NaturalConvectionHeatTransferCoefficients US Units Final Protected

8/12/2019 NaturalConvectionHeatTransferCoefficients US Units Final Protected

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Natural Convection Heat Transfer Coefficient Calcu

Click on tabs at the bottom of the screen to access the following:

Tab 1. Contents (current tab)

Tab 2. Fluid Properties - Set values of fluid properties for other wo

Tab 3. Vertical Plane

Tab 4. Horizontal Plane

Tab 5. Horizontal Cylinder

Workbook Contents


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lator - U.S. Customary Units

rksheets


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Fluid Viscosity Result: 8.076E-06 lbf-sec/ft 2 (from m

(This is the viscosity value that will be used in all of the other worksheets.)

0.43 Btu/lbm- oFTemperature Range ( oF): -139 to 440

oose er u

of the list in the menthis worksheet, if yo

Fluid Sp. Heat (Btu/lbm- oF) fluid properties obtai

Fluid Specific Heat Result: 0.43 Btu/lbm- oF (from m

Unit Conversion: 13.890 Btu/slug-oF

(This is the specific heat value that will be used in all of the other worksheets.)

0.0716 Btu/hr-ft- oF

Temperature Range ( oF):

Choose "Other Fluid


Fluid Th. Cond. (Btu/hr-ft- oF) fluid properties obtai

Fluid Thermal Conductivity 0.0716 Btu/hr-ft- oF (from m

Unit Conversion: 1.9879E-05 Btu/sec-ft-oF

(This is the thermal conductivity value that will be used in all of the other worksheets.)

Thermal Conductivity from above menu selection:

OR

Enter a Thermal Conductivity Obtained Elsewhere

T H E R M A L C O N D U C T I V I T Y

F L U

S P E C I F

I C H E A T

Specific Heat from above menu selection:

OR

Enter a Fluid Specific Heat Obtained Elsewhere


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6.432E-04 oR -1

Choose "Other Fluid


Thermal Exp Coeff ( oR -1) fluid properties obtai

Thermal Expansion Coeff: 6.432E-04 oR -1 (from m

(This is the thermal expansion coefficient value that will be used in all of the other work

DT = 0.2 r 1 =

T1 = 139.8 r 2 =

T2 = 140.2

The equations used to calculate the fluid properties in this worksheet are showThe source for these equations and the constants in the Lookup Table used tothe calculations came from:

Links to the tables for each fluid property are given at the top of the worksheet.

r = 0.062428(MW)(17.863 + 58.606 t 0.35 - 95.396 t 2/3 + 213.89 t - 141.2

T is in K t = 1 - T/647.096 r is in lbm/f

r = 0.062428(MW)(C1 + C2T + C3 T2 + C4 T3) T is in K r is in lb

The density of air is calculated with the Ideal Gas Law

m = 0.0209 exp[C1 + C2/T + C3(lnT) + C4(T C5 )] T is in K, m is in lbf-s/ft

Perry's Chemica l Engineers' Handbook, Ch. 2, Physical and Chemical Da

Density of liquids other than water:

Equations and References

T H E R M

E X P C O E F F

Viscosity of Liquids:

Density of water:

Thermal Exp. Coeff. from above menu selection:

OR

Enter a Thermal Expans. Coeff. Obtained Elsewhere
http://accessengineeringlibrary.com/browse/perrys-chemical-engineers-handbook-eighth-edition?utm_source=HT%20Coeff%20US&utm_medium=Excel&utm_content=Perrys%20Sec2&utm_campaign=FluidProphttp://accessengineeringlibrary.com/browse/perrys-chemical-engineers-handbook-eighth-edition?utm_source=HT%20Coeff%20US&utm_medium=Excel&utm_content=Perrys%20Sec2&utm_campaign=FluidProp


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m = 0.0209(C1T C2 )/(1 + C3/T) T is in K, m is in lbf-s/ft

Cp = {C1 + (C2[(C3/T)/sinh(C3/T)] 2 + C4[(C5/T)/cosh(C5/T)] 2}/28.9

T is in K Cp is in Btu/lbm- oF

Cp = (C1 - C2T + C3T 2 - C4T 3 + C5T 4)/18.015

T is in K Cp is in Btu/lbm- oF

k = 0.000239C1TC2/(1 - C3/T + C4/T 2) T is in K k is in Btu/hr-

k = 0.000239C1T C2 /(1 - C3/T + C4/T 2) T is in K k is in Btu/hr-

b = (1/V)dV/dT = (1/v)dv/dT = r d(1/ r )/dT ~ rD (1/ r )/DT = r [(1/r 2) - (1/ r 1)]/(T

T is in oR, b is in oR -1 The values of r come from the equations at the top of thi

The thermal expansion coefficient of air is calculated as b = 1/T, where T is in oR.

Thermal Conductivity of liquids

Specific Heat of Liquids:

Thermal Conductivity of Air

Viscosity of Air:

Specific Heat of Air:

Thermal Expansion Coefficient of Liquids


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The source for the data in the tables below used to calculate flui

Air Viscosity: Table 2-312

Air Specific Heat: Table 2-156

Air Thermal Cond.: Table 2-314

-139 to 606 0.8792 0.27136Calculations: 51.8839

Range, F c1 c2

1,1,2-Trichloroethane -33 to 624 0.9062 0.25475 (at the bottom 1,2-Butadiene -215 to 354 1.187 0.26114

t to enter fluid 1,2-Propylene glycol -76 to 666 1.0923 0.26106 lsewhere. 1,3-Butadiene -164 to 306 1.2346 0.27216

1-Butanol -128 to 554 0.98279 0.26831-Octanol 5 to 714 0.48979 0.24931

1-Propanol -195 to 507 1.2457 0.27281

2-Butanol -175 to 504 0.9682 0.262442-Octanol -23 to 675 0.50726 0.259722-Propanol -126 to 455 1.1799 0.2644

Acetic acid 63 to 604 1.4486 0.25892 Acetic anhydride -99 to 631 0.86852 0.25187

Acetone -139 to 455 1.2332 0.25886 Acetonitrile -47 to 523 1.3064 0.22597 Acrylic acid 55 to 648 1.2414 0.25822 Air 32 to 932 8.3145

enu selection) Benzene 43 to 552 1.0259 0.26666

Benzoic acid 252 to 892 0.71587 0.24812

Bromobenzene -24 to 747 0.8226 0.26632Butyl acetate -99 to 576 0.67794 0.2637Carbon disulfide -169 to 534 1.7968 0.28749

Carbon tetrachloride -9 to 541 0.99835 0.274

Chlorobenzene -49 to 678 0.8711 0.26805

Chloroform -81 to 505 1.0841 0.2581Chloromethane -144 to 298 1.817 0.25877Cumene -141 to 676 0.58711 0.25583

(at the bottom Cyclohexane 45 to 538 0.88998 0.27376

near the top of Cyclopentane -213 to 945 1.1035 0.27035 want to enter Decane -20 to 651 0.41084 0.25175 ned elsewhere. Dibutyl ether -144 to 592 0.55941 0.27243

Variables

Liquid V iscosity: Ta

Perry's Chemical Eng ineers' Handbook, Ch. 2, Physical and Chemi

Liquid Density: Ta

Liquid S p. Heat: Ta

only) es in
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Diethanol amine 84 to 867 0.68184 0.23796

enu selection) Diethyl ether -177 to 381 0.9554 0.26847

Dimethyl sulfoxide 66 to 853 1.1096 0.25189Diphenyl ether 81 to 921 0.52133 0.26218

Dodecane 16 to 725 0.33267 0.24664Ethanol -173 to 466 1.6288 0.27469Ethyl acetate -117 to 482 0.8996 0.25856Ethyl benzoate -31 to 797 0.48864 0.23894

Ethylene glycol 9 to 837 1.315 0.25125

Ethylenediamine 54 to 608 0.7842 0.20702

Fluorobenzene -44 to 549 1.0146 0.27277

Formamide 37 to 928 1.2486 0.20352

Heptane -130 to 512 0.61259 0.26211 a e o om Hexadecane 64 to 842 0.23289 0.23659

near the top of Hexane -139 to 455 0.70824 0.26411 want to enter Hydrazine 36 to 716 1.0516 0.16613 ned elsewhere. Isopropyl amine -139 to 390 1.2801 0.2828

Methacrylic acid 59 to 732 0.87025 0.24383

enu selection) Methanol -144 to 464 2.3267 0.27073

Methyl acetate -144 to 453 1.13 0.2593

Methyl methacrylate -54 to 559 0.7761 0.25068Methyl tert-butyl ether -162 to 435 0.928 0.289

Methylcyclohexane -233 to 570 0.73109 0.26971Methylethyl ketone -125 to 505 0.93767 0.25035

et y so uty etone - to . .

m-Xylene -54 to 651 0.68902 0.26086

Nonane -63 to 610 0.46321 0.25444

Octane -71 to 565 0.5266 0.25693

Octanoic acid 63 to 790 0.48251 0.25196

o-Xylene -13 to 675 0.69962 0.26143 (at the bottom Pentadecane 50 to 815 0.25142 0.23837

near the top of Pentane -202 to 387 0.84947 0.26726 want to enter Phenol 106 to 790 1.3798 0.31598 ned elsewhere. Phthalic anhydride 268 to 964 0.5393 0.22704

Propionic acid -6 to 622 1.0969 0.25568

enu selection) Propylbenzene -146 to 689 0.57233 0.25171

p-Xylene 55 to 649 0.67752 0.25887

Styrene -22 to 685 0.7397 0.2603

Tetrahydrofuran -162 to 513 1.2543 0.28084Toluene -139 to 606 0.8792 0.27136


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Triethyl amine -175 to 504 0.7035 0.27386

Undecane -13 to 691 0.36703 0.24876

Vinyl chloride -245 to 318 1.5115 0.2707

Water 32 to 176 -13.851 0.64038Other Fluid

(at the bottom

near the top of want to enter ned elsewhere.

enu selection)

sheets.)

51.89060 Preliminary calculations for calculating the thermal expansion coefficient b 51.87725 b = r d(1/ r )/dT ~ r (1/ r )/ T = r [(1/ r 2) - (1/ r 1)]/(T2 - T1)

n below. Copyright McGraw-Hill Global Education Holdings, LLC. All rigmake

.

6 t 4/3 )

3

/ft3

a


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ft-oF

ft-oF

- T1)

s section.


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density, viscosity, specific heat, and thermal conductivity are the tables itemized below fro

591.75 0.29241 92.138 -139 to 232 -226.08 6805.7 37.5428.076E-06

c3 c4 Mol. Weight Range, F c1 c2 c3

602 0.31 133.404 -33 to 237 0.388 736.5 -1.7063452 0.3065 54.09 -212 to 52 -10.143 472.79 -0.028241

626 0.20459 76.094 -76 to 442 -804.54 30487 130.79

425 0.28707 54.09 -9 to 261 17.844 -310.2 -4.5058563.1 0.25488 74.122 181 to 246 0.87669 1602.9 -2.1475652.3 0.27824 130.228 45 to 383 -19.907 2791.7 0.94296

536.8 0.23994 60.095 -195 to 207 23.467 116.07 -5.3372

535.9 0.26749 74.122 -175 to 212 -16.323 3141.7629.8 0.22 130.228 -26 to 356 16.792 1353.6 -4.6357508.3 0.24653 60.095 -126 to 180 -8.8918 2357.6 -0.91376

591.95 0.2529 60.052 63 to 244 -9.03 1212.3 -0.322

606 0.31172 102.09 -81 to 284 -14.164 1350.3 0.4492

508.2 0.2913 58.079 -117 to 133 -14.918 1023.4 0.5961545.5 0.28678 41.052 -47 to 325 -10.906 872.02615 0.30701 72.063 55 to 369 -28.12 2280.2 2.3956

28.96 -315 to 3141 1.425E-06 0.5039 108.3

562.05 0.28394 78.112 43 to 522 7.5117 294.68 -2.794

752 0.2857 122.121 253 to 621 -12.947 2557.9

670.15 0.2821 157.008 -24 to 313 -20.611 1656.5 1.4415575.4 0.29318 116.16 -9 to 259 -17.488 1478.2 0.91828552 0.3226 76.141 -168 to 336 -10.306 703.01

556.35 0.287 153.823 -9 to 360 -8.0738 1121.1 -0.4726

632.35 0.2799 112.557 -9 to 513 0.15772 540.5 -1.6075

536.4 0.2741 119.378 - 81 to 176 -14.109 1049.2 0.5377416.25 0.2833 50.488 -144 to 266 -25.132 1381.9 2.0811

631 0.28498 120.192 -99 to 261 -24.988 1807.9 2.0556

553.8 0.28571 84.159 45 to 338 -33.763 2497.2 3.2236

507 0.28699 70.133 -54 to 126 -3.2612 614.16 -1.156617.7 0.28571 142.282 21 to 118 -10.115 1111.9 -0.015659

584.1 0.29932 130.228 -144 to 286 10.027 206 -3.1607

Excel Vlookup results based on selected fluid:

or Density Calculations: Variables for Viscosity

le 2-313

cal Data

Liquid The rmal Conductivity: Table 2-315

le 2-32

le 2-153
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736.6 0.2062 105.136 68 to 601 -375.21 17177 66.66

466.7 0.2814 74.122 163 to 212 10.197 -63.8 -3.226

729 0.3311 78.133 66 to 376 -37.347 2835 3.7937766.8 0.31033 170.207 68 to 644 -12.373 2017.5

658 0.28571 170.335 12 to 487 -7.8244 1191.9 -0.49963514 0.23178 46.068 -99 to 333 7.875 781.98 -3.0418523.3 0.278 88.105 -63 to 392 14.354 -154.6 -3.7887698 0.28421 150.175 -9 to 417 -40.706 3035 4.2655

720 0.21868 62.068 9 to 577 -20.515 2468.5 1.2435

593 0.20254 43.068 52 to 410 -53.908 4030.8 5.9704

560.09 0.28291 96.102 - 42 to 356 -10.064 1058.7 -0.17162

771 0.25178 45.041 32 to 428 40.153 -912.39 -7.5664

540.2 0.28141 100.202 -135 to 318 -9.4622 877.07 -0.23445723 0.28571 226.441 64 to 556 -20.182 2203.5 1.2289

507.6 0.27537 86.175 -144 to 271 -6.3276 640 -0.694653.15 0.1898 32.045 34 to 482 -75.781 4175.4 9.6508

471.85 0.2972 59.11 -9 to 356 -31.157 1926 2.925

662 0.28571 86.089 59 to 322 -14.527 1497.7 0.51747

512.5 0.24713 32.042 -144 to 149 -25.317 1789.2 2.069

506.55 0.2764 74.079 -9 to 306 13.557 -187.3 -3.6592

566 0.29773 100.116 9 to 261 -0.099 496 -1.5939497.1 0.286 88.148 -162 to 351 -6.921 790.773 -0.654

572.1 0.29185 98.186 -195 to 365 -11.358 1213.1535.5 0.29984 72.106 -125 to 505 -1.0598 520.68 -1.4961

. . . - to - . . - .

617 0.27479 106.165 -54 to 284 -11.91 1094.9 0.13825

594.6 0.28571 128.255 -67 to 608 -68.54 3165.3 9.0919

568.7 0.28571 114.229 -80 to 360 -7.556 881.09 -0.52502

694.26 0.26842 144.211 63 to 464 -60.795 4617.8 7.028

630.3 0.27365 106.165 -13 to 293 -15.489 1393.5 0.63711708 0.28571 212.415 50 to 520 -19.299 2088.6 1.1091

469.7 0.27789 72.149 -202 to 378 -53.509 1836.6 7.1409694.25 0.32768 94.111 64 to 540 -43.335 3881.7 4.3983

791 0.248 148.116 268 to 545 195.25 -11072 -29.084

600.81 0.26857 74.079 -6 to 286 -23.932 1834.6 1.9124

638.35 0.29616 120.192 -99 to 318 -18.282 1549.7 1.0454

616.2 0.27596 106.165 55 to 284 -7.381 911.7 -0.54152

636 0.3009 104.149 -22 to 293 -22.675 1758 1.6701

540.15 0.2912 72.106 -162 to 212 -10.321 900.92 -0.069128591.75 0.29241 92.138 -139 to 232 -226.08 6805.7 37.542


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:

-0.060853 1 -139 to 440 140140 -152.3 0.695 0 04.317E-01

c4 c5 Range, F c1 c2 c3 c4 c5

-33 to 81 103350 159.3 -213 to 63 135150 -311.14 0.97007 -0.00015

-0.15449 1 -76 to 370 58080 445.2

-162 to 171 128860 -323.1 1.015 0.0000323.387E+22 -9.9231 -128 to 244 191200 -730.4 2.29982.304E+24 -10.09 -9 to 381 571370 -4849 19.725 -0.02155

2.88E+09 -4.0267 -195 to 261 158760 -635 1.969

-175 to 210 426790 -3694.6 13.828 -0.01352.666E+31 -13.039 -126 to 356 319198 -1042.21 3.52943

-195 to 180 471710 -4172.1 14.745 -0.014463 to 244 139640 -320.8 0.8985

-9 to 171 36600 511

-139 to 133 135600 -177 0.2837 0.000689 -47 to 179 97582 -122.2 0.3408555 to 215 55300 300

-279 to 252 28958 9390 3012 7580 1484

42 to 176 129440 -169.5 0.64781

252 to 350 -5480 647.12

68 to 431 121600 -9.45 0.358 77 to 259 111850 384.52

-170 to 534 85600 -122 0.5605 -0.00145 2.01E-06

-9 to 240 -752700 8966.1 -30.394 0.034455

-49 to 188 -1307500 15338 -53.974 0.063483

- 40 to 200 124850 -166.34 0.43209-4.5E-27 10 -144 to 212 96910 -207.9 0.37456 0.000488

-141 to 306 61723 494.81

44 to 260 -220600 3118.3 -9.4216 0.010687

-177 to 368 122530 -403.8 1.7344 -0.0011 -21 to 368 278620 -197.91 1.0737

-144 to 350 270720 -259.83 0.95427

Variables for Specific Heat Calculations: alculations:


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-3.6367 0.5 82 to 515 184200 286

163 to 212 44400 1301 -5.5 0.008763

65 to 320 240300 -595 1013 80 to 566 134160 447.67

3.957E+23 -10 15 to 134 508210 -1368.7 3.1015 -173 to 242 102640 -139.63 -0.03034 0.00203 -118 to 272 226230 -624.8 1.472 -30 to 416 124500 370.6

2.5E+12 -5 9 to 428 35540 436.78 -0.18486

52 to 243 184440 -150.2 0.37044

- 28 to 116 -21 11734 -40669 0.047333

1.687E+24 -10 65 to 428 63400 150.6

1.402E+22 -10 -131 to 476 61.26 314410 1824.6 -2547.9 -10 65 to 548 370350 231.47 0.68632

5.688E+21 -10 -140 to 368 172120 -183.78 0.88734-7.27E-09 3 35 to 716 79815 50.929 0.043379

-139 to 116 -32469 1977.1 -7.0145 0.008691

59 to 322 146290 -58.59 0.3582

-144 to 260 105800 -362.23 0.9379

-4 to 212 61260 270.9

-55 to 213 255100 -938.4 2413 -164 to 131 134300 94.356 -0.0032 0.00098

-196 to 116 131340 -63.1 0.8125 -124 to 212 132300 200.87 -0.9597 0.001953 - to - . .

-69 to 513 133860 78754 0.52265

-64 to 125 383080 -1139.8 2.7101

4.634E+22 -10 -70 to 368 224830 -186.63 0.95891

62 to 463 205260 44.392 0.8956

-13 to 292 36500 1017.5 -2.63 0.00302 50 to 519 346910 219.54 0.65632

-1.96E-05 2 -202 to 242 159080 -270.5 0.995373.055E+24 -10 106 to 305 101720 317.61

268 to 545 145400 252.4

-5 to 286 213660 -702.7 1.6605

-147 to 319 174380 -101.8 0.79

56 to 620 -35500 1287.2 -2.599 0.002426

-23 to 293 113340 290.2 -0.6051 0.001357

-163 to 151 171730 -800.47 2.8934 -0.0025-0.060853 1 -139 to 440 140140 -152.3 0.695


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-100 to 192 111480 368.13

570980 -2 -14 to 320 293980 -114.98 0.96936

-100 to 260 -10320 322.8

-5.879E-29 10 32 to 500 276370 -2090.1 8.125 -0.01412 9.37E-06


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Parameters for Heptane Specific Heat Calculation:

T in K

333.2

t for heptane

0.38328

-139 to 396 0.20463 -0.00024252 0 07.156E-02Range, F c1 c2 c3 c4

1,1,2-Trichloroethane -34 to 408 0.20731 -2.4997E-041,2-Butadiene -213 to 52 0.21966 -3.436E-04

1,2-Propylene glycol -76 to 1341 0.214 -1.834E-04

1,3-Butadiene -164 to 25 0.22231 -3.664E-041-Butanol -128 to 246 0.2136 -2.034E-041-Octanol 5 to 1341 0.214 -1.834E-04

1-Propanol -99 to 1341 0.214 -1.834E-04

2-Butanol -175 to 212 0.22787 -3.0727E-042-Octanol -26 to 1341 0.214 -1.834E-042-Propanol -123 to 1341 0.214 -1.834E-04

Acetic acid 63 to 244 0.214 -1.834E-04 Acetic anhydride -99 to 284 0.23638 -2.4263E-04

Acetone -139 to 158 0.2878 -4.27E-04 Acetonitrile -47 to 55 0.33192 -4.3243E-04 Acrylic acid 55 to 412 0.24410 -2.904E-01 Air -333 to 3141 3.1417E-04 0.7786 -0.7116 2121.7

Benzene 43 to 284 0.23444 -3.0572E-04

Benzoic acid 252 to 613 0.2391 -2.325E-04

Bromobenzene -24 to 426 0.16983 -1.981E-04Butyl acetate -99 to 358 0.21721 -2.6563E-04Carbon disulfide -170 to 115 0.2333 -2.75E-04

Carbon tetrachloride -9 to 171 0.1589 -1.987E-04

Chlorobenzene -49 to 270 0.1841 -1.917E-04

Chloroform - 83 to 261 0.1778 -2.023E-04Chloromethane -144 to 171 0.41067 -8.478E-04Cumene -141 to 284 0.1855 -2.0895E-04

Cyclohexane 45 to 178 0.19813 -2.505E-04

Cyclopentane -137 to 345 0.2066 -2.696E-04Decane -22 to 345 0.2063 -2.5E-04

Dibutyl ether -144 to 482 0.19418 -2.2246E-04

Variables for Thermal Conductivity Calculations:


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Diethanol amine 82 to 752 0.0218 1.0315E-03 -1.355E-06

Diethyl ether -177 to 320 0.2495 -4.07E-04

Dimethyl sulfoxide 81 to 496 0.3142 -3.0809E-04Diphenyl ether 81 to 496 0.18686 -1.4953E-04

Dodecane 14 to 421 0.2047 -2.326E-04Ethanol -173 to 176 0.2468 -2.64E-04Ethyl acetate -119 to 171 0.2501 -3.563E-04Ethyl benzoate -31 to 529 0.20771 -2.1265E-04

Ethylene glycol 9 to 387 0.088067 9.4712E-04

Ethylenediamine 52 to 243 0.36434 -4.433E-04

Fluorobenzene - 31 to 176 0.20962 -2.8034E-04

Formamide 37 to 428 0.38470 -1.065E-04

Heptane -132 to 210 0.21500 -3.03E-04Hexadecane 64 to 549 0.20749 -2.1917E-04

Hexane -139 to 207 0.22492 -3.533E-04Hydrazine 36 to 662 1.3675 -1.5895E-03

Isopropyl amine -139 to 90 0.237 -3.320E-04

Methacrylic acid 59 to 495 0.2306 -2.5201E-04

Methanol -144 to 149 0.2837 -2.81E-04

Methyl acetate -144 to 235 0.2777 -4.17E-04

Methyl methacrylate 63 to 194 0.2583 -3.79E-04Methyl tert-butyl ether -164 to 131 0.2253 -3.7273E-04 1.173E-07

Methylcyclohexane 32 to 214 0.1791 -2.291E-04Methylethyl ketone -125 to 176 0.2197 -2.505E-04

et y so uty etone - to . - . -

m-Xylene -54 to 284 0.20044 -2.3544E-04

Nonane -63 to 304 0.209 -2.64E-04

Octane -71 to 259 0.2156 -2.9483E-04

Octanoic acid 63 to 464 0.203 -2E-04

o-Xylene -13 to 291 0.19989 -2.299E-04Pentadecane 50 to 520 0.20649 -2.1911E-04

Pentane -202 to 342 0.2537 -5.76E-04 3.44E-07Phenol 106 to 360 0.18831 -1E-04

Phthalic anhydride 268 to 545 0.2295 -2.1345E-04

Propionic acid -6 to 518 0.1954 -1.64E-04

Propylbenzene -148 to 590 0.18707 -1.9846E-04

p-Xylene 54 to 284 0.20003 -2.3573E-04

Styrene -24 to 293 0.20215 -2.201E-04

Tetrahydrofuran -162 to 151 0.19428 -2.49E-04Toluene -139 to 396 0.20463 -2.4252E-04


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Triethyl amine -175 to 410 0.1918 -2.453E-04

Undecane -15 to 385 0.20515 -2.3933E-04

Vinyl chloride -245 to 162 0.2333 -3.92E-04

Water 32 to 680 -0.4320 5.73E-03 -8.08E-06 1.861E-09


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-139 606 -139 232 -139 440 -139 396

-33 624 -33 237 -33 81 -34 408-215 354 -212 52 -213 63 -213 52

-76 666 -76 442 -76 370 -76 1341

-164 306 -9 261 -162 171 -164 25-128 554 181 246 -128 244 -128 246

5 714 45 383 -9 381 5 1341

-195 507 -195 207 -195 261 -99 1341

-175 504 -175 212 -175 210 -175 212-23 675 -26 356 -126 356 -26 1341

-126 455 -126 180 -195 180 -123 134163 604 63 244 63 244 63 244-99 631 -81 284 -9 171 -99 284

-139 455 -117 133 -139 133 -139 158-47 523 -47 325 -47 179 -47 5555 648 55 369 55 215 55 41232 932 -315 3141 -279 252 -333 3141

43 552 43 522 43 176 43 284

252 892 253 621 252 350 252 613

-24 747 -24 313 68 431 -24 426-99 576 -9 259 77 259 -99 358

-169 534 -168 336 -170 534 -170 115

-9 541 -9 360 -9 240 -9 171

-49 678 -9 513 -49 188 -49 270

-81 505 -81 176 -40 200 -83 261-144 298 -144 266 -144 212 -144 171-141 676 -99 261 -141 306 -141 284

45 538 45 338 44 260 45 178

-213 945 -54 126 -177 368 -137 345-20 651 21 118 -21 368 -22 345

-144 592 -144 286 -144 350 -144 482

Limits of Temperature Range ( oF)

Specific Heat Thermal ConductivityDensity Viscosity


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84 867 68 601 82 515 82 752

-177 381 163 212 163 212 -177 320

66 853 66 376 65 320 66 37681 921 68 644 80 566 81 496

16 725 12 487 15 134 14 421-173 466 -99 333 -173 242 -173 176-117 482 -63 392 -118 272 -119 171-31 797 -9 417 -30 416 -31 529

9 837 9 577 9 428 9 387

54 608 52 410 52 243 52 243

-44 549 -42 356 -28 116 -31 176

37 928 32 428 65 428 37 428

-130 512 -135 318 -131 476 -132 21064 842 64 556 65 548 64 549

-139 455 -144 271 -140 368 -139 20736 716 34 482 35 716 36 662

-139 390 -9 356 -139 116 -139 90

59 732 59 322 59 322 59 495

-144 464 -144 149 -144 260 -144 149 x

-144 453 -9 306 -4 212 -144 235

-54 559 9 261 -55 213 63 194-162 435 -162 351 -164 131 -164 131

-233 570 -195 365 -196 116 32 214-125 505 -125 505 -124 212 -125 176- - - -

-54 651 -54 284 -69 513 -54 284

-63 610 -67 608 -64 125 -63 304

-71 565 -80 360 -70 368 -71 259

63 790 63 464 62 463 63 464

-13 675 -13 293 -13 292 -13 29150 815 50 520 50 519 50 520

-202 387 -202 378 -202 242 -202 342106 790 64 540 106 305 106 360

268 964 268 545 268 545 268 545

-6 622 -6 286 -5 286 -6 518

-146 689 -99 318 -147 319 -148 590

55 649 55 284 56 620 54 284

-22 685 -22 293 -23 293 -24 293

-162 513 -162 212 -163 151 -162 151-139 606 -139 232 -139 440 -139 396


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-175 504 -9 187 -100 192 -175 410

-13 691 -13 460 -14 320 -15 385

-245 318 -225 261 -100 260 -245 162

32 176 32 703 32 500 32 680


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Natural Convection Heat Transfer Coefficient Correlations

Height of Surface, L = 1.50 ft

Preliminary Calculations:

Temperature Diff, T = 70 oF

Prandtl Number, Pr = 5.643

Grashof Number, Gr = 1.949.E+11

Rayleigh Number, Ra = 1.100E+12

NOTE: Go to the Fluid Properties worksheet to change fluid

temperature, surface temperature, or fluid pressure values

Nusselt Number, Nu = 1413.7

Convective H.T. Coeff., h = 67.4 Btu/hr-ft 2-oF

Copyright McGraw-Hill Global Education Holdings, LLC. All rights reserved.

Enter the indicated input data:

P R E L I M

. C A L C U L A T I O N S

Heat Transfer Coefficient Calculation

H . T .

C O E F F

.

Natural Convection from an Isothermal Vertical Plane - (U.S. units)

(Enter Values in yellow cells only)


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The definitions of the dimensionless numbers and the correlation used for Nusselt number are shown

below. For more discussion of natural convection and correlations for Nusselt No., see:

Perry's Chemical Engin eer's Handbook, 8th Ed. - Sect 5.3.2 Natural Convection

Discussion and References
http://accessengineeringlibrary.com/browse/perrys-chemical-engineers-handbook-eighth-edition/p200139d899705_7001?utm_source=HT%20Coeff%20US&utm_medium=Excel&utm_content=Perrys%205.3.2&utm_campaign=Verticalhttp://accessengineeringlibrary.com/browse/perrys-chemical-engineers-handbook-eighth-edition/p200139d899705_7001?utm_source=HT%20Coeff%20US&utm_medium=Excel&utm_content=Perrys%205.3.2&utm_campaign=Vertical


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Area of Plate, A = 0.50 ft2

Perimeter of Plate, P = 3.60 ft



Char. Length, L = A/P = 0.139






Case I: H.T. from upper surface of hot plate or from

lower surface of cool plate.

A. for 10 < Ra < 10 :


Natural Convection Heat Transfer Coefficient Correla

Natural Convection from an Isothermal Horizontal Plane - (U.S.



P R E L I M


Heat Transfer Coefficient Calculation

F F I C I E N T


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B. for 10 7 < Ra < 10 11 :



Case II: H.T. from upper surface of cool plate or from lower surface of hot plate. ( for 10 5 < Ra < 10 10 ):


Convective H.T. Coeff.,h

=0.59

Btu/hr-ft 2-oF

Copyright McGraw-Hill Global Education Holdings, LLC. All rights r

H E A T T R A N S F

E R C O


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The definitions of the dimensionless numbers and the correlations used for Nusselshown below. For more discussion of natural convection and correlations for Nus

Correlation #1: (for heat transfer from the upper surface of a hot plate to a cooleor from the lower surface of a cool plate to a warmer fluid below it)

Nu = 0.54 Ra 1/4 ( 10 4 < Ra < 10 7 )

Nu = 0.15 Ra ( 10 < Ra < 10 )

Correlation #2: (for heat transfer from the upper surface of a cool plate to a war

or from the lower surface of a warm plate to a cooler fluid below it)

Nu = 0.27 Ra 1/4 ( 10 5 < Ra < 10 10 )

ions

units)


Perry's Chemical E ngineer's Handbook, 8th Ed. - Sect 5.3.2 Natural Convection
http://accessengineeringlibrary.com/browse/perrys-chemical-engineers-handbook-eighth-edition/p200139d899705_7001?utm_source=HT%20Coeff%20US&utm_medium=Excel&utm_content=Perrys%205.3.2&utm_campaign=HorizPlanehttp://accessengineeringlibrary.com/browse/perrys-chemical-engineers-handbook-eighth-edition/p200139d899705_7001?utm_source=HT%20Coeff%20US&utm_medium=Excel&utm_content=Perrys%205.3.2&utm_campaign=HorizPlane


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eserved.


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t number areelt No., see:

fluid above it

er fluid above it


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Natural Convection Heat Transfer Coefficient Correlations

Pipe Diameter, D = 2.00 ft










Natural Convection from an Isothermal Horizontal Cylinder - (U.S. units)



P R E L I M


H . T . C

O E F F

.Heat Transfer Coefficient Calculation


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Copyright McGraw-Hill Global Education Holdings, LLC. All rights reserve


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Initial estimate of f #REF!

1st iteration with Colbrook; #REF!2nd iteration with Colbrook; #REF!3rd iteration with Colbrook; #REF!4th iteration with Colbrook; #REF!5th iteration with Colbrook; #REF!6th iteration with Colbrook; #REF!7th iteration with Colbrook; #REF!8th iteration with Colbrook; #REF!9th iteration with Colbrook; #REF!10th iteration with Colbrook; #REF!11th iteration with Colbrook; #REF!12th iteration with Colbrook; #REF!

Churchill Equation

Colebrook Equation


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The definitions of the dimensionless numbers and the correlation used for Nusselt number are shown below. For more discussion of natural convection and correlations for Nusselt No., see:


Perry's Chemical Engine er's Handbook, 8th Ed. - Sect 5.3.2 Natural Convection
http://accessengineeringlibrary.com/browse/perrys-chemical-engineers-handbook-eighth-edition/p200139d899705_7001?utm_source=HT%20Coeff%20US&utm_medium=Excel&utm_content=Perrys%205.3.2&utm_campaign=HorizPlanehttp://accessengineeringlibrary.com/browse/perrys-chemical-engineers-handbook-eighth-edition/p200139d899705_7001?utm_source=HT%20Coeff%20US&utm_medium=Excel&utm_content=Perrys%205.3.2&utm_campaign=HorizPlane


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