Metso Slurry Pump Sizing

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

2.0 BSR 10-W21 Edition 8 2/56 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

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)

Q_US = Flow rate in US gallons per minute. stph = Short tons per hour (solids)

2.0 BSR 10-W21 Edition 8 4/56 Slurry Formulas: Sm C S V = ( -1) + 1 0 0 1 C S x S V m = -( ) ( ) 1 1 0 0 1

[

]

C x C S C C V W W W = - + 1 0 0 1 0 0 ( ) C x S C S W V = + -1 0 0 1 0 0 1 ( )

C

W

=

1 0 0

-

[ 1 0 0 - C S V m ]

Q

=

t p h x

[ 1 1 0 0 1 s + C_W - ] m3/hr

Q

US

= 4

x st p h x

[ 1 1 0 0 1 s + C_W - ] USgpm

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.

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).}

2.0 BSR 10-W21 Edition 8 6/56 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

V₂ = Flow velocity at Point 2 in m/s. g = Gravitational constant = 9.81 m/s2

Therefore, Pump Outlet Head = H₂ + V₂2 / 2g + outlet pipe losses Pump Total Head, H = (Outlet head – inlet head) H = (H₂ + V₂2 _{/ 2g + outlet pipe losses) – (H}

1 – 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.

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:

1. Looked up in a table

2. Extracted from a Moody diagram.

3. Calculated from semi-empirical formula, such as the William & Hazen Formula.

2.0 BSR 10-W21 Edition 8 8/56 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!

Nomograph chart for minimum velocity. (Adapted from Wilson, 1976).

Example : Pipe dia. 250 mm = 0,250 m

Particle size = 0,5 mm (Worst case) Particle S.G. =3,8

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.

R>3xN.B. R=2xN.B Plug Lub

Pipe Long Short R>10xN.B. Dia-phr. Full Valve

Size Radius Radius Rubber Full Bore Rect.

N.B Bend Bend Elbow Tee Hose Open Valve Way

25 0,52 0,70 0,82 1,77 0,30 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.

2.0 BSR 10-W21 Edition 8 12/56 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.

2.0 BSR 10-W21 Edition 8 14/56 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.

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.

2.0 BSR 10-W21 Edition 8 16/56 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 = D1 / D2 or Q2 = Q1 x ( D2 /D1 )

H1 / H2 = ( D1 /D2 )2 or H2 = H1 x ( D2 /D1 )2

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).

2.0 BSR 10-W21 Edition 8 18/56 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.

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.

2.0 BSR 10-W21 Edition 8 20/56 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) H2O Head (m)

0 10,3

1 000 9,2

2 000 8,1

20 40 60 80 100 10 8 6 4 2 Vapour Pressure (m) Temperature (C )o

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.

2.0 BSR 10-W21 Edition 8 22/56 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.

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.

2.0 BSR 10-W21 Edition 8 24/56 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.

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 BSR 10-W21 Edition 8 26/56 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.

Material Physical properties Chemical properties Thermal properties Max. Impeller tip speed m/s Wear resistanc e Hot water, diluted acids Strong and oxidising acids Oils hydro carbons

Highest service temp. C

Contin- Occasi-uously onally

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.

2.0 BSR 10-W21 Edition 8 28/56 Table 1 - Effect of particle size on material selection

Table 2 – Natural and Synthetic Rubber Materials Medium Natural Rubber Butyl Rubber EPDM Rubber Nitrile Rubber Chloroprene Rubber Hypalon Rubber Poly -Urethane Aluminium Chloride _{A A A A A A A} Aluminium Phosphate _{A A A A A A A} Ammonium Nitrate _{C A A A B A U} Animal fats _{U B B A B B A}

Beet Sugar Liquors _{A A A A A A}

Bleach Solution _{U A A C A} Brine _{A A A A} Bunker Oil _{A B} Calcium Hydroxide _{A A A A A A A} Calcium Hypochlorite _{U A A C C A} Chlorine (wet) _{U C C U C U}

Chrome Plating Solutions _{U U U U U C}

Copper Chloride _{A A A A A A A} Copper Cyanide _{A A A A A A A} Copper Sulphate _{B A A A A A A} Creosote _{U U U B C C B} Detergent Solutions _{B A A A A A U} Diesel Oil _{U U U A B B B} Fatty Acids _{C U U B B B} Ferric Chloride _{A A A A A A A} Ferric Nitrate _{A A A A A A} Ferric Sulphate _{A A A A A A} Fluorosilic Acid _{U A A A} Fuel Oil _{U U U A B B B} Gasoline _{U U U A B B A} Glycerine _{A A A A A A A} Glycols _{A A A A A A B}

Hydraulic Oil (Petroleum) _{U U U A B B A}

Hydrochloric Acid (Hot 37%) _{U C C U U C U}

Hydrochloric Acid (Cold 37%) _{B A A B B A U}

Hydrofluoric Acid(Conc.)Cold _{U B B U B A U} Hydrofluoric Acid(Anhydrous) _{U B B A} Hydrogen Peroxide (90%) _{U C C U C} Kerosene _{U U U A C C B} Lacquers _{U U U U U U U} Lacquer Solvents _{U U U U U U U} Lead Acetate _{A A B B}

Lubrication Oils (Petroleum) _{U U U A B B B}

Lye _{B A A B B A B}

Magnesium Chloride _{A A A A A A A}

Mineral Oil _{U U U A B B A}

Naphta _{U U U C C U C}

2.0 BSR 10-W21 Edition 8 30/56 Medium Natural Rubber Butyl Rubber EPDM Rubber Nitrile Rubber Chloroprene Rubber Hypalon Rubber Poly -Urethane

Nitric Acid (Conc.) _{U C C U C B U}

Nitric Acid (Dilute) _{U B B U A A C}

Olive Oil _{U B B A B B A} Phosphoric Acid (20%) _{C A A B B A A} Pickling Solution _{C C C} Pine Oil _{U U U B U U} Potassium Carbonate _{B B B B B B} Salt Water _{A A A A A A} Sewage _{B B B A A A U} Silicone Greases _{A A A A A A A} Silicone Oils _{A A A A A A A} Soda Ash _{A A A A A A} Sodium Bislufite _{B A A A A A} Sulphite Liquors _{B B B B B B}

Sulphuric Acid (Dilute) _{C B B U B A B}

Sulphuric Acid (Conc.) _{U B B U U B U}

Tar, Bituminous _{U U U B C C}

Transformer Oil _{U U U A B B}

Transmission Fluid (Type A) _{U U U A B B A}

Trichloroethylene _{U U U C U U 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

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

2.0 BSR 10-W21 Edition 8 32/56 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

Centigrade 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

2.0 BSR 10-W21 Edition 8 34/56 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.

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 • Wood chips

• Mill scales • Mineral tailings • Leaching residue • Industrial waste

How to feed • 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) • Construction

• Coal

• Waste & Recycling • Power & FGD • Pulp & Paper

• Metallurgy • Chemical • Mining & tunnelling

2.0 BSR 10-W21 Edition 8 36/56 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 diameter.

Recommendation: 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:

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: XM, XR and HM, or staged (in series) HR and VASA HD ranges

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

2.0 BSR 10-W21 Edition 8 38/56 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: VT, VF or VS. Horizontals; all types with variable speed drives.

* 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

Comments: Natural rubber must not be used. Synthetic rubber can be used. Use metallic pumps or wear parts in polyurethane.

Recommendation: 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. Above this temperature the bearings can be over-heated!

Recommendation: 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: All Horizontal ranges

Duty: 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.

2.0 BSR 10-W21 Edition 8 40/56 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.

2.4.3 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.

2.0 BSR 10-W21 Edition 8 42/56 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.

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.

2.0 BSR 10-W21 Edition 8 44/56 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 Sump Pump is normally used.

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.

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: X, H and M ranges

2.0 BSR 10-W21 Edition 8 46/56 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.

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.

2.0 BSR 10-W21 Edition 8 48/56 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

PHYSICAL TERMS CONVERSION VALUES

Metric units U.S. units

Area _{1 m2 1550 in2} 6.4516x10 m2 1 in2 1 m2 10.76 ft2 0.0929 m2 1 ft2 Capacity _{1 m3/hr} 4.4028 US gpm 0.2271 m3/hr 1 USgpm Density _{1 kg/m3 0.06243 lbf/ft3} 16.02 kg/m3 1 lbf/ ft3 Gravitational Constant _{9.81 m/s2 32.2 ft/s2} Length 1 m 3.281 ft. 0.3048 m 1 ft. 0.0254 m 1 in. Power 1 kW 1.341 hp 0.745 kW 1 hp Pressure _{1 N/m2 0.00145 lbf/in2} 6895 N/m2 1 lbf/in2 1 bar = 105 N/m2 14.5 lbf/in2

1.0132 bar _{1 atmosphere = 14.7 lbf/in2}

Velocity 1 m/s 3.281 ft/s 0.3048 m/s 1 ft/s Volume _1m3 264.17 US gallons 0.003785 m3 1 US gallon Weight 1 kg 2.205 lbf 0.4536 kg 1 lbf

2.0 BSR 10-W21 Edition 8 50/56 2.5.2 Table of Useful Equations

PARAMETER METRIC TERM AND SYMBOL U.S.

EQUATION UNIT UNIT EQUATION

Flow Velocity m/s Velocity, V ft/s

(

)

Q D

 

m Pipe inside diameter, D in

₍

_-

₎



 D

_m3/hr Flow rate, Q USgpm

Horsepower kW Horsepower hp (Brake) _QHsg Eff ( ) ( ) 

m3/hr Flow rate, Q USgpm

m Head, H ft _QHsg

Eff ( )

( )



none Specific Gravity, sg none

none Efficiency, Eff none

Pressure bar Pressure, P lbf/in^2

Hsg( )  ×

m Liquid Head, H ft _{Hsg( )}

 ×

none Specific Gravity, sg none Specific Gravity none Specific Gravity, sg none (Relative Density) sg D D L w = kg/m3 Density of Liquid, Dl lbf/ft^3 sg D D L w =

kg/m3 Density of Clear Water, Dw

lbf/ft^3

Temperature _{ }

C=( F-) 

deg C Celsius (Centigrade) deg C _{ }

F=+  C

 ( )

deg F Fahrenheit deg F

Tip Speed m/s Tip Speed, v ft/s

DN



m Impeller diameter, D in

_DN



N Speed, rev/mt N Viscosity cSt Centistoke cSt

{for values

_c

_SSU

ST

= ×

(



)

Seconds Saybolt

Universal

SSU

_SSU

_{= (}

 

_x

₎

_cSt

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:

Class III Class IV

Newly installed, up to: 1,8 2,8

In definite operation, up to: 4,5 7,1 Limited period operation, up to: 11,0 18,0 Stop operation immediately, above: 11,0 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 52/56 2.8 Standard Allowable Flange Forces and Moments for Metso Pumps

FLANGE FX and FY FZ MX and MY MZ

mm inches kN lbf. kN lbf. Nm lb.ft. Nm lb.ft. 32 1¼ 0,35 80 0,70 160 165 120 325 240 50 2 0,51 115 1,00 230 240 175 475 350 80 3 0,80 180 1,60 360 370 270 750 540 100 4 1,10 250 2,20 500 510 375 1 000 750 150 6 2,00 440 4,00 880 895 660 1 790 1 320 200 8 2,90 650 5,80 1 300 1 325 975 2 650 1 950 250 10 4,35 975 8,70 1 950 2 000 1 475 4 000 2 950 300 12 5,80 1 300 11,60 2 600 2 650 1 950 5 300 3 900 350 14 7,60 1 700 15,20 3 400 3 460 2 550 6 900 5 100 400 16 9,70 2 175 19,40 4 350 4 440 3 275 8 880 6 550

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 54/56 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) Flange type

Up to 230 ; (16) ANSI Class 150 EN1092 NP16

231 to 435 ; (16.1-30) Class 300 NP25

436 to 1000 ; (30.1-70) Class 600 NP40

Maximum operating pressure shown in bar

Frame size 250 300 400 500 600 750 900

MM - Pump sizes 100 150 200 250 300 350 400 500

Standard bolting - SA + DA 16 16 16 16 16 16 16 7.5 High Pressure bolting - DA 21 21

MR - Pump sizes 100 150 200 250 300 350

Standard bolting 8 8 8 8 8 8

HM - Pump sizes 50 75 100 150 200 250 300

Standard bolting - SA + DA 16 16 16 16 16 16 16

High Pressure bolting - DA 28 28 28 24 21 21 21

HR - Pump sizes 50 75 100 150 200 250 300

Standard bolting - SA + DA 16 16 16 16 16 10 10 Standard bolting - DA 21 21 21 21 21 10 10

HP - Pump sizes (metal) 75 100 150 200 250

HP bolts and case - SA 40 40 16 16 16 HP bolts and case - DA 40 40 40 40 40

HH - Pump sizes 200

Standard bolting - SA + DA 16 High Pressure bolting - DA 21

HMP – Pump sizes 150

Standard bolting – SA 16 High Pressure bolting – DA 25

HG - Pump sizes 100 150 200 250

10 10 10 10

HMPT- Pump sizes 100 150

High Pressure bolting - DA 40 40

Vasa HD - Pump sizes 302-

50 364-80 455-100 507-150 7010-200 5311-250 5313W-250 8515-350 9015-350 Standard 16 16 25 25 10 10 10 16 16 Optional 25 25 25 Frame size 750 900 1000 1200 1400 XM - Pump sizes 350 400 500 600 700 7.5 7.5 7.5 7.5 7.5 XR - Pump sizes 300 350 400 16 7.5 7.5 XG - Pump sizes 250 350 7.5 7.5 MR – Pump sizes 500 16 Thomas Dredge

All pumps are rated at 10 Bar

Notes:

 Metso follows Hydraulic Institute standard of testing to 1.5 times operating (work) pressure  SA = Offered in Single Adjust only

2.0 BSR 10-W21 Edition 8 56/56

Maximum operating pressure shown in PSI

Frame size 250 300 400 500 600 750 900

MM - Pump sizes 100 150 200 250 300 350 400 500

Standard bolting - SA + DA 230 230 230 230 230 230 230 110 High Pressure bolting - DA 300 300

MR - Pump sizes 100 150 200 250 300 350

115 115 115 115 115 115

HM - Pump sizes 50 75 100 150 200 250 300

Standard bolting - SA + DA 230 230 230 230 230 230 230 High Pressure bolting - DA 400 400 400 350 300 300 300

HR - Pump sizes 50 75 100 150 200 250 300

Standard bolting - SA + DA 230 230 230 230 230 145 145 Standard bolting - DA 300 300 300 300 300 145 145

HP - Pump sizes (metal) 75 100 150 200 250

HP bolts and case - SA 580 580 230 230 230 HP bolts and case - DA 580 580 580 580 580

HH - Pump sizes 200

Standard bolting - SA + DA 230 High Pressure bolting - DA 300

HMP – Pump sizes 150

Standard bolting – SA 230 High Pressure bolting – DA 360

HG - Pump sizes 100 150 200 250

145 145 145 145

HMPT- Pump sizes 100 150

580 580

Vasa HD - Pump sizes 302-

50 364-80 455-100 507-150 7010-200 5311-250 5313W-250 8515-350 9015-350 Standard 230 230 360 360 145 145 145 230 230 Optional 360 360 360 Frame size 750 900 1000 1200 1400 XM - Pump sizes 350 400 500 600 700 110 110 110 110 110 XR - Pump sizes 300 350 400 230 110 110 XG - Pump sizes 250 350 110 110 MR – Pump sizes 500 230

Thomas Dredge

All pumps are rated at 145 PSI

Notes:

 Metso follows Hydraulic Institute standard of testing to 1.5 times operating (work) pressure  SA = Offered in Single Adjust only