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PUMP (SELECTION)
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PUMP (PROCESS DESIGN)
mm 25 mm
m
m
Fluid fro 50
mNs/m
kg/m
kg/h
m/s 32.174 ft/s
Pipe type
Economic pipe diameter, d
Mass flow rate, m
Pipe length, l
Fluid type
Viscosity,
Density,
Pipe cross sectional area, A
Fluid from M-102
Gravitational acceleration, g 9.81
0.740
977.652
5489.516
P-102Pump in charge
Commercial steel pipe
50
7.64
1.9635E-03
Carbon steel or Stainless steel?
Estimated pipe internal diameter:
Stainless steel
Get the economic pipe
diameter from DN
table in Appendix
referring to the
estimated pipe internal
diameter.
Other types:
d = (4A/)A=V/u
V=(m/3600)/u = 2 m/s (typical)
Carbon steel:d, optimum = 293G
0.53-0.37
Stainless steel:
d, optimum = 260G0.52-0.37
(1) Select pipe type with respect to fluid type
(2) Select pipe material
(3) Estimate pipe internal diameter
(4) Choose economic pipe diameter
(5) Determine pipe length
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PUMP (PROCESS DESIGN)
(6) Determine fitting/valve
I O
0
0
1 1 1.6
00
0
0
0
1 0.5
1 1
fully open 0 open 0
open 0
open 0
fully open 0
open 0
Plug valve open 1 0.4
Total: 3.5
1.0
0.15
Globe valve,
bevel seat-
90 square elbow90 standard long elbow
Sudden expansion (tank inlet)
Gate valve
Tee-entry from leg
Tee-entry into leg
Union and coupling
Sharp reduction (tank outlet)
75
45 standard elbow 0.35 15
0.8
0.45
0.2 10
35
23
0.5
1.5
1.2
1.8
45 long radius elbow
90 standard radius elbow
0.04
1
6
8.5
0.4
60
90
2
800
50
7.5
25
016
4
18
450
200
40
300
0
0
0
50
0
0
Unit K, number
of velocity
heads
Number of
equivalent
pipe
diameters
0
Pressurelossinpipe
fittingsandvalves(fortu
rbulentflow,Re>4000)
K, number of velocity
heads per unit
Number of
equivalent pipe
diameters per
unit
0
0
0
0
0
0
Fitting/Valve
85
35
00
Ran e: 0.6 - 0.8
Range: 30 - 40
(7) Calculate number of equivalent pipe diameter
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PUMP (PROCESS DESIGN)z1 1.00
z2 3.90P1 1.013 1.013E+05 N/m
P2 1.013 1.013E+05 N/m
Total Developed Head (TDH)m
N/m
m
mm/s
m
m/h
m/s
mm
m
N/m
m
m
m
m/h
%
Fluid velocity, u =
as head of liquid =
Difference in elevation, z =
Friction factor, f =
2.90
Pipe absolute roughness =
Pipe cross sectional area, A =
Total Developed Head (TDH) =
Pipe relative roughness, e =
Reynolds number, Re =
Dynamic head =
Pressure drop, Pf =Length including misc. losses, L =
2.900S
taticHead
Total static head =0.794
PIPING LAYOUT
Dyna
micHead
Difference in pressure, P = 00.000
Operating volumetric flow, vo =
Pump efficiency =
1.963E-03
5.615
52445
0.000920
0.046
bara
41.39
44.29
Operating point =
bara
(Use: Single- or double-suction pump)
Volumetric flow rate, v =0.001560
m
m
(Satisfactory: Flow is turbulent)
4125
0.007029
11.89
(OK)
Relative roughness, e = absolute roughness/d
Refer to data in Appendix
Re = ( u d) /
v = u A 3600s/1h
L = l + (total equivalent pipe diameters d0.001m/1mm)
Pf= 8f(L/d) ( u)/2
Pressure drop as head of liquid = Pf/ ( g)
TDV = total static head + dynamic head
A = /4 (d 0.001m/1mm)
Take 2 m/s, typical velocity for liquid.
f = 0.04Re-0.16
for turbulent flow in clean commercial
steel pipes. (Genereaux, 1937) Otherwise, refer to Fig.
5.7.
(Genereaux, 1937)
Single-suction centrifugal pumps handle up to 0.0032 m/s at
total heads up to 15 m; either single- or double-suction
pumps used for the flow rates to 0.063 m/s and total headsto 91 m; beyond these capacities and heads double-suction or
multista e um s are used. Cho e 2004Cho e 2004
Refer to
Manufacturers Pump
Curve
(8) Check Reynold number (laminar or turbulent?)(9) Calculate total developed head
(10) Determine pump suction type
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PUMP (PROCESS DESIGN)
Net Positive Suction Head (NPSH)
m 4.20 m (Total length from pump outlet)
m 8.45 m (Total length of outlet piping)
m
m/s
N/m
m (Satisfactory: No Cavitation)
Operating fluid velocity, uo = 0.794
Vapor pressure of liquid at the pump
suction, Pv =
Vertical distance to pump inlet, H = 0.50
Total length of inlet piping, LT = 5.19
Total length to pump inlet, Li = 3.44
NPSH =
N/m71300
52445
0.007029
1800
3.44
Reynolds number, Re =
Friction factor, f =
Pressure drop, Pf =
Re = ( uo d) /
L = l + (total equivalent pipe diameter for miscellaneous
friction loss due to tanker outlet constriction and the pipe
fittings in the inlet piping d0.001m/1mm)
As a general guide,
NPSH should be
above 3 m for pump
capacities up to 100
m/h, and 6 m above
this capacity.
Pf= 8f(LT/d) ( uo)/2
NPSH = P1/g + H - Pf/g - Pv/g
(11) Calculate NPSH
(12) Check: Cavitation possible?
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PUMP (PROCESS DESIGN)
Job no. Sheet no. By LWS 2/4/08P-102 1
Units
C mm
kg/m Flow Norm. Max. Units
mNs/m u2 Velocity 2.90 0.00 m/s
kg/s f2 Friction loss 0.12 0.00 kPa/m
kg/s L2 Line length 4.20 4.20 m
f2L2 Line loss 0.51 0.00 kPaOrifice - - kPa
mm 30% Control valve - - kPa
Flow Norm. Max. Units
u1 Velocity 2.90 0.00 m/s (a) Heat ex. - - kPa
f1 Friction loss 0.12 0.00 kPa/m (b) - - kPa
L1 Line length 3.44 3.44 m (c) - - kPa
f1L1 Line loss 0.42 0.00 kPa (6) Dynamic loss 0.51 0.00 kPa
u1/2 Entrance 4.11 0.00 kPa
(40 kPa) Strainer - - kPa z2 1.00 1.00 m
(1) Sub-total 4.53 0.00 kPa gz2 9.59 9.59 kPaEquip. press (max) 101.30 101.30 kPa
z1 0.00 0.00 m Contigency None None kPa
gz1 0.00 0.00 kPa (7) Sub-total 110.89 110.89 kPa
Equip. press 101.30 101.30 kPa (7) + (6) Discharge press. 111.40 110.89 kPa
(2) Sub-total 101.3 101.3 kPa (3) Suction press. 96.773 101.3 kPa
(2) - (1) (3) Suction press 96.773 101.3 kPa 14.63 9.59 kPa
(4) VAP. PRESS. 0.00 0.00 kPa (8)/ g 1.53 1.00 m(3) - (4) (5) NPSH 96.77 101.30 kPa
(5)/g 10.09 10.56 mValve/(6)
Control valve %
Dyn. loss
Checked
50
DISCHARGE CALCULATION
Line size
%
(8) Diff. press.
0
Static head
Pump and Line Calculation Sheet
Fluid
Temperature
Density
Fluid from M-102
24.84
977.652
Line size
Equipment
Normal flow
0
Static head
0.740
Design max. flow
20%
50
1.525
1.830
SUCTION CALCULATION
Viscosity
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PUMP (MECHANICAL DESIGN)
Cho e 2004Determination of Upper Limits of Specific Speed
(1) Determine upperlimit of specific speed
From total head and suctionhead.
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Selection of the Best Operating Speed of Centrifugal Pump
m/h
%
m/h
m
m
10000 1246
11000 137113000 1620
Max 24075 3000
*Remarks: 1 gpm = 0.2271 m/h and 1 ft = 0.3048 m.
r/min
Conversion:
1gpm 0.2271 m/h
1 ft 0.3048 m
1 in 25.4 mm
Suction specific speed selected, S = 9316
Type of pump selected Volute, Diffuser
Type of pump stage selected Single-suction pump
1371
Operating speed selected, N = 11000
Inse
rttrialN Required specific
speed, Ns
Safety Factor =
Max. pump capacity =
Pump capacity =
6.177
5.615
Operating speed, N
(r/min)
Pump stage type Single-suction pump
Suction specific
speed rating
Specific speed selected, Ns =
Upper limit of specific speed, NsSuction Head =
10
11010
3.44
44.29Total Developed Head, TDH =
Volute, Diffuser
Volute, DiffuserVolute, Diffuser
3000
Required suction specific
speed, S
Turbine
(Use: Single- or double-suction pump)
20389
Average
GoodExcellent
Excellent
Pump type listed by
specific speed
8469
9316
Ns = NQ0.5
/H0.75
(Perry, 1997)
Refer to the comment at cell G55 beside TDH.
Single-suction centrifugal pumps handle up to
0.0032 m/s at total heads up to 15 m; either
single- or double-suction pumps used for the
flow rates to 0.063 m/s and total heads to 91
m; beyond these capacities and heads double-
suction or multistage pumps are used.
Cho e 2004
S = NQ0.5/NPSH
0.75(Perry, 1997)
Obtain the value from Figure 6.10 with respective
system total head and suction head.
Based on Suction Specific-Speed Ratings. Refer to Appendix.
Based on Pump
Types Listed by
Specific Speed.
Refer toAppendix
Select the N with the best speed
rating. Refer to the table above.
The value of this factor of safety can vary from
a low of 5 percent of the required flow to a
high of 50 percent or more.
(Chopey, 2004)
PUMP (MECHANICAL DESIGN)
(2) Select the best operating speed (by trials)
(4) Determine pump type
(3) Calculate specific speed, Ns
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PUMP (MECHANICAL DESIGN)
18 %Percent head rise from BEP to shut off =
Specific speed selected, Ns = 1371
7 vanes 27 with droopVanes
specification
Vanes number, Z 7
By assumption.
Lobanoff 1992
Obtain vanes specification from Figure 3.2
with respect to percent head rise and Ns.
(5) Determine vanes specification and number, Z (from graph)
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PUMP (MECHANICAL DESIGN)
in
mm
2.08
53
Impeller outer
diameter, D2
Head constant, Ku 1.03
Obtain Ku from Figure 3.3 with
respect to vanes number and Ns.
(Lobanoff, 1992)
D2 = 1840 Ku H0.5
whereby H in ft.
RPM
Lobanoff 1992(Lobanoff, 1992)
(6) Determine head constant (from graph)
(7) Calculate impeller outer diameter, D2
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PUMP (MECHANICAL DESIGN)
ft/s
in
mm
Impeller width, b27
0.24
0.125
Cm2 12.09
Capacity constant, Km2
Obtain Km2 from Figure 3.4 with respect to
vanes number and Ns.
b2 = GPM 0.321 (Lobanoff, 1992)
Cm2 (D2 - ZSu)
Estimated Su = in. (This will be confirmed during
vane development and the calculation repeated if
necessary.)
Cm2 = Km2 (2gH)0.5
with g = 32.174 ft/s2
(Lobanoff, 1992)
(Lobanoff, 1992)
Lobanoff 1992
Lobanoff 1992
(8) Determine capacity constant, Km2 (from graph)(9) Calculate Cm2
(10) Calculate impeller width, b2
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PUMP (MECHANICAL DESIGN)
in
mm
in
inmm
mm
0.5D1/D2
1.04
27Eye diameter, D1
0.3Shaft diameter
under impeller eye,
Ds 8
Eye area 0.78501
Obtain D1/D2 ratio from Figure 3.5
with respect to Ns.
Eye area = Area at impeller eye (D1/4) - shaft are (Ds/4)
Lobanoff 1992
(11) Determine eye diameter:impeller OD, D1/D2 (from graph)
(12) Calculate eye area
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ft/s
m/s
ft/s
m/s
ft
m
Suction eye
velocity, Cm1
11.25
Peripheral
velocity, Ut
3.43
49.88
15.20
NPSHR12
3.66
Nss 8898
Ut = D1 (in) RPM (Lobanoff, 1992)
229
Cm1 = GPM 0.321 (Lobanoff, 1992)
Eye area (in)
Obtain NPSHR from
Figure 3.6 with
respect to Cm1 andUt values.
Nss = (RPM GPM0.5
)/NPSHR0.75
Lobanoff 1992
(Lobanoff, 1992)
(13) Calculate suctioneye velocity, Cm1 &peripheral velocity, Ut
(14) Determine NPSHR
(from graph)
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(Lobanoff, 1992)
PUMP (MECHANICAL DESIGN)
in
mm
in
mm
in
mm
0.23Volute area, A8
146
Casing type Single-volute
Volute velocity
constant, K30.40
Cutwater
Diameter, D3
2.20
56
Volute width, b30.42
11
Obtain K3 from Figure 3.8
with respect to Ns.
A8 = 0.04 GPM
K3 H0.5
Refer to Guidelines for
Volute Width in Appendix.
Refer to Guidelines for CutwaterDiameter in Appendix.
(15) Determine volute velocity constant, K3(16) Calculate volute area (As), volute width (b3) & cutwater
diameter (D3)
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PUMP (MECHANICAL DESIGN)
D2 = 53 mm
D1 = 27 mm
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INTERLOCK
Interlock System Condition
Process interlock between V-101,
V-102 and V-103
V-101 or V-102 or V-103 failed closed or plugged.
M-101 overfilled.
P-101 malfunction.
Process interlock between V-112,
V-113, V-114, V-115 and V-
116.
V-112 or V-113 or V-114 or V-115 or V-116 failed
closed or plugged.
M-102 or M-103 overfilled.P-102 or P-103 malfunction.
Pipelines clogged: no flow from M-102 to M-103.
Process interlock between V-123,
V-124, V-125, V-201, V-202
and
V-203.
V-123 or V-124 or V-125 or V-201 or V-202 or V-
203 failed closed or plugged.
M-104 or M-201 overfilled.
P-104 or P-201 malfunction.
Pipelines clogged: no flow from M-104 to M-201.
Process interlock between valve
for buffer tank, V-210 and V-
211.
Buffer tank valve or V-210 or V-211 failed closed
or plugged.
M-202 overfilled.
P-202 malfunction.Pipelines clogged.
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INTERLOCK (CONT)
Process interlock between V-220,
V-221, V-222 and V-223.
V-220 or V-221 or V-222 or V-223 failed closed or
plugged.
M-203 overfilled.
P-203 malfunction.
Pipelines clogged.
Process interlock between V-224,
V-301, V-302, V-303 and V-304.
V-224 or V-301 or V-302 or V-303 or V-304 failed
closed or plugged.M-301 or M-302 overfilled.
P-301 or P-302 malfunction.
Pipelines clogged.
Safety interlock between V-305,
V-306, V-307 and V-308
V-305 or V-306 or V-307 failed closed or plugged.
P-303 malfunction.
Pipelines clogged: no flow from M-303 to HE-301.