Selection of pumps in oil industry

OBJECTIVE
Indian Oil Corporation is the leading company in the field of Oil, Petroleum distribution in
the country. My objective for getting internship at Indian Oil Corporation is to study in
details the functioning of the company and the processes involved in supply distribution
of the Oil & Petroleum products by the company. It is worth mentioning here that
pumps are the very important and integral part any production and distribution system
involved in the field of oil industries. The main objective of the study is to understand
the selection process that is followed by IOCL for various purchases.
In 1st
part of the report we shall study various types of pumps that are used in India
and further study in depth the centrifugal pumps which are generally used in oil
industries. Indian Oil Corporation Limited uses centrifugal pump for various processes
like pumping crude oil from offshore tankers to the port, pumping crude oil to oil
segregation plants , pumping final product to various location all over the country .
As we move further in the report we shall discuss the main characteristics that are
considered while selection of pumps. To understand the main characteristics we need
to know the working of centrifugal pumps and the physical aspects that it changes
(pressure , velocity , head). The main characteristics are used to plot various graphs
which help us in selection pumps while keeping our costs low and efficiency high . the
final selection is done via pump data sheet which is available in API-610 .

CHAPTER -1
1.0.0 INTRODUCTION TO IOCL
1.1.0 Indian Oil Corporation (IOCL) is India's largest commercial enterprise, with a sales
turnover of Rs. 4,50,756 crore and profits of Rs. 5,273 crore for the year 2014-15. It is also
the leading Indian corporate in Fortune's prestigious 'Global 500' listing of the world's
largest corporates, ranked at the 96th position for the year 2014. As India's flagship
national oil company, with a 33,000-strong workforce , Indian Oil has been meeting India’s
energy demands for over half a century. With a corporate vision to be 'The Energy of
India' and to become 'A globally admired company,' Indian Oil's business interests
straddle the entire hydrocarbon value-chain – from refining, pipeline transportation and
marketing of petroleum products to exploration & production of crude oil & gas, marketing
of natural gas and petrochemicals, besides forays into alternative energy and globalization
of downstream operations. Having set up subsidiaries in Sri Lanka, Mauritius and the UAE,
the Corporation is simultaneously scouting for new business opportunities in the energy
markets of Asia and Africa. It has also formed about 20 joint ventures with reputed
business partners from India and abroad to pursue diverse business interests.
1.1.2 BUSINESS
Indian Oil is India’s flagship Maharatna national oil company with business interests
straddling the entire hydrocarbon value chain – from refining, pipeline transportation and
marketing of petroleum products to Research & Development, Exploration & Production,
marketing of natural gas and petrochemicals. By venturing into the Renewables and the
Nuclear Energy, the company has grown and evolved itself from a pure petroleum refining
and marketing company to a full-fledged energy company.
Having set up subsidiaries in Sri Lanka, Mauritius and the United Arab Emirates, Indian
Oil is simultaneously scouting for new business opportunities in the energy markets of
Asia and Africa.
Born out of the vision of achieving self-reliance in oil refining and marketing for the nation,
Indian Oil Corporation Ltd. has the proud possession of the world’s oldest running refinery
at Digboi with a luminous legacy of more than 110 years and also the upcoming Paradip
refinery, which when commissioned would be one of the most modern and complex
refineries.
Indian Oil Group (including two refineries of its subsidiary company Chennai Petroleum
Corporation Ltd. (CPCL)) owns and operates 10 of India’s 22 refineries. The group refining
capacity of 65.7 million metric tons per annum (MMTPA) or 1.31 million barrels per day
(mb/d) is the largest among refining companies in India. It accounts for 30.5% share of

national refining capacity. On a stand-alone basis, the company owns and operates eight
refineries with a capacity of 54.2 MMTPA (1.1 mb/d).
Indian Oil Corporation Ltd.. reaches millions of people every day through an unmatched
countrywide massive and ever-expanding infrastructure network to deliver Petroleum
products. The network, comprising over 42,600 touch points as on 30.11.2014, was
strengthened from 41,640 touches. Largest and most extensive network of retail outlets,
numbering 24,403 (including 6,194 Kisan Seva Kendras), 136 depots and 6,376
consumer pumps for the convenience of large consumers, are some of the vital
components of this network, ensuring availability of products and inventory at the doorstep
of customers. The needs of domestic fuel (LPG) are fulfilled through 91 Bottling plants and
7,626 LPG distributors, serving over 86 million customers.
Continuing its thrust on reaching rural masses through Kisan Seva Kendras (KSKs) and
LPG distributorships under Rajiv Gandhi Gramin LPG Vitaran Yojana (RGGLVY), Indian
Oil Corporation Ltd. has continuously extended its reach to the rural India, with 6,194
KSKs and 1,867 RGGLVYs as on 31st November 2014. The KSKs and RGGLVs also
represent a success story for Indian Oil Corporation Ltd. in its efforts towards inclusive
development in the rural hinterlands of India. The facilities at KSKs inter-alia include
availability of seeds, pesticides, fertilizers, provisions, farm equipment, medicines, Nutan
stoves, banking help including rural ATMs, communication etc, and all under one roof.
Indian Oil Corporation Ltd. places significant thrust on knowledge and research based
growth and has a dedicated world class R&D center. The R&D center has 320 active
patents to its credit as on 30th November 2014, of which 173 are active international
patents. In the context of vagaries of the international crude oil prices and changing
domestic pricing regime, Indian Oil Corporation Ltd. R&D is viewed as a key competitive
advantage driver. Investment in proprietary research in lubricants, catalyst, refinery and
pipelines operations, and product offerings are key thrust areas for Indian Oil. Research in
new businesses, especially, petrochemicals and alternative energy is emerging a major
focus area for Indian Oil Corporation Ltd..
Indian Oil Corporation Ltd. has established itself as a key player in petrochemicals with
good market acceptability and occupies the second largest player in the domestic
petrochemical market. Under the umbrella brand PROPEL, it offers a full products slate
covering all the major segments of petrochemicals Viz. Linear Alkyl Benzene (LAB),
Purified Terephthalic Acid (PTA), Paraxylene (PX), Mono Ethylene Glycol (MEG) & other
glycols (DEG & TEG), Butene-1, Butadiene, Polypropylene (PP), Linear Low Density
Polyethylene (LLDPE), High Density Polyethylene (HDPE) etc. Indian Oil has a market
share of 22% in LAB, 16% in Polymers and 16% in Glycols. The company has also taken
a lead in expanding petrochemicals business globally with exports to 21 new countries
during 2013-14 taking the total to 66 countries with Indian Oil’s footprint.
The gas business of the Corporation is intent upon leveraging the sizeable opportunities
being presented by the country’s growing demand for gas. The company also plans to
exploit the increased international gas sourcing opportunities brought on by the

international unconventional gas revolution. The company also operates a unique concept
of supplying LNG to small customers located away from the pipelines through ‘LNG at the
Doorstep’, which has been highly successful. Indian Oil’s 5 MMTPA LNG import terminal
at Ennore will be the first such terminal on the east coast and a gateway for the
corporation to enter southern Indian gas market. This Terminal will be set up through a
Joint Venture Company led by IndianOil. The Corporation is a partner in two joint ventures,
namely, GSPL India Gasnet Ltd. And GSPL India Transco Ltd. with 26% equity
participation for building of Mehsana-Bhatinda & Bhatinda- Jammu-Srinagar gas pipelines
and Mallavaram-Bhopal-Bhilwara-Vijaypur gas pipeline, respectively.
Indian Oil Corporation Ltd. has been making continuous efforts to expand its E&P
portfolio, both in domestic as well as overseas market. Indian Oil Corporation Ltd.
presently has Participating Interest (PI) in 10 domestic and 7 overseas blocks. These
blocks are in different stages of operations. Out of the 10 domestic blocks, Indian Oil
Corporation Ltd. is operator with 100% PI in 2 onshore exploration blocks in Cambay
basin. In the remaining 8 domestic blocks, it holds non-operating participating interest
ranging from 20% to over 43%. Further, Indian Oil Corporation Ltd. holds non-operating
participating interest ranging from 3.5% to 50% in the 7 overseas blocks located in 7
countries namely Libya, Gabon, Nigeria, Yemen, Venezuela, USA and Canada.
Indian Oil Corporation Ltd foray into renewable energy is aimed not only towards
diversification through inclusion of cleaner forms of energy in its portfolio but also for
alleviating energy poverty and improving energy access at the 'base of the pyramid' in
India. In its quest towards a greener world by offering sustainable and environment-
friendly energy options, Indian Oil Corporation Ltd. is geared up to tap alternate energy
sources such as wind, solar, hydrogen and bio-fuels. Indian Oil Corporation Ltd. aims to
reduce the eco-footprints (carbon, water and waste) of its operations by exploiting these
renewable energy resources.
With a view to expanding its cleaner energy portfolio, the company has set up a Joint
Venture with NPCIL, namely, M/s NPCIL – Indian Oil Nuclear Energy Corporation Limited
(NINECL) for 2*700 MW Rajasthan Atomic Power Project 7&8 where Indian Oil has 26%
equity stake.
1.1.3 PIPELINES
Indian Oil Corporation Ltd. operates a network of 11,214 km long crude oil, petroleum
product and gas pipelines with a capacity of 77.258 million metric tons per annum of oil
and 10 million metric standard cubic meter per day of gas. Cross-country pipelines are
globally recognized as the safest, cost-effective, energy-efficient and environment-
friendly mode for transportation of crude oil and petroleum products.
The operational throughput of pipelines was recorded at 74.20 million metric tons during
2013-14. The offshore terminals of Indian Oil at Vadinar, Mundra and Paradip have
handled 218 tankers including 128 VLCCs during the year. The multi-product pipelines
successfully prepared to transport Euro IV grade fuels from refineries to marketing

centers maintaining the high quality standards of products during transportation.
Beginning with the first batch of Euro-IV MS grade quality fuel to National Capital Region
in January, 2010, Euro IV grade quality fuels have been transported through the
pipelines from refinery locations to the major metros for supply of these environment
friendly products to the consumers as per the new emission norms.
Indian Oil Corporation completed and commissioned the 290-km long Chennai-
Bangalore Pipeline to position the petroleum products from Chennai Petroleum
Corporation’s Manali refinery to Bangalore and surrounding areas in a cost-effective
manner. Crude oil feed for the expansion of Panipat refinery to 15 million tons was
arranged through the augmented Mundra-Panipat Pipeline. The augmentation project
was commissioned during the year at a cost of Rs. 165 crore against approved cost of
Rs. 205 crore.
Integrated crude oil handling facilities being provided at Paradip involves setting up of a
second and third Single Point Mooring (SPM) and concomitant subsea pipelines. Crude
oil blending application installed at Mundra has been an attractive solution for refineries
with the ability to blend different crude types to provide a consistent and optimal
feedstock to refinery operations. The online integrated crude oil blender facility is now
being implemented at Vadinar crude oil terminal to enable the maximization of yields of
higher value products.
Implementation of Paradip-Sambalpur-Raipur-Ranchi Pipeline, branch pipeline from
Koyali-Sanganer Pipeline at Viramgam to Kandla will further strengthen the petroleum
product delivery in central and western India in the coming years.
Nearly 14 pipeline projects are under implementation at an approved cost of over Rs.
6,700 Crore. Upon completion, these projects would result in additional length of over
3,600 km and added capacity of 16 MMTPA. These include the 700 km Paradip-Haldia-
Budge Budge-Kalyani-Durgapur LPG Pipeline, 295 km Sanganer-Bijwasan Naphtha
Pipeline, Augmentation of PHBPL and five additional tanks at Paradip, 270 km branch
pipeline from Patna to Motihari and Baitalpur, 120 km Cauvery Basin Refinery to Trichy
Pipeline and 400 km Ennore-Trichy-Pondicherry LPG Pipeline.

CHAPTER 2
2.0.0 CLASSIFICATION OF PUMPS
2.1.0 Classification of the pumps can be done based on different parameters such as
2.1.1 On the basis of Flow Pattern
a) Centrifugal Pumps
b) Reciprocating Pumps
 Plunger Pumps
 Diaphragm Pumps
 Piston Pumps
 Radial Piston Pumps
2.1.2 Classification of the basis of Service Liquid
2.1.4 Classification on the basis of Impeller type
2.1.5 Classification on the basis of the Mounting
2.1.6 Classification on the basis of different type of construction
2.1.7 Classification on the basis of different Position of Bearing
2.1.8 Classification on the basis of No. of stages
2.1.9 Classification on the basis of Position of Pump with respect to the Fluid
2.1.10 Classification on the basis of Splitting of casing
2.1.11 Types of centrifugal pump
2.1.12 Types of pumps available in the industry.
2.2.0` Classification on the basis of Flow Pattern
2.2.1 Intermittent-Positive Displacement Pumps.
2.2.2 Continuous-Roto-Dynamic or Turbo Pumps.
2.3.0 The two basic type of pumps are :-
1 Centrifugal pumps
2. Reciprocating pumps

2.3.1 Centrifugal Pumps
Centrifugal pumps are used to transport fluids by the conversion of rotational kinetic
energy to the hydrodynamic energy of the fluid flow. The rotational energy typically
comes from an engine or electric motor. The fluid enters the pump impeller along or near
to the rotating axis and is accelerated by the impeller, flowing radially outward into a
diffuser or volute chamber (casing), from where it exits.
Some properties of centrifugal pumps
1. The discharge is continuous and smooth.
2. It can handle large quantity of fluid.
3. It is used for large discharge through small heads.
4. Runs at high speed.
2.3.2 Reciprocating pumps
A reciprocating pump is a class of positive-displacement pumps which includes the
piston pump, plunger pump and diaphragm pumps . It is often used where a relatively
small quantity of liquid is to be handled and where delivery pressure is quite large. In
reciprocating pumps, the chamber in which the liquid is trapped, is a stationary cylinder
that contains the piston or plunger.
Some properties of reciprocating pumps:-
 The discharge is fluctuating and pulsating.
 Handles small quantity of liquid.
 It is meant for small discharge at high heads.
 Runs at low speed .
Types of reciprocating pumps

1. Plunger pumps
2. Diaphragm pumps
3. Piston pumps
4. Radial piston pumps
.
2.4.0 Classification of Pumps on the basis of service liquid
Pumps can be classified as under on the basis of service liquid
 Oil
 Water
 Mud, Slurry

2.5.0 Classification of Pumps can be classified on the basis of type of impeller
Pumps can be classified as under on the basis of type of impeller
 Open
 Semi open
 Closed
2.6.0 Classification of pumps on the basis of mounting
Pumps can be classified as under on the basis of mounting
 Vertical

 Horizontal
1.7 Classification of pumps based on different type of construction
1. Mono block-where motor is attached to shaft and the motor shaft is attached to the
impeller.
2. Other types are where the motor and pump and coupled .
1.8 Classification based on position of bearing
1. OVERHELP -On one side of the pump there is the bearing and shaft . The other side is
free unattached .
2. BETWEEN BEARING PUMPS - On both the sides of the pump there are bearings.
1.9 Classification on the basis of no. of stages
5. Single Stage (1 impeller)
6. Multi Stage (more than 1 impeller)
1.10 Classification based on the position of pump with respect to fluid
7. Submerged pumps
8. Externally placed pumps
1.11 Classification based on the type of splitting of casing
9. Axially split
10. Radially

CHAPTER 3
3.0.0 Types of pumps used in oil industry
There are various types of pumps available in the market but only centrifugal pumps are
usually used in the oil industry. Pumps can be used to pump oil, Slurry, Mud .
Centrifugal pumps are also classified into various types of pumps they are given in the
table below. The process of pump selection is a rigorous one . The API 610 is used for
the process . API-610 is a document which has the standardized rules and regulations
for the production of pumps. A Document called Pump Data sheet is used for the
purchase of pumps by various companies. Pump data sheet consists of various different
aspects of pump required by the purchaser .
3.1.0 Types of Centrifugal Pumps
3.1.1 OH1 :- Foot-mounted single-stage overhung pumps shall be designated pump type OH1.
(This type does not meet all the requirements of this International Standard)

3.1.2 OH2 :-Centreline-mounted single-stage overhung pumps shall be designated pump type
OH2. They have a single bearing housing to absorb all forces imposed upon the pump
shaft and maintain rotor position during operation. The pumps are mounted on a base
plate and are flexibly coupled to their drivers.
3.1.3 OH3 :- Vertical in-line single-stage overhung pumps with separate bearing brackets shall
be designated pump type OH3. They have a bearing housing integral with the pump to
absorb all pump loads. The driver is mounted on a support integral to the pump. The
pumps and their drivers are flexibly coupled.
3.1.4 OH4 :- Rigidly coupled vertical in-line single-stage overhung pumps shall be designated
pump type OH4. Rigidly coupled pumps have their shaft rigidly coupled to the driver
shaft. (This type does not meet all the requirements of this International Standard.)
3.1.5 OH5 :- Close-coupled vertical in-line single-stage overhung pumps shall be designated
pump type OH5. Close coupled pumps have their impellers mounted directly on the
driver shaft. (This type does not meet all the requirements of this International Standard)
3.1.5 OH6 :- High-speed integral gear-driven single-stage overhung pumps shall be
designated pump type OH6. These pumps have a speed increasing gearbox integral
with the pump. The impeller is mounted directly to the gearbox output shaft. There is no
coupling between the gearbox and pump; however, the gearbox is flexibly coupled to its
driver. The pumps may be oriented vertically or horizontally.
3.1.6 BB1 :- Axially split one- and two-stage between-bearings pumps shall be designated
pump type BB1.
BB2 :- Radially split one- and two-stage between-bearings pumps shall be designated
pump type BB2.
3.1.7 BB3 :- Axially split multistage between-bearings pumps shall be designated pump type
BB3.
3.1.8 BB4 :- Single-casing radially split multistage between-bearings pumps shall be
designated pump type BB4. These pumps are also called ring-section pumps,
segmental-ring pumps or tie-rod pumps. These pumps have a potential leakage path
between each segment. (This type does not meet all the requirements of this
International Standard.)
3.1.9 BB5 :- Double-casing radially split multistage between-bearings pumps (barrel pumps)
shall be designated pump type BB5.

3.1.10 VS1 :- Wet pit, vertically suspended, single-casing diffuser pumps with discharge
through the column shall be designated pump type VS1.
3.1.11 VS2 :- Wet pit, vertically suspended single-casing volute pumps with discharge through
the column shall be designated pump type VS2.
3.1.12 VS3 :- Wet pit, vertically suspended, single-casing axial-flow pumps with discharge
through the column shall be designated pump type VS3
3.1.13 S4 :-Vertically suspended, single-casing volute line-shaft driven sump pumps shall be
designated pump type VS4.
3.1.14 VS5 :- Vertically suspended cantilever sump pumps shall be designated pump type VS5.
3.1.15 VS6 :- Double-casing diffuser vertically suspended pumps shall be designated pump
type VS6.
3.1.16 VS7 :- Double-casing volute vertically suspended pumps shall be designated pump type
VS7.

CHAPTER 4
4.1.0 PARTS Of CENTRIFUGAL PUMPS
Following are the parts of the Centrifugal Pumps
4.1.1 Casing:- The casing of a centrifugal pump serves to house the impeller and
create a chamber for liquid to be pumped through. The drive pieces of a
centrifugal pump also are housed in the casing.
4.1.2 Suction and Discharge Nozzles :-Built into the casing itself, the suction and
discharge nozzles serve as ports for water to enter and exit from, respectively.
Typically, suction nozzles are placed on the end of the pump and discharge
nozzles are located on the top.
4.1.3 Seal Chamber and Stuffing Box :-Both seal chamber and stuffing box refer to
the portion of the pump between the shaft and casing where the sealing
mechanism of the pump is housed. Seal chambers utilize a mechanical seal,
whereas stuffing boxes achieve the sealing purpose through some form of
packing. Regardless of the method used, the chamber is used to prevent liquid
from exiting the pump.
4.1.4 Bearing Housing:-The bearing housing is used to enclose and protect the shaft
bearings, ensuring proper alignment. The housing will also include some type of
method for lubricating the bearings and cooling the pump.
4.1.5 Impeller :-The main moving portion of the centrifugal pump. An impeller is a
specially designed component critical for proper functioning of the pump.
Depending on the suction type and mechanical construction of the pump, the
actual design of the impeller may vary.
4.1.6 Shaft:- The shaft transfers the electrical or mechanical energy powering the
pump directly to the impeller. In addition, the shaft is responsible for supporting
any other moving parts on the pump. The shaft is responsible for a great deal of
both energy transfer and structural support and therefore must be carefully
machined.

4.1.7 Oil ring :- The bearings are most frequently oil bath or oil ring lubricated.

CHAPTER 5
5.0.0 IMPORTANT CHARACTERISTICS
Objective of understanding the characteristics of the pumps is to understand the
functioning of the pump as a whole based on following parameters:-
 Working of Pumps
 Head of a Pump
 Importance of Head
 Total Head
 NPSHR
 NPSHA
 Volume Flow Rate
5.1.0 Working of a Pump
Centrifugal pumps are used to induce flow or raise pressure of a liquid. Its working is
simple. At the heart of the system lies impeller. It has a series of curved vanes fitted
inside the shroud plates. The impeller is always immersed in the water. When the
impeller is made to rotate, it makes the fluid surrounding it also rotate. This imparts
centrifugal force to the water particles, and water moves radially out. Since the rotational
mechanical energy is transferred to the fluid, at the discharge side of the impeller, both
the pressure and kinetic energy of the water will rise. At the suction side, water is getting
displaced, so a negative pressure will be induced at the eye. Such a low pressure helps
to suck fresh water stream into the system again, and this process continues. A
rotodynamic or centrifugal pump is a dynamic device for increasing the pressure of liquid.
In passing through the pump, the liquid receives energy from the rotating impeller. The
liquid is accelerated circumferentially in the impeller, discharging into the casing at high
velocity which is converted into pressure as effectively as possible.
5.2.0 Head of a Pump
It is assumed that a pump designed to move water clamped into a process line. There is
a suction line and a discharge line, both running horizontally. Assuming that we are able
to “move” the discharge line so it pumps straight up into the air. The pump is then turned
on. Once the pump is running, it will move the fluid to some height measured in feet.
That height to which the pump can raise the water to is its head.
5.3.0 Importance of Head

As the manufacturers do not know for what kind of fluid the purchaser requires the
pump .The pump manufacturer's want to tell you how much head their pump's will
produce but they don't know what type of water supply will be available, so how can they
get around this. Ingeniously simple, they subtract the head available at the suction from
the head produced at the discharge, they call this Total Head. Then it doesn't matter
what the suction tank level is, they are telling you only what the pump can do regardless
of the water supply pressure at the suction head is it is independent of the type of fluid
being pumped (assuming the viscosity is relatively low and similar to water). Whether
you’re pumping water or a heavy caustic solution, the head achieved will be the same.
The pressure at the discharge of the pump, however, will be higher for the heavier
solution. The relationship between head and pressure can be characterized by the
following formula.
5.4.0 Total Head
Total Dynamic Head (TDH) is the total equivalent height that a fluid is to be pumped,
taking into account friction losses in the pipe.
TDH = Static Height + Static Lift + Friction Loss
Static Height is the maximum height reached by the pipe after the pump (also known as
the 'discharge head').
Static Lift is the height the water will rise before arriving at the pump (also known as the
suction head).
Friction Loss (or Head Loss).- this depends on the length of pipes and their diameter and
the flow rate . Friction losses are different for different flow rates .
The relationship of head to pressure is expressed as
h=2.31p/SG
where
h = height of the fluid column above a reference point
p = pressure.
SG= Specific gravity
Net positive Suction head
NPSH is defined as the total suction head in feet of liquid (absolute at the pump centerline
or impeller eye) less the vapor pressure (in feet) of the liquid being pumped.
5.5.0 Net positive suction head required

Net positive suction head required (NPSHR) is defined as the amount of NPSH required to
move and accelerate the liquid from the pump suction into the pump itself. It is determined
either by test or calculation by the pump manufacturer for the specific pump under
consideration. NPSHR is a function of liquid geometry and the smoothness of the surface
areas. For centrifugal pumps, other factors that control NPSHR are:
 Type of Impeller
 Design of impeller
 Rotational Speed
5.6.0 Net positive suction head available
NPSHA must be equal to or greater than NPSHR. If this is not the case, cavitation or
flashing may occur in the pump suction. Cavitation occurs when small vapor bubbles
appear in the liquid because of a drop in pressure and then collapse rapidly with
explosive force when the pressure is increased in the pump. Cavitation results in
decreased efficiency, capacity, and head and can cause serious erosion of pump parts.
Flashing causes the pump suction cavity to be filled with vapors and, as a result, the
pump becomes vapor locked. This usually results in the pump freezing up, which is
called pump seizure.
NPSHA is not a function of the pump itself but of the piping system for the pump. It can
be calculated from
pA = atmospheric pressure
pva = liquid vapor pressure at pumping temperature.
NPSHA decreases with increases in liquid temperature and pipe friction losses. Because
pipe friction losses vary as the square of the flow, NPSHA also varies as the square of
the flow. Thus, NPSHA will be the lowest at the maximum flow requirement.
5.7.0 Volume flow rate (Q)
Also referred to as capacity, is the volume of liquid that travels through the pump in a
given time (measured in gallons per minute or gpm). It defines the rate at which a pump
can push fluid through the system. In some cases, the mass flow rate (ṁ) is also used,
which describes the mass through the pump over time.

CHAPTER 6
6.0.0 CHARACTERISTIC CURVES : The objective is to study characterstic curves i.e
 Performance Curve
 The System Curve
Following terms are used to understand the characterstics curves Terms Used
 Shut off Head
 Cut off Head
 Pump Runout
 BHP
 Impeller Trim
6.1.0 The performance or characteristic curve of the pump
The pump characteristic is normally described graphically by the manufacturer as a
pump performance curve. The pump curve describes the relation between flow rate and
head for the actual pump. Other important information for proper pump selection is also
included - efficiency curves, NPSHr curve,pump curves for several impeller diameters
and different speeds, and power consumption.
During a test, the total head that a centrifugal pump can develop is a function of the
speed at which the impeller is turned and the diameter of the impeller. If a pump impeller
is being turned at its rated speed and a valve on the discharge side of the pump is
closed, it will develop a certain maximum head. Under these conditions, this head is
read on a pressure gauge. The gauge reading translated into feet registers the height to
which the pump is capable of elevating water. This is known as the “shut off head.” If the
valve is slowly opened, the pressure gauge reading will fall as the flow increases, and

this will continue until some point of maximum flow and minimum head is reached. If the
total head being developed at any given rate of flow is plotted against the quantity of
water being delivered, the result will be a performance curve for this particular pump at
this particular speed.
Each pump will have its own maximum efficiency point. The best efficiency point (BEP)
is the point of highest efficiency of the pump. All points to the right or left of the BEP
have a lower efficiency.
Increasing the impeller diameter or speed increases the head and flow rate capacity -
and the pump curve moves upwards.
The head capacity can be increased by connecting two or more pumps in series, or the
flow rate capacity can be increased by connecting two or morepumps in parallel.The
pump performance curves can made for trimmed impeller for same conditions
The units considered are different for different purposes . This curve is used to find the
head flow of a trimmed impeller for a specific efficiency and flow rate . The impeller is
trimmed to adjust to the requirement of a particular buyer.
6.2.0 The System Curve

A fluid flow system can in general be characterized with the System Curve - a graphical
presentation of the Energy Equation.
The system head visualized in the System Curve is a function of the elevation - the static
head in the system, and the major and minor losses and can be expressed as:
H=dh+h
where
H= System Head
dh= elevation (static) head - difference between inlet and outlet of the system
h= Head loss
Head loss = kq^2
Increasing the constant - k - by closing some valves, reducing the pipe size or similar - will
increase the head loss and move the system curve upwards. The starting point for the
curve - at no flow, will be the same.
Centrifugal pumps always pump somewhere on their curve, but should be selected to
pump as close to the best efficiency point (B.E.P.) as possible. The B.E.P. will fall some
where between 80% and 85% of the shut off head (maximum head).

6.3.0 Terms used
6.3.1 Shut off Head: The highest point the pump will lift liquid. At this point the pump will
pump 0 gallons per minute.
6.3.2 Cut-off Head: The head at which the energy supplied by a pump and the energy
required to move the liquid to a specified point are equal and no discharge at the desired
point will occur.
6.3.3 Pump run out: is the maximum flow that can be developed by a centrifugal pump
without damaging the pump. Centrifugal pumps must be designed and operated to be
protected from the conditions of pump runout or operating at shutoff head.
6.3.4 BHP : Break Horse Power . The pump performance curve will give information on the
brake horsepower (BHP) required to operate a pump (horsepower required at the pump
shaft) at a given point on the performance curve. The brake horsepower curves run
across the bottom of the pump performance curve usually sloping upward from left to
right. These lines correspond to the performance curves above them (the top
performance curve corresponds to the top BHP line and so on). Like the head-capacity
curve, there is a brake horsepower curve for each different impeller trim.
6.3.5 Impeller Trims : Impeller trims or impeller diameter is measured in either inches or
millimeters. Pump performance curves generally show performance for various impeller
diameters or trims. Manufacturers will put several different trim curves on a pump
performance curve to make pump specification easier, although this sometimes makes
the pump performance curve more difficult to read. It is good practice to select a pump
with an impeller that can be increased in size permitting a future increase in head and
capacity.

CHAPTER 7
7.0.0 FACTORS FOR PUMP SELECTION
7.1.0 Various factors considered while selecting the pumps are studied in this chapter: They
are broadly classified as under:-
7.1.1 Definition of the technological process outline and main process parameters, such as
flow, pressure and temperature.
7.1.2 Determination of the required pumping services.
7.1.3 Complete description of the fluid to be handled in each pumping operation (type of fluid,
temperature, density, viscosity, vapour pressure, solids in suspension, toxicity, volatility)
7.1.4 General layout of the plant and determination of available space in three dimensions;
7.1.5 General arrangement and dimension of the piping according to the recommended
velocities for each fluid and type of pipe;
7.1.6 Determination of elevation for suction and discharge points of vessels, relative to the
centre line of the pump;
7.1.7 Preliminary calculation of friction losses and plotting of system characteristic curves;
7.1.8 Definition of the working parameters of the pump, namely capacity, head, suction and
discharge pressures – taking into account any possibility of variations in pressure or
temperature at different pumping conditions;
7.1.9 Determination of any possible exceptional start, stop or running conditions;
7.1.10 Determination of available NPSH (Net Positive Suction Head);
7.1.11 Preliminary selection of the pump type, design, position, driver, type of sealing, and
cooling of seal and bearings – if required;
7.1.12 Establishing the type of drive unit (electric motor, steam turbine, etc) and its main
operating parameters
7.2.0 Factors to be discussed in the report
7.2.1 Primary Factors
 Total Head
 Flow Rate
 Service

a) Head
The total head, suction lift and flow rate are dependent upon the piping system and the
pump’s characteristics. The piping system and the pump interact to determine the
operating point of the pump – flow rate and pressure.The pump cannot independently
control these parameters. As the flow rate is increased the work to move each unit of
water or total dynamic head the pump must produce increases.
Total head and flow are the main criteria that are used to compare one pump with
another or to select a centrifugal pump for an application. Total head is related to the
discharge pressure of the pump.
Steps are
 Determine the static head
 Determine the Friction Head
 Calculate the total Head
Select the pump based on the pump manufacturer’s catalog information using the total
head and flow required as well as suitability to the application
B) Flow rate
Flow rate is directly proportional to speed or the velocity of the impeller . Changing the
impeller diameter gives a proportional change in peripheral velocity which thus causes a
change in the flow rate .
C) Services
By service it means whether it is operated continuously or weekly , quarterly , monthly
etc.This is required as the pipelines might get clogged if not operated continuously and
cleaning operations need to be done. For example In oil industry if a pipeline is not used
continuously then grease and other materials are clogged inside the pipeline . Thus to
reach the optimum flow warm crude oil is first transported through the pipes so that the
grease and other substances would melt within days.
7.2.2 Secondary Factors
 NPSH
 Purpose
 Efficiency
 Range
NPSH - Net positive suction head
For safe operation, NPSHA should exceed NPSHR (net positive suction head required)
by more than 1m at the rated condition. As the NPSHR varies, depending on the head
and flow, it is safer to select the margin at the end of the curve.

If the incoming liquid is at a pressure with insufficient margin above its vapour pressure,
then vapour cavities or bubbles appear along the impeller vanes just behind the inlet edges.
This phenomenon is known as cavitation and has three undesirable effects:
 The collapsing cavitation bubbles can erode the vane surface, especially when
pumping water-based liquids.
 Noise and vibration are increased, with possible shortened seal and bearing life
 The cavity areas will initially partially choke the impeller passages and reduce the
pump performance. In extreme cases, total loss of pump developed head occurs
The three undesirable effects of cavitation described above begin at different values of
NPSHA and generally there will be cavitation erosion before there is a noticeable loss of
pump head. However for a consistent approach, manufacturers and industry standards,
usually define the onset of cavitation as the value of NPSHR when there is a head drop
of 3% compared with the head with cavitation free performance. At this point cavitation is
present and prolonged operation at this point will usually lead to damage. It is usual
therefore to apply a margin by which NPSHA should exceed NPSHR.
7.3.0 Cost
The ultimate deciding factor for a pump in the Oil pipeline Industry is the cost . The cost
is to be minimized.
7.4.0 Purpose
That is the desired function of the pump . The function of the pump is same creating a
head difference so that product can be transported . For example for irrigation a pump
might be used to extract water from an underground well . For this the pump can be
place in the ground immersed in water or if the net suction is sufficient it can be placed
above ground and water can be pumped out .
7.5.0 Efficiency
Selecting a correct pumping plant not only will conserve valuable energy supplies but
also will reduce total annual pumping costs. Inefficient pumping plants can increase
costs dramatically.
The efficiency of a pump is a measure of the degree of its hydraulic and mechanical
perfection. Pump efficiency is the ratio of the output water horsepower to the input shaft
horsepower.
Some of the energy losses that result in lower efficiency are friction in the bearings that
support the pump shaft, friction between the shaft and the packing in the stuffing box,
unavoidable leakage between areas of high pressure and adjacent areas of low
pressure inside the pump case, and the friction caused by the water moving across the
metallic surfaces in the pump. There are also other losses of a more complex nature.

To conserve maximum energy the BEP should be between the rated point and the
normal operating point.
The efficiency of a pump is determined by actual tests. The power required to turn the
pump during the process of maximum flow and minimum head, you will note that the
power is at a minimum for this typical centrifugal pump when there is no water being
discharged from the pump and that the power required will gradually increase as the rate
of flow increases and the head decreases. The maximum efficiency will be about
midway between zero flow and maximum flow.
7.6.0 Range
The range is basically region of operation of that unit .It is the region where the efficiency
is maximum according to our requirements .The lowest mark on the range corresponds
to the NPSHR to avoid cavitation .running the pump outside the recommended operating
range could and most likely will damage the pump by shortening bearing and seal life or
even damage the shaft
7.7.0 Cost
A cost analysis of pumping will consider initial cost of capital investment, annual fixed
cost and operating cost. All three costs are somewhat dependent on each other. The
type of pumping equipment, size of pipelines, size of pumps and type of water supply
affect not only the initial cost but also the fixed cost as well as the operating cost. For
example, piping systems using large pipes may cost more but could allow the use of
smaller horsepower pumps which cost less, require smaller power sources and cost less
to operate than a piping system with small diameter pipe. The lowest priced system is
not always the best buy, especially if the lower price means less efficient pumps. To get
the most efficient pump, an analysis should be made of all pumping requirements.

CHAPTER 8
8.0.0 SPILLING OF PARAMETERS
8.1.0 OBJECTIVES
 Why should we split the parameters
 Pumps in parallel
 Pumps in Series
8.1.0 Why should we split the parameter.
Using circulating pumps in parallel or series configurations can attain many economic
and operational gains as opposed to using one large pump to supply a system’s
pumping requirements.
Employing a combination of in-line pumps rather than base-mounted pumps to
accomplish a pumping requirement eliminates the need for pump mounting pads,
grouting, and shaft alignment. Equipment room floor space can be utilized for something
else. The installed cost of two low-cost stock in-line pumps will be less than the installed
cost of one large base-mounted pump, and can provide standby protection at no extra
cost.
Often a designer will specify two pumps, each one capable of handling the entire load.
In some cases, this may be essential, but on many installations, the cost of providing full
standby capacity is prohibitive.
8.2.0 Pumps in parallel
Energy efficient method of flow control, particularly for systems where static head is a
high proportion of the total, is to install two or more pumps to operate in parallel.
Variation of flow rate is achieved by switching on and off additional pumps to meet
demand. The combined pump curve is obtained by adding the flow rates at a specific
head.

The head/flow rate curves for two and three pumps are shown in Figure
The system curve is usually not affected by the number of pumps that are running. For a
system with a combination of static and friction head loss the operating point of the
pumps on their performance curves moves to a higher head and hence lower flow rate
per pump, as more pumps are started. It is also apparent that the flow rate with two
pumps running is not double that of a single pump. If the system head were only static,
then flow rate would be proportional to the number of pumps operating. It is possible to
run pumps of different sizes in parallel providing their closed valve heads are similar. By
arranging different combinations of pumps running together, a larger number of different
flow rates can be provided into the system.

8.3.0 WORKING
The total system flow divides into two parallel paths. The check valves prevent any flow
short-circuiting, especially if only one pump runs. Since almost all installations of parallel
pumps are with identical pumps, each pump will pump exactly one half of the total flow
rate. Each pump will produce the same pressure head. Each pump will operate at the
same point on its pump curve. In short, when both pumps are running, each pump s
upplies one-half of the total flow rate at the total system head.
If one of the pumps should fail, the other pump should still be able to supply enough flow
to satisfy system demand, except in the worst weather.
8.4.0 Advantages of pump in series
Applying parallel pumps in a system can be a cost-effective solution when capacity
requirements call for an unrealistically large pump and motor. Using parallel pumps can
also reduce current surge during motor startup by staging two or more smaller pumps.
This is a problem which may otherwise require expensive equipment such as electronic
soft starters or part winding type motors. One of the most notable benefits of parallel
pumps is the redundancy built into the system. If one pump were to fail in a two pump
system, the second pump would not only continue to operate, but would also increase its
output
The beauty of parallel pump systems: If one pump were to fail, the second pump would
run out on its curve until it crossed the system curve.

8.5.0 PUMPS IN SERIES
Putting your centrifugal pumps in series, or connected along a single line, will let you add
the head from each together and meet your high head, low flow system requirements.
This is because the fluid pressure increases as the continuous flow passes through each
pump, much like how a multi-stage pump works.
Some things to consider when you connect pumps in series:
 Both pumps must have the same width impeller or the difference in capacities (GPM or
Cubic meters/hour.) could cause a cavitation problem if the first pump cannot supply
enough liquid to the second pump.
 Both pumps must run at the same speed (same reason).
 Be sure the casing of the second pump is strong enough to resist the higher pressure.
Higher strength material, ribbing, or extra bolting may be required.
 The stuffing box of the second pump will see the discharge pressure of the first pump.
You may need a high-pressure mechanical seal.
 Be sure both pumps are filled with liquid during start-up and operation.
 Start the second pump after the first pump is running.
After All the factor have been considered a Pump Data sheet is filled. The pump Data
sheet is used by a purchaser to list its requirements and narrow down a few pumps .

CHAPTER 9
9.0.0 PUMP DATA SHEET : The objective is to study the pump data sheet is to get acquitted
with the various terms used for following pumps such as
9.1.0 Terms and definitions used in pump data sheet
9.1.1 Barrel Pump :- horizontal pump of the double-casing type.
9.1.2 Best Efficiency Point (BEP) :- flow rate at which a pump achieves its highest efficiency..
9.1.3 Critical Speed :- shaft rotational speed at which the rotor-bearing-support system is in a
state of resonance.
9.1.4 Dry Critical Speed :- rotor critical speed calculated assuming that there are no liquid
effects, that the rotor is supported only at its bearings and that the bearings are of infinite
stiffness.
9.1.5 Wet Critical Speed :-rotor critical speed calculated considering the additional support
and damping produced by the action of the pumped liquid within internal running
clearances at the operating conditions and allowing for flexibility and damping within the
bearings.
9.1.6 Suction Pressure max :- highest suction pressure to which the pump is subjected
during operation
9.1.7 NPSH ,Net Pressure suction Head :-total absolute suction pressure determined at the
suction nozzle and referred to the datum elevation, minus the vapour pressure of the
liquid
9.1.8 NPSHA , Net Pressure Suction Head Available :- NPSH determined by the purchaser
for the pumping system with the liquid at the rated flow and normal pumping temperature.
9.1.9 Rated flow :The pump inlet flow, which will be measured, and guaranteed, when the
pump is tested. Rated flow is associated with rated differential head for rotodynamic
pumps, and rated outlet pressure for positive displacement pumps.
9.1.10 Suction Pressure: Operation of the pump creates suction (a lower pressure) at the
suction side so that fluid can enter the pump through the inlet. Pump operation also
causes higher pressure at the discharge side by forcing the fluid out at the outlet.
9.1.11 Rated Suction pressure :Rated suction pressure would be the suction pressure needed
when the pump is discharging its rated flow.
9.1.12 Discharge Pressure: Discharge pressure describes the pressure of a liquid as it leaves
a pump.

9.1.13 Differential Pressure. it is the amount of head that is added to the system .Differential
pressure is the pressure increase provided by the pump between the pump inlet and
outlet. It is measured as the difference between the pressure at the pump’s discharge
flange and the suction flange.
9.1.14 NPSHA :The absolute pressure at the suction port of the pump.NPSHA MUST be
greater than NPSHR for the pump system to operate without cavitating.
NPSHA = HA ± HZ - HF + HV – HVP
HA=The absolute pressure on the surface of the liquid in the supply tank
HZ=The vertical distance between the surface of the liquid in the supply tank and the
centerline of the pump
HF=Friction losses in the suction piping
HV=Velocity head at the pump suction port
HP=Absolute vapor pressure of the liquid at the pumping temperature .
9.1.15 Area classification : method of analysing and classifying the environment where
explosive gas atmospheres may occur so as to facilitate the proper selection and
installation of equipment to be used safely in that environment
9.1.16 Class : The Class defines the general nature (or properties) of the hazardous material
in the surrounding atmosphere which may or may not be in sufficient quantities
a) Class I—Locations in which flammable gases or vapors may or may not be in
sufficient quantities to produce explosive or ignitable mixtures
b) Class II—Locations in which combustible dusts (either in suspension,
intermittently, or periodically) may or may not be in sufficient quantities to
produce explosive or ignitable mixtures.
c) Class III—Locations in which ignitable fibers may or may not be in sufficient
quantities to produce explosive or ignitable mixtures.
9.1.17 Division—The Division defines the probability of the hazardous material being able to
produce an explosive or ignitable mixture based upon its presence.
a. Division 1 indicates that the hazardous material has a high probability of producing
an explosive or ignitable mixture due to it being present continuously, intermittently, or
periodically or from the equipment itself under normal operating conditions.
b. Division 2 indicates that the hazardous material has a low probability of producing an
explosive or ignitable mixture and is present only during abnormal conditions for a short
period of time

9.1.18 Group—The Group defines the type of hazardous material in the surrounding
atmosphere. Groups A, B, C, and D are for gases (Class I only) while groups E, F, and
G are for dusts and flying’s (Class II or III).
a) Group A—Atmospheres containing acetylene.
b) Group B—Atmospheres containing a flammable gas, flammable liquid-produced
vapor, or combustible liquid-produced vapor whose MESG is less than 0.45 mm
or MIC ratio is less than 0.40.
c) Group C—Atmospheres containing a flammable gas, flammable liquid-produced
vapor, or combustible liquid-produced vapor whose MESG is greater than 0.45
mm but less than 0.75 mm or MIC ratio is greater than 0.40 but less than 0.80.
Typical gases include ethyl either, ethylene, acetaldehyde, and cyclopropane.
D) Group D—Atmospheres containing a flammable gas, flammable liquid-produced
vapor, or combustible liquid-produced vapor whose MESE is greater than 0.75
mm or MIC ration is greater than 0.80. Typical gases include acetone, ammonia,
benzene, butane, ethanol, gasoline, methane, natural gas, naphtha, and propane.
e) Group E—Atmospheres containing combustible metal dusts such as aluminum,
magnesium, and their commercial alloys.
f) Group F—Atmospheres containing combustible carbonaceous dusts with 8% or
more trapped volatiles such as carbon black, coal, or coke dust.
g) Group G—Atmospheres containing combustible dusts not included in Group E or
Group F. Typical dusts include flour, starch, grain, wood, plastic, and chemical .
9.1.19 Location of pump : Location of pumps are based on the application .
Typical applications include
 Water disposal
 Secondary recovery
 Glycol dewatering
 Amine sweetening
 Chemical injection
 Crude transfer
 Fire protection
 Pipeline Transfer
 Produced water disposal
 Secondary recovery (water flood)
 Chemical injection Glycol dehydration
 Well servicing
 Blow out preventer
 Liquefied natural gas
 Lean oil circulation
 Closed drain pump-out
 Knockout drum pump-out

 Driver Type : can be and induction motor or a steam turbine or other type of
power sources
9.2.0 Full Load : Full Load is the expected performance of the motor at the rated or
nameplate hp. Maximum Load is often also referred to as service factor amps or max
amps
9.3.0 Locked Motor AMPS : Locked Rotor Current" also called LRA which stands for Locked
Rotor Amps, is commonly found on electric motor nameplates. Locked Rotor essentially
means the motor is not turning. The current or amps in this case have to do with the
amount of electrical energy required to start the motor. At the instant the motor is switched
on, it is not turning, and draws the maximum current. As the motor starts to turn, the
current goes down. This required energy is much greater than the Full Load Amps or
Running Amps, which is the current drawn when the motor is running at normal speed
under full load. The current required to start the motor will depend on the type of motor as
well as the specified design voltage required for the motor, typically the higher the voltage,
the lower the required amperage or current.
9.4.0 Radial Bearing : Radial bearings accommodate loads that are predominantly
perpendicular to the shaft. The bearings are typically classified by the type of rolling
element and shape of the raceways.
9.5.0 Classfication of Flammable Liquid : a flash point below 100 degrees Fahrenheit (38
degrees Celsius). Less-flammable liquids (with a flashpoint between 100 degrees and
200 degrees Fahrenheit) are defined as combustible liquids.
9.6.0 Flash Point : Flash point is the lowest temperature at which a liquid can form an
ignitable mixture in air near the surface of the liquid. The lower the flash point, the easier
it is to ignite the material.
9.7.0 Chloride conc : The concentration of these salts in the crude oil depends on the oil
field from which the crude is extracted, but it is usually present within the range of 3 to
300 pounds per barrel. In heavy crude oils this value tends to be higher.
9.8.0 H2S conc : Crude oils usually contain sulfides that can cause corrosion at high
temperatures. This is called sulfidation. It is a well-known corrosion in different units in oil
refineries. The amount of total sulfur in a crude oil depends on the type of oil field and it
varies from 0.05 percent to 14 percent. Of course, sulfur values as low as 0.2 percent
are enough to create sulfidation corrosion in plain steels and low alloy steels. These
kinds of steels are usually proposed to be used in several parts of refinery units.
9.9.0 Pump Performance Curve : The pump characteristic is normally described graphically
by the manufacturer as a pump performance curve. The pump curve describes the
relation between flow rate and head for the actual pump.
9.10.0 Impeller Diameter : The calculations are based on the affinity laws which in turn are
derived from a dimensionless analysis of three important parameters that describe pump
performance . If the speed (revolutions per minute) of the impeller remains the same
then the larger the impeller diameter the higher the generated head. Note that as you
increase the diameter of the impeller the tip speed at the outer edge of the impeller
increases commensurately. However, the total energy imparted to the liquid as the
diameter increases goes up by the square of the diameter increase. This can be

understood by the fact that the liquid's energy is a function of its velocity and the velocity
accelerates as the liquid passes through the impeller. A wider diameter impeller
accelerates the liquid to a final exit velocity greater than the proportional increase in the
diameter.
9.11.0 Maximum allowable Pressure : MAWP being the maximum pressure based on the
design codes that the weakest component of a Pressure vessel can handle. Commonly
standard wall thickness components are used in fabricating pressurized equipment, and
hence are able to withstand pressures above their design pressure.
9.12.0 Design Pressure : The most severe condition of coincident internal or external pressure
and temperature (minimum or maximum) expected during service”.
9.13.0 OTHER TERMS AND DEFINITIONS USED IN PUMP DATA SHEET
 OPERATING CONDITIONS
 SITE DATA
 DRIVER TYPE
 MOTOR DRIVER
 LIQUID
 MATERIAL
 PERFORMANCE
 UTILITY
 CONSTRUCTION
 SURFACE PREPARATION AND PAINT
 HEATING AND COOLING
 BEARINGS AND LUBRICATION
9.13.1 OPERATING CONDITIONS
PARAMETER GIVEN BY REQUIREMENTS
Flow, Rated Purchaser Rated flow is associated with rated
differential head for roto-dynamic pumps,
and rated outlet pressure for positive
displacement pumps.
Suction pressure max. Purchaser Some factor like pump's suction flange
which limits suction pressure to the given
maximum value.
Suction Pressure rated Purchaser It depends on rated flow .
Discharge Pressure Discharge pressure depends on the
pressure available on the suction side of
the pump
Differential Pressure Determined by evaluating all pressure (or
head) losses from the liquid level in the
receiver through all piping and

components of the system and back to the
receiver.
NPSHA Purchaser It depends on five factors
1)The absolute pressure on the surface of
the liquid in the supply tank.
2)The vertical distance between the
surface of the liquid in the supply tank and
the centerline of the pump
3)Friction losses in the suction piping
4)Velocity head at the pump suction port
5)Absolute vapor pressure of the liquid at
the pumping temperature
Service:
continuous/intermittent/
parallel operations required
Purchaser The type of service depends on the
requirement of the product , the cost of
operation that is incurred , the eeficiency.
9.13.2 SITE DATA
PARAMETER GIVEN
Location: Purchaser Based on the application of pump and the
location of the plant.
Altitude Purchaser Based on location of plant.
Barometer Purchaser Based on location of plant
Range of ambient
temperature
Purchaser Based on location of plant
Relative Humidity Purchaser Based on location of plant
Usual Conditions
1)Dust
2)Fumes
Purchaser Based on location of plant
ELECTRICAL
CLASSIFICATION AREA
Class Purchaser It depends on the general nature of the
explosive material . It might be
1)gas or vapour
2)Dusts
4)Fiber
Group Purchaser Depends on the type of hazardous
material in the surrounding atmosphere.
Groups A, B, C, and D are for gases
(Class I only) while groups E, F, and G
are for dusts and flyings (Class II or III).
Division Purchaser Depends on the probability of the
hazardous material being able to produce
an explosive or ignitable mixture based
upon its presence.

9.13.3 DRIVER TYPE
PARAMETER GIVEN BY REQUIREMENT
Driver type Purchaser The types of drives that can be used are
turbines , induction motor , engines etc.
9.13.4 MOTOR DRIVER
Power Manufacturer The power at which the motor driver
operates and provides the required
impeller speed , head , flow rate.
Frame Manufacturer The Frame type of the motor driver .
VOLTS/PHASE/HERTZ Manufacturer The specifications of electricity supply
required by the motor.
Minimum Starting Voltage Manufacturer The voltage below which the motor will
not start.
Insulation Manufacturer The insulation of motor from the liquid
being used.
Temperature rise manufacturer The rise in temperature in the motor due
the working of the motor driver , the
friction when coupled.
Full Load AMPS Manufacturer expected performance of the motor at the
rated or nameplate hp.
LOCKED rotor AMPS Manufacturer depend on the type of motor as well as
the specified design voltage required for
the motor
Starting Method Manufacturer The motor driver is and electrical device
it is important to mention the starting
method . Is it battery operated or another
electrical supply is attached
Radial Bearing Type Manufacturer The type of bearings used to reduce the
friction . These are lubricated .

9.13.5 LIQUID
Liquid type ;
Hazardous/Flammable
Purchaser a flash point below 100 degrees
Fahrenheit (38 degrees Celsius). Less-
flammable liquids (with a flashpoint
between 100 degrees and 200 degrees
Fahrenheit) are defined as combustible
liquids.
Pumping Temp. Purchaser The temperature at which the liquid is to
be pumped.
Vapour Pressure Purchaser Vapor pressure or equilibrium vapour
pressure is defined as the pressure
exerted by a vapor in thermodynamic
equilibrium with its condensed phases
(solid or liquid) at a given temperature in
a closed system. It is The property of the
liquid .
Relative Density Purchaser Relative density, or specific gravity, is the
ratio of the density (mass of a unit
volume) of a substance to the density of
a given reference material.It is the
property of the liquid used
Viscosity Purchaser The viscosity of a fluid is a measure of its
resistance to gradual deformation by
shear stress or tensile stress. For liquids,
it corresponds to the informal concept of
"thickness"
Specific Heat Purchaser The specific heat is the amount of heat
per unit mass required to raise the
temperature by one degree Celsius. It is
the property of the liquid.
Chloride Concentration Purchaser The concentration of these salts in the
crude oil depends on the oil field from
which the crude is extracted,
H2S concentration purchaser Total sulfur in a crude oil depends on the
type of oil field and the conc with H2.

9.13.6 MATERIALS
ANNEX H CLASS Purchaser Materials and material
specifications for pump parts
reduced hardness material
required
Purchaser Annexure H
Barrel case Purchaser Annexure H
Impeller Purchaser Annexure H
Impeller Wear Rings Purchaser Annexure H
Shaft Purchaser Annexure H
Diffusers Annexure H
9.13.7 PERFORMANCE
Proposal Curve No. Purchaser A pump can be selected by
combining the System Curve
and the Pump Curve
Impeller dia
(Rated/max./min)
Purchaser The calculations are based
on the affinity laws which in
turn are derived from a
dimensionless analysis of
three important parameters
that describe pump
performance . three things
are Head , Flow and speed of
impeller
Impeller type Purchaser Closed , open or semi open.
Efficiency Purchaser Required efficiency that is
calculated using the pump
curves and system curves
Rated Power Purchaser Power that is supplied for the
impeller to produce the
required efficiency
Min. continuous Flow
(Thermal/Stable)
Purchaser The minimum rate of flow
required to avoid problems
like Cavitation
Preferred Operation Region Purchaser Range of operation where the
efficiency obtained is
maximum and cavitation is
avoided
Max. head @rated impeller Purchaser Maximum head generated if

the impeller runs at the given
parameters
9.13.8 UTILITY
Electricity Purchaser Electricity requirement of the
driver used .
Steam Purchaser The maximum /allowable
pressure of the steam used in
the turbine (if a turbine is
used)
Cooling water Purchaser Maximum and allowable
temperature and pressure of
the cooling water used in the
turbine . a better cooling
system provides a better
efficiency of the turbine
9.13.9 CONSTRUCTION
PARAMETER
Rotation Purchaser Viewed from coupling end
Pump Type Purchaser Which type of pump required .
Max. Allowable
working pressure
Purchaser The should be able to withstand design
pressure.
Hydrotest Pressure Purchaser Pressure above the design pressure . Pipes
are deformed
Nozzle Connection
1)Size Purchaser The size of the nozzle is dependent on the
head that is to be provided.
2)Flange Rating Purchaser A flange is a connection between the main
pipeline and the pump thus the pressure in the
pipeline decides the flange rating. flange rating
decides the flange size , the flange bolt size.
Coupling Manufacturer It includes Model , Rating , Spacer length ,
Type of coupling , coupling guard .
9.13.10 SURFACE PREPARATION AND PAINT

Parameter Given By Requirement
Pump Surface Preparation Purchaser Rp standard
Primer Purchaser Rp standard
finish coat purchaser Rp standard
9.13.11 HEATING AND COOLING
Parameter Given By Requirement
Cooling water piping plan Purchaser Cooling water required for
pumping volatile liquids which
become flammable at room
temperature
C.W.Piping Material Purchaser The material is important as it
indicates the efficiency of rate
of cooling.
9.13.12 BEARINGS AND LUBRICATION
Parameter Given Requirement
Oil Heater Requirement Purchaser If the liquid transported is at a
particular temperature then
the lubricant used should be
at the same temperature so
as to reduce the loss of
energy .

Selection of pumps in oil industry

Selection of pumps in oil industry

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Selection of pumps in oil industry