Scambiatori di calore

C

C C C

C C C C

C

C C C C

C

C

C

C C C

C

C C

C

C C C C

C C

C

C C C

C

C

C C C C C

C C

C 1,1-Dimethylcyclohexane 1,2,4-Trimethylbenzene 1,3,5-Trimethylbenzene

1-Methylcyclopentene 2-Methyl-2-propanol glycol

Methylcyclopentane 2-Methyl-1-butanol

3-Methyl-1-butanol

Methylcyclohexane p-Isopropyltoluene

Ethylcyclopentane Isopropylbenzene

Ethylcyclohexane glycol

3 Propylbenzene

Vinylacetylene 1,2-Propylene

Ethylbenzene

Cyclopentene

Cyclopentane Cyclohexanol

Naphthalene m-Terphenyl

Cyclohexene

Cyclohexane 1-Heptanol

1-Propanol 2-Propanol 1-Pentanol

1-Heptyne 1-Hexanol

1-Butanol

2-Butanol

Methanol

1-Hexyne

2-Hexyne

3-Hexyne m-Xylene

1-Octyne m-Cresol

Ethylene

Biphenyl

p-Xylene

o-Xylene

Benzene p-Cresol

o-Cresol

Toluene Ethanol

Styrene Phenol 100

61 72 83

84

85

86

87 89

90 92

93

94

95 99

62 65 67

68

69 71 74

75

76 88 91 98

51 63

64 73 77

78 96

52

53

54

55

56 57

58

59

60 66 79

80 82 97

70 81 Project,

Prop-

max

1E−05 0.2965

0.6980 0.5966 0.9066

0.7960 1.3125 0.8939

1.5018

1.8101 1.3122 1.6603

0.7132 4.1847 4.9183

1.9909 6.4799

0.6574

0.7541

2.0467 2.3216

2.0142 1.3158 0.5119

0.6708

1.1880 0.7105

1.3391

1.3577 0.7843

1.8198 0.6395 0.8775

2.5809

0.5976

T

at Physical

p

C

× Hydrocarbon

533.15

319.99 401.15

239.12

305.37

495.08 653.15 292.67 298.85

319.67

308.85 303.15

206.45 for

, 4.6

max

K 40 98 142

112 552

360 32 290

115 370

150 132

300

429 135

400 200

420 185 350 Institute

T Center

min

1E−05 0.1087

0.3666 0.5541 0.5365

0.5593 0.7577 0.7615

1.3675

1.3617 0.1262 0.7827

0.5307 0.7575 0.6733

0.6229 0.5912

0.6711

0.7755

1.4960 1.0557

1.5195 0.9708 0.4288

0.4523

0.5424 0.7029

1.2337

1.1236 0.7747

1.4466 0.6215 0.8688

2.5809

0.5955 Design

T Research

at

p

C

× 1993,

Thermodynamics

24.56 54.36

63.15 161.11 273.16

239.99

227.95 13.95 203.15 187.68

68.15

172.12

293.15 245.25

274.69 189.79

83.78 259.83 197.67

303.15

185.15

, July,

2.2 109.5

265.9 182.3

min

K 58 220

75

286

200

230

200

280 165

T Release,

3.2129E+03

1.3841E+00 −3.3241E−03 2.7963E−03

7.4902E−03 2.0080E−06 9.3701E−06 .

c

T/T

Sponsor

C5 0

0 0 0

0 0 0

0 0

0

0

0 0

0 0 0

0

0 0

0

0 0

0 0 0

0

0 temperature,

Compounds,”

801

4.7333E−02

6.3483E−02 −4.2494E+04

4.7827E+02 1.1301E+00 −9.2382E−01

−2.2182E+00 6.0052E−01

−1.4520E−03

4.1616E−01 −2.6510E+03 −1.6230E+03 −1.4116E−02

1.8879E+00

−1.6255E+02 1.9596E+03 Project reduced

Related

C4 0

0

0 0

0 0 0

0

0 0

0

0 0

0 0 0

0

0 Properties, the

and is

Hydrocarbons r

T

−4.0669E+01

−5.3974E+01 −1.2363E+02 −1.3960E+02

−1.6230E−01

−6.7000E−01 −4.3333E+02

3.5800E−01 −1.0612E+02 2.1180E+05 1.1392E+02

2.4800E+02 4.8844E+01 5.6050E−01

−6.5259E+02

7.1540E+03

4.7218E−01 7.9940E+02

4.3379E−02 6.2970E−01 2.2493E+01 8.1250E+00

1.1043E+01 −8.4739E+02 3.8830E−01 Compound and

C3 )

0

0

0 0

0 0 0

0

0 r

T

specified.

−

(1

Pure

of =

t

Properties .

3.2280E+02

1.1734E+04

1.5338E+04

−9.4500E+00

1.1752E+02

2.1501E+02 −1.3877E+05 −2.2302E+02

−4.6557E+05 −6.1523E+03

−1.2281E+04 −2.4320E+04 −1.2200E+02

5.4373E+01

2.6660E+02

8.3496E+00 6.7659E+03 7.5299E+03

4.6350E+01

3.2850E+02 8.0925E+04

5.0929E+01 2.8723E+04

1.0437E+05 9.0000E+01 5.7443E+00

0.0000E+00

4.9354E+04 −2.0901E+03

9.1851E+03 −1.9894E+03 9.9000E+00

7.6602E+04 −1.9752E+02 5

of otherwise

)t

2/5

Compilation (C4

C2 −

of 4

as

C4/2)t

Values except

Data

) −1.0320E+04

−9.9120E+05

−1.3075E+06

9.6344E+04

6.9362E+04 1.2160E+05 3.8722E+05

1.0341E+06 6.2520E+04

6.7556E+04

7.0010E+04

1.1094E+05 6.6653E+01 −9.4585E+04

6.3936E+04

3.7570E+04

1.7543E+05

2.8197E+05

6.1289E+01

7.9815E+04 3.1322E+06

6.5429E+01

−8.3043E+06

8.5600E+04 4.7300E+04 8.5743E+04

2.5809E+05

6.4666E+01 2.7637E+05

−2.1446E+05 1.3439E+05 5.7720E+04

−2.9796E+06 9.5398E+04

(Concluded ×

“Selected (C3

used

Btu/(lbmol·°F).

DIPPR

C1 −

be

3

)t

should

2/3

Stebbins,

Center,

Liquids (C3

kmol-K. heating.

−

20.006

28.010 36.461 27.026

30.006 80.912

4.003 18.015

34.082

96.104 44.013

78.541

78.541 62.499 112.558

157.010

112.986

112.986 2.016 37.997

70.905

159.808

31.999

28.014

17.031

32.045 52.036 44.010

76.143 64.065

80.064

28.951 20.180

39.948

wt ,

4 2

=

T

C4)t

Research

Mol K.

J/

2.390059E−04

C. ×

Organic in C5 on

473

C. ×

are (C1 violently

+ data.

and above

7664393

630080 7647010 74908

10102439 10035106

7440597 7732185

7783064

462066 10024972

540545

75296 75014 108907

108861

78999

78875 1333740 7782414

7782505

7726956

7782447

7727379

7664417

302012 460195 124389

75150 7446095

7446119

132259100 7440019

7440371 3

capacities

Thermodynamics T

2-6a. −

Sibul, ×

CAS 1994). predicted

no.

and C3)t

C4 hypothetical decomposes

Table ×

+

M. ×

J/(kmol·K)

Inorganic (extant 2

heat C1

T

H.

in × on

Formula ×

2 2 C3

Br

Cl

Cl

Cl

Cl

Cl Cl Danner, liquid

order

F (2 based K.

HCN

4 Texas

7 7 6 6 3 5 5 5 2 are

H

3 O

HBr

O

H

H

H

H

H

H

H

H N HCl

2 +

from

S −

2 3

NH compound

2

NO HF

CO

CO

2 2.2

SO

SO

He 2

Ne CS

2 2 2

2 2 2

2

Br cal/(gmol·°C);

Ar

3 3 3 3 2 6 6 6 2

Cl

2 T

H

H C2

H

N N

N

O

C

C

C C

C C

C

C C

F alphabetical and

kelvins;

of × are below

Station,

and

P. +

C2

2)

Capacities 2) monomer

/t

R. and

2

(eqn. + capacity.

(eqn. C1

NY;

E., properties

C1

in hypothetical; hypothetical.

1,1-Dichloropropane

1,2-Dichloropropane hypothetical

College =

bromide

chloride expressed

fluoride

2) T.

cyanide York,

2) =

monoxide capacity

sulfide

2-Chloropropane

1-Chloropropane in

disulfide =

capacity

(eqn. Daubert,

(eqn.

Chlorobenzene

Bromobenzene dioxide

Fluorobenzene

Name the

2.390E−04

listed

trioxide heat

dioxide

chloride oxide New

Heat oxide University, for superfluid

Hydrazine

6 Hydrogen

Hydrogen Hydrogen

Hydrogen

Hydrogen

Hydrogen

Cyanogen

Ammonia

Helium-4 saturated

Nitrogen heat

Chlorine

Bromine

Fluorine are are are are

are

are

Nitrous

Oxygen Carbon

Carbon

Carbon heat

AIChE,

Sulfur

Sulfur

Argon from

Water

Nitric

Neon

Vinyl substances Temperatures is

2-196 Coefficients Coefficients

Coefficients

Coefficients

×

Air 1,

2

J/(kmol·K)

Compiled A&M Exhibits

Equation

Equation the

Data,

Cmpd. 2-174

TABLE For

204

205

203 208 223

199

200

198 215

216 224 231

206

207 209

210 212

213

214 217 221

222 229

219

220

201

202 218 225 230

211 226

227

228

no. Texas

All erty 1 2 3 4 5 6

844 PROCESS HEAT TRANSFER

TABLE I1. DiMENB1ONE OF S1 9E1. PIr IPS)

TSurfoce per lin tt, Weigh

Nominal Flow area /t.

in.chedule ID, in

OD, per pipe,

81ze, per lin f,

PRe No.

IPS, in. Outside Inside b atcel

In

0.405 40 0.209 058 0.070 25

006

80t 0.215 .036 9.32

056

0.540 104

40 0.364 ,14!

0. 0.005 43

80 0.

.072

0.302 54

0.079

0.675 40 0.192

0.493 0.1

177 .37

0.129

0.423

80t 0.111 0.74

.141

0.840 63

0.622

40* .304 85

0.

220

80 0.546 0.235 0.143

0.824

40 0.534 0.216

1.05 3

0.273

0.742

80 432 0. 94

.32 40 .049 0.274

0.344

0.864 .b8

80t 0.250

0.718 2.17

0.957

40

1.66

1 . 28

0.362

).436

1.380 50

80T 1,278 0.336 3.00

1.28

1 40

1.90 2.04

1.810 0.422

,498 3.

500

80t 0.393

76

2.38 40

2 022 66

2.067 3.35 ,542

.

80 1.9 0.508

2 40

2.88 2.469 647

4.70 0.753 .

80t 2:323 .67

0.609

3 3.50 0.91

40 .068 0.804

38

2

80t 8.8

900 . 780

4.

026 1178 055 0

4.5 80f .826 . 002

40

6.625 28. 590

. .065 1.734

5.761

80+ 28.6

26 1.10

7.

.625 981 2.258 2.090

7.825 2.000

10.75 78.8

40 2.814

10 2.82

10.02 ).5

60 74 2.55

9 .76 54

8

12 .75 115

30 12 09 338 43 8

138

14. 685

30 13.

26 3 3 o4,6

183

16.0 15.25 4.189

30 4.00 62.

234

17. .712 52

4

20

18 25

20 19.25 291

N

20 05

.236

21,225

20f 355 . .747 84 0

23.25

24.0 6.283 8

425

20 4 7

*Commonly kaown a standard.

1 Com monly koown Bs extra hesvy.

Approziuatoly. 2-95

2.591

2.268

4.878 3