Page 180 - APPLIED PROCESS DESIGN FOR CHEMICAL AND PETROCHEMICAL PLANTS, Volume 1, 3rd Edition

Fluid Flow 153

Table 2-22: Cameron Hydraulic Data (concluded)

Friction Losses in Pipe; C =-100

60 in. Inside d la 72 in. inside dla
Discharge Head Discharge Head
in US gallons Vc!oc- loss in US gallons Veloc- Ioss
ity Veloc- In ity Veloc- in
feet ity feet feet ity feet
I'<;' per per head per per per per head
1&i'lt
mm 24 hr sec -- -- min 24 hr sec -- --
in ft 100 ft
in ft
5000 7,200,000 .56 .005 .003 10000 14,400,000 .78 .009 .005
10000 IH00,000 1.12 .019 .011 20000 28,800,000 1.57 .038 .011
16000 21,600,000 1.70 .045 .024 25000 36,000,000 1. 97 .060 .02,
20000 28,800,000 2.26 .079 .042 30000 43,200,000 2.36 .086 .036
25000 36,000,000 2.83 .124 .062 35000 50,400,000 2. 76 .118 .048
30000 43,200,000 3.40 .179 -088 40000 57,600,000 3.16 .154 .062
32000 46,080,000 3.63 .205 -09' 45000 64,800,000 3.54 .194 .011
34000 48,960,000 3.86 .230 .111 5 � 000 72,000,000 3.94 .240 -094
36000 51,840,000 4.09 .259 -124 5 000 74,880,000 4.09 .259 .100
38000 54,720,000 4.32 .290 .137 54000 77,760,000 4.25 .280 ,107
40000 57,600,000 4.55 .320 -150 56000 80,540,000 4.41 .302 -114
42000 60,480,000 4. 78 .354 -164 58000 83,520,000 4.57 .324 .122
44000 63,360,000 5.00 .387 -180 60000 86,400,000 4.73 .347 .130
46000 66,240,000 5.22 .422 .196 62000 89,280,000 4.88 .370 -138
48000 69,020,000 5.45 .460 .212 64000 92,160,000 5.04 .384 .146
50000 72,000,000 5.68 .500 .229 66000 95,040,000 5.20 .420 .165
52000 74,880,000 5.90 .540 -246 68000 97,920,000 5.36 .447 -164
54000 77,760,000 6.12 .582 .263 70000 100,800,000 5.51 .473 .174
56000 80,540,000 6.35 .626 .281 72000 103,680.000 5.67 .499 -183
.672 .m
68000 83,520,000 6.68 74000 106,560,000 5.83 .528 .193
60000 86,400,000 6.81 . 720 -319 76000 109,440,000 5. 99 .558 .203
62000 89,280,000 7.03 . 768 .339 78000 11%,320,000 6.15 .588 -214
64000 92,160,000 7.25 .819 .360 80000 115,200,000 6.31 .620 .225
66000 95,040,000 7.49 .870 .381 82000 118,080,000 6.46 .650 .235
68000 97,920,000 7. 72 . 925 -403 84000 120,960,000 6. 62 .680 .245
70000 100,800,000 7.95 .980 -425 86000 123,840,000 6. 78 . 712 .256
72000 103,680,000 8.17 1.04 .447 88000 126,720,000 6. 93 . 746 -266
74000 106,560,000 8.40 .10 -470 9b000 129,600,000 7.09 . 780 .277
76000 109,440,000 8.62 1.15 .493 i5000 136,800,000 7. 49 .870 -30f
78000 112,320,000 8.86 1.22 .517 1 0000 144,000,000 7. 88 .965 .33
80000 115,200,000 9.06 1.28 .541 105000 151,200,000 8.28 1.06 .367
85000 122,400,000 9.64 i.44 .607 110000 15R,400,000 8. 67 1.16 -401
,0000 129,600,000 10.20 I. 61 -676 1!5000 165.600,000 9.05 1.27 .,m
95000 136,800,000 10. 78 1.80 .747 1 0000 112,roo,ooo 9. 45 1.38 .473
100000 144,000,000 11.36 2.00 .822 125000 i80, 00,000 I 9.85 1.51 .512
Factor for correcrtng to --Factor for correct ing to
other pipe size• other pipe sizes
Head 1088 Head Ioss
Dia Velocity Velocity ft per Dia Velocity Velocity ft per
ft per sec
iu
ft per sec head ft
100 ft
in
---- --- head ft 100 ft --- --- --- ----
59 1.034 1.070 1-085 70 1.058 1.119 1-147
58 1.070 1.145 1.179 68 1.121 1.257 1-3!8
57 1.108 1.228 1.284 66 1.190 1.416 1-5 7
56 1.148 1.318 I 1.399 64 l.266 1. 602 1-774
(text continued Jro11,. page 141) Step 6: Note the velocity given by this line as 16.5 ft/s,
Step 2: Proceed left horizontally across the chart to the then proceed to the insert on the right, and read upward
intersection, with: from 600 psig to 200 psig to find the velocity correction
Step 3: The 1,000-lb/h flowrate projected diagonally up factor as 0.41.
from the bottom scale.
Step 7: Multiply 0.41 by 16.5 to get a corrected velocity
Step 4: Reading vertically up from this intersection, it of 6.8 ft/s.
can be seen that a Lin. line will produce more than the
allowed pressure drop, so a 1!1,--in. size is chosen. The author has compared this method with Dukler
Step 5: Read left horizontally to a pressure drop of 0.28 [29] and others and reports good agreement for reason-
psi/100 ft on the left-hand scale. ably good cross section of flow regimes.