LINE SIZING PROCEDURE IN PROCESS INDUSTRY

LINE SIZING PROCEDURE
IN PROCESS INDUSTRY

A DETAILED DISCUSSION OF DESIGN & CALCULATION
METHODS FOR SIZING OF PIPES (LINES), ITS BASIC
FUNDAMENTALS & ITS LIMITATIONS.

INTRODUCTION
FLOW OF FLUIDS (LIQUID, GAS, VAPOUR, SUSPENSION,
SLURRY ETC.) THROUGH A PIPE OR TUBE IS THE MOST
EFFICIENT AND WIDELY USED METHOD OF MATERIAL
TRANSPORTATION IN PROCESS INDUSTRIES.
SIZING OF PIPES (LINES) IS VERY IMPORTANT & CRUCIAL
FOR
PROPER AND SMOOTH FUNCTIONING OF THE PLANT.
SAFETY OF PERSSONEL, ENVIRONMENT AND THE PLANT
ITSELF.
REDUCING COST ETC.

AREA OF DISSCUSION
OUR DISCUSSION IS LIMITED TO
NEWTONIAN FLUIDS ONLY.
 NEWTONIAN FLUID IS WELL EXPLORED.
 CONSIDERABLY LARGE AMOUNT OF DATA,
CORRELATION EQUATIONS ARE AVAILABLE.
• SINGLE PHASE OR MIXED PHASE.
FLOW THROUGH CIRCULAR PIPES OR TUBES.
A NEWTONIAN FLUID IS THE ONE WHERE SHEAR STRESS IS
PROPORTIONAL TO SHEAR RATE (d U/ d Y)

METHOD OF APPROACH
CONSIDERATIONS TO MAKE BEFORE LINE SIZING ARE
GENERAL CONSIDERATIONS
 ECONOMIC CONSIDERATION
 VELOCITY AND PRESSURE DROP CONSIDERATIONS
SPECIAL CONSIDERATIONS
 STRUCTURAL AND MECHANICAL EQUIREMENTS
 UNUSUAL FLOW SITUATION
a) VORTEXING. b) VIBRATION. c ) WATER HAMMER
VELOCITY LIMITATIONS
a) EROSION VELOCITY
b) SETTLING OF SOLID PARTICLES
c) STATIC ELECTRICITY

MODE OF OPERATION.
EQUIPMENT LIMITATION.
SPACE LIMITATION.
CODE/STATUTORY REQUIREMENTS.

BASIC DATA REQUIREMENT
LINE SIZING CALCULATION IS BASED ON THE PRESSURE DROP
OF THE FLOWING FLUID ACROSS THE PIPE / LINE.
SINGLE PHASE & SOME TWO PHASE FRICTION LOSS (ΔP)
FOLLOWS THE DARCY CONCEPT.
THE TRANSITION FROM LAMINAR TO TURBULANT CONDITION IS
IDENTIFIED AS BETWEEN REYNOLDS No. 2000 & 4000.
FOR INCOMPRESSIBLE FLUID – LAMINAR OR TURBULANT
ΔP = { ρ f L V2
/ D (2g) } kg/m2
f = DARCY FRICTION FACTOR = f (Re) WHERE Re = (D V ρ)/µ

STATE OF FLUID - LIQUID/VAPOUR/MIXED.
FLOW RATE - FLUID QUANTITY ESTABLISHED BY
PROCESS CONDITION.
-LIQUID-m3
/hr, VAPOUR-kg/hr.
FLUID PROPERTIES - DENSITY ,VISCOSITY, MW. TEMP
PRESSURE AT FLOWING CONDITION
PIPE PROPERTIES - NOMINAL DIA, ID, PIPE CLASS, SCH
NO.

BASIC FUNDAMENTALS
TOTAL LINE PRESSURE DROP
IT IS FRICTION DROP IN PIPE +VALVES + FITTINGS + SUDDEN
CONTRACTION & ENLARGMENT + ΔP ACROSS CONTROL VALVE
+ DROP IN EQUIPMENTS + STATIC DROP DUE TO ELEVATION OR
PRESSUR LEVEL.
TWO METHODS MAINLY USED FOR ΔP CALCULATION
ARE
RESISTANCE COEFFICIENT METHOD
EQUIVALENT LENGTH METHOD

FROM DARCY EQN. K = (f L/D)
WHERE K = RESISTANCE COEFFICIENT.
HEAD LOSS THROUGH A VALVE (FOR INSTANCE)
HL = (K V2
/ 2g)
K REPRESENTS THE NUMBER OF VELOCITY HEADS LOST DUE TO FLOW
THROUGH THE RESPECTIVE SYSTEM COMPONENT.
 IT IS INDEPENDENT OF FRICTION FACTOR.
 CONSTANT FOR ANY COMPONENT OBSTRUCTION.

FIGURE 2-12A FROM APPLIED PROCESS DESIGN, E .E. LUDWIG, VOL 1

TABLE 2-2 FROM APPLIED PROCESS DESIGN, E .E. LUDWIG, VOL 1

IMPORTANT POINTS
K VALUES GIVEN IN REFERENCES ARE BASED ON STANDARD
ANSI PIPE/FITTING DIMENSIONS. FOR ACTUAL PIPE DIMENSION
K IS CORRECTED AS FOLLOWS
K Corrected = KStd. Pipe Sch. (I.D. Actual Pipe Sch ÷ I.D. Std. Pipe Sch.)4
RESISTANCE COEFFICIENT (K) GIVEN IN REFERENCES IS FOR
FULLY TURBULENT FLOW.
FOR LOW Re No, K VARIES ALMOST SIMILARLY TO FRICTION
FACTOR & SHOULD BE CORRECTED AS FOLLOWS:
K Corrected = K Turbulent (ƒ at Actual Reynolds Number ÷ ƒ in Complete
Turbulent Range)

EQUIVALENT LENGTH CONSISTS OF TWO COMPONENTS
 STRAIGHT LENGTH OF PIPE
 EQUIVALENT STRAIGHT LENGTH OF VARIOUS PIPE FITTINGS &
VALVES
POINTS TO REMEMBER
 EQUIVALENT LENGTHS (L/D) ARE BASED ON STANDARD PIPE
SCHEDULES.
 CORRECTED (L/D) FOR DIFFERENT PIPE SCHEDULE IS
(L/D) CORRECTED = (L/D)STD. (I.D. ACTUAL PIPE SCH ÷ I.D. STD. PIPE SCH.)4.82
 EQUIVALENT LENGTHS (L/D) GIVEN ARE FOR Re No >1000
 FOR Re No < 1000 , CORRECTED (L/D) IS GIVEN AS
(L/D) CORRECTED = (L/D) FOR RE>1000 (ACTUAL REYNOLDS NUMBER ÷ 1000)

FIGURE 2-20 FROM E.E LUDWIG VOL 1

FRICTION FACTOR
Re No ESTABLISHES TYPE OF FLUID FLOW IN A PIPE.
THERE ARE THREE REGIONS OF FLUID FLOW
 Re No BELOW 2000 TO 2100 LAMINAR OR VISCOUS FLOW
 Re No BETWEEN 2000 TO 3000-4000 TRANSITION FLOW
 Re No ABOVE 4000 TURBULENT FLOW
FOR LAMINAR FLOW , f = 64/ Re
FOR TRANSITION & TURBULANT FLOW
FRICTION FACTOR USED IS MOODY FRICTION FACTOR.
DIRECT SOLUTION TO FRICTION FACTOR IS AVAILABLE IN
LITERATURE. e.g. f = 1.8 log10 (Re/7) -2
- COLEBROOK EQN.

RELATIVE ROUGHNESS (ε/D)
IN DESIGNING ATTENTION MUST BE GIVEN TO
 THE INITIAL INTERNAL PIPE CONDITION.
 EXPECTD CONDITION AFTER SOME REASONABLE LIFE
PERIOD USUALLY 10 TO 15 YEARS.
TO ACCOUNT THESE CONDITION RELATIVE ROUGHNESS
FACTOR (ε/D ) IS USED
WHERE, ε = ABSOLUTE ROUGHNESS FACTOR , ft.
D = PIPE INSIDE DIAMETER, ft.

RECOMMENDED PIPE SIZING CRITERIA
( FOR BOTH LIQUID AND GASES)
THE DESIGNER HAS TO SELECT APPROPRIATE SIZING CRITERIA
TO DECIDE ALLOWABLE VELOCITY AND PRESSURE DROP.
LITERATURE IS AVAILABLE IN THE FORM OF STANDARDS, CODES,
ETC. FOR RECOMMENDED VELOCITY & ΔP CRITERIA.
DIFFERENT COMPANIES HAVE THEIRE OWN SPECIFIC
RECOMENDATE VELOCITY AND PRESSURE DROP CRITERIA
REFERENCES FOR VELOCITY AND PRESSURE DROP CRITERIA
1. PROCESS ENGINEERING MANUAL
2. NORSOK STD. PROCESS DESIGN P-001 REV. 4 TABLE 3, 6, 7
3. API 14E FIGURE 2.1, 2.2
4. APPLIED PROCESS DESIGN, E.E LUDWIG VOL 1, FIG 2-22,2-23,
TABLE 2-4,2-5, 2-6.

Type of Service
Recommended
Velocity (m/s)
Max. Allowable
Pr. Drop
(kg/cm2
/km)
1 General recommendation 1.5 - 4.5 8.8
2 Laminar flow 1.2 - 1.5
3 Turbulent flow: liquid density
(kg/m3
)
1600 1.5 - 2.5
800 1.8 - 3.0
320 3.0 – 4.5
4 Pump suction
Boiling liquid 0.6 – 1.8 1.1
Non-boiling Liquid 1.2 – 2.5 2.2
Table 1.1 : Recommended Velocity and Pressure Drop for Carbon Steel Liquid Lines
in Various Services
Note: Velocity higher than 3.0 m/s for any line should be used only after due
consideration for velocity limitations explained in section 1.2.3.

RECOMMENDED PRACTICE FOR PIPE SIZING
LINE SIZING GRAPHS SHALL BE USED FOR ΔP AND VELOCITY
CALCULATION.
FOR HIGHLY VISCOUS LIQUIDS, HYDRAULIC INSTITUTE’S
TABLES SHOULD BE USED.
OVERDESIGN MARGIN SHALL BE EITHER 10% IN FLOW RATE OR
20% IN ΔP UNLESS RECOMMENDED OTHERWISE FOR SPECIFIC
CASES.
FOR CIRCULATING OIL & HEATING OIL LINES 25% (MIN) IN FLOW
& IN ADDITION 25% OF FLOW SHALL BE CONSIDERED AS
RECIRCULATED.
PUMP SUCTION LINES SIZE IS BASED ON NPSH REQUIREMENT.
100% OVERDESIGN IN CALC. ΔP IN SUCTION LINE.

IMPORTANT CONSIDERATIONS FOR LINE SIZING
 LINE DRAW-OFF LINES FROM COLUMN.
 LIQUID OVERFLOW LINE
 PRESSURE RELIEF VALVE INLET PIPING
 LINES IN WHICH VORTEXING CAN OCCUR
 SIZE OF CONTROL VALVE ISOLATION AND BYPASS VALVES LINE
API 14E HAS GIVEN SURGE FACTORS ON FLOW RATE
(OFFSHORE)

BASIS OF LIQUID LINE SIZING GRAPHS
FOLLOWING EQUATIONS HAVE BEEN USED IN DEVELOPING
THESE GRAPHS
(AFTP- FRENCHASSOCIATION OF PETROLEUM TECHNOLOGIST )
Re = 3.54X104 Q/D; & P = 63.7X100Q2ƒd/D5
Re = REYNOLDS NUMBER
Q = FLOW VELOCITY, m3
/hr
 = VISCOSITY, CENTISTOKES
D = INSIDE DIAMETER OF PIPE, cm
d = SPECIFIC GRAVITY WITH RESPECT TO WATER = 1.0
ƒ = FRICTION FACTOR
P = PRESSURE DROP, Kg/cm2
per Km OF PIPE
MOODY DIAGRAMS HAVE BEEN EMPLOYED FOR
DETERMINATION OF FRICTION FACTOR.

STEPWISE PROCEDURE FOR LINE SIZING
LIQUID LINE
 ASSUME A LINE SIZE.
 FOR A GIVEN FLOW RATE AND VISCOSITY READ THE ΔP
IN Kg/cm2
/km BASED ON S.G. OF 1.0 AND VELOCITY IN m/sec.
 DETERMINE ΔP FOR THE ACTUAL FLUID BY MULTIPLYING
BY SPECIFIC GRAVITY OF FLUID AT OPERATING CONDITIONS.
 CHECK IF THESE VALUES OF VELOCITY AND PRESSURE DROP IF
THEY MEET THE CRITERIA APPLICABLE IN THAT CLASS.
 IF NOT, ASSUME ANOTHER PIPE SIZE AND REPEAT
CALCULATIONS.
 THE LINE SIZING GRAPHS ARE APPLICABLE TO SCH. 40 PIPE
ONLY. SO, CORRECTED ΔP AND VELOCITY FORACTUAL PIPE
SCHEDULE WILL BE
Actual velocity = Velocity from chart x (I.D. Of SCH. 40 pipe ÷ actual I.D. Of pipe used)2
Actual pressure drop = p from chart x (I.D. Of SCH. 40 pipe ÷ actual I.D. Of pipe used)4.82

THE LINE SIZING GRAPHS ARE BASED FOR AN ABSOLUTE
ROUGHNESS,  OF 0.0018 INCH FOR COMMERCIAL STEEL PIPE.
FOR A DIFFERENT ROUGHNESS FACTOR ΔP WILL BE CORRECTED
AS FOLLOWS
 CALCULATE NEW  /D FOR ASSUMED DIAMETER.
 CALCULATE Re No FOR FLOW SYSTEM BASED ON ASSUMED DIAMETER.
 FROM f, Re No & /D CORRELATION GRAPHS READ VALUE OF FRICTION
FACTOR (ƒ) FOR STANDARD ROUGHNESS VALUE & FOR NEW  AGAINST
REYNOLDS NUMBER
 MULTIPLY ΔP BY A CORRECTION FACTOR AS GIVEN BELOW
ƒ (Friction Factor) for new roughness
ƒ (Friction Factor) for standard roughness (0.0018)
CHECK IF THE NEW VALUE MEET THE CRITERIA APPLICABLE IN
THAT CLASS.
IF NOT ASSUME ANOTHER PIPE SIZE & REPEAT THE
CALCULATIONS.
CONTD.

FIG 2-22 FROM APPLIED PROCESS DESIGN, E. E. LUDWIG, VOL 1,

FIG 2-23 FROM APPLIED PROCESS DESIGN, E. E. LUDWIG, VOL 1.

GAS, VAPOR, AIR & STEAM ARE THE COMPRESSIBLE FLUID.
A COMPESSIBLE FLUID IS ONE WHOSE DENSITY CHANGES
WITH PRESSURE.
• SPECIFIC SEMI EMPIRICAL FORMULAS HAVE BEEN DEVELOPED
TO FIT PARTICULAR SYSTEM.
• BASED ON P-V RELATIONSHIP GAS & VAPOR FLOW IN PROCESS
SYSTEM MAY BE
1. ADIABATIC FLOW – NO EXCHANGE OF HEAT INTO OR FROM THE PIPE.
2. ISOTHERMAL FLOW – FLOW AT CONSTANT TEMPERATURE.
3. POLYTROPIC FLOW – FLOW IN BETWEEN ADIABATIC & ISOTHERMAL.
FOR GAS & VAPOR FLOW IN PROCESS LINES, ISOTHERMAL FLOW IS
OFTEN CLOSE TO PRACTICAL EXPERIENCES.

THE MEAN VELOCITY IS [4]
V = (21220 W V )/d5
= (21220 W)/d2
ρ
WHERE,
V = VELOCITY, m/min
W = MASS FLOW RATE, kg/hr.
V = SP. VOLUME, m3
/kg.
d = I.D, mm
ρ = DENSITY, kg/m3
.
THE VELOCITY CAN BE OBTAINED
FROM THE NOMOGRAPGH ALSO
ΔP IS GIVEN AS [4]
ΔP100 = (62530 f W2
V)/d5
= (62530 f W2
)/d5
ρ
OR
ΔP100 = (93650 f q’h
2
Sg
2
)/d5
ρ
& W = 1.225q’hSg
WHERE,
ΔP100 = PRESSURE DROP,
bar/100m
q’h = VOL. FLOW RATE, m3
/hr.
Sg = SP. GRAVITY W.R.T AIR
THE ΔP100 CAN BE OBTAINED
FROM THE NOMOGRAPGH ALSO

FIG: VELOCITY OF COMPRESSIBLE FLUID IN PIPES FROM CRANE

FIG: REYNOLDS NO & FRICTION FACTOR FOR CLEAN STEEL PIPE FROM CRANE

FIG: ΔP FOR COMPRESSIBLE FLOW FROM CRANE

IT IS AQUARATE FOR FULLY TURBULANT FLOW.
IT PROVIDES GOOD APPROXIMATION IN CALCULATIONS OF
COMPRESSIBLE FLOW THROUGH COMMERCIAL STEEL PIPE AT
NORMAL FLOW CONDITIONS.
THE SIMPLIFIED FORMULA IS :
C1 = DISCHARGE FACTOR.
C2 = SIZE FACTOR.
C1 & C2 CAN BE OBTAINED FROM CRANE

THE MAXIMUM POSSIBLE VELOCITY OF A COMPRESSIBLE FLUID
IN A PIPE IS THE SONIC VELOCITY.
IT IS THE SPEED OF SOUND IN THE FLUID.
VS = [{68.1(CP/CV) P’ }/ρ] ½
ft/sec WHERE P’ = PREESURE ,psi a
 APPLICABLE REGARDLESS OF THE DOWNSTREAM PRESSURE FOR
A FIXED UPSTREAM PRESSURE. [1]
 ALL COMPRESSIBLE FLOW APPROACHES A MAXIMUM MASS FLOW
RATE DEPENDING UPON SPECIFIC UPSTREAM PRESSURE. [1]
V = 3.06 W V / d2
, WHERE, V IN 1000 feet/min.
WHEN COMPRESSIBLE FLUID VELOCITY REACHES THE SONIC
VELOCITY IT CREATS SHOCK & DETONATION WAVES.

BASIS OF VAPOUR LINE SIZING GRAPHS [2]
EQUATIONS USED TO DEVELOPING THESE GRAPHS
(AFTP- FRENCH ASSOCIATION OF PETROLEUM TECHNOLOGIST )
Re = 3.54 M/D & P = 63.7X100M2ƒ/D5
d
Re = REYNOLDS NUMBER
M = FLOW VELOCITY, Kg/hr
 = VISCOSITY, CENTISTOKES
D = INSIDE DIAMETER OF PIPE, cm
d = SPECIFIC GRAVITY WITH RESPECT TO WATER = 1.0
ƒ = FRICTION FACTOR
P = PRESSURE DROP, Kg/cm2
per Km OF PIPE
MOODY DIAGRAMS HAVE BEEN EMPLOYED FOR
DETERMINATION OF FRICTION FACTOR.

STEPWISE PROCEDURE FOR LINE SIZING
VAPOUR LINE
 ASSUME A LINE SIZE.
 FOR A GIVEN FLOW RATE AND VISCOSITY READ THE ΔP
IN bar/km & VELOCITY IN m/sec BASED ON VAPOUR DENSITY
OF 1 kg/m3
.
 ΔP & VELOCITY FOR THE ACTUAL FLUID IS OBTAINED BY
DIVIDING ΔP BY ACTUAL VAPOUR DENSITY AT OPERATIN
CONDITIONS.
 CHECK IF THESE VALUES OF VELOCITY & MEET ΔP THE
CRITERIA APPLICABLE IN THAT CLASS.
 IF NOT, ASSUME ANOTHER PIPE SIZE .

TWO PHASE FLOW OCCURES IN
 REFINERY TRANSFER LINES.
 CONDENSATE LINES.
 OIL FIELD GATHERING LINES.
 OIL AND NATURAL GAS PIPELINES.
2-PHASE FLOW IS DIFFICULT TO ANALYSIS.
NO SINGLE CORRELATION IS AVAILABLE FOR WIDE RANGE OF
PARAMETERS.
VARIOUS EMPIRICAL EQUATIONS ARE AVAILABLE BUT WITH
SPECIFIC LIMITATIONS.
VAPOR WITH ABOVE 7% - 8% IN LIQUID CAN BE CONSIDERED
AS TWO PHASE.

Sl
NO
Types of
Flow
Horizontal Pipe
Superficial
velocities (ft/s)
Liquid Gas
1. Bubble or
forth flow
Bubbles of gas are dispersed throughout the liquid.
5 - 15 1 - 10
2. Plug flow Alternate plugs of liquid and gas move along the
upper part of the pipe.
<2 <3
3. Stratified
flow
Liquid flows along the bottom of the pipe and the
gas flows over a smooth liquid-gas interface.
<0.5 2 - 10
4. Wavy
flow
Similar to stratified flow except the interface has
waves traveling in the direction of flow.
<1 15
5. Slug flow Wave forms periodically by rapidly moving gas to
form a frothy slug, which passes along the pipe at a
velocity greater than average liquid velocity.
- -
6. Annular
flow
The liquid flow as a film around the pipe inside wall
and the gas flows as a core. >20 -
7. Spray or
dispersed
flow
Nearly all the liquid is entrained as fine droplets by
the gas - >200

FIG : REPRESENTATIVE
FORMS OF HORIZONTAL
2 PHASE FLOW PATERNS
[1]

LIQUID HOLD UP
VOLUME FRACTION OF LIQUID IN INLET STREAM AT NO SLIP.
ACTUAL LIQUID HOLD UP IS THE VOL. OF LIQUID IN A PIPE
SECTION DIVIDED BY TOTAL VOL. OF PIPE SECTION.
PRESSURE DROP DUE TO FRICTION :
SEMI EMPIRICAL EQUATIONS ARE AVAILABLE.
THEIR BASIS IS THE SINGLE-PHASE PRESSURE DROP FOR EITHER
PHASE MULTIPLIED BY A FACTOR FOUND TO BE A FUNCTION OF
THE SINGLE-PHASE.
AV. PROPERTIES FOR BOTH PHASES :
IMPORT. PROPERTIES TO BE AVAREGED ARE DENSITY &
VISCOSITY.
SIGNIFICANT CHANGES IN AV. PROPERTIES OCCUR DUE TO
 LIQUID FLASHING DUE TO PRESSURE LOSS.
 PRESSURE LOSS & LIQUID FLASHING OCCURS ADIABATICALLY GIVING RISE TO
TEMP.

CONTD.
EROSION VELOCITY :
LOSS OF WALL THIKNESS OCCURS BY A PROCESS OF
EROSION/CORROSION.
IT IS ACCELERATED BY
 HIGH FLUID VELOCITY.
 PRESENCE OF SAND.
 PRESENCE OF CORROSIVE CONTAMINANTS (CO2,H2S)
 PRESENCE OF FITTINGS.
FLUID EROSION VELOCITY IS GIVEN AS
VE = C/(ρm)1/2
VE = feet/sec.
C = EMPIRICAL CONST.
= 100 FOR CONTINOUS SERVICE.
= 125 FOR INTERMITTENT SERVICE.
ρm = GAS/LIQD MIX. DENSITY , lbs/ft3
.

CONTD.
GAS – LIQD. MIXTURE DENSITY IS GIVEN BY:
ρm ={(12409 S1P) + (2.7 R SG P)}/ {(198.7 P) + RTZ} [3]
WHERE:
MINIMUM VELOCITY: 10 feet/sec TO MINIMIZE SLUGGING
OF SEPARATION EQUIPMENT

FROM API 14E THE PRESSURE DROP IS

ASSUME A LINE SIZE.
USING VISCOSITY OF THE LIQUID AND TOTAL FLOW RATE OF
THE MIXED PHASE,READ THE VELOCITY AND PRESSURE DROP
FOR FLUID DENSITY OF 1 kg/m3
FROM THE VAPOR LINE SIZING
GRAPH.
DETERMINE THE ACTUAL VELOCITY AND PRESSURE DROP BY
DIVIDING THE VALUES OBTAINED IN STEP 2 ABOVE BY AVERAGE
LIQUID DENSITY IN kg/m3
.
CHECK THESE VALUES OBTAINED AGAINST THE RECOMMENDED
VALUES AND REPEAT FOR ANOTHER LINE SIZE IF NECESSARY.
CORRECT PRESSURE DROP AND VELOCITY FOR ACTUAL PIPE I.D.
AND ROUGHNESS FACTOR.
IN A VERY STRICT SENSE, THIS FORMULA IN NOT APPLICABLE
FOR PRESSURE DROP CORRECTION IN TWO-PHASE FLOW
SYSTEMS.

Code
Diameter
inch
Pressure
barg Description Max velocity Maxv2 MaxP Max Mach
up to up to m/s kg/m.s2
= Pa bar number
PSNB 2 Pump suction - Non boiling liquid 0.57
PSNB Pump suction - Non boiling liquid 3.57
PSB 2 Pump suction - Liquid bubble point 0.60 1
PSB Pump suction - Liquid bubble point 1.80 1
PD 18 50 Pump discharge 4.50 4.5
PD 50 Pump discharge 6.00 4.5
PD 18 Pump discharge 4.50 9
PD Pump discharge 6.00 9
ULNB 2 Unit line - Non boiling liquid 0.57 3.5

Code Diameter
inch
Pressure
barg Description
Max
velocity Maxv2
Max
P
Max
Mach
= Pa bar number
ULNB Unit line - Non boiling liquid 3.57 3.5
ULB 2 Unit line liquid bubble point 0.6 1
ULB 6 Unit line liquid bubble point 1 1
ULB 18 Unit line liquid bubble point 1.4 1
ULB Unit line liquid bubble point 1.8 1

Code
Diameter
inch
Pressure
barg Description
Max
velocity Maxv2 MaxP Max Mach
= Pa bar number
GAS 20 Gas, general 30 6000
GAS Gas, general 30 25000
PW 2 Service water 1.5 3.5
PW 6 Service water 2.5 3.5
PW Service water 3 3.5
SWL Sea water lines 3
FLANT 2 Upstream PSV or BDV 25000 0.6
FLANT 50 Upstream PSV or BDV 30000 0.6
FLANT Upstream PSV or BDV 50000 0.6
FLDHR Flare main header - Gas phase 100000 0.7
FMP Downstream relieving devices multiphase 50000 0.25
FSMN Fire system main nodes 5
FSTN Fire system terminal nodes 3
MXP Mixed phase 15000

LINE SIZING PROCEDURE IN PROCESS INDUSTRY

LINE SIZING PROCEDURE IN PROCESS INDUSTRY

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