This document provides an overview of compressors used in various industries. It begins by defining compression as boosting gas pressure and listing common applications in oil and gas, refineries, petrochemical plants, fertilizer production, and refrigeration. The main types of compressors - centrifugal and positive displacement - are described along with subtypes like reciprocating, screw, and liquid ring. Key concepts covered include compression processes, surge control, drives, seals, lubrication systems, performance calculations, control strategies, protection methods, and potential operational issues.
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COMPRESSOR TRAINING MATERIAL.pdf
1. Compressors 1
Compressors
Jan 2018
RecommendedReading
GPSA Engg Databook, Section 13, Compressorsand Expanders
“Knowledge as to how process equipment really functions is
disappearing from the process industries.This is not only my
opinion,but the general view of senior technical managers, in
many large corporations”,Norman Lieberman, ‘A Working
Guide to Process Equipment’
Compression
• To boost gas pressure to suit process
• Applications
– Oil & Gas: Gas to Dehydration, Dew Point Control,
LPG Recovery, Pipeline Transport -
onshore/offshore. Vapour Recovery. Flare Gas
Recovery
– Refinery: Make up and recycle Hydrogen, Wet Gas,
Fuel Gas, FCC Air and Plant Air
– Petrochemical: C2/C3 Compression
– Fertilizer: Syngas
– Refrigeration
Classification & Selection
Dynamic
Centrifugal
Single/
Multistage
Horiz/ Vertical
Split Barrel
Axial
Positive
Displacement
Reciprocating
Piston or
Plunger
Diaphragm
Rotary
Screw /
Helical Lobe
Sliding Vane
Liquid Ring
• Centrifugal - Constant head
– Large flow ~ low head
– Widely used. Preferred
– Low Capex and Opex. Reliable
• PD - Constant Flow
– Low or moderate flow ~ high head
– Flexibility in capacity and pressure range
– Higher efficiency and lower power cost
– Less sensitive to changes in gas
composition and density
Centrifugal
Single Stage
Rotary Screw
Axial
Flow
Head
Recip - Single Stage
Rotary - Liquid Ring
Rotary - Straight Lobe
Rotary - Sliding Vane
Fans & Blowers Excluded
Compression
• Isothermal
– No change in temperature
• Isentropic “adiabatic”
– No heat added or removed
– pvk = constant
– k = MCp/MCv = MCp/(MCp-R)
– Ideal
• Polytropic
– pvn = constant
– Real or irreversible process
with entropy change
• Power Required
– Simple calculations
– p-h chart
– Simulation software
– With efficiency get BHP
• Number of stages
– By compression ratio 3~4
– Discharge temperature <
150°C (300°F) to avoid
damaging lube oil. For H2
120°C (250°F)
– Interstage pressure drop 35-
70 kPa (5-10 psi)
Volume
v1,p1
p2
Isothermal
Isentropic
Polytropic
Pressure
Centrifugal
Recip
Axial
Inlet Volume Flow
Pressure
2. Compressors 2
Centrifugal Compressor
• Centrifugal
– Gas sucked and accelerated by
rotating impeller/ vane
– Stationary Diffuser/blades convert
velocity head to static pressure
– Multi wheel for large inlet volume
flow; otherwise single wheel
• Characteristic: Constant head
– High flow ~ low heads
– Flow reduces with higher
backpressure
– Multistage for high discharge
pressure
• Inlet guide vanes distribute gas to first stage impeller
• Impeller accelerates gas, imparting kinetic energy
• Diffusers change kinetic energy to pressure
• Casing return bends direct gas to the next impeller
• Note: Impellers getting smaller as gas volume reduces
• Dry Gas seals avoid process gas leak to atmosphere
Drive Shaft
Bearing
Impeller
Diffusers
Gas Seals
Open, semi open or closed impeller
Axial Compressor
• High flow - low head
– Air compressor. Gas turbine air compressor
– Axial flow. Stationary vanes direct gas to next row
of rotating blades
– Low head/ stage
– Twice no of stages than
in centrifugal
Centrifugal Compressor
• Design Info
– Flow and Suction/ Discharge Conditions. To API Std 617
– Molecular Weight changes. Sizing based on low mol weight. Hi volume
• For the same head, higher Molecular Weight means higher pressure
• Capacity & Head
– Impeller diameter ~ speed
• Affinity law
– Flow α speed N, dia d
– Head α N² or d²
– Power α N³ or d³
• Single Speed Drive. Constant head
– Head curve -Theoretically straight line
• Less due to internal losses
• Gradually reducing
• Flow decided by intersection of head
and system resistance curves
80
100
120
60
25 50 75 100 125
Capacity, %
Head
%
100% N
Drooping Unstable
System Resistance - Closed Loop ∆P=Flow²
Plant air compressors are Recip or Screw. Do you know why?
• Capacity usually low. Capacity smaller impeller dia. To get
10 bar discharge pressure, impeller tip velocity or
compressor speed has to be very high
• With hi capacity + integral Air Separation units, centrifugal
compressors are used
Centrifugal Compressor
• Variable Speed Drive
– Constant capacity at variable pressure or variable
capacity at constant pressure or variable capacity and
variable pressure
– Speed changed to suit process flow and pressure
condition within driver + compressor limits
– Flow decided by intersection of head and system
resistance curves
80
100
120
60
25 50 75 100 125
Capacity, %
Head
%
105% N
100% N
95% N
System Resistance - Closed Loop ∆P=Flow²
3. Compressors 3
Centrifugal Compressor
• Surge
– At surge point, developed head
< system resistance
– Discharge gas flows back
– As flow drops, discharge
pressure drops and compressor
resumes forward flow
– Cycle is repeated. Large
pressure and flow fluctuation
– Machinery damage. Thrust
bearing affected due to rotor
shifting back and forth
• Stonewall or choked flow
– At high flow - low head (low
system resistance) gas may
reach sonic velocity
– For a given gas, maximum flow
reached
• Interstage Cooling
– Head and Power αT1
– Interstage cooling, allows
lower temperature to next
wheel inside stage/ next stage
– Internal cooling
• Water cooling through jackets
in diffuser diaphragms
• Liquid injection in return
channels. In refrigeration units
– External cooling
Energy saved
with interstage
cooling
Pressure
P2
P1
Volume
V2 V1
Compressor Surging Video
Shaft Seals
• Oil or gas seals. Eliminate process gas
leak along shaft to atmosphere
• Injected at a pressure marginally
higher than process between 2 sleeves.
Gap between sleeves 5 microns
• Seal gas flows towards process and
atmosphere presenting a barrier to
direct passage of process gas
• A separation or buffer gas (air or inert
gas) used if seal gas is process gas
Red = Rotating
Yellow = Stationary
Seal
Gas
Leak
Separation
Gas
Process
Single Gas Seal
Inner
Seal
Seal Separation
Seal
Leak
Buffer
Gas
Double Gas Seal
Seal
Gas
Separation
Gas
Inner
Seal
Inboard
Seal
Separation
Seal
Outboard
Seal
Py Seal
Leak
Seal
Gas
Separation
Gas
Tandem Gas Seal
Sy Seal
Leak
Inner
Laby
Primary
Seal
Separation
Seal
Secondary
Seal
Lube & Seal Oil System
• Lubrication oil for bearings
• Older compressors have seal oil
• Combined lube and seal oil
system
– With booster pumps for seal
• Separate lube and seal oil
system for contaminated gas
• Buffer gas injection to form a
barrier between process gas and
seal oil
• Degassing tank: in seal oil return
line to remove oil-entrained gas
• Outer sleeve seal oil returned
via atmospheric drain system
• Inner sleeve seal oil returned or
discarded if contamination by
process gas
• Overhead run down tank
provides 15 minutes of seal oil
for compressor coastdown after
a trip
Lube
& Seal Oil
Buffer
Gas
Seal
Oil
Lube
Oil
Carbon
Seal
Shaft
Bearing
Process
Seal Oil
& Buffer Gas
Caution Seal Gas:
• Good filter as gap between sleeve faces 5 μ
• Seal gas superheating may be required
• Saturated process gas is known to drop out
heavy condensate while cooling after a
shutdown and damage the seals
Positive Displacement - Reciprocating
• Piston or Plunger
– Constant flow in each stroke
– Single or multistage
• Diaphragm
– Flexible diaphragm
• Characteristic: Constant flow
– Can compress against any head
– Lubricated/ non-lubricated
• Non-lubricated in air and O2 service
– Interstage coolers
– Compressor and outlet piping will be
damaged with closed outlet. PSV
required
Integral Engine Compressor
(Compressor Driven By Gas Engine)
Suction
Discharge
Clearance Pocket
• Cooled and Lubricated Cylinder
• Lubricated Packing Case
• Dry Liner on cylinder Inner Wall
• Pistons may have Teflon Wear Rings
• Double acting pistons in LP Stage
• Single Acting in LP
Packing case
Double Acting Piston Video
4. Compressors 4
Recip Compressors
• To API Std 618
• “Pulsating” on each suction
stroke - from no flow to
filling
• Pulsation dampeners on
suction and discharge
– For smooth flow and to avoid
vibration
– Limit peak to 2% of average
pressure
– Analog studies done
• Startup Unloading. Manual/
automatic
– Discharge venting
– Discharge to suction bypass
– Inlet valves kept open with
valve lifters
• Capacity Control
Constant volume flow
– On-off, based on discharge
pressure
– Variable Displacement: Inlet
valve/ Clearance unloading
100, 75, 50, 25, 0%
– Variable speed drive or
transmission
Screw & Sliding Vane Compressor
Sliding Vane
• Eccentrically mounted
rotor. Sliding Vanes
• Gas trapped and pushed
by vanes
– Vapor Recovery &
Vacuum Service
Screw/ Helical lobe
• Intermeshed rotors
– Progressively reducing
interlobe spacing
compresses gas
– Air and Refrigeration
services
– Capacity control by a slide
valve ~ 10-100%
• To API Std 619
Liquid Ring Compressor
• Vacuum pump
• Eccentrically mounted rotor
• Vanes churn liquid, typically
water
• Liquid ring seals spaces
between vanes -
compression chambers of
reducing volume
– Make-up filtered liquid
– Liquid acts as a coolant
• Good for wet, saturated,
dirty, toxic, explosive and
corrosive gases
– H2S, Dry and Wet Chlorine,
H2, VCM
• Ideal for gases with liquids,
dust and dirt - flare gas
recovery
Hyper Compressor
• High-pressure recip
compressor for LDPE
(Low Density
Polyethylene) plants
• Ethylene to 3,500 bar
(50,000 psia)
From: https://www.burckhardtcompression.com/
Separator Extruder PE Pellets
Reactor
Hyper
Compressor
Booster
Compressor
C2 =Storage
5. Compressors 5
Compressor Performance
• Isentropic Performance
– Head His = ZavRT1/(M(k-1)/k)*[(P2/P1)(k-1)/k-1]
– k = Cp/Cv
– Power, Pgas = w.His/(ηis*CF)
w = kg/s or lb/min CF = 1,000 SI or 33,000 FPS
– T2 = T1 + {T1*[(P2/P1)(k-1)/k-1]}/ηis
• Polytropic Performance
– Replace k with n
– n/(n-1) = k/(k-1)*ηp
– T2 = T1*(P2/P1)(n-1)/n
– BHP = Pgas + Mechanical Losses
towards bearing/ gear @ Pgas
0.4
P1
Enthalpy
Pressure
P2
Entropy Lines
1
2 2’
Temp Lines
∆his
∆h
Head/ Enthalpy Change from p-h Dgm
ηp = 0.7-0.85 based
on flow/ BHP
Compressor Sizing Calc
Compressor Drives
• Electrical Motors
– Constant speed
– Variable speed drive VSD
• Variable Speed
– Internal combustion
engines
– Gas turbines
• Power delivery based on
ambient temperature.
Can load more during
nights and in winter
– Steam turbines
– Turbo Expanders
• Common driver for 2
separate compressors
• N+1 compressors
– Lead/ lag control
– Base load/ swing load
Compressor Control
• Controls
– Affinity law: Q α N. H α
N². HP α N³
– On reducing flow, speed
is reduced or suction is
throttled to maintain inlet
flow away from surge. On
further reduction ASV,
anti-surge valve opens to
recycle discharge flow to
suction
– Suction pressure with an
override from discharge
pressure to control variable
speed drives
– Suction or discharge throttling
or inlet guide vanes in fixed
speed drivers
– Anti-surge protection via
recycle back to suction
– Hot gas bypass to suction for
anti-surge protection during
coastdown
PIC PIC
SC
Speed
Control
GT
PIC
M
PCV
Instead of speed,
% throttling
Instead of PC,
FC can be used
80
100
120
60
25 50 75 100 125
Capacity, %
Head
%
105% N
100% N
95% N
Compressor Control
Compressor Surge Control Video
Inlet flow measurement and operating speed decide approach
to surge and Anti Surge Valve is opened to increase inlet flow
For seal oil / fire case/ reduce start-up load BDV is opened
PAHH
PALL
PAH
PAL
LAHH
LALL
LAH
LIC
LAL
LG
LV
Suction
Scrubber
Discharge
Cooler
PIC
PCV
FCV
PG
TG
PG
TG
PAHH
PALL
TAHH
PALL
TAHH
FIC
PAH
PAL
PIC
SC
ASC
Anti Surge
Valve
Compressor
Speed Control
Compressor
Surge Control
To Flare
Hot gas Bypass
Bearing - Vibration,
Shaft - Axial Movement
Temperature Trips
To Flare
RO
BDV
FAH
FAL
LO
PSV
LO
PSV
6. Compressors 6
Compressor Protection
• Low suction pressure d/s of
suction filter. Very commonfor
suction filter to get plugged
with debris and mill scale
• High discharge
pressure/temperature
• Anti-surge*
• Vibrations
• High temperature of bearings
• High axial movement
• Lube oil/ Seal failure
• Suction KOD
– High level trip
• Piping from KOD to compressor
heat traced /sloped to KOD
• Suction side designed to settle out
pressure = (VsPs+VdPd)/(Vs+Vd)
• Discharge PSV
• API 14 C
– Compressor Unit
Compressor Settle Out Calc
* Dynamic Simulation Studies
• Close inlet SDV
– ASV and suctionPCV response.Suction
PALL set point.SDV closure time
• Close outlet SDV
– ASV response. Discharge PAHH set point.
SDV closure time
• Fail open ASV
– Compressorcontrols response
• Trip one or both compressors
– CheckASV Cv
– Hot gas bypass requirement
Some systems may
have inlet coolers
Operational Issues
• Centrifugal
– High discharge resistance
– Dirt or coke buildup on
rotor or diffusers
– Changes to gas mol wt
– Poor surge control
response. Hot bypass
required
• PD Compressors
– Dirt or liquid
– Poor adjustments.
Coolant and lube oil
– Leaking suction/
discharge valves
• Safety Alert
– Poor min flow recycle
resulted in vacuum in
suction, pulling in air. On
compression air:HC
exploded
– Vibration in compressor
outlet piping. 1/4" bolt on
local TG support, cut thru
pipe, releasing H2. During
plant walk about check
and avoid sharp objects
close to piping
Thank You