1era lista -transf de masa ii

7/28/2019 1era Lista -Transf de Masa II

1/34

KN/m2

(mm.Hg) C5H12 C6H14

1.3 10 223.1 248.2

2.6 20 233 259.1

5.3 40 244 276.98 60 251 279

13.3 100 260.6 289

26.6 200 275.1 304.8

53.2 400 291.7 322.8

101.3 760 309.3 341.9

curvas de Presiones

DESTILACION

Presin de vapor Temperatura (K)

y = 0.0001x3 - 0.0893x2 + 22.5358x - 1,904.7182

R = 0.9996

80

90

100

110


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n-pentano

KN/m2

mmHg t t2

t3

1.3 10 223.1 49773.61 11104492.39

2.6 20 233 54289 12649337

5.3 40 244 59536 14526784

8 60 251 63001 15813251

13.3 100 260.6 67912.36 17697961.02

26.6 200 275.1 75680.01 20819570.75

53.2 400 291.7 85088.89 24820429.21

101.3 760 309.3 95666.49 29589645.36

Hallando la presin de vapor a su respectivo intervalo de temperatura

P= 8.0 KN/m2

T Pentano PA T Pentano PA

251 8 291.7 53.2

256 10.271215 297.7 67.39312987

261 13.2851302 303.7 83.62205409

266 17.0810121 309.7 102.5077505

271 21.7833354 315.7 124.2653114

276 27.5165748 321.7 149.109829

279 31.5031396 322.8 154.0164865

P=53.2 KN/m2

Presion de vapor Temperatura K

* Con analisis de Datos para el n-Pentano

y = 0.0002x3 - 0.1143x2 + 26.4305x - 2,048.8115

R = 0.9999

0

10

20

30

40

50

60

0 50 100 150 200 250 300 350


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* Con analis de datos para el n-Hexano

KN/m2 mmHg t t2 t3

1.3 10 248.2 61603.2400 15289924.1680

2.6 20 259.1 67132.8100 17394111.07105.3 40 276.9 76673.6100 21230922.6090

8 60 279 77841.0000 21717639.0000

13.3 100 289 83521.0000 24137569.0000

26.6 200 304.8 92903.0400 28316846.5920

53.2 400 322.8 104199.8400 33635708.3520

101.3 760 341.9 116895.6100 39966609.0590

Hallando la Presion de Vapor a su respectivo intervalo de Temperatura

P=8 KN/m2 P=53.2KN/m2

T Hexano PB T Hexano PB

251 1.3 291.7 14.3255

256 2.14186363 297.7 19.10386709

261 2.84052104 303.7 25.07509818

266 3.71514691 309.7 32.39274145

271 4.8546218 315.7 41.21038251

276 6.34782627 321.7 51.68160697

279 8 322.49 53.19164288

XA= (PT-PB)/(PA-PB

P= 8 YB= PA.XA/PT

T PA PB XA YA X=Y

251 8 1.3 1 1 1

256 10.271215 2.14186363 0.72061547 0.925199555 0.72061547

261 13.2851302 2.84052104 0.49398487 0.820331674 0.49398487

266 17.0810121 3.71514691 0.3205818 0.684482695 0.3205818

271 21.7833354 4.8546218 0.18580137 0.505921699 0.18580137

276 27.5165748 6.34782627 0.07804778 0.268450932 0.07804778

279 31.5031396 8 0 0 0

a.4 Hallar el equilibrio liquido-vapor

Presin de Vapor Temperatura


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Curva de equlibrio Liquido-Vapor X-Y*

XA= (PT-PB)/(PA-PB

P= 53.2 YB= PA.XA/PT

T PA PB XA YA* X=Y

291.7 53.2 14.3255 1.00 1.00 1.00297.7 67.3931299 19.1038671 0.71 0.89 0.71

303.7 83.6220541 25.0750982 0.48 0.76 0.48

309.7 102.50775 32.3927414 0.30 0.57 0.30

315.7 124.265311 41.2103825 0.14 0.34 0.14

321.7 149.109829 51.681607 0.02 0.04 0.02

322.5 154.016486 53.1916429 0.00 0.00 0.00

Curva de equilibrio Liquido-Vapor X-Y*

0

0.1

0.2

0.3

0.4

0.5

0.6

0.7

0.8

0.9

1

0 0.1 0.2 0.3 0.4 0.5 0.6 0.7 0.8 0.9 1

Series1

x y

0.

0.

0.

0.

0.

0.

0.

0.

0.

0.90

1.00


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B. PARA CADA PRESION, CALCULE LAS VOLATILIDADES RELATIVAS Y DETERMINE SU VA

volatilidad PA/PB

P= 8

PA PB Volatilidad x y

8 1.3 6.15384615 0 0.0000

10.271215 2.14186363 4.79545703 0.1 0.3436

13.2851302 2.84052104 4.67700469 0.2 0.540917.0810121 3.71514691 4.59766802 0.3 0.6688

21.7833354 4.8546218 4.48713336 0.4 0.7585

27.5165748 6.34782627 4.33480276 0.5 0.8249

31.5031396 8 3.93789245 0.6 0.8761

promedio 4.71197207 0.7 0.9166

0.8 0.9496

0.9 0.9770

1 1.0000

0.00

0.10

0.20

0.30

0.40

0.50

0.60

0.70

0.80

0.00 0.10 0.20 0.30 0.40 0.50 0.60 0.70 0.80 0.90 1.00

X-Y*

X=Y


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Resumen

Estadsticas de la regresin

Coeficiente d 0.99996911


R^2 ajustado 0.99989189

Error tpico 0.36190279Observacione 8

ANLISIS DE VARIANZA

Grados de libert a de cuadra dio de los cua F alor crtico de

Regresin 3 8479.57611 2826.52537 21580.8742 7.1561E-09

Residuos 4 0.52389451 0.13097363

Total 7 8480.1

Coeficientes Error tpico Estadstico t Probabilidad Inferior 95%

Intercepcin -2048.81147 146.69935 -13.9660569 0.00015246 -2456.11416

Variable X 1 26.4304647 1.67606591 15.7693469 9.4481E-05 21.7769597

Variable X 2 -0.11431226 0.00634625 -18.0125799 5.5844E-05 -0.13193226

Variable X 3 0.00016597 7.9628E-06 20.8428031 3.1311E-05 0.00014386

C5H12

C6H14


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Resumen

Estadsticas de la regresinCoeficiente d 0.99980884


R^2 ajustado 0.999331

Error tpico 0.9002534

Observacione 8

ANLISIS DE VARIANZA


Regresin 3 8476.85818 2825.61939 3486.45548 2.7398E-07

Residuos 4 3.24182472 0.81045618

Total 7 8480.1


Intercepcin -1904.71817 392.900128 -4.8478431 0.00835246 -2995.58381

Variable X 1 22.5357861 4.05277028 5.56058808 0.00512137 11.2834919

Variable X 2 -0.08927194 0.01385515 -6.44323096 0.00298556 -0.12774

Variable X 3 0.00011851 1.5697E-05 7.54967129 0.00164921 7.4925E-05


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Diagrama de t-XY*

DIAGRAMA T-XY*

251 253 255 257 259 261 263 265 267 269 271 273 275 277 279

T-X

T-Y*

0.90

1.00


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LOR PROMEDIO

P= 53.2

PA PB Volatilidad x y

53.2 14.3255 3.71365746 0 0

67.3931299 19.1038671 3.52772188 0.1 0.26347511

83.6220541 25.0750982 3.33486447 0.2 0.44594857102.50775 32.3927414 3.16452841 0.3 0.57979761

124.265311 41.2103825 3.01538845 0.4 0.68217284

149.109829 51.681607 2.8851624 0.5 0.7630077

154.016486 53.1916429 2.89550159 0.6 0.82845339

promedio 3.21954638 0.7 0.88252259

0.8 0.92794447

0.9 0.96663989

1 1

0.00

0.10

0.20

0.30

0.40

0.50

0.60

0.70

0.80

291 293 295 297 299 301 303 305 307 309 311 313 315 317 319 321 323


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F

Superior 95% Inferior 95.0% uperior 95.0%

-1641.50878 -2456.11416 -1641.50878

31.0839697 21.7769597 31.0839697

-0.09669226 -0.13193226 -0.09669226

0.00018807 0.00014386 0.00018807


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F


-813.852538 -2995.58381 -813.852538

33.7880803 11.2834919 33.7880803

-0.05080387 -0.12774 -0.05080387

0.00016209 7.4925E-05 0.00016209


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15/34

T-X

T-Y*


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T (C) Pv (mmHg)

44.4 171.6 5

84.9 10

99.3 20

115.4 40

125.8 60

139.9 100

161.2 200

185.8 400

210.6 760

T (C) Pv (mmHg)

45 71.97

50 92.65

y = 0.0003x3 - 0.0760x2 + 6

R = 0.999

-100

0

100

200

300

400

500

600

700

800

40 60 80 100 12

800


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55 118.23

60 149.61

65 187.83

70 234.03

75 289.49

80 355.63

85 434.0490 526.41

100 760

utilizando el analisis de datos para el nitrobenceno

PV T T2

T3

1 44.4 1971.36 87528.384

5 71.6 5126.56 367061.696

10 84.9 7208.01 611960.049

20 99.3 9860.49 979146.657

40 115.4 13317.16 1536800.26

60 125.8 15825.64 1990865.51

100 139.9 19572.01 2738124.2200 161.2 25985.44 4188852.93

400 185.8 34521.64 6414120.71

760 210.6 44352.36 9340607.02

para agua

Pv (mmHg) t t2 t3

71.97 45 2025 91125

92.65 50 2500 125000

0

100

200

300

400

500

600

700

45 50 55 60 65


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118.23 55 3025 166375

149.61 60 3600 216000

187.83 65 4225 274625

234.03 70 4900 343000

289.49 75 5625 421875

355.63 80 6400 512000

434.04 85 7225 614125526.41 90 8100 729000

a)calculamos la temperatura de destilacion

T PA PB PT97.80 19.5337079 699.104869 718.638577

98.00 8381414.38 704.051062 8382118.43

98.20 8432813.9 709.023973 8433522.92

98.40 8484423.13 714.023684 8485137.15

98.60 8536242.49 719.05028 8536961.54

98.80 8588272.43 724.103841 8588996.53

99.00 8640513.36 729.184451 8641242.54

99.26 8708742.7 735.829817 8709478.53

99.40 8745629.9 739.427147 8746369.33

99.60 8798506.38 744.589399 8799250.97

99.80 8851595.55 749.779029 8852345.33

100.00 8904897.85 754.996121 8905652.85


19/34

.1964x - 157.4363

1

140 160 180 200 220


20/34

Resumen




R^2 ajustado 0.99867796


Observacione 10

ANLISIS DE VARIANZA


Regresin 3 538129.694 179376.565 2267.21306 1.4972E-09Residuos 6 474.705887 79.1176478

Total 9 538604.4


Intercepcin -157.436334 39.7968784 -3.95599706 0.007486 -254.815787

Variable X 1 6.19642329 1.12887404 5.48902986 0.00153045 3.43416804

Variable X 2 -0.07603768 0.00966721 -7.86552213 0.00022351 -0.09969249

Variable X 3 0.00031883 2.5257E-05 12.623531 1.5138E-05 0.00025703

Resumen




R^2 ajustado 0.99999625


y = 0.0019x3 - 0.2041x2 + 10.976x - 180.84

R = 1

70 75 80 85 90 95 100


21/34

Observacione 10

ANLISIS DE VARIANZA


Regresin 3 210844.296 70281.4321 799767.098 3.4209E-17

Residuos 6 0.52726424 0.08787737

Total 9 210844.824


Intercepcin -138.206909 12.2837015 -11.2512429 2.9463E-05 -168.264044

Variable X 1 8.91788889 0.57192828 15.5926699 4.4053E-06 7.5184308

Variable X 2 -0.17193939 0.00865629 -19.8629456 1.0564E-06 -0.19312057

Variable X 3 0.00172081 4.2671E-05 40.3272687 1.5542E-08 0.0016164

PT = PA +PB


22/34


23/34

F


-60.0568807 -254.815787 -60.0568807

8.95867854 3.43416804 8.95867854

-0.05238286 -0.09969249 -0.05238286

0.00038063 0.00025703 0.00038063


24/34

F


-108.149774 -168.264044 -108.149774

10.317347 7.5184308 10.317347

-0.15075822 -0.19312057 -0.15075822

0.00182522 0.0016164 0.00182522


25/34

La ecuacion de antoine correlaciona la presiones de vapor de los liquidos puros con La temperatura

logp1=A-B/T+C

Teniendo en cuenta que las constantes de dicha escuacin para el benceno y el toluen

A B C

Benceno 6.90565 1211.033 220.79

Tolueno 6.95334 1343.943 219.377

a) construya el diagrama lquido-Vapor (t-xy*) a presion constante

Encontrar las presiones de vapor

T Benceno Tolueno

80.1 760.00 292.22

85 881.67 345.10

90 1020.99 406.73

95 1176.84 476.87

100 1350.49 556.32

105 1543.23 645.93

110 1756.38 746.59

110.62 1784.29 759.89

XA= (P-PB)/(PA-PB)

Calcular la fraccin en el Liquido- vapor PT= 760

T PA PB XA YA*

80.10 760.00 292.22 1.000 1.000

85.00 881.67 345.10 0.773 0.897

90.00 1020.99 406.73 0.575 0.773

95.00 1176.84 476.87 0.404 0.626

100.00 1350.49 556.32 0.256 0.456

105.00 1543.23 645.93 0.127 0.258

110.00 1756.38 746.59 0.013 0.031

110.62 1784.29 759.89 0.000 0.000

b) Grafique el diagrama xy*

0.8

1

0.700

0.800

0.900

1.000


26/34

c)Una mezcla liquida contine 55% de benceno y 45% de tolueno en peso calcular :

c.1) L a temperatura de Burbuja

c.2) La composicindel vapor en el Equilibrio

La temperatura de Burbuja

f(TBP)= XA .PA +XB.PB -PT

T (C) PA PB F(TBP)

80.1 760.00 292.22 -210.502 XA

100 1350.49 556.32 233.115 XB

90 1020.99 406.73 -15.425 PT

95 1176.84 476.87 101.855

92 1081.28 433.72 29.878

92.1 1084.36 435.11 32.19992.112 1084.73 435.28 32.477

La composicin del vapor en el equilibrio PA=XA.PA

PB=XB.PB

PA= 596.60 mmHg YA= 0.79

PB= 195.87 mmHg YB= 0.26

d) Una mezcla liquida contiene 80% de benceno y 20% de tolueno en peso calcular :

d.1) La temperuatura de Rocio

d.2) La composicin del lIquido en el equilibrio

La temperatura de Rocio

0

0.2

0.4

0.6

800.000

0.100

0.200

0.300

0.400

0.500

0.600

80.00 85.00 90.00 95.00 100.00 105.00 110.00

T- X

T- Y*


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f(TRP)=YA.P/PA + YB.P/PB -1

T(C) PA PB f(TRP)

80.1 760.00 292.22 0.3202 YA=

100 1350.49 556.32 -0.2766 YB=

95 1176.84 476.87 -0.1646 PT

90 1020.99 406.73 -0.0308

88 963.35 381.11 0.0300

88.95 990.40 393.11 0.0005

La composicin del Liquido

PA'=YA.P XA=PA'/PA

PB'=YB.P XB=PB'/PB

PA'= 608 XA= 0.614

PB'= 152 XB= 0.387


28/34

segn la ecuacin:

o

YA*= PA*XA/P


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0.55

0.45

760

YA=PA/P

YB=PB/P

85 90 95 100 105 110

T-X

T-Y*


30/34

0.8

0.2

760


31/34

4. Una Solucin de hiudrocarburos a una presin absoluta de 10 bars, tiene la siguiente composici

Hidrocarburo Fraccin mol

Etano 0.0025

Propano 0.25

I-butano 0.185N-butano 0.56

I-pentano 0.0025

utilice los coeficientes de distribucin en el equilibrio del monograma de Depriester.

a) calcule el punto de burbuja

b) calcule el punto de rocio

Punto de burbuja :

Primera estimacin

C F Bar

t= 60 140 P= 10

Componentes Xi mi ic4 ic4.Xi

Etano 0.0025 5 7.14 0.018

Propano 0.25 1.96 2.80 0.700

I-butano 0.185 0.93 1.33 0.246

N-butano 0.56 0.7 1.00 0.560

I-pentano 0.0025 0.325 0.46 0.001

1.525

segunda iteraccin

C F Bar

t= 57.22 135 P= 10

Componentes Xi mi ic4 ic4.Xi

Etano 0.0025 4.8 7.38 0.018

Propano 0.25 1.84 2.83 0.708

I-butano 0.185 0.85 1.31 0.242

N-butano 0.56 0.65 1.00 0.560

I-pentano 0.0025 0.24 0.37 0.001

1.529

Punto de Rocio


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Primera iteraccin

C F Bar

t= 80 176 P= 10

Componentes Xi mi ic4 yi/ic4

Etano 0.0025 5.99 6.11 0.000

Propano 0.25 2.54 2.59 0.096

I-butano 0.185 1.4 1.43 0.130

N-butano 0.56 0.98 1.00 0.560

I-pentano 0.0025 0.49 0.50 0.005

0.791

Primera iteraccin

C F Bar

t= 68.33 155 P= 10

Componentes Xi mi ic4 yi/ic4

Etano 0.0025 5.39 6.82 0.000

Propano 0.2500 2.19 2.77 0.090

I-butano 0.1850 1.09 1.38 0.134

N-butano 0.5600 0.79 1.00 0.560

I-pentano 0.0025 0.4 0.51 0.005

0.790


33/34

expresada como fraccin mol:

Psia

145

ic4=mi/mC4

mc4=1/ic4.Xi

mc4= 0.656

Psia

145

mc4= 0.654


34/34

Psia

145

ic4=mi/mC4

mc4=ic4.Xi

Psia

145

ic4=mi/mC4

mc4=ic4.Xi

1era lista -transf de masa ii

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