NC0020567_AtC Design Calculations_20180827

2017 WWTP IMPROVEMENTS PROJECT
YADKIN VALLEY SEWER AUTHORITY
SURRY COUNTY, NORTH CAROLINA
CWSRF: CS370541-03
DESIGN CALCULATIONS
April 30, 2018
BENJAMIN B. THOMAS, P.E.
WEST CONSULTANTS, PLLC
MORGANTON, NORTH CAROLINA
WEST
CONSULTANTS {

The WAS pumps to be replaced will have the same nominal capacity as the existing pumps (80
GPM). However, in checking the various design conditions (different suction side and discharge
side static water levels), the critical condition will reduce flow to about 65 GPM. This will be for
the condition of moving sludge from the thickener when nearly empty to a full digester or
holding tank. The following calculations show the various pumping scenarios.
The theoretical sludge volume to be wasted, at plant design capacity, is estimated as follows:
Sludge Age = MLSS x Basins Volume
Qw SSW + Qe SSe
Where:
Sludge Age = 20 days (extended aeration process
MLSS = 3,500 mg/I_
Basins Volume = 1.8 MG
QW = Sludge Wasting Rate (MGD)
SSW = Sludge Wasted Solids Concentration (use 7,500 mg/L)
Qe = Effluent Flow (1.8 MGD)
SSE = Effluent Solids Concentration (use 15 mg/L)
Then Qw=0.0384 MGD=38,400 GPD =27 GPM
Therefore, sludge pump will need to run approximately 8 hours/day.

o
GPM
If
FT11OOFT
0.009
YVSA WVV'rP
K
2.00
ADJUSTED Hf
FEET
027
Hs
FEET
27.11
TDH
FEET
2738
WAS PUMP CALCS
Hf
FEET
0 06
K
200
ADJUSTED Hf
FEET
0.13
SYSTEM CURVE-.
Sludge Digester
VELOCITY
FPS
40
0.27
50
FORCEMAIN SIZ[.E S ,....._1
ID = 7 755 INCHES
PIPE
I.D. IIN•1
PIPE I.D.
ON,
EQUIVALENT LENGTH =
1504 LF
2' SDR21
2
2" SDR21
2
0.34
60
3" SDR21
3 146
3" SDR21
3
LOW WATER ELEVATION=
953 89 MSL (sludge thickener full)
4" SDR21
4 048
4" SDR21
4
HIGH POINT=
981 00 MSL
6" SDR21
5 955
6' SDR21
6
STATIC HEAD=
27.11 FEET
B' SDR21
7.755
8" SDR21
8
G=
100
Cm 160
27.42
044
70
o
GPM
If
FT11OOFT
0.009
Hf
FEET
0.13
K
2.00
ADJUSTED Hf
FEET
027
Hs
FEET
27.11
TDH
FEET
2738
If
FT1100FT
0.004
Hf
FEET
0 06
K
200
ADJUSTED Hf
FEET
0.13
Hs
FEET
27 11
TDH
FEET
27.24
VELOCITY
FPS
40
0.27
50
0.013
0.20
2.00
041
2711
2752
0 006
010
2.00
0.19
27 11
27.30
0.34
60
0.019
0.28
2.00
057
27.11
2768
0.009
013
2.00
0.27
2711
27.38
041
65
0.022
0.33
200
066
2711
2777
0 010
016
2 DO
031
2711
27.42
044
70
0.025
0.38
200
0.76
27.11
27.87
0 012
0.18
200
036
2711
27.47
0.48
75
1 0.029
0.43
2 00
0.86
27.11
27.97
1 0 013
0.20
200
041
2711
2752
1 051
EQUIVALENT LENGTH CALCULATIONS 8 " FORCE MAIN Suction Line Diameter -
EQ LENGTH Pump Discharge Diameter =
ITEM _ _ PER UNIT OTY EQ LENGTH (feet) Foreemain Diameter =
PS
SUCTION PIPE
342 0
342 0
(SUCT'N
SUCTION 90' BEND
0•
70
840
SIDE)
SUCTION 45' BEND
so
385
DISCHARGE 94' BBEND
_
jilt5q;
5D
6-60
PS
DISCHARGE PIPE
291.0
291.0
(DISCH
GATE VALVE (DIS. SIDE)
0.0
SIDE)
CHECK VALVE
00
TEE BRANCH FLOW
3.0
_ 720
TOTAL
887 5
EQUIVALENT LENGTH CALCULATIONS
6 " FORCE MAIN
EQ LENGTH
ITEM
PER UNIT
QTY
EO LENGTH (feet)
PS
SUCTION PIPE
'.1.0
r
0.0
(SUCT'N
SUCTION 90' BEND
IZ6
0.0
SIDE)
SUCTION 45' BEND
0 0
DISCHARGE 90' BEND
M B.Q.
R 8.0
289.0
PS
DISCHARGE PIPE
IiO
40.0
162 4
(DISCH
GATE VALVE (DIS. SIDE)
3
3.0
390
SIDE)
CHECK VALVE
!320.0
I
0 0
REDUCER (8' TO 6")
i3.0
10
52 8
TEE BRANCH FLOW10
731
TOTAL
616.2
This page assumes the WAS pumps are pumping from the sludge th ckener that is full to the sludge digester tank The sludge thickener is at 953 89' when full and the
digester is at 981' This would be the highest head condition for the pumps and has a static head of 27 11' The page includes a friction loss table and an equivalent
length table, but the friction loss table Is to be ignored since a rheology method was used to calculate friction losses and can be seen on page 5 The friction loss was
calculated to be 9 72' conservatively assuming the amount of solids in the sludge is 49§ Adding the static head and friction lasses gives a TDH of 36.83'.

Sy§TEM r4URVE-
FORCEMAIN StZL .1
EOUIVALENT LENGTH =
LOW WATER ELEVATION=
HIGH POINT=
STATIC HEAD=
YVSA WW7P
f
FT1100FT
Hf
FEET
K
ADJUSTED Hf
FEET
WAS PUMP CALCS
TDH
FEET
f
FT1100FT
0 004
Hf
FEET
0.06
S'udge Digester
ADJUSTED Hf
FEET
013
Hs
FEET
35.00
TDM
FEET
3513
VELOCITY
FPS
ID = 7 755 INCHES
PIPE I.D.
(IN.l
PIPE
I.D. (IN.)
1504 LF
2' SDR21
2
2" SDR21
2
0 006
3' SDR21
3.146
3" SOR21
3
94600 MSL (s'udge thickener half way)
4" SDR21
4.046
4" SDR21
4
981.00 MSL
6" BOR21
5 955
6" SDR21
6
35 00 FEET
8' SDR21
775S
8" SDR21
8
C= 100 1 G= 160
Q
GPM
f
FT1100FT
Hf
FEET
K
ADJUSTED Hf
FEET
He
FEET
TDH
FEET
f
FT1100FT
0 004
Hf
FEET
0.06
K
200
ADJUSTED Hf
FEET
013
Hs
FEET
35.00
TDM
FEET
3513
VELOCITY
FPS
40
0.009 0.13 2.00 027 3500 3527
027
50
0.013
0.20
2.00
041
3500
35.41
0 006
010
200
019
35.00
3519
034
60
0.019
0.28
200
057
3500
35.57
0 009
0.13
200
0.27
35,00
3527
0.41
65
0 022
0.33
2.00
066
35.00
3566
0 010
016
200
0.31
35 00
3531
044
70
0 025
0,38
2.00
0.76
35.00
3576
0 012
018
200
036
3500
35.36
0.48
75
1 0.029
0.43
2.00
086
3500
3586
1 0.013
020
2.00
0.41
3500
35.41
1 0.51
EQUIVALENT LENGTH CALCULATIONS 8 "FORCE MAIN Suction Line Diameter =
EQ LENGTH Pump Discharge Diameter =
,TEM PER UNIT QTY EQ LENGTH (feet) Forcemain Diameter=
PS
SUCTION PIPE
1.11
3420
342.0
(SUCT'N
SUCTION 90' BEND
12.11
70
84.0
SIDE)
SUCTION 45' BEND__
9=7
5.0
38.5
DISCHARGE 90' BEND
sizo "
5.0
Boo
PS
DISCHARGE PIPE
1.0.
2910
291 0
(DISCH
GATE VALVE (D.S. SIDE)
3z
00
SIDE)
CHECK VALVE
90.6
00
TEE BRANCH FLOW'
0
30
720
TOTAL
887.5
EQUIVALENT LENGTH CALCULATIONS
6 " FORCE MAIN
EQ LENGTH
ITEM
PER UNIT
QTY
EQ LENGTH (feet)
PS
SUCTION PIPE
1.0
i
0 0
(SUCT'N
SUCTION 90' BEND
12. 0
00
SIDE)SUCTIONr45'
BENd
7.7
00
DISCHARGE 90' BEND 4�.
8.9
80
289.0
PS
DISCHARGE PIPE
•t,0
400
162.4
(DISCH
GATE VALVE (DIS. SIDE)
3.2
30
390
SIDE)
CHECK VALVE
90.0
00
REDUCER (8" TO 6")
13:0
1.0
52.8
TEEABRANCH FLOW)
183
10
731
TOTAL'
616+2
This page assumes the WAS pumps are pump ng from the sludge thickener that is drawn down half way to the sludge digester tank. The sludge thickener Is at 953.69'
when full and the d gester is at 946' when half full, giv ng a static head of 35' The page includes a friction loss table and an equivalent length table, but the friction loss
table Is to be ignored since a rheology method was used to calculate friction lasses and can be seen on page 5. The friction loss was calculated to be 9.72'
conservatively assuming the amount of solids In the sludge is 4% Adding the static head and friction losses gives a TDH of 44 72'

YVSA WWTP
WAS PUMP CALCS
SYSTEM CURVE: Sludge Digester
FORCEMAIN SIZF SO�tM�..1 1 0 7.755 INCHES PIPE I.O. (IN.) PIPE I.D. IINJ
EQUIVALENT LENGTH =
1504 LF
2" SDR21
2
2" SDR21
2
TOM
FEET
If
FT1100FT
0,004
3" SDR21
3 146
3" SDR21
3
LOW WATER ELEVATION=
940 39 MSL (invert effluent pipe;
4" SDR21
4 046
4" SDR21
4
HIGH POINT=
981 00 MSL
6' SDR21
5.955
6' SDR21
6
STATIC HEAP=
40 61 FEET
e" SDR21
7 755
B" SDR21
8
034
60
C = 100
Cm 150
200
0.57
4061
Q
GPM
f
FT1100FT
Hf
FEET
K
ADJUSTED Hf
FEET
He
FEET
TOM
FEET
If
FT1100FT
0,004
Hf
FEET
0.06
K
2.00
ADJUSTED Hf
FEET
013
His
FEET
4061
TOM
FEET
4074
VELOCITY
FPS
40
0.009 0.13 2.00 0.27 4061 40.88
0.27
50
0 013
020
200
0.41
4061
41.02
0.006
010
2.00
019
4061
4080
034
60
0,019
0.28
200
0.57
4061
41 18
0.009
013
2.00
027
40.61
4088
0.41
65
0.022
033
200
066
4061
4127
0.010
0.16
2.00
031
40.61
4092
0.44
70
0 025
038
200
076
40.61
4137
0.012
018
2.00
036
40.61
4097
0.48
75
1 0 029
0.43
200
0.86
4061
41.47
1 0.013
020
2.00
041
40.61
41.02
1 051
This page assumes the WAS pumps are pumping from the sludge thickener that is drawn down the the Invert of the effluent pipe to the sludge d gester tank The
sludge thickener Is at 940 39' when drawn down all the way and the digester is at 981' when full, giving a static head of 40 59' The page Includes a friction loss table
and an equivalent length table, but the friction loss table is to be ignored since a rheology method was used to calcutate fnction losses and can be seen on page 5 The
friction loss was calculated to be 9 72' conservatively assuming the amount of solids in the sludge is 4% Add ng the static head and fnction losses gives a TDH of
50.31'
EQUIVALENT LENGTH CALCULATIONS
8 " FORCE MAIN
Suction Line Diameter s
EQ LENGTH
EQ LENGTH
Pomp Discharge Diameter =
PER UNIT
ITEM
PER UNIT
QTY
EQ LENGTH (feet)
Forcemaln Diameter=
PS
SUCTION PIPE
.1.0
342.0
342.0
(SXrN
SUCTION 90' BEND
X120
7.0
840
0.0
SIDE;
SUCTION 45' BEND
T-
5,0
385
PS
DISCHARGE PIPE
DISCHARGE 90' BEND
Q4,0
S l]
60.0
GATE VALVE (DIS SIDE)
FS
DISCHARGE PIPE
1A
2910
291.0
1)0.0
(DISCH
GATE VALVE (DIS SIDEI
3.2.
REDUCER (a" TO 6")
00
1 0
SIDE)
CHECK VALVE
90,0
00
73.1
TEE BRANCH FLOW _ _
A4, 0.
3.0
72.0____
TOTAL
887.5
This page assumes the WAS pumps are pumping from the sludge thickener that is drawn down the the Invert of the effluent pipe to the sludge d gester tank The
sludge thickener Is at 940 39' when drawn down all the way and the digester is at 981' when full, giving a static head of 40 59' The page Includes a friction loss table
and an equivalent length table, but the friction loss table is to be ignored since a rheology method was used to calcutate fnction losses and can be seen on page 5 The
friction loss was calculated to be 9 72' conservatively assuming the amount of solids in the sludge is 4% Add ng the static head and fnction losses gives a TDH of
50.31'
EQUIVALENT LENGTH CALCULATIONS
6 "FORCE MAIN
EQ LENGTH
ITEM
PER UNIT
QTY
EQ LENGTH feet
PS
SUCTION PIPE
•1,0
0.Q
(SuCT'N
SUCTION 90' BEND
"12.0
0.0
SIDE)
SUCTION 48 BEN
70
0.0
_
DISCHARGE 90' BENDµ a
69
8.0
289 0
PS
DISCHARGE PIPE
1.0
40.0
1624
(DISCH
GATE VALVE (DIS SIDE)
3.2
3.0
390
SIDE)
CHECK VALVE
1)0.0
00
REDUCER (a" TO 6")
lia.
1 0
528
TEE (BRANCH FLOW�w w.. ,JyE
i D
73.1
TOTAL
616.2
This page assumes the WAS pumps are pumping from the sludge thickener that is drawn down the the Invert of the effluent pipe to the sludge d gester tank The
sludge thickener Is at 940 39' when drawn down all the way and the digester is at 981' when full, giving a static head of 40 59' The page Includes a friction loss table
and an equivalent length table, but the friction loss table is to be ignored since a rheology method was used to calcutate fnction losses and can be seen on page 5 The
friction loss was calculated to be 9 72' conservatively assuming the amount of solids in the sludge is 4% Add ng the static head and fnction losses gives a TDH of
50.31'

O
GPM
f
FTI100FT
YVSA WWTP
K
ADJUSTED Hf
FEET
Hs
FEET
TDH
FEET
f
FT1100FT
0 004
WAS PUMP CALCS
K
2 OD
ADJUSTED Hf
FEET
0 O5
Hs
FEET
4.51
SYSTEM CURVE:
Sludge Digester
44
0.009 0.05 2.00 oil 4 51 462
0.27
50
FORCEMAIN SIZr 1
I D. = 7.755
INCHES PIPE I.D.
(IN.)
PIPE
I.D. IIN.t
EQUIVALENT LENGTH =
004
592 LF 2" SDR21
2
2" SDR21
2
0.34
60
3" SDR21
3.146
3' SUR21
3
LOW WATER ELEVATION=
951-59 MSL (top of
water at clarifier) 4" SDR21
4.046
4" SOR21
4
HIGH POINT=
956.10 MSL
6' SDR21
5 955
6" SDR21
6
STATIC HEAD=
4.51 FEET
8' SDR21
7 755
8" SDR21
6
C=
100
Cm 160
463
044
70
O
GPM
f
FTI100FT
Hf
FEET
K
ADJUSTED Hf
FEET
Hs
FEET
TDH
FEET
f
FT1100FT
0 004
Hf
FEET
0.02
K
2 OD
ADJUSTED Hf
FEET
0 O5
Hs
FEET
4.51
TDH
FEET
4.56
VELOCITY
FPS
44
0.009 0.05 2.00 oil 4 51 462
0.27
50
D.013
008
2.00
0.16
451
467
0 006
004
200
0.08
4 51
459
0.34
60
0.019
Oil
200
022
4.51
473
0 009
005
200
Oil
4.51
462
041
65
0.022
013
200
0.26
4.51
4.77
0 010
006
200
012
451
463
044
70
0,025
015
200
030
4.51
481
0 012
007
200
0.14
4.51
465
0.48
75
1 0 029
0.17
200
0.34
4.51
485
0.413
0 08
2 00
0.16
4,51
467
1 051
EQUIVALENT LENGTH CALCULATIONS 8 "FORCE MAIN Suction Lina Diameter a
EQ LENGTH Pump Discharge Diameter=
ITEM PER UNIT OTY EO LENGTH Oeetl Forcemaln Diameter =
PS SUCTION PIPE
(SUCT'N SUCTION 90' BEND
SIDE) SUCTION 45' BEND
DISCHARGE §15"t IfW0
PS DISCHARGE PIPE
(DISCH GATE VALVE (DIS SIDE)
SIDE) CHECK VALVE
TEESBRANCH FLOW)
?#!0 196.0 1960
TIZO
1.0
120
'fes
5.0
38 5
11:0
5.0
Soo
'7.0
2130
2130
3.2-
SUCTION PIPE
00
00.0
(SUCT'N
00
24.0.
_ 30
72.0
SU_CTIO_N 45- _PEND
TOTAL
591.5
T
TOTAL 4.0 1/-
This page assumes the WAS pumps are pumping from the clarifier to the sludge thickener The clarifier Is i4
941.59' nd the thickener, when full is at 953.89' although
the high spat is where the 8" d scharge pipe branches toward the thickener This would be the lowest head ca n for the pumps and has a static head of 4 51' The
page includes a friction loss table and an equivalent length table, but the friction loss table is to be gnored since a rheology method was used to calculate friction losses
and can be seen on page 5 The friction loss was calculated to be 3 82' conservatively assuming the amount of solids in the sludge is 4% Adding the static head and
friction losses gives a TDH of 8 33',
EQUIVALENT LENGTH CALCULATIONS
6 " FORCE MAIN
EQ LENGTH
ITEM
PER UNIT
QTY EQ LENGTH feet
PS
SUCTION PIPE
-1.0
00
(SUCT'N
SUCTION 9o" BEND
lu
0.0
SIDE)
SU_CTIO_N 45- _PEND
7W7 _
_ _0.0
µ
DISCHARGE 90' BEND
8119
0-0
PS
DISCHARGE PIPE
d'o
00
(DISCH
GATE VALVE (DIS SIDE)
3.2
00
SIDE)
CHECK VALVE
X0.0
00
REDUCER (8"TO6")
TEE BRANCH CLO
134
113 0
00
0 0 f
T
TOTAL 4.0 1/-
This page assumes the WAS pumps are pumping from the clarifier to the sludge thickener The clarifier Is i4
941.59' nd the thickener, when full is at 953.89' although
the high spat is where the 8" d scharge pipe branches toward the thickener This would be the lowest head ca n for the pumps and has a static head of 4 51' The
page includes a friction loss table and an equivalent length table, but the friction loss table is to be gnored since a rheology method was used to calculate friction losses
and can be seen on page 5 The friction loss was calculated to be 3 82' conservatively assuming the amount of solids in the sludge is 4% Adding the static head and
friction losses gives a TDH of 8 33',

Velocity (ft1s)
6' Pipe
_
Eq. Length (ft)
1504
Pipe Diameter (ft)
067
Yield Stress (s.,)
0 105 from fig 13.6a
Coefficient of Rigidity (ri)
001 from fig 13.6b
Sludge Solids (%)
4°%
Velocity (ft1s)
044
will change with Q
Unit weight (kglm3)
1016
0 105 from fig 13-6a
Unit weight (lblft�)
63.43
YvD
NR =
4'!�
9
Irl,
Reynolds Number (NA)
f .a7E+03
D2Sygy
Hedstrom Number (He)
9.53E+05
Nc z
9
Friction Factor (f) 0.35 from fg 13-6c
1
now is laminar
�fyLvz
Pressure Drop Op (bfft1) 606.250472 GP = D
Friction Loss AP (H) 9.71555244 g
Thickener TDH (full) = 36 03
h ckener TOH (half full) = 44 72
Thickener TDH (low) = 50 33
9" Suction Moe for NPSH
Eq. Length (ft)
4645
Pipe Diameter (ft)
067
Yield Stress (sr)
0 105 from fig 13-6a
Coefficient of Rigidity (q)
001 from fig 13.6b
Sludge Solids (%)
4'!�
Velocity fts)
044 will change with 0
Unit weight (kg/m3)
1016
Unit weight (lb/ft)
63.43
NR = yvD
9
Reynolds Number ft)
1.87E+03
DzSygy
Hedstrom Number (He)
9.53E+OS
He = z
n
Friction Factor (f)
035 from fig 13.6c
1
Row is laminar
Pressure Drop, Op (ibffO)
107 273317
2fyLvz
GP =
Friction Loss, Ap (ft)
3.00117494
gD
5
YVSA WWTP
WAS PUMP CALCS

YVSA WWTP
WAS PUMP CALCS
Lowest Head
Eq. Length (R)
591.5
Pipe Diameter (ft)
067
Yield Stress (sr)
0 105 from fig 13-6a
Coefficient of Rigidity (rl)
0 0' from fig 13.6b
Sludge Solids (%)
4^ -
Velocity (ftls) 0.44 will change with 0
Unit weight (kgfm3) 1016
Unit weight (Iblft?) 63.43 YvD
NA = —
Reynolds Number (NR) 1 87E+03 D%gy
Hedstrom Number (He) 9.53E+05 Ne = Z
n
Friction Factor (f) 0 3� tram fig 13-6c
I
flow is lam nar
Pressure Drop, dp (IbMe) 238 476139 Ap a 440
Friction Loss, dp (ft) 3.821733 gD
Lowest Head TRH = 8 33
This page calculates the head lass accounting for an assumed sludge
percentage of 4% This method calculates the pressure drop due to
friction which can then be converted to feet

YVSA WWTP
WAS PUMP CALCS
-'For Open Systems"'
Air Pressure Calc
Elevation (ft) = 960
Elevation (m) = 292.6
Temperature (F) = 90
Temperature (K) = 3054
Gravity = 9.61
Molar Mass of Air (M) = 0.03
Gas Constant R = 8.31
Air Pressure (Pa) = 98061 81
Air Pressure (psi) = 14.22
Air Pressure, He (ft) = 32.81
0
NPSH Calc - source below pump I—
z
Sludge Thickener High EL = 953.89
Sludge Thickener Low EL = 94039 A
Pump Center EL = 95051 L9
Hz (ft) _ -10.12 inv out at sludge holding
Hv (H) = 0.0030 changes with velocity
Suction Eq L (ft) = 4645
Hf (f )= 3.00
Hvp (psi) = 0 698 changes with temp
Hvp (H) = 1.61
NPSHa = 18.08
NPSH Cale - source above pump ri— a
Sludge Thickener High EL = 95389 z
Sludge Thickener tow EL = 94039 A
Pump Center EL = 95051
Hz (ft) = 3.38 top of water level at sludge holding
Hv (ft) = 00030
Suction Eq L (ft) = 464.5
Hf (ft) = 300
Hvp (psi) = 0.69E
Hvp (ft) = 1.61
NPSHa= 3158
This page calculates the NPSH availabe for ti --e pump based on an elevation of 960' and a
temperature of 90 This calcu ation was sent to Penn Va ley Pumps to review and check the
acceleration head To av6d cavitat;on they saw that when the s.udge thickener is empty (highest
head condition) the max flaw should be approx'mate y 65 GPM. when the s . dge thickener is full the
max flow should be approximaWy 75 GPM and when the pumps pini from the clarifier to the sludge
th ckener (lowest head condition) the pump can handle the Idea.'flow of 80 GPM without cavitation
The ideal flow is 80 GPM based from the treatment plant operato.'s observations where flows over
80 GPM tend to pi 1 out water without much solids

PENN VALLEY PUMP CO., INC.
998 EASTON RD
WARRINGTON, PA 18976
P: 215-343-8750 - F: 215-343-8753
www.pennvalleypump.com
Project: YVSA - Elkin, NC
Engineer West Associates, Inc.
Date: 4/2412018
Quote; 16235
Application: WAS Transfer to Thickener and Thickend Sludge Transfer to Digester
Pump Size: 4DDSX30CNU-MK3
Pipe Size: 8" diameter
Flow (GPM): 65GPM @ 53.22 TDH
NPSH= hp-hvpa+l-hst-hfs-ha= -60.4163 ft head loss
Acceptable applications are (-70) and below due to suction pulsations dampener providing for improved suction
pressure thereby improving NPSH by this amount_
where:
hp= absolute pressure (ft) on the surface of the liqud supply level.
Barometric pressure for open tanks or sump ; absolute pressure
existing in closed tanks or systems
hvpa= vapor pressure of the fluid at pumping temperature (ft)
hst= static pressure (ft.) developed by column of fluid above (+) or
below (-) the centerline of suction inlet
hfs= suction line loss (ft) including entrance losses, friction loss, pressure drip
across valves, fittings, other system components, etc
Acceleration Head as part of NPSHA for Double Disc Pumps
ha= LVnCSG ha= 3043.8 ha= 78.77329 ft
KG 38.64
ha= acceleration head in psi
L= length of suction line in feet
342
V`= velocity in suction line in fps
0.445
n= pump speed in rpm
200
C= Constant for type pump
0.1
C= .100 simplex
C= 060 duplex
SG"= specfic gravity of liquid 1 0
K= 1 1 2
a factor representing the reciprocal fraction of the theoretical acceleration head
which must be provided to avoid a noticeable disturbance in the suction line.
K= 1.2 for typical municipal condition
g= gravitation constant (32.174 fUsec2) 32.2
` Based on New Ductile Iron Pipe.
" Based on water at 70 degree F.
33,96
0 783
-
10.92
3.9

Puyn p w r i% G�ti ':' &.5 (7P-&? (� ZOO R PAA i
Power Consumption Curve
10 I;I; II 1111 11lIlI I �I;II�
g 1111 1�11IIIIII 1 11 11 111
s I 11111 II I� 500 RPM ILII
I 400`` RPM
7 I 1 I I I N I I I i I 380 rpm
6 I
= 6 I i I I ! I I M 1 1 1 200 RPM
i
4low
I I l i I 1 1 I 'i00 RPM
3 I ,III l
2 I�i�ll I .1�1 III �II ��I I'll
1 1 I I I 1 I Performance based on water (32SSU) at 60 degrees F.
0
0 20 40 60 80 100 120 140 160
TQH (FT)
Copyright 2009 Penn Valley Pump Co:, Inc,
SLS -04-30-0312012