01 OPERATING MANUAL PUMP.docx

PROJECT TITLEHYDROSTATIC & HYDRAULIC EXPERIMENT RIG

DOCUMENT TITLE

OPERATING MANUAL HYDROSTATIC & HYDRAULIC EXPERIMENT RIG

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NameDIDAKTIK ENGINEERING WERKS SDN BHD

BRAND DEW

M0DEL PPT

SERIES 101

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PPT-101

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020-

MAY-15

ISSUED FOR APPROVAL MOHD MASRI LEW

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TULIP GMI

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CONTENT

1.0 INTRODUCTION 4

2.0 EXPERIMENTAL PROCEDURES 10

3.0 RESULTS 11

4.0 ANALYSIS 12

5.0 REFERENCES 21

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1.0 INTRODUCTION

1. Introduction

Pump is a mechanical device used to add energy onto a liquid in order to

move it from one location to another. It’s often been used in the critical processes in

order to transfer fluid from low level to high ground, from low pressure areas to

higher pressure areas and from local locations to distant locations. By adding a

pump on the pipeline, fluids can be transferred to other places or higher level and

some energy are required to overcome the losses due to friction between the fluid

and the pipe walls.

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Figure 1: A typical pumping system

Because pump designs are so numerous, it can be classified in any number of

ways. Some examples of how pumps can be put into different classes are as

follows:

a) By the applications the pumps serve.

b) By the materials from which the pumps are constructed.

c) By the liquids the pumps can handle.

d) By the pump orientation.

All of the above classes are limited and usually overlap each other.

Therefore, a more basic classification system is needed. If pumps are categorized by

the way in which energy is added to the liquid, there is no overlap and the

classification is related to the pump only.

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Figure 2: Pump Classifications

The applications of the pump can be classified on the basis of the applications

they serve, the materials from which they are constructed, the liquids or fluids they

handle, and even their orientation in space. All pumps may be divided into two

major categories:

a) Kinetic pump in which energy is continuously added to increase the fluid

velocities within the machine to values greater than those occurring at the

discharge so subsequent velocity reduction within or beyond the pump

produces a pressure increase, and

b) Positive displacement pump, in which energy is periodically added by

application of force to one or more movable boundaries of any desired

number of enclosed, fluid-containing volumes, resulting in a direct increase in

pressure up to the value required moving the fluid through valves or ports

into the discharge line.

1.1 Kinetic Pump

Kinetic pumps may be further subdivided into several varieties of centrifugal

and other special-effect pumps. Displacement pumps are essentially divided into

reciprocating and rotary types, depending on the nature of movement of the

pressure-producing members. Each of these major classifications may be further

subdivided into several specific types of commercial importance. In this manual, the

experimental work will be focused on centrifugal pump.

Kinetic pumps add energy continuously. This energy increases the fluid velocity within the pump to levels above those occurring at the discharge. When the

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high-speed fluid reaches the discharge it has to slow down to equal the lower fluid velocity found there. The resulting velocity reduction within or beyond the pump produces a pressure increase. This increase in pressure moves the pumped fluid if it exceeds the resistance found in the system. If the pump pressure does not exceed the system resistance, the fluid does not move. Kinetic pumps are further classified as Centrifugal, Regenerative Turbine, and Special Effect.

2. Type of pump

2.2 Centrifugal Pump

Figure 3: Centrifugal Pump Unit

The most common form of Kinetic pump, by far, is the Centrifugal

pump. This type of pump is a machine that uses the dynamic principle of

accelerating fluid, through centrifugal activity, and converting the kinetic

energy into pressure. Centrifugal pumps will only pump, or build pressure, to

a designed level. When this level is reached, the fluid no longer moves and

all the kinetic energy is converted to heat. This heat can cause the fluid to

vaporize or build pressure within the pump, sometimes exceeding its design

limit. Caution should be used when operating a Centrifugal pump at low or

zero flows.

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This experimental work is focused on the centrifugal pumps due to

their widely used in the industry in order to move liquids through the

pipelines. As stated above, the centrifugal force can add energy to a liquid in

a form of velocity and pressure. Centrifugal force is a force that causes an

object to move outward and away from the center of rotation. This energy

creates a pressure difference which forces liquid to flow. The major parts of

the centrifugal pump are the impeller and the casing. Impeller is the rotating

part of a centrifugal pump. The rotating impeller adds energy to the liquid by

increasing its velocity. Casing is the stationary part of a centrifugal pump. The

casing surrounds the impeller, and its shape is designed to convert the

velocity energy added to the liquid by the impeller into pressure energy.

Figure 4: The Major Parts of Centrifugal Pump

Most impellers have vanes, or blades which are designed to guide the liquid

as the impeller rotates. During operation, the liquid is whirled outward along the

vanes, away from the center. This creates a low pressure area at the suction eye of

the impeller. More liquid will be drawn into the pump through the suction nozzle

because the pressure at the center of the impeller is lower. For any rotating object, a

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point near the edge is moving faster than a point near the center. A point on the

outer tip of the impeller vane would be traveling faster than a point near the center.

In a centrifugal pump, the liquid will be traveling at its fastest speed or velocity when

it leaves the tip, or end of the impeller vane. There are various types of impellers

used in centrifugal pumps such as open, partial open and closed. The open impeller

consists of nothing but vanes. The partially open impeller has a wall or shroud on

one side of the impeller. This gives the vanes greater structural support than the

open impeller. The enclosed impeller has a shroud on both sides of the vanes.

Completely open impeller Semi-open impeller Closed impeller

Figure 5: Different Types of Impellers Used in Centrifugal Pump

The impeller and the casing are considered part of the liquid end assembly

because they are on direct contact with the pumped substance. The impeller shaft

extends through the casing wall and is coupled to the driver. The structure that

supports the shaft, casing, and driver is the frame assembly. Both sides of the

impeller maintain close clearance with the casing. Wear rings at the eye minimize

leakage from the discharge back to suction. A collar at the back of the impeller has

the same inside dimension as the suction eye. Wear rings between the collar and the

casing minimize leakage into the collar. Any leakage into the collar flows back into

suction through a hole in the impeller. This hole equalizes pressure between the left

and right sides of the impeller.

The packing box is designed to prevent or control leakage at the point where

the impeller shaft extends through the casing wall. The packing box is basically a

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cavity stuffing which is filled with a material called packing, which forms a seal

around the shaft to control leakage. The material used for packing must be

substantial enough so that it will not be damaged by the pumped liquid. The packing

should also be a non-abrasive, low-friction material that will not damaged the shaft.

Most pumps have shaft sleeve to protect the section of the shaft which extends

through the packing box, so that the sleeve will take most of the wear and abuse

from the packing. Most packing is formed into rings which fit over the shaft. The

rings are usually split on one side so they can be placed over the shaft and then

pushed into the packing box.

Figure 6: Packing Box

Since the packing wears against the shaft or shaft sleeve, it must be

lubricated to reduce friction. For many liquids, a small amount of leakage to the

outside can be tolerated. In some cases, the pumped liquid is allowed to leak into

the packing box to lubricate the packing. If leakage of the pumped liquid to the

outside cannot be tolerated, or if the pumped liquid is not suitable for lubrication of

the packing, an outside source of lubrication may be required.

In pumps where it is very critical that there be absolutely no leakage,

mechanical seals may be used instead of packing. Mechanical seals are more widely

used then shaft packing because they required less maintenance and hold leakage to

a minimum. The stationary seal ring is usually made of carbon. The rotating seal ring

is faced with special metal where it comes in contact with the stationary seal ring.

The spring holder is held in place on the shaft by a set screw. The compression ring

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and the rotating seal ring are free to move along the shaft. The springs push against

the compression ring and compress the flexible O-ring against the shaft and the

rotating seal members to prevent leakage at this point. The O-ring is made of rubber

or some other flexible material, depending on the liquid being pumped. It makes a

tight seal between the rotating elements and the shaft.

Heat generated between the stationary and rotating faces. Oil is circulated in

the packing box to cool and lubricate the seal. The lubricant also helps to keep

corrosive or erosive material out the seal. A single seal has one set sealing faces. This

seal has two sets of sealing faces. Some mechanical seals are lubricated by an

independent seal oil lubricating system. During operation, it is very important to

check to be sure the lubrication system is working properly.

Figure 7: Mechanical Seals

Some pumps do not require a seal on the shaft connecting the pump and

driver. This is because the pump and motor are housed within the same casing. Since

the shaft does not pass through the casing, there is no opening where liquids can

leak out the pump. The pump motor consists of a rotor and a coil of motor windings.

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When electric current is passed through the coil, it sets up a rotating magnetic field

which causes the rotor to move or rotate. The rotor, in turn is attached to the pump

shaft. The spinning rotor causes the shaft to rotate the impeller.

Figure 8: Seal-Less Pumps

The function of bearings is to support the shaft and allow it to rotate freely.

The bearings also control radial and axial movement of the shaft. Radial movement is

movement perpendicular to the axis of rotation of the shaft. Axial movement is

movement can damage the shaft and reduce the time to failure of the packing or

mechanical seal. To provide adequate support for the shaft, most pumps are

provided with sets of bearings. These will include radial bearings to control radial

movement of the shaft and thrust bearings to control axial movement or thrust. One

of the most common types of bearings used in pumps are ball bearings. Ball bearings

may be used both as radial bearings and as thrust bearings. The most important

thing to remember about bearings is that they require lubrication. Either grease or

oil may be used to lubricate the bearings. In grease, lubricated bearings, extreme

care must be taken to avoid over-lubrication. Excess grease can cause the bearing to

overheat.

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Figure 9: Rotation and Movement of Shaft

Figure 10: Bearing Unit

3.0 Pump Terms

During pump operations, the performance of the system is monitored based on the pump curve. From the catalogue or product brochure, students are able to get familiarized with pump term such as:

1. Capacity / Flowrate2. head / pressure3. pressure drop4. total dynamic head5. NPSHA6. NPSHR

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3.1 Capacity / Volumetric Flowrate

Capacity is defined as the volume of liquid per unit time delivered by the pump. It can also be described as the volumetric flowrate of the fluid being transferred. The most common units for capacity are usually gallons per minute (GPM)or cubic meters per hour. Centrifugal pumps do not offer a large amount of flexibility in capacity variations without affecting the pump efficiency. Capacity is often designated by the letter “Q” in current nomenclature.

When specifying capacity requirements for a centrifugal pump a range of capacities should be stated. Minimum and maximumcapacity limits are very important. These limits ensure proper pump operation, both mechanically and hydraulically.

Capacity / Volumetric Flowrate Units: cubic meters per second (m3/s), cubic feet per second (ft3/s)

Example:

1 m3 * 3.28084 ft x 3.28084 ft x 3.28084 ft = 35.3148 ft3

s 1 m3 s

1 m3 * 60 s = 60 m3

s 1 min s

1 m3 * 3600 s = 3600 m3

s 1 hr hr

35.3148 ft3

* 60 s = 2118.888 ft3

s 1 min min

35.3148 ft3

* 3600 s = 127133.28 ft3

s 1 hr min

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3.2 Head

Head is a pump term often used to describe the mechanical energy added to the fluid by centrifugal force. It is the quantity used to express the energy content of the liquid per unit weight of the liquid. Head is a good term to use with centrifugal pumps because they are constant energy devices. This means that for a given pump operating at a certain speed and handling a definite fluid volume, the energy transferred to this fluid (in foot - lbs. per foot or Newtons per meter of fluid) is the same for any fluid regardless of density.

The head generated by a given pump at a certain speed and capacity will remain constant for all fluids, barring any viscosity effects. Therefore, head when applied to centrifugal pumps is commonly expressed in feet (or meters) of liquid. Head can also be used to represent the vertical height in feet (or meters) of a static column of liquid.

3.3 PRESSURE / HEAD CONVERSION

Pressure and head are two pump terms that are related by a constant. This lesson will identify the conversions needed to complete head and pressure calculations.

1 psi = 2.3 ft of water1 bar = 10.2 m of water

1 kg/cm2 = 10 m of water

Figure 11: Equation for Pressure to Head Conversion

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3.4 TEMPERATURE EFFECT

Temperature can greatly affect any or all of the physical properties of a fluid in terms of specific gravity, viscosity and vapour pressure. A fluid’s specific gravity will vary inversely with temperature. Typically, a fluid’s specific gravity will decrease with increasing temperatures and vice versa.

Figure 12: Specific Gravity vs Temperature Chart for Various Liquid

A fluid’s viscosity will vary inversely with temperature. Typically, a fluid’s viscosity will decrease with increasing temperatures and vice versa. This explains why most fluids flow faster and easier when they are heated. A chart showing how temperature affects viscosity of various fluids is shown below

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Figure 13: Viscosity vs Temperature Chart for Various Liquid

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Every fluid has its own unique vapour pressure curve where the vapour pressure is plotted in relation to temperature. As temperatures increase, the vapour pressure of the fluid also increases. This means that as a fluid’s temperature increases, it requires more pressure to keep it from boiling and remain liquid. A chart showing the effects of temperature on the vapour pressure of various liquids is shown below

Figure 14: Vapour Pressure vs Temperature chart for various liquid

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OPERATING MANUALPIPE PRESSURE LOST

EXPERIMENT RIG TRAINING SKID

Doc. No.DEW-1207-OM-101

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4.0 Pump Selection Factors

One of the earliest decisions in the traditional design of a system is the selection of the Head and Capacity for which the pump should be sized. Regardless of how the Head Capacity conditions may be selected, much more information is required to ensure an optimal selection of pump style. For example, let's consider the liquid itself

Is it corrosive? Is it abrasive? Are there solid particles and, if so, what size and percentage are they? Is it a viscous liquid and if so, what is the viscosity? Does it tend to crystallize or otherwise solidify? What is the vapour pressure? Is it temperature sensitive?

If the liquid to be pumped is cold, clean potable water, most people are sufficiently aware of the character of that liquid to understand that none of the above factors will play a significant part in the pump selection process. However, even 'water' comes in different forms, from Condensate to Brine, which could require a wide variety of corrosion resistant materials. Even Sea Water can vary in corrosiveness from one part of the ocean to another. In addition, the abrasiveness of the water in a particular mine may dictate the use of a rubber lining in the Mine Dewatering pump purchased, while other mines have less expensive cast iron pumps performing what, at first glance, appears to be the same service. It is also worthwhile to remember that numerous new chemicals are now being introduced to many industrial processes, therefore a detailed knowledge of the liquid should never be assumed.

Consequently, the following items should be considered the minimum data required for the selection of an appropriate centrifugal process pump to suit the service for which it is intended.

a. The liquid to be pumped. b. Flow rate required.c. Total Dynamic Headd. Net Positive Suction Head availablee. Operating temperaturef. Specific Gravity.g. Nature of the liquid. (See listing above.)h. Operational experience.

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For example;

Figure 15: Pump Specification

a. Type of liquid to be pumped = Waterb. Maximum Flow Rate = 70L/min

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70L 1 gal (US) 18.52 gal

min 3.78L min

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c. Total Dynamic Head

Calculate the equivalent Length of pipe

Based on pipe lost equivalent length

Pipe ID : 0.027 m

Pipe length : 3200 + 1300+ 3600+600

8.7 m

Ball Valve : 2 Units

Bend Elbow : 2 Units

Tee-equal : 1 Unit

Equivalent Length : (2x65D) + (2x20D)+(1x20D)+(2x65x0.027) + (2x20x0.027)+(1x20x0.027)

5.13 m

=16.83ft

Then, Divide the equivalent Length by 100

16.83ft/100 = 0.1683 ft

CALCULATION OF FRICTION HEAD LOSS

Then, Find the friction loss per 100 feet of 1.0 inch pipe (based on pipe

friction loss chart)

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Figure 16: Pipe friction Loss Chart

For flowrate 18.52 GPM~20GPM and steel piping of 1 in pipe the friction loss is

42.1

Thus, it is 42.1 per 100 feet

Hence, 0.1683ft x 42.1 =7.09 ft of friction loss

ELEVATION HEAD

Based on drawing available

Figure 17: Schematic Diagram of Pipe Loss System

Elevation Height= we assume the highest elevation height is 1230mm

= 1.23m

= 4.04ft

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PRESSURE HEAD

Pressure Caculation

SG Water = 1

Maximum discharge pressure is = 30psi

= (30 x2 .31)÷1

= 69.3ft

TOTAL DYNAMIC HEAD

Therefore,

(7.09+4.04+69.3)ft=80.42ft

d. Net Positive Suction Head available

NPSHA = {Atmospheric pressure(converted to head) + static head + surface

pressure head - vapor pressure of your product - loss in the piping, valves and

fittings}

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Figure 19: Schematic Diagram of Pipe Loss System

Atmospheric pressure = 14.7 psi Gauge pressure = 0psi Liquid level above pump centerline = 600mm=0.6m=1.97ft Piping =

o Pipe ID : 0.027 mo Pipe length : 3200 + 1300+ 3600+600+8.7 mo Ball Valve : 2 Unitso Bend Elbow : 2 Unitso Tee-equal : 1 Unito Equivalent Length : (2x65D) + (2x20D)+(1x20D)+

(2x65x0.027) + (2x20x0.027)+(1x20x0.027)5.13 m

=16.83ft

Pumping =18.52 gpm. 77°F. fresh water with a specific gravity of one (1). Vapor pressure of 68°F. Water = 0.4 psia from the vapor chart. Specific gravity = 1 NPSHR (net positive suction head required, from the pump curve) = 12 feet

Then,

Static head = 1.97 feet Atmospheric pressure = pressure x 2.31/sg. = 14.7 x 2.31/1 = 34 feet absolute Gauge pressure = 0 (surface pressure head)

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Static Pressure Head

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Vapour pressure of 77°F. water converted to head = pressure x 2.31/sg = 0.4 x 2.31/1 = 0.924 feet

Looking at the friction charts:

Used the TDH calculation=

For flowrate 18.52 GPM~20GPM and steel piping of 1 in pipe the friction

loss is 42.1

Thus, it is 42.1 per 100 feet

Hence, 0.1683ft x 42.1 =7.09 ft of friction loss

Therefore,

NPSHA, (34 + 1.97 – 0 -0.924-7.09) =27.96 feet > NPSHR 7 feet + 0.5m

NPSH value of the available must be at least 0.5 m higher than the NPSH

value of the required

The pump required minimum of 12 feet of head at 18.52 gpm. And pump that we used have 27.96 feet so no cavitation will occur.

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To calculate Total Discharge Pressure,

Total Discharge Pressure= Final Pressure Required + Losses in Pipe + Vapour

Pressure

Final Pressure required= 12 psi

= 12 psi x 2.31/1 = 27.72 feet

Losses in Pipe = 1.92 feet

Vapour Pressure at 77°F = 0.4 x 2.31/1 = 0.924 feet

So, Total Discharge Pressure = (27.72 + 1.92 + 0.924) feet = 30.564 feet

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5.0 Pump Curves

A pump head- capacity performance curve identifies how a pump will operate in a given system. It is the pump’s fingerprint. This section will define the pump head- capacity performance curve, how it is created and why it is used. A pump curve, as it is commonly called, is the basis for identifying pump operation in a system

5.1 Single Pump Performance Curve

A pump head- capacity performance curve, or pump curve, is determined from actual pump performance data in a laboratory. This curve is a plot of a pump’s ability to generate fluid flow (capacity) against a certain head. Every pump, regardless of the manufacturer, has its own unique curve. As discussed earlier, a pump takes mechanical energy from a motor and transforms it to velocity energy at the impeller vanes. The pump casing then changes the velocity energy to a pressure energy at the pump discharge. This pressure energy dissipates as the fluid moves through a system (i.e., pressure drop) the pump’s head- capacity curve defines how much energy is available at a given flow rate, impeller diameter and shaft speed for each pump size. This pump curve is often called a “Single Pump Performance Curve”.

There are numerous other elements for which curves are often generated from test data in addition to the head- capacity curve. It will be further defined in the next lesson, but are listed below:

• Efficiency• Power requirements• Net Positive Suction Head Required (NPSHR)

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1. Selecting the correct size

Figure 20: Pump Curve Model Selection

Example;

Flow Rate: 4m3/hr

Total Dynamic Head: 80.42 feet = 24.5m

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24.5m

4m3/hr

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Step 1: Select the pump size and model

Pump Size is fall under Small Flow Rates under flowrate range from 1 to

10.8m3/hr

(As refer to table below)

Table 1: Pump Selection Table

Then, it has 4 models that can be selected which is K20/41M-T, K30/70M-

T,K30/100M-T and K36/100M-T

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Thus, if refer to table the best selection for pump model after consider the

flow rate and Total Dynamic Head Pump Model K 30/70M-T is the best model

to be selected.

Step 2: NPSHR (Nett Positive Suction Head Required)

Figure 21: Performance Curve Pump Model K30/70

As refer to the figure above the maximum required NPSHR for flowrate of 4m3/hr is

only 2m= 6.56 feet or 7 feet + 0.5m

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Step 3: Power Consumption of the pump

Find the power consumption of the pump at the point in the diagram where

the power curve of the impeller used meets the design flow rate. Select the motor

with the next higher power rating

Figure 22: Pump Curve

Power Consumption according to diagram is N = 0.75kW

But for this experiment we use 1.2kW power consumption which is following

the rules where selecting the next high power rating

Horse power of the pump is =1 HP

Efficiency according to diagram is nearly 40%

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6.0 Pump Installation

Improper installation of pumps can lead to premature failure and increased maintenance costs. However, when correctly installed and given reasonable care and maintenance, they will operate satisfactorily for a long period of time.

6.1 Pre-Installation

Prior to installation, we must consider few criteria as listed below;

When installing in a potentially explosive environment, make sure that the motor is properly certified.

You must earth (ground) all electrical equipment. This applies to the pump equipment, the driver, and any monitoring equipment. Test the earth (ground) lead to verify that it is connected correctly.

Electrical Connections must be made by certified electricians in compliance with all international, national, state, and local rules.

6.2 Pump Location

Table 2: Guideline on the installation of pump location

Guideline Explanation1. Keep the pumps as close to the

liquid source as practically possible

This minimize the friction loss and keeps the suction piping as short as possible

2. Make sure that the space around the pump is sufficient

This facilitates ventilation, inspection, maintenance and service

3. If you require lifting equipment such as hoist or tackle, make sure that there is enough space above the pump.

This makes it easier to properly use the lifting equipment and safely remove and relocate the component to a safe location

4. Protect the unit from weather and water damage due to rain, flooding and freezing temperature

This is applicable is nothing else specified

5. Do not install and operate the equipment in close systems unless the system is constructed with properly size safety device and control device

Acceptable devices; Pressure Relief Valve Compression Tanks Pressure Control Temperature Control Flow Control

6. Take into consideration the occurrence of unwanted noise and vibration

The best pump location for noise and vibration absorption is on a concrete floor with subsoil underneath

7. If pump located is overhead, undertake special precaution to reduce possible noise transmission

Make a noise testing and consult a noise specialist

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6.3 Foundation Requirements

A proper foundation and grouting can mean the difference between a unit that gives many years of trouble-free service and one that requires constant realignment. It should therefore be everyone's concern that only the best of materials, together with proper design, be used when performing this important function. The concrete foundation must be sufficiently substantial to absorb any vibration and to form a permanent rigid support for the baseplate. A rule of thumb that is frequently used is that the foundation should be about 5 times the weight of the pump/motor assembly, and approximately 6 inches longer and wider than the baseplate.

Listed below are the basic lists of foundation requirements;

a. The foundation must be able to absorb any type of vibration and form a permanent, rigid support for the unit.

b. The location and size of the foundation bolt holes must match those shown on the assembly drawing provided with the pump data package.

c. The foundation must weigh between two and three times the weight of the pump

d. Provide a flat, substantial concrete foundation in order to prevent strain and distortion when you tighten the foundation bolts

e. Sleeve-type and J-type foundation bolts are most commonly used. Both designs allow movement for the final bolt adjustment

6.4 Type of Bolt

a) b)

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Figure 23: a) Sleeve Type Bolt b) J- Type Bolt

7.0 Pump Performance Calculation

The fluid quantities involved in all hydraulic machines are the flow rate (Q) and the head (H), whereas the mechanical quantities associated with the machine itself are the power (P), speed (N), size (D) and efficiency (ɳ). Although they are of equal importance, the emphasis placed on certain of these quantities is different for different pumps. The output of a pump running at a given speed is the flow rate delivered by it and the head developed. Thus, a plot of head and flow rate at a given speed forms the fundamental performance characteristic of a pump. In order to achieve this performance, a power input is required which involves efficiency of energy transfer. Thus, it is useful to plot also the power P and the efficiency ɳ against Q.

7.1 Fluid Power Calculation

The hydraulic Power Output Po is the usable power transferred by the pump to the pump media

Po= ρ x g x Q x TDH

P o= 62.4 lb/ft3 x 32.174 ft/s2 x 18.52 gpm x 80.42 ft = 0.28 kW

The absorbed power Pi (Power Input, Brake Horsepower) is the power input at the coupling or shaft and it is higher than the hydraulic power.

Now the mechanical power input Pi provided by the torque T rotating the drive shaft at angular speed ω is

Pi=Tω= Q XTDH x ρ

ɳ

In engineering practice, rotational speeds are most commonly expressed in units of revolutions per minute (rpm) or in units of revolutions per second (rev/s). Conversion between

ω =rad/s, n= rev/s, and N= rev/min

ω = 1 rad/s = 9.55 r/min (rpm) = 0.159 r/s (rps)

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Is expressed by

ω=2πn=2πN60

Where; ω is expressed in units of rad/s T is expressed in units of N.m So, Pi appears in units of N m/s or in units of W

Frequency rotation of pump = 2800 rpm

Therefore; ω = 2800rpm/9.55rpm = 293.2 rad/s

If given torque value = 50 N.mPi = 50 N.m x 293.2 rad/s = 14,660 N.m/s

OrSince Efficiency, ɳ= 40% =0.4

Pi = Q XTDH x ρ

ɳ

= 18.52gpmx 80.42 ft x62.4 lb / ft30.4

= 0.7kW

Where, Q= Flowrate (gpm), ρ= Density (lb/ft3), TDH= Total Dynamic Head (feet), N = Pump Speed (rpm), ɳ= efficiency, ω= angular speed (rad/s)

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7.2 Pump Efficiency

The pump efficiency, ɳ is the ratio of pump hydraulic power output to the absorbed power at the pump coupling or shaft at the operating point.

The pump efficiency is given by the following equation;

Where;

Po=Pu= Power Output

Pi = Power Input

Thus,

ɳ = 0.28kW0.7kW

ɳ= 0.4 = 40%

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Date 20-MAY-2015

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6.0 References

i) Rishel, J.B. "Water Pumps and Pumping Systems", McGraw-Hill, New York, 2002.

ii) Karassik, I.J. (ed). "Pump Handbook ", 3rd Edition, McGraw-Hill, New York, 2001.

iii) McGuire, J. T. "Pumps for Chemical Processing". Marcel Dekker, New York, 2002.

iv) Lambeck, R.P. "Hydraulic Pumps and Motors: Selection and Application for Hydraulic

Power Control Systems, Marcel Dekker, New York, 1983.

v) Piping and Pipeline Calculations Manual Construction, Design, Fabrication, and Examination, J. Phillip Ellenberger, Elsevier Inc, 2010.

vi) Piping Handbook, Mohinder L. Nayyar, P.E., Mcgraw-Hill, 2000.

vii) Technical Note: Friction Factor Diagrams for Pipe Flow, Jim McGovern, Dublin Institute of Technology, 2011.

viii) Ross MacKay “Practical Pumping Handbook”, Elsevier Science and Technology Books, Canada, 2004

ix) Kimberley Fernandez. Et al, “Understand the Basics of Centrifugal Pump Operation”, CEP Magazine, 2002

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