory for duty conditions not within the above listed limit
2.0
BSR
10-W21
Edition 8
54/56
Product Information
Slurry Pumps
Maximum operating pressure shown in bar
Frame size
250
300
400
500
600
350
16
21
750
900
400
16
500
7.5
MM - Pump sizes
Standard bolting - SA + DA
High Pressure bolting - DA
100
16
150
16
200
16
250
16
300
16
21
MR - Pump sizes
Standard bolting
100
8
150
8
200
8
250
8
300
8
350
8
HM - Pump sizes
Standard bolting - SA + DA
High Pressure bolting - DA
50
16
28
75
16
28
100
16
28
150
16
24
200
16
21
250
16
21
300
16
21
HR - Pump sizes
Standard bolting - SA + DA
Standard bolting - DA
50
16
21
75
16
21
100
16
21
150
16
21
200
16
21
250
10
10
300
10
10
75
40
40
100
40
40
150
16
40
200
16
40
250
16
40
HP - Pump sizes (metal)
HP bolts and case - SA
HP bolts and case - DA
HH - Pump sizes
Standard bolting - SA + DA
High Pressure bolting - DA
200
16
21
HG - Pump sizes
100
10
HMPT- Pump sizes
High Pressure bolting - DA
Vasa HD - Pump sizes
Standard
Optional
Frame size
30250
16
364-80
750
XM - Pump sizes
XR - Pump sizes
XG - Pump sizes
300
16
250
7.5
MR – Pump sizes
Thomas Dredge
150
10
200
10
100
40
150
40
16
455100
25
507150
25
900
1000
1200
350
7.5
350
7.5
400
7.5
400
7.5
350
7.5
500
16
500
7.5
7010200
10
25
5311250
10
250
10
5313W250
10
8515350
16
25
9015350
16
25
1400
600
7.5
700
7.5
All pumps are rated at 10 Bar
Notes:



2.0
Metso follows Hydraulic Institute standard of testing to 1.5 times operating (work) pressure
SA = Offered in Single Adjust only
DA = Offered in Double Adjust only
BSR
10-W21
Edition 8
55/56
Product Information
Slurry Pumps
Maximum operating pressure shown in PSI
Frame size
300
400
500
MM - Pump sizes
Standard bolting - SA + DA
High Pressure bolting - DA
250
100
230
150
230
200
230
250
230
300
230
300
600
MR - Pump sizes
100
115
150
115
200
115
250
115
300
115
350
115
350
230
300
750
900
400
230
500
110
HM - Pump sizes
Standard bolting - SA + DA
High Pressure bolting - DA
50
230
400
75
230
400
100
230
400
150
230
350
200
230
300
250
230
300
300
230
300
HR - Pump sizes
Standard bolting - SA + DA
Standard bolting - DA
50
230
300
75
230
300
100
230
300
150
230
300
200
230
300
250
145
145
300
145
145
75
580
580
100
580
580
150
230
580
200
230
580
250
230
580
HP - Pump sizes (metal)
HP bolts and case - SA
HP bolts and case - DA
HH - Pump sizes
Standard bolting - SA + DA
High Pressure bolting - DA
200
230
300
HG - Pump sizes
100
145
HMPT- Pump sizes
Vasa HD - Pump sizes
Standard
Optional
Frame size
30250
230
36480
230
750
900 1000
XM - Pump sizes
XR - Pump sizes
XG - Pump sizes
300
230
250
110
MR – Pump sizes
Thomas Dredge
350
110
350
110
455100
360
400
110
400
110
350
110
500
230
150
145
200
145
100
580
150
580
507-150
360
7010200
145
360
1200
500
110
5311250
145
250
145
5313W250
145
8515350
230
360
9015350
230
360
1400
600
110
700
110
All pumps are rated at 145 PSI
Notes:



2.0
Metso follows Hydraulic Institute standard of testing to 1.5 times operating (work) pressure
SA = Offered in Single Adjust only
DA = Offered in Double Adjust only
BSR
10-W21
Edition 8
56/56