Resolución de problema de destilación por el método de Ponchon-Savarit (página 2)
Enviado por Ponchon & Savarit�
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 |
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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
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