Coker A.K. Fortran Programs for Chemical Process Design, Analysis, and Simulation
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Heat Transfer 607
Figure 8-8 shows the heat transfer coefficient of fluids inside tubes. The
heat transfer coefficient based on the outside of the tube, h~o, is:
('D /
h,o - h, ~ (8-24)
(9) Recently, Hedrick [12] developed a new correlation for the heat
transfer coefficient in the transition region between laminar and turbu-
lent
flow. The equations for determining the inside film coefficient and
based on the outside tube diameter, h~o, are:
E //~
h,o-/'61 oo)B, 33
(8-25)
where
B~
-
(-3.08
+
3. 075X
+
0.32567X 2
-
0.02185X 3)
( 10. ID )['-(x/'o~'> ~-~"]
• L
100
hD,
m
100
9 , i ; " i , L ; ', ; ; i ~" '
i
i
t ~, ~ I
' ,
i i ~i~li i i I fill ;/ '
I I , I I I~t I t t I iii /
I i , ~ltll ~ I i ii!i./
...... t I I tlt~
II1
r t , ~ 1'
,,,,I , /,# I i i ~',,I
i i i if ii#1' : ~ , t
~;,
i I I 1 I ! ~"/ill
c =
Specific Heat,
D~ =
Inside Tube Diameter,
t I i i L,.,,- ,''''~'~ W// G~=
Mass Velocity Inside
Tube,
~~ L ~"-,/~,~_~,J,,~ "~ l~,J"'~ ~/_/'~1 ~
h = Coefficient Of Heat T .... fer,
k =
Thermal Conductivity,
/ L =
Length,
- "~ ~,,,,,~_ ~ p = Vi
.... ity
At A
.... ge Fluid Temperature,
Ib./(hr.)(ft.)
r ~ ~'~'S~'/'~
Ill pw=Vi .... ityAtTube-WellTemperat ....
Ib./(hr.)(ft.)
1,000 I 0,000
Figure 8-8. Coefficient of heat transfer fluids inside tubes.
' i ' " 1 100
'* i i i
' i i
i I
IL
D i ltl
I
, ,I
BTUI(Ib)(~
Feet
Ib.l(hr.)(sq.ft.)
BTUl(hr.)(sq.ft.)(~
BTUl(hr.)(sq.ft.)(~
Feet
I O0 000
608 Fortran Programs for Chemical Process Design
and
X
Re t
l, 000
Simplified Equations
For common gases, Equation 8-23 can be simplified to give the
approximate equation,
0. 014CpG~ s
h i --
(8-26)
(ID/12) ~
Similarly for water at ordinary temperature and pressure,
150(1 + 0 011tb)V~ 8
9 (8-27)
h i -
ID 0.2
where Cp = heat capacity of fluid, Btu/lb~
ID = tube inside diameter, inch
G t = mass velocity inside tube, lb/ftZhr
t b =
average (i.e., bulk) temperature of water, ~
vt ~ velocity of water, ft/sec
Total Pressure Drop, APT
(10) From Re~, determine the friction factor from Figure 8-9. Using
the regression method in chapter one of the text, for Re t _< 1000, the
friction factor correlation in Figure 8-9 can be approximated by
0.45
ft ReO.9853
(8-28)
similarly, If Re, > 1000, the friction factor is approximated by
0.0028
ft --- r~ 0 2514
(8-29)
Ke t 9
(11) The fluid velocity,
Vt,
is:
Vt = Gt (8-30)
3600. p
(3
8
0
o"
+I ! '+'' ' ' / !
IJ
Ill,,]
_ ~ i + i + i
71 t
I1
I1 i
.......
+
II - !t ........ / ...... 4'
1t_ [ I! k' ~ i 1'4"
LL ++ i ~
Jj i! ~ . ,
I
i
I
i + +
t
i • +
tl !+ .....
t1-'"
1t i+
ilL., i,,,,
11
+ E J
I I , I R + I '
- ,, ' 'k • : ,- I i t +tt t 4
11 i i ! I
il
' + .....
t I I I ,
!
JJ__J /: II + I 1 ' ' '
11 i tJ • ~
/
I i , ~ , , + I+p, ,
II ' i II I J +,P I ] ' I I I M I I I '
.IL'' ~ .... / i i ' '
II
.I
i ...1
. i • .,
I +' ' I I
ill ++ +.,.:"
0 + . , I
{ ', ........
1 Jill+ I '+ '
Ill ~ r + 2 ............
I ~ I I I I I 1 1 I t ~ L !
t~l~ "q _ , t i
11
:
! !!!!-! ! ~ i It I ' i ./ .... ill!
I
....
LSIJ' .... + _ ' I i I
o LJ_ ...... . i r
"1 .....
i
o ~
',Ul.'b+,i / 11 ,;bll ,.,i t
<,.D
..,.9,o
~>
"F-
I>
~!: !: i i ¸
610 Fortran Programs for Chemical Process Design
(12) Tube pressure drop, AP~, psi
AP t =
2 Ln
ft. Gt . 9
2gp(ID/12)
(8-31)
where
G t -
lb/ft2.s
g - acceleration due to gravity, 32.17
ft/sec 2
Alternatively,
AP t can be expressed as:
AP t =
f~.G~.L.n
5.22 x 10J~ (ID/12). s. ~)~
(8-32)
where G~ = lb/ftZhr and ~)~ = bt/~ = 1
s = specific gravity
L = length of tube, ft
n = number of tube passes
(13) The pressure drop of return losses, psi using Frank's [13] corre-
lation is"
2
AP~ - - K. n. p. V~ (8-33)
2g(144)
where K is the number of velocity heads loss per tube pass, where K - 2.5
(14) The pressure loss in both nozzles can be estimated from
1 ) n
ANn - l'5p -~g 1-~
(8-34)
(15) Total pressure drop AP T, psi
AP T - AP t + AP~ + AP n
(8-35)
If AP, is unacceptable, it is necessary to assume a new pass arrange-
ment and repeat the calculations. The heat transfer coefficient of the
shell and tube heat exchanger is only acceptable if the design is within
limits of the allowable pressure drop for the streams being heated or
cooled. The selection of the optimum allowable pressure drop for an
exchanger is a function of the overall process design.
Pressure drop calculations for more complex geometries of shell and
tube exchangers, and for plate and spiral plate exchangers, are given by
Heat Transfer 611
Sandler and Luckiewicz [ 14]. The acceptable range of pressure drops in
a heat exchanger depends on the system operating pressure. Table 8-2
shows typical pressure drop ranges.
For high pressure drop design, fluid velocity may be the more limit-
ing criterion, but a liquid velocity exceeding 15 ft/s can result in ero-
sion-corrosion in an exchanger.
Shell Side
(1) Equivalent diameter,
D e,
is calculated as follows"
Square pitch"
D e =
4 x free area
wetted perimeter
De __ __
4(P 2 - n. OD 2/4) , inch (8-36)
n. OD
Triangular pitch"
De-(
1 72p2 - 0. 5 ~" OD2 )0.5. n. OD-
(8-37)
Clearance, C, between tubes is"
C - PT -- OD (8-38)
Tube Arrangement
Tubes can be arranged in triangular, square, or rotated square pitch.
Triangular tube layouts give better shell side heat transfer coefficients
and provide more surface area for a given shell diameter. Alternatively,
square pitch or rotated square pitch layouts are used when mechanical
Table 8-2
Acceptable Pressure Drop Range for
Shell and Tube Heat Exchanger
SYSTEM PRESSURE PRESSURE DROP RANGE
Vacuum 5-10% of absolute system pressure.
1-10 psig 0.5-5 psi.
> 10 psig 5 psi - 50% of system pressure.
612
Fortran Programs for Chemical Process Design
cleaning of the outside of the tube is required. Widely spaced triangular
patterns also allow for better cleaning. Both types of square pitches
result in less shell-side turbulence and give low pressure drops, but lower
heat transfer coefficients than triangular pitch.
Tables 8-3 to 8-10 show estimated tube counts for different square or
triangular pitch arrangements. Figure 8-10 shows the tube layouts.
(2) Flow area a~ (assuming a plausible baffle spacing for the pressure
drop allowed), is:
Table 8-3
Tube Count for 3/8-in. OD Tubes on 13/16-in. A Pitch
Tube Count for s/o in. OD Tubes on 13/1e-in. A Pitch
TEMA TEMA TEMA TEMA
Type L or M Type P Type S Type U
Fixed Outside Packed Inside
Tubesheet Floating Head Floating Head U-Tube
Shell No. of Passes No. of Passes No. of Passes No. of Passes
ID in. 1 2 4 6 1 2 4 6 1 2 4 6 2 4 6 8
5.047
6.065
7.981
10.02
12.00
13.25
15.25
17.25
19.25
21.25
23.25
25.00
27.00
29.00
31.00
33.00
35.00
22 20 16
37 30 28
68 66 60
110 106 96
170 164 148
212 196 188
283 270 252
364 348 332
454 440 420
562 554 524
668 646 612
922 902 868
1230 1212 1172
1590 1560 1516
19 18 12 19 14 12
31 26 24 31 26 16
61 52 48 56 52 44
104 98 84 96 90 76
151 142 128 151 138 128
178 168 156 187 184 160
241 232 220 258 242 224
316 298 292 336 326 304
396 388 352 421 412 392
490 484 456 526 502 480
588 570 548 608 598 556
812 808 764 868 836 804
1106 1092 1040 1152 1124 1088
1438 1430 1336 1496 1468 1424
Tube Count for 5/a in. OD Tubes on 7/8 in. /~ Pitch
TEMA TEMA TEMA TEMA
Type L or M Type P Type S Type U
Fixed Outside Packed Inside
Tubesheet Floating Head Floating Head U-Tube
Shell No. of Passes No. of Passes No. of Passes No. of Passes
ID in. 1 2 4 6 1 2 4 6 1 2 4 6 2 4 6 8
5.047
6.065
7.981
10.02
12.00
13.25
15.25
17.25
19.25
21.25
23.25
25.00
27.00
29.00
31.00
33.00
35.00
22 18 16 19 14 12 14 14 12
31 30 24 26 26 16 22 20 16
61 52 48 55 48 44 51 48 40
96 94 80 88 82 76 85 76 72
151 138 132 130 124 112 130 120 112
187 176 168 151 148 132 163 152 144
241 232 224 206 196 184 216 214 196
313 302 292 270 266 252 288 282 264
396 384 352 336 334 312 358 350 340
482 472 456 418 416 396 450 436 416
568 554 536 506 492 472 526 506 484
792 780 752 704 700 660 724 720 696
1062 1030 1008 946 930 896 994 978 948
1356 1346 1304 1234 1220 1180 1288 1252 1220
Courtesy of Tubular Exchanger Manufacturers Association (TEMA ).
Heat Transfer 613
ID.C.B
a, = , ft 2 (8-39)
144. PT
(3) Mass velocity, G~ is"
o w lib /
a~ ftJihr (8-40)
Table 8-4
Tube Count for 5/8-in. OD Tubes on 7/8-in. D Pitch
Tube Count for sis-in. OD Tubes on 7/a-in. [] Pitch
TEMA TEMA TEMA TEMA
Type L or M Type P Type S Type U
Fixed Outside Packed Inside
Tubesheet Floating Head Floating Head U-Tube
Shell No. of Passes No. of Passes No. of Passes No. of Passes
ID in. 1 2 4 6 1 2 4 6 1 2 4 6 2 4 6
5.047 21 16 16 13 12 12 12 12 12
6.065 26 26 24 22 22 16 21 16 16
7.981 52 52 52 45 44 44 45 38 32
10.02 89 82 80 76 76 68 74 70 68
12.00 128 124 120 109 104 92 109 92 88
13.25 158 158 148 137 128 120 138 136 128
15.25 213 208 208 177 176 164 188 184 176
17.25 277 266 264 241 236 220 246 244 240
19.25 344 332 336 293 284 284 316 308 304
21.25 420 404 400 366 364 360 394 388 384
23.25 502 476 488 436 432 432 456 448 444
25.00
27.00 694 668 664 612 608 608 640 636 624
29.00
31.00 922 910 908 828 812 812 862 848 840
33.00
35.00 1181 1166 1160 1070 1064 1048 1122 1112 1100
Tube Count for a/4-in. OD Tubes on 1s/Is-in. A Pitch
TEMA TEMA TEMA TEMA
Type L or M Type P Type S Type U
Fixed Outside Packed Inside
Tubesheet Floating Head Floating Head U-Tube
Shell No. of Passes No. of Passes No. of Passes No. of Passes
ID in. 1 2 4 6 1 2 4 6 1 2 4 6 2 4 6 8
5.047 19 14 12 14 14 8 10 10 4 6 4
6.065 27 26 20 18 22 18 16 19 18 12 14 8
7.981 55 48 40 38 42 40 36 32 42 40 32 30 32 24
10.02 85 76 72 68 74 72 60 54 73 66 60 54 56 52
12.00 126 118 104 98 109 106 96 86 109 106 92 86 92 80
13.25 151 148 140 134 130 124 112 108 140 138 124 108 114 104
15.25 206 196 180 176 174 168 156 152 187 184 168 152 83 74
17.25 268 266 240 230 241 222 216 210 253 242 224 210 220 204
19.25 340 330 320 302 288 282 264 260 320 294 280 260 290 268
21.25 416 408 392 384 384 368 344 338 400 380 352 338 360 340
23.25 499 480 460 456 469 449 430 418 454 436 416 410 220 210
25.00 576 558 530 516 544 529 500 490 514 498 471 465 506 488
27.00 675 661 632 596 643 616 600 575 607 587 560 558 614 580
29.00 790 773 736 720 744 732 704 695 707 690 663 657 720 684
31.00 896 875 858 859 835 812 800 816 797 769 760 830 804
33.00 1018 1011 976 973 959 926 900 931 910 876 870 944 916
35.00 1166 1137 1098 1118 1093 1054 1010 1062 1039 998 993 1076 940
37.00 1307 1277 1242 1253 1224 1184 1150 1200 1177 1135 1124 1218 1184
39.00 1464 1425 1386 1392 1359 1318 1286 1341 1318 1282 1264 1366 1324
42.00 1688 1669 1618 1616 1602 1552 1482 1558 1554 1502 1482 1600 1552
45.00 1943 1912 1878 1870 1833 1800 1770 1875 1834 1736 1708 1854 1800
48.00 2229 2189 2134 2145 2107 2060 2025 2132 2100 1998 1964 2122 2064
51.00 2513 2489 2432 2411 2395 2344 2305 2431 2392 2286 2250 2410 2356
54.00 2823 2792 2752 2737 2683 2642 2612 2730 2684 2574 2536 2732 2668
60.00 3527 3477 3414 3400 3359 3294 3220 3395 3346 3228 3196 3398 3336
Courtesy of TEMA.
614 Fortran Programs for Chemical Process Design
(4) Shell velocity, V~, ft/s is"
W
V = (8-41)
3600. a~. p~
(5) Reynolds number, Re~, is"
Re~ -- D~. G+ (8-42)
~t
Table 8-5
Tube Count for 3/4-in, OD Tubes on 1-in. A Pitch
Tube Count for s/4-in. OD Tubes on 1-in. /~ Pitch
TEMA TEMA TEMA TEMA
Type L or M Type P Type S Type U
Fixed Outside Packed Inside
Tubesheet Floating Head Floating Head U-Tube
Shell No. of Passes No. of Passes No. of Passes No. of Passes
ID in. 1 2 4 6 1 2 4 6 1 2 4 6 2 4 6 8
5.047 14 14 12 10 10 8 10 10 4 6 4
6.065 22 20 16 22 19 18 16 19 14 12 10 8
7.981 42 40 36 40 38 36 32 28 37 32 28 26 28 24
10.02 73 72 64 64 64 62 60 58 61 60 48 46 56 44
12.00 109 86 80 98 96 94 84 78 96 94 80 78 86 72
13.25 139 134 124 122 121 110 100 98 121 118 104 98 106 96
15.25 187 180 168 164 151 146 140 138 163 164 144 140 148 136
17.25 241
232 220 212
208 196 188 160 216 214 196 158 200 184
19.25 296 290 280 270 258
242 232 230 276 270 260
235 254 240
21.25 372 354 344 330 320 316 296 298 338 338 324 300 314 300
23.25 434 420 404 404 380 372 364 335 396 396 376 339 388 368
25.00 507 489 476 482 475 466 452 430 460 440 420 414 452 432
27.00 604 594 568 582 530 526 508 495 558 554 536 494 538 524
29.00 689 679 660 672 653
642 620 610 624
605 589 581 632 612
31.00 808 804 772 724 696 688 669 756 744 716 669 732 708
33.00 906 891 860 859 848 818 805 818 797 783 771 838 808
35.00 1030 1026 1000 946 922 904 880 980 978 944 880 950 916
37.00 1152 1134 1090 1106 1081 1054 996 1047 1039 1001 996 1074 1040
39.00 1273 1259 1222 1218 1208 1174 1125 1172 1164 1130 1125 1200 1164
42.00 1485 1461 1434 1426 1399 1376 1306 1367 1350 1322 1306 1406 1364
45.00 1721 1693 1650 1652 1620 I586 1635 1608 1536 1504 1632 1584
48.00 1968 1941 1902 1894 1861 1820 1887 1842 1768 1740 1870 1832
51.00 2221 2187 2134 2142 2101 2060 2143 2104 2019 1992 2122 2076
54.00 2502 2465 2414 2417 2379 2326 2399 2366 2270 2244 2396 2340
60.00 3099 3069 3010 2990 2957 2906 2981 2940 2932 2800 2992 2936
Tube Count for a/4-in. OD Tubes on 1-in. [] Pitch
TEMA TEMA TEMA TEMA
Type L or M Type P Type S Type U
Fixed Outside Packed Inside
Tubesheet Floating Head Floating Head U-Tube
Shell No. of Passes No. of Passes No. of Passes No. of Passes
ID in. 1 2 4 6 1 2 4 6 1 2 4 6 2 4 6 8
5.047 12 12 12 12 12 4 9 8 4 6 4
6.065 21 16 16 16 16 12 16 16 12 8 8
7.981 38 38 32 37 32 32 12 32 32 32 12 24 20
10.02 61 60 52 57 56 52 24 56 52 52 24 44 40
12.00 97 90 88 89 82 76 56 89 82 80 56 68 68
13.25 117 116 112 97 94 88 80 104 104 96 80 90 88
15.25 158 158 148 137 128 120 114 145 140 140 114 128 120
17.25 216 208 188 177 176 164 160 188 184 180 160 176 168
19.25
262 256 244 224 216
208 198 238 236 232 198 112 108
21.25 316 316 308 274 270
268 260 304 292 284 260
138 134
23.25 370 372 368 333 332 316 308 344 332 332 308 340 332
25.00 442 432 428 414 406 392 344 398 386 366 344 400 388
27.00 524 524 500 464 456 448 424 484 472 468 424 472 460
29.00 602 596 580 570 562 548 496 554 532 510 496 554 544
31.00 698 692 688 628 620 612 576 650 648 640 576 640
624
Courtesy of TEMA.
Heat Transfer 615
(7) Prandtl number, Pr~, is:
pr s __ __ C~
k
(8) The heat transfer coefficient, h o, can be expressed as"
(8-43)
hO" DC
0.55 -,,0.33 )0.1
Table 8-6
Tube Count for 3/4-in. OD Tubes on 1-in. Fq Pitch
(8-44)
Tube Count for 3/4-in. OD Tubes on 1-in. [--1 Pitch
TEMA TEMA TEMA TEMA
Type L or M Type P Type S Type U
Fixed Outside Packed Inside
Tubesheet Floating Head Floating Head U-Tube
Shell No. of Passes No. of Passes No. of Passes No. of Passes
ID in. 1 2 4 6 1 2 4 6 1 2 4 6 2 4 6 8
33.00 782 768 768 742 732 732 668 730 712 682 668 724 720
35.00 894 892 880 816 812 804 760 848 828 824 760 836 812
37.00 1004 978 964 952 931 928 872 937 918 882 872 940 924
39.00 1102 1096 1076 1062 1045 1026 972 1048 1028 996 972 1048 1040
42.00 1283 1285 1270 1232 1222 1218 1140 1224 1200 1170 1140 1222 1204
45.00 1484 1472 1456 1424 1415 1386 1336 1421 1394 1350 1336 1420 1400
48.00 1701 1691 1670 1636 1634 1602 1536 1628 1598 1548 1536 1624 1604
51.00 1928 1904 1888 1845 1832 1818 1764 1862 1823 1779 1764 1852 1820
54.00 2154 2138 2106 2080 2066 2044 1992 2096 2048 2010 1992 2084 2064
60.00 2683 2650 2636 2582 2566 2556 2476 2585 2552 2512 2476 2596 2564
Tube Count for 3/4-in. OD Tubes on 1-in. 0 Pitch
TEMA TEMA TEMA TEMA
Type L or M Type P Type S Type U
Fixed Outside Packed Inside
Tubesheet Floating Head Floating Head U-Tube
Shell No. of Passes No. of Passes No. of Passes No. of Passes
ID in. 1 2 4 6 1 2 4 6 1 2 4 6 2 4 6 8
5.047 12 10 8 12 10 8 4 4
6.065 21 18 16 16 12 8 10 8
7.981 37 32 28 32 28 24 24 20
10.02 61 54 48 52 46 40 42 36
12.00 97 90 84 81 74 68 66 64
13.25 113 108 104 97 92 84 86 80
15.25 156 146 136 140 134 128 124 116
17.25 208 196 184 188 178 168 174 164
19.25 256 244 236 241 228 216 218 202
21.25 314 299 294 300 286 272 272 260
23.25 379 363 352 359 343 328 334 320
25.00 448 432 416 421 404 392 390 380
27.00 522 504 486 489 472 456 468 452
29.00 603 583 568 575 556 540 550 532
31.00 688 667 654 660 639 624 626 608
33.00 788 770 756 749 728 708 720 700
35.00 897 873 850 849 826 804 818 796
37.00 1009 983 958 952 928 908 928 904
39.00 1118 1092 1066 1068 1041 1016 1036 1016
42.00 1298 1269 1250 1238 1216 1196 1220 1192
45.00 1500 1470 1440 1432 1407 1378 1412 1384
48.00 1714 1681 1650 1644 1611 1580 804 788
51.00 1939 1903 1868 1864 1837 1804 1834 1804
54.00 2173 2135 2098 2098 2062 2026 2072 2036
60.00 2692 2651 2612 2600 2560 2520 2584 2544
Courtesy of TEMA.
616 Fortran Programs for Chemical Process Design
For turbulent flow, the viscosity ratio can be omitted, and Equation
8-44
becomes"
h o 0.36 k R o.55 prO.33
- e~ ~ (8-45)
D
Figure 8-11 shows the shell side heat transfer coefficient as a function
of the Reynolds number.
Table 8-7
Tube Count for 1-in. OD Tubes on 11/4-in.
A
Pitch
Tube Count for 1-in. OD Tubes on 1114-in. z3 Pitch
TEMA TEMA TEMA TEMA
Type L or M Type P Type S Type
U
Fixed Outside Packed Inside
Tubesheet Floating Head Floating Head U-Tube
Shell No. of Passes No. of Passes No. of Passes No. of Passes
ID in. 1 2 4 6 1 2 4 6 1 2 4 6 2 4 6 8
5.047 8 6 4 7 4 4 0 0
6.065 14 14 8 10 10 4 4 4
7.981 26 26 16 22 18 16 14 18 14 8 12 14 8
10.02 42 40 36 38 36 28 24 33 28 16 18 26 24
12.00 64 61 56 56 52 48 46 51 48 42 44 44 36
13.25 85 76 72 73 72 60 44 73 68 52 44 56 52
15.25 110 106
100 100
98 88 80 93 90 78 76 86 76
17.25 147 138 128 130 126 116 104 126 122 112 102 114 104
19.25 184 175 168 170 162 148 140 159 152 132 136 152 136
21.25 227 220 212 212 201 188 176 202 192 182 172 192 176
23.25 280 265 252 258 250 232 220 249 238 216 212 232 220
25.00 316 313 294 296 294 276 250 291 278 250 240 270 256
27.00 371 370 358 355 346 328 300 345 330 298 288 322 304
29.00 434 424 408 416 408 392 360 4.00 388 356 348 378 364
31.00 503 489 468 475 466 446 420 459 450 414 400 444 424
33.00 576 558 534 544 529 510 498 526 514 484 464 508 492
35.00 643 634 604 619 604 582 566 596 584 548 536 578 560
37.00 738 709 684 696 679 660 646 672 668 626 608 660 632
39.00 804 787 772 768 753 730 723 756 736 704 692 740 712
42.00 946 928 898 908 891 860 840 890 878 834 808 872 836
45.00 1087 1069 1042 1041 1017 990 968 1035 1008 966 948 1010 980
48.00 1240 1230 1198 1189 1182 1152 1132 1181 1162 1118 1092 1156 1124
51.00 1397 1389 1354 1348 1337 1300 1280 1350 1327 1277 1254 1322 1284
54.00 1592 1561 1530 1531 1503 1462 1440 1520 1492 1436 1416 1496 1452
60.00 1969 1945 1904 1906 1879 1842 1802 1884 1858 1800 1764 1866 1828
Tube Count for 1-in. OD Tubes on 11A-in. 0 Pitch
TEMA TEMA TEMA TEMA
Type L or M Type P Type S Type U
Fixed Outside Packed Inside
Tubesheet Floating Head Floating Head U-Tube
Shell No. of Passes No. of Passes No. of Passes No. of Passes
ID in. 1 2 4 6 1 2 4 6 1 2 4 6 2 4 6 8
5.047 8 6 4 5 4 4
6.065 12 10 8 12 10 8
7.981 24 20 16 21 18 16
10.02 37 32 28 32 32 28
12.00 57 53 48 52 46 40
13.25 70 70 64 61 58 56
15.25 97 90 84 89 82 76
17.25 129 120 112 113 112 104
19.25 162 152 142 148 138 128
21.25 205 193 184 180 174 168
23.25 238 228 220 221 210 200
25.00 275 264 256 261 248 236
27.00 330 315 300 308 296 286
29.00 379 363 360 359 345 336
31.00 436 422 410 418 401 388
0 0
4 4
10 8
24 10
36 32
50 44
70 64
96 88
124 120
156 152
200 188
232 220
282 268
330 320
382 368
Courtesy of TEMA.