Partes: 1, 2

Y5 = 0.651	X5 = 0.284
Y6 = 0.502	X6 = 0.124
Y7 = 0.235	X7 = 0.039
Y8 = 0.06	X8 = 0.0056
Y9 = 0.056

H´D = 76,488.6 KJ / kg mol

H´D = Qc /D

Qc = H´D  D

Qc =  76,488.6 KJ / kg mol (84.512 Kg mol)

Qc = 6,464,204.563 KJ

H´B  = HB - QB / B

QB = (45,000 + 5700) KJ / Kg mol (132.25)  Kg mol

QB = 6,705,075 KJ

V1 = L0 + D

V1 / D = L0/ D + D / D

V1 =  (L0 / D +1 ) D

V1 = (1.059 +1) 84.512

V1 = 174.010 Kg mol

L0 = 89.498 Kg mol

Plato 1

V2 = L1l +D

V2y2 = L1x1 + DxD

L1y2 + Dy2 = L1x1 + DxD

L1 = D (x2 - y2) / (y2 - x1)

L1 = 84.512 (0.914 - 0.845) / (0.845 - 0.873)

L1 = 94.053

V2 = 94.053 + 84.512

V2 = 178.56

Plato 2

V3 = L2 + V2  

 V3y3 = L2x2 + V2y2

L2y3  + V2y3 = L2x2 + V2y2

L2y3  + V2y3 = L2x2 + V2y2

L2 = V2 (y2 - y3) / (y3 - x2)

L2 = 178.56 (0.845 - 0.783) / (0.783 - 0.656)

L2 = 87.71 kgmol

V3 = 265.73 kgmol

Plato 3

V4 = V3  + L3

V4y4 = V3y3  + L3x3

L3 = V3 (y3 - y4) / (y4 - y3)

L3 = 265.73 (0.783 - 0.718) / (0.718 - 0.52)

L3 = 87.23 kgmol

V4 = 87.23 + 265.73

V4 = 352.96 kgmol

Plato 4

L4 = V4 (y4 - y5) / (y5- x4)

L4 = 352.96 (0.718 - 0.651) / (0.651 - 0.383)

L4 = 88.24 kgmol

V5 = v4 + L4

V5 = 441.2 kgmol

Plato 5

F + V6  = V5 + L5

Fxf + V6y6  = V5y5 + L5x5

Ordenando y eliminando los términos correspondientes:

F (xf - y6 ) + V5 (y6 - y5) = L5 (x5 - y6)

L5 = F (xf - y6 ) + V5 (y6 - y5) / (x5 - y6)

L5 = 216.762 (0.36 - 0.502 ) + 441.2 (0.502 - 0.651) / (0.284 - 0.502)

L5 = 442.74 kgmol

V6 = 667.178 kgmol

DATOS OBTENIDOS DEL MANUAL DEL INGENIERO QUÍMICO Y TABLAS CRÍTICAS INTERNACIONALES

Datos de equilibrio líquido-vapor, a presión constante, para sistemas binarios seleccionados.

T	X	Y	M prom
100	0	0	18.02
96.4	0.02	0.134	18.3004
93.5	0.04	0.23	18.5808
91.2	0.06	0.304	18.8612
89.3	0.08	0.365	19.1416
87.7	0.1	0.418	19.422
84.4	0.15	0.517	20.123
81.7	0.2	0.579	20.824
78	0.3	0.665	22.226
75.3	0.4	0.729	23.628
73.1	0.5	0.779	25.03
71.2	0.6	0.825	26.432
69.3	0.7	0.87	27.834
67.5	0.8	0.915	29.236
66	0.9	0.958	30.638
65	0.95	0.979	31.339
64.5	1	1	32.04

TABLAS CRÍTICAS INTERNACIONALES

%mol de metanol	Cp de tablas (kJ)
0.0588	4.17
0.123	4.0494
0.273	3.82389
0.458	3.38187
0.696	2.95236
1	2.502

DATOS GRÁFICA INTERNET

CL
X	Cp
0.06	4.16483252
0.11	4.08670515
0.16	4.00197645
0.21	3.91162062
0.26	3.81661183
0.31	3.71792424
0.36	3.61653204
0.41	3.5134094
0.46	3.40953049
0.51	3.30586949
0.56	3.20340058
0.61	3.10309793
0.66	3.00593571
0.71	2.91288811
0.76	2.82492929
0.81	2.74303342
0.86	2.6681747
0.91	2.60132728
0.96	2.54346535
1	2.5043

CALOR DE SOLUCIÓN

X	Q
0.06	6.77990755
0.11	5.82355683
0.16	4.98055491
0.21	4.24255579
0.26	3.60121347
0.31	3.04818195
0.36	2.57511523
0.41	2.17366731
0.46	1.83549219
0.51	1.55224387
0.56	1.31557635
0.61	1.11714363
0.66	0.94859971
0.71	0.80159859
0.76	0.66779427
0.81	0.53884075
0.86	0.40639203
0.91	0.26210211
0.96	0.09762499

HL = CL (tL - T0) Mp + Hs

MONOGRAMA DE CALOR LATENTE DE VAPORIZACIÓN

X	T	Cpv (kJ)	Y*		Cpw (J)	
0.06	91.2	3.03576	0.304	1000.8	2323	2164.23
0.08	89.3	3.02325	0.365	1017.4	2323	2165.4
0.1	87.7	3.01074	0.418	1034.16	2323	2230.97
0.15	84.4	2.99823	0.517	1038.3	2323	2239.29
0.2	81.7	2.97738	0.579	1038.3	2323	2253.46
0.3	78	2.9607	0.665	1042.5	2323	2301.84
0.4	75.3	2.95236	0.729	1042.5	2323	2306.01
0.5	73.1	2.93985	0.779	1042.5	2323	2335.2
0.6	71.2	2.92734	0.825	1050.84	2323	2376.9
0.7	69.3	2.919	0.87	1075.86	2323	2376.9
0.8	67.5	2.91966	0.915	1075.86	2323	2381.07
0.9	66	2.89815	0.958	1084.2	2323	2381.07
0.95	65	2.88564	0.979	1084.2	2323	2381.07
1	64.5	2.8773	1	1086	2323	2381.07

DATOS DE LA GRÁFICA PARA LA SOLUCIÓN PROBLEMA

X*	HG	Y*	HL
0	47060	0	5576
0.05	46217.42	0.05	5242.767131
0.1	45489.04	0.1	4983.8061
0.15	44862.36	0.15	4783.766131
0.2	44324.86	0.2	4628.9736
0.25	43864.03	0.25	4507.432031
0.3	43467.37	0.3	4408.8221
0.35	43122.38	0.35	4324.501631
0.4	42816.57	0.4	4247.5056
0.45	42537.32	0.45	4172.546131
0.5	42272.25	0.5	4096.0125
0.55	42008.8	0.55	4015.971131
0.6	41734.47	0.6	3932.1656
0.65	41436.75	0.65	3846.016633
0.7	41103.13	0.7	3760.6221
0.75	40721.09	0.75	3680.757031
0.8	40278.14	0.8	3612.8736
0.85	39761.77	0.85	3565.101131
0.9	39159.46	0.9	3547.2461
0.95	38458.7	0.95	3570.792131
1	37647	1	3648.9

BIBLIOGRAFÍA

·              TREYBAL, ROBERT E. Mass Transfer Operations. Third Edition. McGraw Hill Book Company. United States of America, 1987.

·              GEANKOPLIS, CHRISTIE J. Procesos de transporte y operaciones unitarias.3ª Edición. Ed.CECSA. México DF 1999.

·              PERRY, JOHN H. Manual del Ingeniero Químico. Tomo I y II. Primera Edición. Editorial UTEHA. México DF,1974.

 

 

 

 

Autor:

Ponchon & Savarit

INSTITUTO TECNOLÓGICO DE MORELIA

México

Departamento de Ingeniería Bioquímica

10 de diciembre de 2003