2-diagrama-h-x-y
DESCRIPTION
masaTRANSCRIPT
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Clculo de Entalpas Molares
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HL = CL . Mwprom (tL t0) + DHsUnidades: BTU/lb mol , KJ/ Kmol, Kcal/KmolUnidades: BTU/lb-F , KJ/ Kg-K, Kcal/Kg-C
Lquido saturado o subenfriado
HL = Entalpa molar de un lquido
CL = Capacidad calorfica de la solucin
CL debe evaluarse a la temperatura promedio entre tL y t0.
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Mwprom = Peso molecular promedio de la solucinMwprom = MwA . xA + MwB . xBMwA = Peso molecular de AMwB = Peso molecular de BUnidades: lb/lb mol , Kg/ Kmol, g/molCuando no se tiene informacin sobre CL, como una aproximacin se puede calcular CL . MwpromCL . Mwprom = CLA . MwA . xA + CLB . MwB . xB
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CLA = Capacidad calorfica del componente A como lquido puro CLA y CLB deben evaluarse a la temperatura promedio entre tL y t0CLB = Capacidad calorfica del componente B como lquido puro tL = Temperatura de la solucintL = Temperatura de burbuja Lquido saturadotL < Temperatura de burbuja Lquido subenfriadot0 = Temperatura de referencia
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DHs = Calor integral de solucin calor de mezclaLa temperatura a la cual estn disponibles los datos de calor de mezcla debe utilizarse como temperatura de referencia (t0).Unidades: BTU/lb mol , KJ/ Kmol, Kcal/Kmol
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HV = yA [CLA . MwA (tV t0) + lA . MwA] +Unidades: BTU/lb mol , KJ/ Kmol, Kcal/KmolyB [CLB . MwB (tV t0) + lB . MwB] MwA = Peso molecular de AMwB = Peso molecular de BUnidades: lb/lb mol , Kg/ Kmol , g/mol
Vapor saturado o sobrecalentado
HV = Entalpa molar de un vapor
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CLA = Capacidad calorfica del componente A (lquido)CLB = Capacidad calorfica del componente B (lquido) CLA y CLB deben evaluarse a la temperatura promedio entre tV y t0lA = Calor latente de vaporizacin del componente AlB = Calor latente de vaporizacin del componente BUnidades: BTU/lb , KJ/ Kg , Kcal/KglA y lB deben evaluarse a la temperatura tV Unidades: BTU/lb-F, KJ/ Kg-K, Kcal/Kg-C
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tv = Temperatura del vaportV = Temperatura de roco Vapor saturadotV > Temperatura de roco Vapor sobrecalentadot0 = Temperatura de referencia
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Clculo de Entalpa molar para una mezcla Lquido - Vapor
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LFVFzF = 0.40
T = 80 CLquido + Vaporxy
T Cxy80
Grfico1
100100
96.496.4
93.593.5
91.291.2
89.389.3
87.787.7
84.484.4
81.781.7
7878
75.375.3
73.173.1
71.271.2
69.369.3
67.667.6
6666
6565
64.564.5
Hoja1
T CT Kxy
100.0373.150.0075.445510.004347.92500.00092.2758075.4455132442.640940799.213545147.13851870.549513416119423.0484120231
96.4369.550.0275.74709-110.313982.30470.13491.7682275.4201332748.452140966.652044058.72331713.253580891818954.7941224392
93.5366.650.0476.03921-209.703678.18340.23091.3637675.4006932991.283241099.845643277.83771582.415577990418618.8442035463
91.2364.350.0676.32553-296.563430.41630.30491.0457875.3859433181.715041204.430742679.08021475.822056889118361.248767071
89.3362.450.0876.60706-371.863223.30560.36590.7849875.3742033337.625441290.135942188.75881386.71959025918150.3043864311
87.7360.850.1076.88484-436.563048.62600.41890.5666675.3646433467.954641361.829441766.51581311.569528142717968.6484106375
84.4357.550.1577.56201-557.822702.11090.51790.1201875.3458633734.042941508.332740976.85021162.492976306417628.9211792347
81.7354.850.2078.21692-631.612444.66590.57989.7586875.3314833949.102941626.853340472.76001051.73586979717412.0532206495
78.0351.150.3079.49991-681.092151.48950.66589.2688475.3132334240.071441787.342539782.4811925.606488362417115.0837472666
75.3348.450.4080.74678-655.322003.67400.72988.9154475.3010134449.751741903.075639276.0923862.013805038116897.2268881619
73.1346.250.5081.96089-595.291923.36840.77988.6300175.2917634618.997141996.530638882.4478827.465034335316727.8745109816
71.2344.350.6083.14492-516.321880.75170.82588.3853375.2843034764.029542076.639038525.7873809.130586778316574.4332244108
69.3342.450.7084.28284-416.161853.57720.87088.1423575.2773234908.031042156.195738178.9266797.439676484616425.2080034092
67.6340.750.8085.39540-287.761866.76430.91587.9263775.2715135036.015942226.915637838.4858803.11301076716278.7447065192
66.0339.150.9086.47855-136.541906.94730.95887.7243475.2664135155.743842293.080937516.0742820.40038752216140.0378790412
65.0338.150.9586.98192-62.761905.63620.97987.5986875.2634135230.219942334.241637355.9004819.836317476716071.1284624388
64.5337.651.0087.536030.001937.17231.00087.5360375.2619635267.356842354.766837204.5291833.403684721816006.0060080707
D =80KJ/Kmol - KKJ / Kmol
T = K
% rec metanol = 96 %
Tc
F =200lb mol/h
0.40Metanol1.0580E+05-3.6223E+029.3791E-010.0000E+000.0000E+00Metanol5.2390E+070.368200512.64 K
T =25 CT=81.7CAgua2.7637E+05-2.0901E+038.1250E+00-1.4116E-029.3701E-06Agua5.2053E+070.3199-0.2120.25795647.13 K
metanol - aguaR = 2
32.042lb / lb molKJ/Kmol mezcla
18.015lb / lb molB =42.37C
32.042lb / lb mol
0.96
Balance de materia total:
F = D + BB =120lb mol/h
Balance de materia referido al componente ms voltil:
0.02667
Condicin trmica de la alimentacin:
La condicin trmica de la alimentacin se determina utilizando el diagrama temperatura - composicin. Para este caso, la alimentacin tiene una composicin 0.40 fraccin molar de metanol y est a una temperatura de 81.7 C.
T Cxy
100.00.000.000
96.40.020.134
93.50.040.230
91.20.060.3040.2081.7
89.30.080.3650.57981.7
87.70.100.418
84.40.150.5170.2081.7
81.70.200.5790.264
78.00.300.665
75.30.400.7290.57981.7
73.10.500.7790.57964.0
71.20.600.825
69.30.700.8700.464
67.60.800.9150.481.7
66.00.900.958
65.00.950.979
64.51.001.000
Del diagrama:x =0.200y =0.579
Zona de Enriquecimiento
0.96
Q' =
16133.47507746BTU/lb mol
37500.8195KJ/Kmol
822.5497909257BTU/lb mol
1911.9434KJ/Kmol
Q' =46755.3256505286BTU/lb mol
Q' =108678.571795065KJ/Kmol
Zona de Empobrecimiento
0.02667D =80lb mol/h
B =120lb mol/h
Q" =
entalpa de la alimentacin, que en este caso corresponde a una mezcla lquido-vapor
0.2001051.735869797
0.57917412.0532206495
0.4009685.1487198511
0.4000
0.4009685.1487198511
0.0009685.1487198511
0.2001051.735869797
0.2000
0.57917412.0532206495
0.5790
1051.735869797BTU/lb mol
9685.1487198511BTU/lb mol17412.0532206495BTU/lb mol
Q" =(200 * 9685.72 - 80 * 46755.32565) / 120 =-15028.3026BTU/lb mol
0.96Q'=46755.3256505286
0.02667Q" =-15028.3025672672
0.9646755.32565052860.9646755.3256505286
0.960146755.3256505286
0.02667-15028.30256726720.02667-15028.3025672672
0.0266716000.00000-15028.3025672672
Nmero de etapas de equilibrio
EnriquecimientoEmpobrecimiento
0.9646755.32565052860.02667-15028.3026
0.9600.0266720000
0.9646755.32565052860.02667-15028.3026
0.900.0520000
0.9646755.32565052860.02667-15028.3026
0.800.120000
0.9646755.32565052860.02667-15028.3026
0.700.220000
0.9646755.32565052860.02667-15028.3026
0.600.320000
0.9646755.32565052860.02667-15028.3026
0.500.420000
0.9646755.32565052860.02667-15028.3026
0.400.520000
0.9646755.3256505286
0.30
F0.49685.1487198511
00
11
EnriquecimientoEmpobrecimiento
0.2380.4980.026670.02667
0.2680.5200.0390.041
0.3150.5460.0600.100
0.4120.6050.1060.195
0.5100.6680.1520.288
0.6080.7300.1980.380
0.7050.7870.2450.470
0.8030.8580.2680.520
0.9010.9220.2800.540
0.9600.960
HV1 =
HL0 =
16133.47507746BTU/lb mol
37500.8195347646KJ/Kmol
822.5497909257BTU/lb mol
1911.9434046145KJ/Kmol
822.5497909257BTU/lb mol
Q' =46755.3256505286BTU/lb mol
3.674622E+06BTU/h
Balance de energa alrededor de todo el sistema ( Columna + Condensador + Recalentador ), considerando despreciables las prdidas de calor:
D
F
(Depende de la condicin trmica)
B
1669.640913258BTU/lb mol
2.003753E+06BTU/h
Calor suministrado a la alimentacin
F =200lb mol/hF =200 lb mol/h
0.400.40
T =25 CT =81.7 C
Q
Balance de energa, considerando despreciables las prdidas de calor:
Q =
Q =Calor suministrado a la alimentacin
-867.4264339158BTU/lb mol
9685.1487BTU/lb mol
Q =2110515.03075338BTU/h
d) R = 1.5 Rmin
D =80
0.96
F =200lb mol/h
0.40
T =25 CT=81.7C
metanol - agua
32.042lb / lb mol
18.015lb / lb molB =120lb mol/h
0.02667
Clculo de la relacin de reflujo mnimo
9685.1487198511BTU/lb mol
33858.7047000026BTU/lb mol1051.735869797BTU/lb mol
17412.0532206495BTU/lb mol
16133.47507746BTU/lb mol
822.54979BTU/lb mol
1.1577
R =1.7365
0.2001051.735869797
0.57917412.05322064950.57917412.0532206495
0.4009685.14871985110.9633858.7047000026
0.4000
0.4009685.14871985110.960
0.0009685.14871985110.9633858.7047000026
0.2001051.735869797
0.2000
0.57917412.0532206495
0.5790
F =100moles/s0.98
0.4% recup =95%
0.4-842.5177866089
D = ( 95 / 100 ).( 100 * 0.40 ) / 0.98 =38.4615
B =61.5385
0.0375
16066.1375493555BTU/lb mol
827.8793551962BTU/lb mol
29,000BTU/lb mol
0.84878
R =1.27316
Hoja1
0.475
0.96
HF
H
F
DD
Q'
DB
Q"
xD
xB
zF
Hoja2
Hoja3
L
F
V
HF
H
F
L
V
HF
H
F
L
V
DD min
Q'min
HF
H
F
DD
DB
Q"
xD
xB
zF
x , y
T CT Kxy
100.0373.150.0075.445510.004347.92500.00092.2758075.4455132442.640940799.213545147.1385
96.4369.550.0275.74709-110.313982.30470.13491.7682275.4201332748.452140966.652044058.7233
93.5366.650.0476.03921-209.703678.18340.23091.3637675.4006932991.283241099.845643277.8377
91.2364.350.0676.32553-296.563430.41630.30491.0457875.3859433181.715041204.430742679.0802
89.3362.450.0876.60706-371.863223.30560.36590.7849875.3742033337.625441290.135942188.7588
87.7360.850.1076.88484-436.563048.62600.41890.5666675.3646433467.954641361.829441766.5158
84.4357.550.1577.56201-557.822702.11090.51790.1201875.3458633734.042941508.332740976.8502
81.7354.850.2078.21692-631.612444.66590.57989.7586875.3314833949.102941626.853340472.7600
78.0351.150.3079.49991-681.092151.48950.66589.2688475.3132334240.071441787.342539782.4811
75.3348.450.4080.74678-655.322003.67400.72988.9154475.3010134449.751741903.075639276.0923
73.1346.250.5081.96089-595.291923.36840.77988.6300175.2917634618.997141996.530638882.4478
71.2344.350.6083.14492-516.321880.75170.82588.3853375.2843034764.029542076.639038525.7873
69.3342.450.7084.28284-416.161853.57720.87088.1423575.2773234908.031042156.195738178.9266
67.6340.750.8085.39540-287.761866.76430.91587.9263775.2715135036.015942226.915637838.4858
66.0339.150.9086.47855-136.541906.94730.95887.7243475.2664135155.743842293.080937516.0742
65.0338.150.9586.98192-62.761905.63620.97987.5986875.2634135230.219942334.241637355.9004
64.5337.651.0087.536030.001937.17231.00087.5360375.2619635267.356842354.766837204.5291
KJ/Kmol - K
T = KKJ / Kmol
Tc
Metanol1.0580E+05-3.6223E+029.3791E-010.0000E+000.0000E+00Metanol5.2390E+070.368200512.64 K
Agua2.7637E+05-2.0901E+038.1250E+00-1.4116E-029.3701E-06Agua5.2053E+070.3199-0.2120.25795647.13 K
KJ/Kmol mezcla
to =42.37C
32.042lb / lb molKJ / Kmol * 0.430166 = BTU/lb mol
18.016lb / lb molKJ / Kmol * 0.430166 = BTU/lb mol
00
00
00
00
00
00
00
00
00
00
00
00
Benceno-Tolueno 16 C
MBD0000809B.doc
Debe separarse en forma continua una mezcla de metanol y agua, disponible a una temperatura de 25 C y con 40 moles % de metanol, en una columna de destilacin fraccionada que opera a la presin atmosfrica.
La alimentacin, antes de ingresar a la columna, es precalentada mediante un sistema de intercambio calrico de modo tal que alcanza una temperatura de 81.7 C y se introduce por la posicin ptima a razn de 200 lb mol/h.
La columna de destilacin estar provista de un recalentador y de un condensador total, retornndose la corriente de reflujo en su punto de burbuja; y se desea obtener un destilado a razn de 80 lb mol/h, recuperndose el 96 % del metanol cargado a la columna.
Si se opera con una relacin de reflujo igual a 2, determinar:
a) El nmero de platos ideales requeridos y la posicinptima del plato de carga, para efectuarla separacin.
b) Las cargas calricas en el condensador y en el recalentador.
c) La cantidad de calor suministrada a la alimentacin.
d) Repetir los clculos anteriores si se utiliza una relacin de reflujo igual a 1.5 Rmin
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Regla de mezclas LF HVF HF--- = --------- VF HF - HLF LF y zF--- = ------- VF zF - x xyzFVFLFFHF
Grfico3
1870.549513416119423.0484120231
1713.253580891818954.7941224392
1582.415577990418618.8442035463
1475.822056889118361.248767071
1386.71959025918150.3043864311
1311.569528142717968.6484106375
1162.492976306417628.9211792347
1051.73586979717412.0532206495
925.606488362417115.0837472666
862.013805038116897.2268881619
827.465034335316727.8745109816
809.130586778316574.4332244108
797.439676484616425.2080034092
803.11301076716278.7447065192
820.40038752216140.0378790412
819.836317476716071.1284624388
833.403684721816006.0060080707
H
Hoja1
T CT KxCL . MwpromDHsHLyCLA MWACLB MWBlA MWAlB MWBHVHLHV
100.0373.150.0075.445510.004347.92500.00092.2758075.4455132442.640940799.213545147.13851870.549513416119423.0484120231
96.4369.550.0275.74709-110.313982.30470.13491.7682275.4201332748.452140966.652044058.72331713.253580891818954.7941224392
93.5366.650.0476.03921-209.703678.18340.23091.3637675.4006932991.283241099.845643277.83771582.415577990418618.8442035463
91.2364.350.0676.32553-296.563430.41630.30491.0457875.3859433181.715041204.430742679.08021475.822056889118361.248767071
89.3362.450.0876.60706-371.863223.30560.36590.7849875.3742033337.625441290.135942188.75881386.71959025918150.3043864311
87.7360.850.1076.88484-436.563048.62600.41890.5666675.3646433467.954641361.829441766.51581311.569528142717968.6484106375
84.4357.550.1577.56201-557.822702.11090.51790.1201875.3458633734.042941508.332740976.85021162.492976306417628.9211792347
81.7354.850.2078.21692-631.612444.66590.57989.7586875.3314833949.102941626.853340472.76001051.73586979717412.0532206495
78.0351.150.3079.49991-681.092151.48950.66589.2688475.3132334240.071441787.342539782.4811925.606488362417115.0837472666
75.3348.450.4080.74678-655.322003.67400.72988.9154475.3010134449.751741903.075639276.0923862.013805038116897.2268881619
73.1346.250.5081.96089-595.291923.36840.77988.6300175.2917634618.997141996.530638882.4478827.465034335316727.8745109816
71.2344.350.6083.14492-516.321880.75170.82588.3853375.2843034764.029542076.639038525.7873809.130586778316574.4332244108
69.3342.450.7084.28284-416.161853.57720.87088.1423575.2773234908.031042156.195738178.9266797.439676484616425.2080034092
67.6340.750.8085.39540-287.761866.76430.91587.9263775.2715135036.015942226.915637838.4858803.11301076716278.7447065192
66.0339.150.9086.47855-136.541906.94730.95887.7243475.2664135155.743842293.080937516.0742820.40038752216140.0378790412
65.0338.150.9586.98192-62.761905.63620.97987.5986875.2634135230.219942334.241637355.9004819.836317476716071.1284624388
64.5337.651.0087.536030.001937.17231.00087.5360375.2619635267.356842354.766837204.5291833.403684721816006.0060080707
C2 + C3 . Tr + C4 . Tr2
D =80CLi . Mwi =(C1 + C2 . T + C3 . T2 + C4 . T3 + C5 . T4 )/103KJ/Kmol - Kli . Mwi=(C1/103). (1 - Tr )KJ / Kmol
xD =T = K
% rec metanol = 96 %
C1C2C3C4C5C1C2C3C4Tc
F =200lb mol/h
zF =0.40PT = 1 atmsferaMetanol1.0580E+05-3.6223E+029.3791E-010.0000E+000.0000E+00Metanol5.2390E+070.368200512.64 K
T =25 CT=81.7CAgua2.7637E+05-2.0901E+038.1250E+00-1.4116E-029.3701E-06Agua5.2053E+070.3199-0.2120.25795647.13 K
metanol - aguaR = 2
DHs =-6.348.6164 x6 + 10345.5832 x5 + 5571.5608 x4 - 21789.6758 x3 + 18218.6411 x2 - 6002.3764 x + 2.6229
MwA =32.042lb / lb molKJ/Kmol mezcla
MwB =18.015lb / lb molB =to =42.37C
xB =
MwA =32.042lb / lb molHL =(KJ / Kmol) * 4.302166 E-01 = BTU/lb mol
xD = ( % recup / 100) . ( F . zF ) / D
xD = (96/ 100).( 200 * 0.40) / 80 =0.96
Balance de materia total:
F = D + BB =120lb mol/h
Balance de materia referido al componente ms voltil:
F . zF = D . xD + B . xB
( 200 * 0.40 ) = ( 80 * 0.96 ) + 120 * xBxB =0.02667
Condicin trmica de la alimentacin:
La condicin trmica de la alimentacin se determina utilizando el diagrama temperatura - composicin. Para este caso, la alimentacin tiene una composicin 0.40 fraccin molar de metanol y est a una temperatura de 40 C.
T Cxy
100.00.000.000
96.40.020.134
93.50.040.230
91.20.060.3040.2081.7
89.30.080.3650.57981.7
87.70.100.418
84.40.150.5170.2081.7
81.70.200.5790.264
78.00.300.665
75.30.400.7290.57981.7
73.10.500.7790.57964.0
71.20.600.825
69.30.700.8700.464
67.60.800.9150.481.7
66.00.900.958
65.00.950.979
64.51.001.000
Del diagrama T-x-y, se determina que la alimentacin est en la condicin de una mezcla de lquido y vapor, es decir representa a un sistema de dos fases: un lquido de composicin " x " (fraccin molar) y un vapor de composicin " Y " (fraccin molar).
Del diagrama:x =0.200y =0.579
Ubicacin del Punto Polar DDZona de Enriquecimiento
xD =0.96
Q' =HV1 + R (HV1 - HLO)
HV1 =entalpa de un vapor saturado de composicin y1HV1 =16133.47507746BTU/lb mol
37500.8195KJ/Kmol
Entalpa de un lquido saturado, de composicin xDHL0 =822.5497909257BTU/lb mol
HL0 =1911.9434KJ/Kmol
Entalpa de un lquido subenfriado, de composicin xD
Q' =46755.3256505286BTU/lb mol
Q' =108678.571795065KJ/Kmol
Ubicacin del Punto Polar DBZona de Empobrecimiento
xB =0.02667D =80lb mol/h
B =120lb mol/h
Q" =( F . HF - D . Q' ) / B
HF =entalpa de la alimentacin, que en este caso corresponde a una mezcla lquido-vapor
0.2001051.735869797
0.57917412.0532206495
0.4009685.1487198511
0.4000
0.4009685.1487198511
0.0009685.1487198511
0.2001051.735869797
0.2000
0.57917412.0532206495
0.5790
HL =1051.735869797BTU/lb mol
Del diagrama: HF =9685.1487198511BTU/lb molHV =17412.0532206495BTU/lb mol
Q" =(200 * 9685.72 - 80 * 46755.32565) / 120 =-15028.3026BTU/lb mol
xD =0.96Q'=46755.3256505286
xB =0.02667Q" =-15028.3025672672
0.9646755.32565052860.9646755.3256505286
0.960146755.3256505286
0.02667-15028.30256726720.02667-15028.3025672672
0.0266716000.00000-15028.3025672672
Nmero de etapas de equilibrio
Para determinar el nmero de etapas de equilibrio, uno de los mtodos consiste en representar las lneas de operacin en el diagrama de distribucin (Las lneas de operacin no son rectas) . Luego se trazan escalones entre las lneas de operacin y las l
EnriquecimientoEmpobrecimiento
0.9646755.32565052860.02667-15028.3026
0.9600.0266720000
0.9646755.32565052860.02667-15028.3026
0.900.0520000
0.9646755.32565052860.02667-15028.3026
0.800.120000
0.9646755.32565052860.02667-15028.3026
0.700.220000
0.9646755.32565052860.02667-15028.3026
0.600.320000
0.9646755.32565052860.02667-15028.3026
0.500.420000
0.9646755.32565052860.02667-15028.3026
0.400.520000
0.9646755.3256505286
0.30
F0.49685.1487198511
00
11
EnriquecimientoEmpobrecimiento
0.2380.4980.026670.02667
0.2680.5200.0390.041
0.3150.5460.0600.100
0.4120.6050.1060.195
0.5100.6680.1520.288
0.6080.7300.1980.380
0.7050.7870.2450.470
0.8030.8580.2680.520
0.9010.9220.2800.540
0.9600.960
HV1 =
HL0 =
Carga calrica en el Condensador: Qc
Qc = V1 . ( HV1 - HD )
HV1 =Entalpa de un vapor saturado de composicin y1HV1 =16133.47507746BTU/lb mol
37500.8195347646KJ/Kmol
HD =Entalpa de un lquido saturado, de composicin xDHD =822.5497909257BTU/lb mol
1911.9434046145KJ/Kmol
De la definicin de Q' : Q' = (Qc / D ) + HD
Qc = D ( Q' - HD )HD = HL0 =822.5497909257BTU/lb mol
Q' =46755.3256505286BTU/lb mol
Qc =3.674622E+06BTU/h
Carga calrica en el Recalentador: QR
QcBalance de energa alrededor de todo el sistema ( Columna + Condensador + Recalentador ), considerando despreciables las prdidas de calor:
D
xDF . HF + QR = Qc + D . HD + B . HB
FHD
zFQR = Qc + D . HD + B . HB - F . HF
HF
HB =Entalpa de un lquido saturado,de composicin xB
HF =Entalpa de la alimentacin, de composicin zF
(Depende de la condicin trmica)
B
QRxB
HB
De la definicin de Q" : Q" = HB - (QR / B )
QB = B ( HB - Q" )HB =1669.640913258BTU/lb mol
QB =2.003753E+06BTU/h
Calor suministrado a la alimentacin
F =200lb mol/hF =200 lb mol/h
zF =0.40zF =0.40
T =25 CT =81.7 C
H'F =QHF =
Balance de energa, considerando despreciables las prdidas de calor:
F . H'F + Q = F . HFQ =F ( HF - F . H'F )
Q =Calor suministrado a la alimentacin
H'F = Entalpa de la alimentacin a 25 C =-867.4264339158BTU/lb mol
HF = Entalpa de la alimentacin a 81.7 C =9685.1487BTU/lb mol
Q =2110515.03075338BTU/h
d) R = 1.5 Rmin
D =80
xD =0.96
F =200lb mol/h
zF =0.40PT = 1 atmsfera
T =25 CT=81.7C
metanol - aguaR = 1.5 Rmin
MwA =32.042lb / lb mol
MwB =18.015lb / lb molB =120lb mol/h
xB =0.02667
Clculo de la relacin de reflujo mnimo
Dado que la lnea de equilibrio es cncava, la relacin de reflujo mnimo se determina evaluando Q'min en el diagrama entalpa - concentracin. Para tal efecto, se buscar la lnea de equilibrio que pase por F y se prolonga hasta cortar la abscisa xD, par
Q'min =HV1 + Rmin (HV1 - HLO)
Rmin = (Q'min - HV1) /(HV1 - HLO)
HF =9685.1487198511BTU/lb mol
Del diagrama Q'min =33858.7047000026BTU/lb molHL =1051.735869797BTU/lb mol
HV =17412.0532206495BTU/lb mol
HV1 =16133.47507746BTU/lb mol
HL0 =822.54979BTU/lb mol
Rmin =1.1577
R =1.5 Rmin =1.7365
0.2001051.735869797
0.57917412.05322064950.57917412.0532206495
0.4009685.14871985110.9633858.7047000026
0.4000
0.4009685.14871985110.960
0.0009685.14871985110.9633858.7047000026
0.2001051.735869797
0.2000
0.57917412.0532206495
0.5790
F =100moles/sxD =0.98
zF =0.4% recup =95%
zF =0.4HF =-842.5177866089
D = ( % recup / 100) . ( F . zF ) / xD
D = ( 95 / 100 ).( 100 * 0.40 ) / 0.98 =38.4615
B =61.5385
xB = (F . zF - D . xD ) / B =0.0375
Rmin = (Q'min - HV1) /(HV1 - HLO)
HV1 =16066.1375493555BTU/lb mol
HL0 =827.8793551962BTU/lb mol
Q'min =29,000BTU/lb mol
Rmin =0.84878
R =1.27316
Hoja1
000000000
000000000
00
00
00
00
00
00
00
00
00
00
00
00
00
00
00
HF
H
F
DD
Q'
DB
Q"
xD
xB
zF
Hoja2
000000
000000
00
00
00
00
00
00
00
00
00
00
00
00
00
00
00
Hoja3
000000000
000000000
00
00
00
00
00
00
00
00
00
00
00
00
00
00
00
LF
F
V
HF
H
F
L
V
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
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
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
0
0
0
0
0
0
0
HF
H
F
L
V
DD min
Q'min
0000
000
00
00
00
00
00
00
00
00
00
00
00
00
00
00
00
HF
H
F
DD
DB
Q"
xD
xB
zF
x , y
0000
0000
000
000
000
000
000
000
000
00
0
0
0
0
0
0
0
T CT KxCL . MwpromDHsHLyCLA MWACLB MWBlA MWAlB MWBHV
100.0373.150.0075.445510.004347.92500.00092.2758075.4455132442.640940799.213545147.1385
96.4369.550.0275.74709-110.313982.30470.13491.7682275.4201332748.452140966.652044058.7233
93.5366.650.0476.03921-209.703678.18340.23091.3637675.4006932991.283241099.845643277.8377
91.2364.350.0676.32553-296.563430.41630.30491.0457875.3859433181.715041204.430742679.0802
89.3362.450.0876.60706-371.863223.30560.36590.7849875.3742033337.625441290.135942188.7588
87.7360.850.1076.88484-436.563048.62600.41890.5666675.3646433467.954641361.829441766.5158
84.4357.550.1577.56201-557.822702.11090.51790.1201875.3458633734.042941508.332740976.8502
81.7354.850.2078.21692-631.612444.66590.57989.7586875.3314833949.102941626.853340472.7600
78.0351.150.3079.49991-681.092151.48950.66589.2688475.3132334240.071441787.342539782.4811
75.3348.450.4080.74678-655.322003.67400.72988.9154475.3010134449.751741903.075639276.0923
73.1346.250.5081.96089-595.291923.36840.77988.6300175.2917634618.997141996.530638882.4478
71.2344.350.6083.14492-516.321880.75170.82588.3853375.2843034764.029542076.639038525.7873
69.3342.450.7084.28284-416.161853.57720.87088.1423575.2773234908.031042156.195738178.9266
67.6340.750.8085.39540-287.761866.76430.91587.9263775.2715135036.015942226.915637838.4858
66.0339.150.9086.47855-136.541906.94730.95887.7243475.2664135155.743842293.080937516.0742
65.0338.150.9586.98192-62.761905.63620.97987.5986875.2634135230.219942334.241637355.9004
64.5337.651.0087.536030.001937.17231.00087.5360375.2619635267.356842354.766837204.5291
CLi . Mwi =(C1 + C2 . T + C3 . T2 + C4 . T3 + C5 . T4 )/103KJ/Kmol - KC2 + C3 . Tr + C4 . Tr2
T = Kli . Mwi=(C1/103). (1 - Tr )KJ / Kmol
C1C2C3C4C5C1C2C3C4Tc
Metanol1.0580E+05-3.6223E+029.3791E-010.0000E+000.0000E+00Metanol5.2390E+070.368200512.64 K
Agua2.7637E+05-2.0901E+038.1250E+00-1.4116E-029.3701E-06Agua5.2053E+070.3199-0.2120.25795647.13 K
DHs =-6.348.6164 x6 + 10345.5832 x5 + 5571.5608 x4 - 21789.6758 x3 + 18218.6411 x2 - 6002.3764 x + 2.6229KJ/Kmol mezcla
to =42.37C
MwA =32.042lb / lb molHL =KJ / Kmol * 0.430166 = BTU/lb mol
MwB =18.016lb / lb molHV =KJ / Kmol * 0.430166 = BTU/lb mol
00
00
00
00
00
00
00
00
00
00
00
00
Benceno-Tolueno 16 C
MBD0000809B.doc
Debe separarse en forma continua una mezcla de metanol y agua, disponible a una temperatura de 25 C y con 40 moles % de metanol, en una columna de destilacin fraccionada que opera a la presin atmosfrica.
La alimentacin, antes de ingresar a la columna, es precalentada mediante un sistema de intercambio calrico de modo tal que alcanza una temperatura de 81.7 C y se introduce por la posicin ptima a razn de 200 lb mol/h.
La columna de destilacin estar provista de un recalentador y de un condensador total, retornndose la corriente de reflujo en su punto de burbuja; y se desea obtener un destilado a razn de 80 lb mol/h, recuperndose el 96 % del metanol cargado a la columna.
Si se opera con una relacin de reflujo igual a 2, determinar:
a) El nmero de platos ideales requeridos y la posicinptima del plato de carga, para efectuarla separacin.
b) Las cargas calricas en el condensador y en el recalentador.
c) La cantidad de calor suministrada a la alimentacin.
d) Repetir los clculos anteriores si se utiliza una relacin de reflujo igual a 1.5 Rmin
-
LF HVF HF--- = --------- VF HF - HLF LF--- = VF LF y zF--- = ------- VF zF - x HVF = Entalpa de un vapor saturado de composicin y HLF = Entalpa de un lquido saturado de composicin x HVF + (LF/VF) . HLFHF = ----------------- 1 + LF/VF
-
Capacidad calorfica de sustancias purasFuente: Manual del Ingeniero Qumico 7ma EdicinCLi. Mwi. = C1 + C2 . T + C3 . T2 + C4 . T3 + C5 . T4 Ecuacin 1Ecuacin 2CLi. Mwi. = C12 / t + C2 (2 C1 . C3) t (C1. C4) t2 (C3)2/3 t3 - (C3 . C4 / 2) t4 (C4)2/5.t5Tabla 2.196CLi. Mwi = J / Kmol - KT = K t = (1 Tr) Tr = T / Tc
-
J / Kmol - K x 2.390 x 10-4 = cal/ mol -CJ / Kmol - K x 2.390059 x 10-4 = BTU/lb mol - FFactores de conversin
-
Calores latentes de vaporizacinFuente: Manual del Ingeniero Qumico 7ma Edicinli. Mwi = J / Kmol Tr = T / Tc T = KFactores de conversinJ / Kmol x 2.390 x 10-4 = cal/ mol J / Kmol x 4.302106 x 10-4 = BTU/lb mol Tabla 2.193
-
Calores de mezcla : DHsFuente: Tablas Crticas Internacionales
-
moles A moles AxA = ------------ = ---------------- moles totales moles A + moles B % peso A/MwAxA = ----------------------------- % peso A/MwA + % peso B/MwBDHs =( Q J /g mezcla ) * Mwprom J / g mol mezcla
-
nxA = ------ n + 1 1DHs =( Q KJ /g mol B) * ------ (n + 1) n = moles A / mol BKJ / g mol mezcla
-
100 - nDHs =( Q KJ / mol B) * -------- 100 KJ / g mol mezclan = % molar A
-
Calores de mezcla del sistema Disulfuro de Carbono Tetracloruro de carbonoT = 25 CPgina 155Tabla N 3
xCCl4KJ/g mol mix
0.81530.17900.66930.26400.53930.31100.40010.30700.28380.27600.14250.18000.09340.1270
xCCl4KJ/g mol mix1.00000.00000.81530.17900.66930.26400.53930.31100.40010.30700.28380.27600.14250.18000.09340.12700.00000.0000
-
Calores de mezcla del sistema Disulfuro de Carbono (A) Tetracloruro de carbono (B) a 25 C.
xBxAKJ/g mol mixKJ/Kmol mix1.00000.00000.00000.0000.81530.18470.1790179.0000.66930.33070.2640264.0000.53930.46070.3110311.0000.40010.59990.3070307.0000.28380.71620.2760276.0000.14250.85750.1800180.0000.09340.90660.1270127.0000.00001.00000.00000.000
-
Grfico1
0
179
264
311
307
276
180
127
0
xA
DHS
Calor de Mezcla CS2 - CCl4 25 C
Ecuaciones
Clculo de Entalpas Molares
Lquido saturado o subenfriado
HL = CL . Mwprom (tL - tO) + DHs
HL =Entalpa molar de un lquido
CL =Capacidad calorfica de la solucin
CL debe evaluarse a la temperatura promedio entre tL y to.
Mwprom = Peso molecular promedio de la solucin
Mwprom = MwA . xA + MwB . xB
MwA = Peso molecular de A
MwB = Peso molecular de B
Cuando no se tiene informacin sobre CL, como una aproximacin se puede calcular CL . Mwprom
CL . Mwprom = CLA . MwA . xA + CLB . MwB . xB
CLA = Capacidad calorfica del componente A como lquido puro
CLB = Capacidad calorfica del componente B como lquido puro
CLA y CLB deben evaluarse a la temperatura promedio entre tL y to
tL =Temperatura de la solucin
Lquido saturadotL = Temperatura de burbuja
Lquido subenfriadotL < Temperatura de burbuja
to =Temperatura de referencia
DHs =Calor integral de solucin o calor de mezcla
La temperatura a la cual estn disponibles los datos de calor de mezcla debe utilizarse como temperatura de referencia
Vapor saturado o sobrecalentado
HV = yA [ CLA . MwA (tV - tO) + lA . MwA ] + yB [ CLB . MwB (tV - tO) + lB . MwB ]
HV =Entalpa molar de un vapor
CLA = Capacidad calorfica del componente A como lquido puro
CLB = Capacidad calorfica del componente B como lquido puro
CLA y CLB deben evaluarse a la temperatura promedio entre tG y to
MwA = Peso molecular de A
MwB = Peso molecular de B
lA = Calor latente de vaporizacin de A
lB = Calor latente de vaporizacin de B
Los calores latentes de vaporizacin deben evaluarse a tG
tV =Temperatura de la mezcla en fase vapor
Vapor saturadotG = Temperatura de roco
Vapor sobrecalentadotG > Temperatura de roco
to =Temperatura de referencia
Pgina &P
Ejemplo
Construccin de datos entalpa - concentracin para el sistema CS2 ( A )- CCl4 ( B ) a 1 atm.
a) Capacidad calorfica de solucin
CL . Mwprom = CLA . MwA . xA + CLB . MwB . xB
CLi . Mwi =C1 + C2 . T + C3 . T2 + C4 . T3 + C5 . T4J/Kmol - KT = K
C1C2C3C4C5
ACS28.5600E+04-1.2200E+025.6050E-01-1.4520E-032.0080E-06
BCCl4-7.5270E+058.9661E+03-3.0394E+013.4455E-020.0000E+00
b) Calores latentes molares de vaporizacin
C2 + C3 . Tr + C4 . Tr2
li =C1 (1 - Tr )J / Kmol
C1C2C3C4Tc
ACS23.4960E+070.289600552.0 K
BCCl44.1860E+070.358400556.35 K
c) Calores de mezcla a 25 C DHs
xBxAKJ/gmol mixKJ/Kmol
1.00000.00000.00000.000
0.81530.18470.1790179.000
0.66930.33070.2640264.000
0.53930.46070.3110311.000
0.40010.59990.3070307.000
0.28380.71620.2760276.000
0.14250.85750.1800180.000
0.09340.90660.1270127.000
0.00001.00000.00000.000
xDHs
0.000.00
0.0557.96
0.10107.92
0.15151.49
0.20189.59
0.25222.71
0.30250.99
0.35274.38
0.40292.68
0.45305.66
0.50313.04
0.55314.59
0.60310.08
0.65299.26
0.70281.87
0.75257.54
0.80225.72
0.85185.56
DHs =- 1888.8191 x6 + 5483.3753 x5 - 6493.4512 x4 + 3684.4967 x3 - 2037.5618 x2 + 1251.6472 x + 0.04710.90135.83
0.9574.73
R2 =0.99970.9746.57
1.000.00
xDHs
0.000.00
0.0557.96
0.10107.92
0.15151.49
0.20189.59
0.25222.71
0.30250.99
0.35274.38
0.40292.68
0.45305.66
0.50313.04
0.55314.59
0.60310.08
0.65299.26
0.70281.87
0.75257.54
0.80225.72
0.85185.56
0.90135.83
0.9574.73
0.9746.57
1.000.00
Lquido saturado
HL = CL . Mwprom (tL - tO) + DHs
x =0.30
tL =62.2 C =335.35K
to =25 C =298.15K
DHs =292.68KJ / Kmol
CL debe evaluarse a tprom y en funcin de la concentracin. Como no se tiene datos de CL, se calcular como una aproximacin CL . Mwprom
CL . Mwprom = CLA . MwA xA + CLB . MwB . xB
CLA y CLB se calcularn a la tprom
tprom = ( tL+tO ) / 2 =316.75K
CLA . MwA =7.72606E+04J / Kmol - K =77.26062KJ / Kmol - K
CLB . MwB =1.32835E+05J / Kmol - K =132.83482KJ / Kmol - K
CL . Mwprom =116.16256KJ / Kmol - K
HL =116.16256 * ( 62.2 - 25 ) + 292.68 =4613.9319KJ / Kmol
Vapor saturado
HV = y [ CLA . MwA (tv - tO) + lA . MwA ] + (1 - y) [ CLB . MwB (tv - tO) + lB . MwB ]
y =0.30
tv =68.8 C =341.95
to =25 C =298.15K
CLA y CLB se calcularn a la tprom
tprom =( tL + tO ) / 2 =320.05 K
CLA . MwA =7.74342E+04J / Kmol - K =77.43416KJ / Kmol - K
CLB . MwB =1.33133E+05J / Kmol - K =133.13277KJ / Kmol - K
lA y lB se calcularn a tvTrA =0.6195TrB=0.6146
lA . MwA =2.64272E+07J / Kmol =2.64272E+04KJ / Kmol
lB . MwB =2.97425E+07J / Kmol =2.97425E+04KJ / Kmol
Hv =31413.9875KJ / KmolHv =13508.1647149056BTU/lb mol
Pgina &P
Ejemplo
0
179
264
311
307
276
180
127
0
xA
DHS
Calor de Mezcla CS2 - CCl4 25 C
Construccin
Disulfuro de carbono ( A ) - Tetracloruro de Carbono ( B )
Datos de equilibrio del sistema a 1 atmsfera de presin
T Cxy
76.700.000.000x =fraccin molar del CS2 en el lquido
73.700.050.120y =fraccin molar del CS2 en el vapor
70.600.100.227
68.200.150.325
65.900.200.412
64.000.250.489
62.200.300.550
60.050.350.599
59.000.400.642
57.500.450.682
56.000.500.720
54.800.550.755
53.700.600.787
52.500.650.817
51.600.700.846
50.500.750.873
49.600.800.898
48.700.850.924
47.900.900.950
46.900.950.976
46.500.970.986
46.301.001.000
a) Capacidad calorfica de solucinb) Calores latentes molares de vaporizacin
CLi . Mwi =(C1 + C2 . T + C3 . T2 + C4 . T3 + C5 . T4)/1000C2 + C3 . Tr + C4 . Tr2
li . Mwi =C1 (1 - Tr )/1000KJ / Kmol
KJ/Kmol - KT = K
CS2CCl4CS2CCl4
C18.5600E+04-7.5270E+05C13.4960E+074.3252E+07
C2-1.2200E+028.9661E+03C20.29860.37688
C35.6050E-01-3.0394E+01C300
C4-1.4520E-033.4455E-02C400
C52.0080E-060.0000E+00
Tc K552.00556.35
c) Calores de mezcla a 25 C DHs
xBxAKJ/gmol mixKJ/Kmol
1.00000.00000.00000.000
0.81530.18470.1790179.000
0.66930.33070.2640264.000
0.53930.46070.3110311.000
0.40010.59990.3070307.000
0.28380.71620.2760276.000
0.14250.85750.1800180.000
0.09340.90660.1270127.000
0.00001.00000.00000.000
xDHs
0.000.00
0.0557.96
0.10107.92
0.15151.49
0.20189.59
0.25222.71
0.30250.99
0.35274.38
0.40292.68
0.45305.66
0.50313.04
0.55314.59
0.60310.08
0.65299.26
0.70281.87
0.75257.54
0.80225.72
0.85185.56
0.90135.83
0.9574.73
0.9746.57
1.000.00
DHs =- 1888.8191 x6 + 5483.3753 x5 - 6493.4512 x4 + 3684.4967 x3 - 2037.5618 x2 + 1251.6472 x + 0.0471
R2 =0.9997
Datos entalpa - concentracin
T CxCLA . MWACLB . MWBCL . MwpromDHsHLyCLA . MWACLB . MWBlAlBHG
76.700.0077.65338133.56703133.567030.006905.420.00077.65338133.5670325900.1729770.5236675.94
73.700.0577.56863133.39144130.6003057.966418.190.12077.56863133.3914426014.3529932.7935632.51
70.600.1077.48300133.22388127.64979107.925928.750.22777.48300133.2238826131.1130098.9634696.28
68.200.1577.41803133.10338124.75058151.495540.720.32577.41803133.1033826220.6830226.5733892.90
65.900.2077.35685132.99508121.86744189.595173.970.41277.35685132.9950826305.8430348.0333184.60
64.000.2577.30710132.91070119.00980222.714864.090.48977.30710132.9107026375.7030447.7632579.63
62.200.3077.26062132.83482116.16256250.994572.240.55077.26062132.8348226441.4930541.7532091.02
60.050.3577.20593132.74915113.30903274.384245.860.59977.20593132.7491526519.5730653.4031663.97
59.000.4077.17955132.70921110.49735292.684049.590.64277.17955132.7092126557.5130707.6831343.28
57.500.4577.14222132.65423107.67383305.663805.060.68277.14222132.6542326611.4930784.9431019.49
56.000.5077.10533132.60162104.85347313.043563.500.72077.10533132.6016226665.2130861.8930712.25
54.800.5577.07612132.56117102.04439314.593355.520.75577.07612132.5611726708.0030923.2330442.70
53.700.6077.04958132.5253499.23989310.083158.260.78777.04958132.5253426747.0930979.2730199.00
52.500.6577.02090132.4875796.43423299.262951.200.81777.02090132.4875726789.5831040.2229964.66
51.600.7076.99956132.4601193.63772281.872772.640.84676.99956132.4601126821.3431085.8029753.44
50.500.7576.97368132.4275490.83715257.542573.890.87376.97368132.4275426860.0431141.3629546.19
49.600.8076.95268132.4016888.04248225.722391.560.89876.95268132.4016826891.6131186.7029361.88
48.700.8576.93182132.3765185.24852185.562205.950.92476.93182132.3765126923.0931231.9329173.71
47.900.9076.91341132.3546982.45753135.832024.110.95076.91341132.3546926951.0031272.0428991.85
46.900.9576.89056132.3281479.6624374.731819.330.97676.89056132.3281426985.7931322.0728805.68
46.500.9776.88147132.3177478.5445546.571735.270.98676.88147132.3177426999.6831342.0428732.88
46.301.0076.87693132.3125876.876930.001637.481.00076.87693132.3125827006.6231352.0228644.10
to =25 CMwA =76.13Kg/KmolHL =KJ / Kmol
MwB =153.84Kg/KmolHG =KJ / Kmol
Construccin
xA
DHS
Calor de Mezcla CS2 - CCl4 25 C
y = -1888.8x6 + 5483.4x5 - 6493.5x4 + 3684.5x3 - 2037.6x2 + 1251.6x + 0.0471R2 = 0.9997
Diagrama
x , y
T
6905.41565366436675.9394548977
6418.191623613835632.5142124651
5928.754842372234696.2802467973
5540.716668231433892.8951741159
5173.972411151233184.5952615494
4864.092304773832579.6263442666
4572.239979459932091.0168818703
4245.861679149531663.9674949602
4049.594475872531343.28222393
3805.058552525631019.4862457691
3563.501995391630712.2536617052
3355.516316812230442.6973607963
3158.260479933930198.9964103443
2951.200826296329964.6560527211
2772.636249922729753.4442456638
2573.891150807129546.1855607511
2391.564746240529361.8767877595
2205.953770019129173.7125076042
2024.10919926128991.8492814184
1819.334177726728805.6793952847
1735.273408156228732.8780820646
1637.478653480228644.09628704
x , y
H
Diagrama Entalpa - Concentracin CS2 - CCl4
-
Grfico1
0
179
264
311
307
276
180
127
0
xA
DHS
Calor de Mezcla CS2 - CCl4 25 C
y = -1888.8x6 + 5483.4x5 - 6493.5x4 + 3684.5x3 - 2037.6x2 + 1251.6x + 0.0471R2 = 0.9997
Ecuaciones
Clculo de Entalpas Molares
Lquido saturado o subenfriado
HL = CL . Mwprom (tL - tO) + DHs
HL =Entalpa molar de un lquido
CL =Capacidad calorfica de la solucin
CL debe evaluarse a la temperatura promedio entre tL y to.
Mwprom = Peso molecular promedio de la solucin
Mwprom = MwA . xA + MwB . xB
MwA = Peso molecular de A
MwB = Peso molecular de B
Cuando no se tiene informacin sobre CL, como una aproximacin se puede calcular CL . Mwprom
CL . Mwprom = CLA . MwA . xA + CLB . MwB . xB
CLA = Capacidad calorfica del componente A como lquido puro
CLB = Capacidad calorfica del componente B como lquido puro
CLA y CLB deben evaluarse a la temperatura promedio entre tL y to
tL =Temperatura de la solucin
Lquido saturadotL = Temperatura de burbuja
Lquido subenfriadotL < Temperatura de burbuja
to =Temperatura de referencia
DHs =Calor integral de solucin o calor de mezcla
La temperatura a la cual estn disponibles los datos de calor de mezcla debe utilizarse como temperatura de referencia
Vapor saturado o sobrecalentado
HV = yA [ CLA . MwA (tV - tO) + lA . MwA ] + yB [ CLB . MwB (tV - tO) + lB . MwB ]
HV =Entalpa molar de un vapor
CLA = Capacidad calorfica del componente A como lquido puro
CLB = Capacidad calorfica del componente B como lquido puro
CLA y CLB deben evaluarse a la temperatura promedio entre tG y to
MwA = Peso molecular de A
MwB = Peso molecular de B
lA = Calor latente de vaporizacin de A
lB = Calor latente de vaporizacin de B
Los calores latentes de vaporizacin deben evaluarse a tG
tV =Temperatura de la mezcla en fase vapor
Vapor saturadotG = Temperatura de roco
Vapor sobrecalentadotG > Temperatura de roco
to =Temperatura de referencia
Pgina &P
Ejemplo
Construccin de datos entalpa - concentracin para el sistema CS2 ( A )- CCl4 ( B ) a 1 atm.
a) Capacidad calorfica de solucin
CL . Mwprom = CLA . MwA . xA + CLB . MwB . xB
CLi . Mwi =C1 + C2 . T + C3 . T2 + C4 . T3 + C5 . T4J/Kmol - KT = K
C1C2C3C4C5
ACS28.5600E+04-1.2200E+025.6050E-01-1.4520E-032.0080E-06
BCCl4-7.5270E+058.9661E+03-3.0394E+013.4455E-020.0000E+00
b) Calores latentes molares de vaporizacin
C2 + C3 . Tr + C4 . Tr2
li =C1 (1 - Tr )J / Kmol
C1C2C3C4Tc
ACS23.4960E+070.289600552.0 K
BCCl44.1860E+070.358400556.35 K
c) Calores de mezcla a 25 C DHs
xBxAKJ/gmol mixKJ/Kmol
1.00000.00000.00000.000
0.81530.18470.1790179.000
0.66930.33070.2640264.000
0.53930.46070.3110311.000
0.40010.59990.3070307.000
0.28380.71620.2760276.000
0.14250.85750.1800180.000
0.09340.90660.1270127.000
0.00001.00000.00000.000
xDHs
0.000.00
0.0557.96
0.10107.92
0.15151.49
0.20189.59
0.25222.71
0.30250.99
0.35274.38
0.40292.68
0.45305.66
0.50313.04
0.55314.59
0.60310.08
0.65299.26
0.70281.87
0.75257.54
0.80225.72
0.85185.56
DHs =- 1888.8191 x6 + 5483.3753 x5 - 6493.4512 x4 + 3684.4967 x3 - 2037.5618 x2 + 1251.6472 x + 0.04710.90135.83
0.9574.73
R2 =0.99970.9746.57
1.000.00
xDHs
0.000.00
0.0557.96
0.10107.92
0.15151.49
0.20189.59
0.25222.71
0.30250.99
0.35274.38
0.40292.68
0.45305.66
0.50313.04
0.55314.59
0.60310.08
0.65299.26
0.70281.87
0.75257.54
0.80225.72
0.85185.56
0.90135.83
0.9574.73
0.9746.57
1.000.00
Lquido saturado
HL = CL . Mwprom (tL - tO) + DHs
x =0.30
tL =62.2 C =335.35K
to =25 C =298.15K
DHs =292.68KJ / Kmol
CL debe evaluarse a tprom y en funcin de la concentracin. Como no se tiene datos de CL, se calcular como una aproximacin CL . Mwprom
CL . Mwprom = CLA . MwA xA + CLB . MwB . xB
CLA y CLB se calcularn a la tprom
tprom = ( tL+tO ) / 2 =316.75K
CLA . MwA =7.72606E+04J / Kmol - K =77.26062KJ / Kmol - K
CLB . MwB =1.32835E+05J / Kmol - K =132.83482KJ / Kmol - K
CL . Mwprom =116.16256KJ / Kmol - K
HL =116.16256 * ( 62.2 - 25 ) + 292.68 =4613.9319KJ / Kmol
Vapor saturado
HV = y [ CLA . MwA (tv - tO) + lA . MwA ] + (1 - y) [ CLB . MwB (tv - tO) + lB . MwB ]
y =0.30
tv =68.8 C =341.95
to =25 C =298.15K
CLA y CLB se calcularn a la tprom
tprom =( tL + tO ) / 2 =320.05 K
CLA . MwA =7.74342E+04J / Kmol - K =77.43416KJ / Kmol - K
CLB . MwB =1.33133E+05J / Kmol - K =133.13277KJ / Kmol - K
lA y lB se calcularn a tvTrA =0.6195TrB=0.6146
lA . MwA =2.64272E+07J / Kmol =2.64272E+04KJ / Kmol
lB . MwB =2.97425E+07J / Kmol =2.97425E+04KJ / Kmol
Hv =31413.9875KJ / KmolHv =13508.1647149056BTU/lb mol
Pgina &P
Ejemplo
0
179
264
311
307
276
180
127
0
xA
DHS
Calor de Mezcla CS2 - CCl4 25 C
Construccin
Disulfuro de carbono ( A ) - Tetracloruro de Carbono ( B )
Datos de equilibrio del sistema a 1 atmsfera de presin
T Cxy
76.700.000.000x =fraccin molar del CS2 en el lquido
73.700.050.120y =fraccin molar del CS2 en el vapor
70.600.100.227
68.200.150.325
65.900.200.412
64.000.250.489
62.200.300.550
60.050.350.599
59.000.400.642
57.500.450.682
56.000.500.720
54.800.550.755
53.700.600.787
52.500.650.817
51.600.700.846
50.500.750.873
49.600.800.898
48.700.850.924
47.900.900.950
46.900.950.976
46.500.970.986
46.301.001.000
a) Capacidad calorfica de solucinb) Calores latentes molares de vaporizacin
CLi . Mwi =(C1 + C2 . T + C3 . T2 + C4 . T3 + C5 . T4)/1000C2 + C3 . Tr + C4 . Tr2
li . Mwi =C1 (1 - Tr )/1000KJ / Kmol
KJ/Kmol - KT = K
CS2CCl4CS2CCl4
C18.5600E+04-7.5270E+05C13.4960E+074.3252E+07
C2-1.2200E+028.9661E+03C20.29860.37688
C35.6050E-01-3.0394E+01C300
C4-1.4520E-033.4455E-02C400
C52.0080E-060.0000E+00
Tc K552.00556.35
c) Calores de mezcla a 25 C DHs
xBxAKJ/gmol mixKJ/Kmol
1.00000.00000.00000.000
0.81530.18470.1790179.000
0.66930.33070.2640264.000
0.53930.46070.3110311.000
0.40010.59990.3070307.000
0.28380.71620.2760276.000
0.14250.85750.1800180.000
0.09340.90660.1270127.000
0.00001.00000.00000.000
xDHs
0.000.00
0.0557.96
0.10107.92
0.15151.49
0.20189.59
0.25222.71
0.30250.99
0.35274.38
0.40292.68
0.45305.66
0.50313.04
0.55314.59
0.60310.08
0.65299.26
0.70281.87
0.75257.54
0.80225.72
0.85185.56
0.90135.83
0.9574.73
0.9746.57
1.000.00
DHs =- 1888.8191 x6 + 5483.3753 x5 - 6493.4512 x4 + 3684.4967 x3 - 2037.5618 x2 + 1251.6472 x + 0.0471
R2 =0.9997
Datos entalpa - concentracin
T CxCLA . MWACLB . MWBCL . MwpromDHsHLyCLA . MWACLB . MWBlAlBHG
76.700.0077.65338133.56703133.567030.006905.420.00077.65338133.5670325900.1729770.5236675.94
73.700.0577.56863133.39144130.6003057.966418.190.12077.56863133.3914426014.3529932.7935632.51
70.600.1077.48300133.22388127.64979107.925928.750.22777.48300133.2238826131.1130098.9634696.28
68.200.1577.41803133.10338124.75058151.495540.720.32577.41803133.1033826220.6830226.5733892.90
65.900.2077.35685132.99508121.86744189.595173.970.41277.35685132.9950826305.8430348.0333184.60
64.000.2577.30710132.91070119.00980222.714864.090.48977.30710132.9107026375.7030447.7632579.63
62.200.3077.26062132.83482116.16256250.994572.240.55077.26062132.8348226441.4930541.7532091.02
60.050.3577.20593132.74915113.30903274.384245.860.59977.20593132.7491526519.5730653.4031663.97
59.000.4077.17955132.70921110.49735292.684049.590.64277.17955132.7092126557.5130707.6831343.28
57.500.4577.14222132.65423107.67383305.663805.060.68277.14222132.6542326611.4930784.9431019.49
56.000.5077.10533132.60162104.85347313.043563.500.72077.10533132.6016226665.2130861.8930712.25
54.800.5577.07612132.56117102.04439314.593355.520.75577.07612132.5611726708.0030923.2330442.70
53.700.6077.04958132.5253499.23989310.083158.260.78777.04958132.5253426747.0930979.2730199.00
52.500.6577.02090132.4875796.43423299.262951.200.81777.02090132.4875726789.5831040.2229964.66
51.600.7076.99956132.4601193.63772281.872772.640.84676.99956132.4601126821.3431085.8029753.44
50.500.7576.97368132.4275490.83715257.542573.890.87376.97368132.4275426860.0431141.3629546.19
49.600.8076.95268132.4016888.04248225.722391.560.89876.95268132.4016826891.6131186.7029361.88
48.700.8576.93182132.3765185.24852185.562205.950.92476.93182132.3765126923.0931231.9329173.71
47.900.9076.91341132.3546982.45753135.832024.110.95076.91341132.3546926951.0031272.0428991.85
46.900.9576.89056132.3281479.6624374.731819.330.97676.89056132.3281426985.7931322.0728805.68
46.500.9776.88147132.3177478.5445546.571735.270.98676.88147132.3177426999.6831342.0428732.88
46.301.0076.87693132.3125876.876930.001637.481.00076.87693132.3125827006.6231352.0228644.10
to =25 CMwA =76.13Kg/KmolHL =KJ / Kmol
MwB =153.84Kg/KmolHG =KJ / Kmol
Construccin
xA
DHS
Calor de Mezcla CS2 - CCl4 25 C
y = -1888.8x6 + 5483.4x5 - 6493.5x4 + 3684.5x3 - 2037.6x2 + 1251.6x + 0.0471R2 = 0.9997
Diagrama
x , y
T
6905.41565366436675.9394548977
6418.191623613835632.5142124651
5928.754842372234696.2802467973
5540.716668231433892.8951741159
5173.972411151233184.5952615494
4864.092304773832579.6263442666
4572.239979459932091.0168818703
4245.861679149531663.9674949602
4049.594475872531343.28222393
3805.058552525631019.4862457691
3563.501995391630712.2536617052
3355.516316812230442.6973607963
3158.260479933930198.9964103443
2951.200826296329964.6560527211
2772.636249922729753.4442456638
2573.891150807129546.1855607511
2391.564746240529361.8767877595
2205.953770019129173.7125076042
2024.10919926128991.8492814184
1819.334177726728805.6793952847
1735.273408156228732.8780820646
1637.478653480228644.09628704
x , y
H
Diagrama Entalpa - Concentracin CS2 - CCl4
-
Calor de mezcla Etanol - AguaT = 42.05 CPgina 160Tabla N 6 100 - nDHS = Q . -------- 100 n = % molar agua
xaguaKJ/gmol etanol0.95-6.23600.90-4.52800.85-3.28100.80-2.35600.75-1.69100.70-1.20000.65-0.87000.60-0.64900.55-0.46500.50-0.3430
xaguaKJ/gmol etanol0.45-0.24300.40-0.16700.35-0.10900.30-0.07500.25-0.04200.20-0.02300.15-0.01300.10-0.00630.05-0.0029
-
xaguaDHs BTU/lbmol mezcla1.000.0000.95-134.0470.90-194.6640.85-211.5810.80-202.5750.75-181.7450.70-154.7680.65-130.9080.60-111.6050.55-89.9590.50-73.730
xagua DHs BTU/lbmol mezcla0.45-57.4580.40-43.0770.35-30.4590.30-22.5700.25-13.5420.20-7.9100.15-4.7510.10-2.4380.05-1.1840.000.000
-
xetanolDHs BTU/lbmol mezcla0.000.0000.05-134.0470.10-194.6640.15-211.5810.20-202.5750.25-181.7450.30-154.7680.35-130.9080.40-111.6050.45-89.9590.50-73.730
xetanolDHs BTU/lbmol mezcla0.55-57.4580.60-43.0770.65-30.4590.70-22.5700.75-13.5420.80-7.9100.85-4.7510.90-2.4380.95-1.1841.000.000
-
Grfico1
0-211.5813609114-111.6052449306
-134.0466693735-202.5746972701-89.9591583272
-194.6643101101-181.7454441233-73.7299672789
-211.5813609114-154.7684444338-57.4577849961
-130.9083092503-43.0772170341
-111.6052449306-30.4592896893
-22.5703981466
-13.542238888
-7.91038716
-4.7505314194
-2.4376029998
-1.1844085123
0
DHS Etanol - Agua 42.05 C
Datos
xAyAT C00
0.00000.0000100.0011
0.01900.170095.50
0.07210.389189.00
0.09660.437586.70
0.12380.470485.30
0.16610.508984.10
0.23370.544582.70
0.26080.558082.30
0.32730.582681.50
0.39650.612280.70
0.50790.656479.80
0.51980.659979.7000
0.57320.684179.3011
0.67630.738578.74
0.74720.781578.41
0.89430.894378.15
Etanol - Agua 42.05 C
xBxAQ KJ/gmol ADHs BTU/lbmol mezcla
1.000.000.00000.000
0.950.05-6.2360-134.047
0.900.10-4.5280-194.664
0.850.15-3.2810-211.581
0.800.20-2.3560-202.575
0.750.25-1.6910-181.745
0.700.30-1.2000-154.768
0.650.35-0.8700-130.908
0.600.40-0.6490-111.605
0.550.45-0.4650-89.959
0.500.50-0.3430-73.730
0.450.55-0.2430-57.458
0.400.60-0.1670-43.077
0.350.65-0.1090-30.459
0.300.70-0.0750-22.570
0.250.75-0.0420-13.542
0.200.80-0.0230-7.910
0.150.85-0.0130-4.751
0.100.90-0.0063-2.438
0.050.95-0.0029-1.184
0.001.000.00000.000
0.00 - 0.15DHS = - 3.9638 E+04 x3 + 2.0631 E+04 x2 - 3.6134 E+03 x - 1.7508 E -11
0.15- 0.40DHS = 304377.9407 x5- 404404.2131 x4 + 200403.6399 x3 -44920.8245 x2 + 4725.6825 x - 404.4615
0.40 - 1.00DHS = - 9026.2367 x6 + 40170.9625 x5 - 72534.4323 x4 + 68074.4801 x3 - 35447.5407 x2
+ 10128.0566 x - 1365.3326
Datos
000
000
000
000
00
00
0
0
0
0
0
0
0
DHS Etanol - Agua 42.05 C
Tablas
Sistema Etanol - aguaKJ /Kmol
T CT KxCL . MwpromDHsHLyCLA . MwACLB . MwBlA . MwAlB . MwBHVxHLyHV
100.00373.150.000018.031370.00001880.852260.000032.0511618.0313715844.849417552.254119433.10640.00004371.93380.000045171.1473
95.50368.650.019018.28468-61.47871697.690220.170031.7504018.0238716013.212417642.139819323.80600.01903946.18410.170044917.0847
89.00362.150.072118.97369-168.13431435.332360.389131.3247618.0139816250.395117769.251519138.32240.07213336.34820.389144485.9386
86.70359.850.096619.28258-192.26591357.475350.437531.1766218.0107616332.703317813.479719076.10120.09663155.37400.437544341.3091
85.30358.450.123819.62795-206.34881321.687430.470431.0870818.0088716382.405117840.213219035.38330.12383072.18700.470444246.6627
84.10357.250.166120.16716-209.82821316.624410.508931.0107118.0073016424.770617863.015718994.93890.16613060.41830.508944152.6519
82.70355.850.233721.02411-189.66761348.666410.544530.9220518.0055116473.925617889.488918950.78670.23373134.89810.544544050.0227
82.30355.450.260821.36719-176.09851371.954700.558030.8968118.0050116487.916717897.027218936.38460.26083189.03040.558044016.5459
81.50354.650.327322.20735-140.94591435.997960.582630.8464318.0040316515.828817912.070018908.38180.32733337.89530.582643951.4549
80.70353.850.396523.07555-113.03561492.330390.612230.7962218.0030616543.647917927.068018877.48140.39653468.83690.612243879.6287
79.80352.950.507924.47158-70.38921592.454840.656430.7399118.0020016574.834317943.887318836.61770.50793701.57050.656443784.6435
79.70352.850.519824.61986-66.58201601.906070.659930.7336618.0018816578.292317945.752618832.73640.51983723.53930.659943775.6216
79.30352.450.573225.28524-50.67791644.697280.684130.7087118.0014216592.110017953.207118811.94510.57323823.00500.684143727.2934
78.74351.890.676326.57157-25.80011729.039320.738530.6738318.0007816611.416717963.624718771.91710.67634019.05330.738543634.2504
78.41351.560.747227.45466-14.04561782.807190.781530.6533218.0004116622.773217969.753518742.34530.74724144.03360.781543565.5126
78.15351.300.894329.30144-2.69691901.310600.894330.6371818.0001116631.709917974.577018677.65840.89434419.48800.894343415.1515
0 - 0.15DHS = - 3.9638 E+04 x3 + 2.0631 E+04 x2 - 3.6134 E+03 x - 1.7508 E -11
0.15 - 0.40DHS = 304377.9407 x5- 404404.2131 x4 + 200403.6399 x3 -44920.8245 x2 + 4725.6825 x - 404.4615
0.40 - 1.0DHS = - 9026.2367 x6 + 40170.9625 x5 - 72534.4323 x4 + 68074.4801 x3 - 35447.5407 x2 + 10128.0566 X - 1365.3326
CLi . Mwi =( C1 + C2 . T + C3 . T2 + C4 . T3 + C5 . T4 ) . 2,390059E-04BTU / lb mol - Fto =42.05 C =315.20 K
T = K
C1C2C3C4C5
etanol1.0264E+05-1.3963E+02-3.0341E-022.0386E-030.0000E+00
agua2.7637E+05-2.0901E+038.1250E+00-1.4116E-029.3701E-06
C2 + C3 . Tr + C4 . Tr2
li . Mwi =C1 (1 - Tr )* 4,302106E-04BTU / lb mol
C1C2C3C4Tc K
etanol5.6900E+070.33590.00000.0000513.92
agua5.2053E+070.3199-0.21200.25795647.13
Diagramas
Diagramas
1880.852258499419433.1063618257
1697.690223068219323.8059724818
1435.332362196819138.3223529462
1357.475349521419076.1011718106
1321.68742872519035.3833164666
1316.624414461618994.9388665644
1348.666409451318950.7866909009
1371.954697611318936.3846144607
1435.997955137118908.3817906574
1492.330388816518877.4814038358
1592.454844743818836.6177483892
1601.906070551818832.73643491
1644.697278271818811.9451328083
1729.039319125418771.9170616742
1782.80719370818742.3453023277
1901.310601254318677.6583963037
Diagrama H-x-y Etanol-Agua BTU/lb mol
00
0.171
0.3891
0.4375
0.4704
0.5089
0.5445
0.558
0.5826
0.6122
0.6564
0.6599
0.6841
0.7385
0.7815
0.8943
100100
95.595.5
8989
86.786.7
85.385.3
84.184.1
82.782.7
82.382.3
81.581.5
80.780.7
79.879.8
79.779.7
79.379.3
78.7478.74
78.4178.41
78.1578.15
-
Construccin del diagrama entalpa-concentracin para el Sistema Cloroformo (A) - Benceno (B) a 760 mm Hg
-
Datos de equilibrio a 760 mm Hg
T Cxy80.600.000.000080.000.050.063079.500.100.130079.100.150.200678.300.200.272277.900.250.342777.100.300.414676.800.350.484875.900.400.548875.300.450.605274.700.500.6586
T Cxy74.700.500.658673.400.550.710272.900.600.755872.000.650.796671.000.700.834369.800.750.870768.800.800.904766.200.850.932964.100.900.957263.000.950.979461.401.001.0000
-
Grfico2
80.680.6
8080
79.579.5
79.179.1
78.378.3
77.977.9
77.177.1
76.876.8
75.975.9
75.375.3
74.774.7
73.473.4
72.972.9
7272
7171
69.869.8
68.868.8
66.266.2
64.164.1
6363
61.461.4
Ejemplo
Entalpa - concentracin para el sistema Cloroformo ( A ) - Benceno ( B ) a 1 atm.
a) Capacidad calorfica de solucin
CL . Mwprom = CLA . MwA . xA + CLB . MwB . xB
CLi . Mwi =C1 + C2 . T + C3 . T2 + C4 . T3 + C5 . T4J/Kmol - KT = K
C1C2C3C4C5
ACloroformo1.2944E+05-1.6950E+026.4781E-010.0000E+000.0000E+00
BBenceno1.2485E+05-1.6634E+024.3209E-010.0000E+000.0000E+00
b) Calores latentes molares de vaporizacin
C2 + C3 . Tr + C4 . Tr2
li =C1 (1 - Tr )J / Kmol
C1C2C3C4Tc
ACloroformo4.1860E+070.358400536.40
BBenceno4.7500E+070.452380.0534-0.1181562.16
c) Calores de mezcla a 18 C DHs
% peso AxAJ/g mezclaKJ/Kmol
00.00000.000.00
100.0678-1.13-91.43
200.1406-2.01-168.66
300.2190-2.64-230.08
400.3037-3.10-281.00
500.3955-3.31-312.58
600.4953-3.31-326.22
700.6042-3.18-327.70
800.7235-2.89-312.05
900.8548-2.05-232.46
1001.00000.000.00
xDHs
0.000.00
0.0557.96
0.10107.92
0.15151.49
0.20189.59
0.25222.71
0.30250.99
0.35274.38
0.40292.68
0.45305.66
0.50313.04
0.55314.59
0.60310.08
0.65299.26
0.70281.87
0.75257.54
0.85185.56
DHs =- 436.5958 x6 + 4003.4297 x5 - 5617.3018 x4 + 1994.4031 x3 + 1487.6691 x2 - 1430.9938 x - 0.49290.90135.83
0.9574.73
R2 =0.99990.9746.57
1.000.00
xDHs
0.000.00
0.05-68.11
0.10-127.24
0.15-177.48
0.20-218.96
0.25-252.24
0.30-278.14
0.35-297.66
0.40-311.82
0.45-321.54
0.50-327.57
0.55-330.32
0.60-329.80
0.65-325.52
0.70-316.37
0.75-300.56
0.80-275.50
0.85-237.77
0.90-183.01
0.95-105.85
1.000.00
Lquido
HL = CL . Mwprom (tL - tO) + DHs
T Cxy
80.600.000.0000
80.000.050.0630
79.500.100.1300
79.100.150.2006
78.300.200.2722
77.900.250.3427
77.100.300.4146
76.800.350.4848
75.900.400.5488
75.300.450.6052
74.700.500.6586
73.400.550.7102
72.900.600.7558
72.000.650.7966
71.000.700.8343
69.800.750.8707
68.800.800.9047
66.200.850.9329
64.100.900.9572
63.000.950.9794
61.401.001.0000
x =0.30to =18 C =291.15K
tL =25 C =298.15KDHs =-278.14KJ / Kmol
CL debe evaluarse a tprom y en funcin de la concentracin. Como no se tiene datos de CL, se calcular como una aproximacin CL . Mwprom
CL . Mwprom = CLA . MwA xA + CLB . MwB . xB
CLA y CLB se calcularn a la tprom
tprom = ( tL+tO ) / 2 =294.65K
CLA . MwA =1.35739E+05J / Kmol - K =135.73880KJ / Kmol - K
CLB . MwB =1.13351E+05J / Kmol - K =113.35138KJ / Kmol - K
CL . Mwprom =120.06760KJ / Kmol - K
HL =120.07660 * ( 25 - 18 ) - 278.14 =562.3312KJ / Kmol
T Cxy
80.600.000.0000
80.000.050.0630
79.500.100.1300
79.100.150.2006
78.300.200.2722
77.900.250.3427
77.100.300.4146
76.800.350.4848
75.900.400.5488
75.300.450.6052
74.700.500.6586
73.400.550.7102
72.900.600.7558
72.000.650.7966
71.000.700.8343
69.800.750.8707
68.800.800.9047
66.200.850.9329
64.100.900.9572
63.000.950.9794
61.401.001.0000
Vapor saturado
HV = y [ CLA . MwA (tv - tO) + lA . MwA ] + (1 - y) [ CLB . MwB (tv - tO) + lB . MwB ]
y =0.30
tv =68.8 C =341.95
to =25 C =298.15K
CLA y CLB se calcularn a la tprom
tprom =( tL + tO ) / 2 =320.05 K
CLA . MwA =1.29440E+05J / Kmol - K =129.44000KJ / Kmol - K
CLB . MwB =1.24850E+05J / Kmol - K =124.85000KJ / Kmol - K
lA y lB se calcularn a tvTrA =0.6195TrB=0.6146
lA . MwA =0.00000E+00J / Kmol =0.00000E+00KJ / Kmol
lB . MwB =0.00000E+00J / Kmol =0.00000E+00KJ / Kmol
Hv =2890.5983KJ / KmolHv =1242.9710797898BTU/lb mol
Pgina &P
Ejemplo
xA
DHS
Calor de Mezcla Cloroformo-Benceno 18 C
Construccin
Diagrama
Disulfuro de carbono ( A ) - Tetracloruro de Carbono ( B )
Datos de equilibrio del sistema a 1 atmsfera de presin
T Cxy
80.600.000.0000x =fraccin molar del CS2 en el lquido
80.000.050.0630y =fraccin molar del CS2 en el vapor
79.500.100.1300
79.100.150.2006
78.300.200.2722
77.900.250.3427
77.100.300.4146
76.800.350.4848
75.900.400.5488
75.300.450.6052
74.700.500.6586
73.400.550.7102
72.900.600.7558
72.000.650.7966
71.000.700.8343
69.800.750.8707
68.800.800.9047
66.200.850.9329
64.100.900.9572
63.000.950.9794
61.401.001.0000
a) Capacidad calorfica de solucinb) Calores latentes molares de vaporizacin
CLi . Mwi =(C1 + C2 . T + C3 . T2 + C4 . T3 + C5 . T4)/1000C2 + C3 . Tr + C4 . Tr2
li . Mwi =C1 (1 - Tr )/1000KJ / Kmol
KJ/Kmol - KT = K
CloroformoBencenoCloroformoBenceno
C11.2944E+051.2485E+05C14.1860E+074.7500E+07
C2-1.6950E+02-1.6634E+02C20.35840.45238Tc
C36.4781E-014.3209E-01C300.0534
C40.0000E+000.0000E+00C40-0.1181
C50.0000E+000.0000E+00
Tc K536.4562.16
c) Calores de mezcla a 25 C DHs
xBxAKJ/gmol mixKJ/Kmol
1.00000.00000.00000.000
0.81530.18470.1790179.000
0.66930.33070.2640264.000
0.53930.46070.3110311.000
0.40010.59990.3070307.000
0.28380.71620.2760276.000
0.14250.85750.1800180.000
0.09340.90660.1270127.000
0.00001.00000.00000.000
xDHs
0.000.00
0.0557.96
0.10107.92
0.15151.49
0.20189.59
0.25222.71
0.30250.99
0.35274.38
0.40292.68
0.45305.66
0.50313.04
0.55314.59
0.60310.08
0.65299.26
0.70281.87
0.75257.54
0.80225.72
0.85185.56
0.90135.83
0.9574.73
0.9746.57
1.000.00
DHs =- 1888.8191 x6 + 5483.3753 x5 - 6493.4512 x4 + 3684.4967 x3 - 2037.5618 x2 + 1251.6472 x + 0.0471
R2 =0.9997
Datos entalpa - concentracin
T CxCLA . MWACLB . MWBCL . MwpromDHsHLyCLA . MWACLB . MWBlAlBHv
80.600.000.000000.000000.000000.000.000.00000.000000.000000.000.000.00
80.000.050.000000.000000.0000057.960.000.06300.000000.000000.000.000.00
79.500.100.000000.000000.00000107.920.000.13000.000000.000000.000.000.00
79.100.150.000000.000000.00000151.490.000.20060.000000.000000.000.000.00
78.300.200.000000.000000.00000189.590.000.27220.000000.000000.000.000.00
77.900.250.000000.000000.00000222.710.000.34270.000000.000000.000.000.00
77.100.300.000000.000000.00000250.990.000.41460.000000.000000.000.000.00
76.800.350.000000.000000.00000274.380.000.48480.000000.000000.000.000.00
75.900.400.000000.000000.00000292.680.000.54880.000000.000000.000.000.00
75.300.450.000000.000000.00000305.660.000.60520.000000.000000.000.000.00
74.700.500.000000.000000.00000313.040.000.65860.000000.000000.000.000.00
73.400.550.000000.000000.00000314.590.000.71020.000000.000000.000.000.00
72.900.600.000000.000000.00000310.080.000.75580.000000.000000.000.000.00
72.000.650.000000.000000.00000299.260.000.79660.000000.000000.000.000.00
71.000.700.000000.000000.00000281.870.000.83430.000000.000000.000.000.00
69.800.750.000000.000000.00000257.540.000.87070.000000.000000.000.000.00
68.800.800.000000.000000.00000225.720.000.90470.000000.000000.000.000.00
66.200.850.000000.000000.00000185.560.000.93290.000000.000000.000.000.00
64.100.900.000000.000000.00000135.830.000.95720.000000.000000.000.000.00
63.000.950.000000.000000.0000074.730.000.97940.000000.000000.000.000.00
61.401.000.000000.000000.000000.000.001.00000.000000.000000.000.000.00
to =25 CMwA =76.13Kg/KmolHL =KJ / Kmol
MwB =153.84Kg/KmolHV =KJ / Kmol
Pgina &P
Diagrama
xA
DHS
Calor de Mezcla CS2 - CCl4 25 C
00
00
00
00
00
00
00
00
00
00
00
00
00
00
00
00
00
00
00
00
00
x , y
H
Diagrama Entalpa - Concentracin CS2 - CCl4
-
CLi. Mwi. = C1 + C2 . T + C3 . T2 + C4 . T3 + C5 . T4
C1C2C3C4C5Cloroformo1.2485E+05-1.6634E+024.3209E-010.0000E+000.0000E+00Benceno1.2944E+05-1.6950E+026.4781E-010.0000E+000.0000E+00
C1C2C3C4Tc KCloroformo4.1860E+070.358400536.40Benceno4.7500E+070.452380.0534-0.1181562.16
-
Calor de mezcla: DHs18 CPgina 158 % peso A/MwAxA = ------------------------- % peso A/MwA + % peso B/MwBDHs =( Q J /gmezcla ) * Mwprom J / g mol mezclaA CloroformoB Benceno
% peso cloroformo J/g mezcla00.0010-1.1320-2.0130-2.6440-3.1050-3.3160-3-3170-3.1880-2.8990-2.051000.00
-
Calor de mezcla: DHs 18 C
% peso CCl4 J/g mezcla00.0010-1.1320-2.0130-2.6440-3.1050-3.3160-3-3170-3.1880-2.8990-2.051000.00
xCCl4KJ/Kmol mezcla0.00000.000.0678-91.430.1406-168.660.2190-230.080.3037-281.000.3955-312.580.4953-326.220.6042-327.700.7235-312.050.8548-232.461.00000.00
-
DHs = - 436.5958 x6 + 4003.4297 x5 - 5617.3018 x4 + 1994.4031 x3 + 1487.6691 x2 - 1430.9938 x - 0.4929
Grfico1
0
-91.4254027954
-168.6645070725
-230.0755065697
-281.0048211474
-312.5830896101
-326.2199076219
-327.704137534
-312.0539087257
-232.4641095965
0
xA
DHS
Calor de Mezcla Cloroformo-Benceno 18 C
Ejemplo
Entalpa - concentracin para el sistema Cloroformo ( A ) - Benceno ( B ) a 1 atm.
a) Capacidad calorfica de solucin
CL . Mwprom = CLA . MwA . xA + CLB . MwB . xB
CLi . Mwi =C1 + C2 . T + C3 . T2 + C4 . T3 + C5 . T4J/Kmol - KT = K
C1C2C3C4C5
ACloroformo1.2944E+05-1.6950E+026.4781E-010.0000E+000.0000E+00
BBenceno1.2485E+05-1.6634E+024.3209E-010.0000E+000.0000E+00
b) Calores latentes molares de vaporizacin
C2 + C3 . Tr + C4 . Tr2
li =C1 (1 - Tr )J / Kmol
C1C2C3C4Tc
ACloroformo4.1860E+070.358400536.40
BBenceno4.7500E+070.452380.0534-0.1181562.16
c) Calores de mezcla a 18 C DHs
% peso AxAJ/g mezclaKJ/Kmol
00.00000.000.00
100.0678-1.13-91.43
200.1406-2.01-168.66
300.2190-2.64-230.08
400.3037-3.10-281.00
500.3955-3.31-312.58
600.4953-3.31-326.22
700.6042-3.18-327.70
800.7235-2.89-312.05
900.8548-2.05-232.46
1001.00000.000.00
xDHs
0.000.00
0.0557.96
0.10107.92
0.15151.49
0.20189.59
0.25222.71
0.30250.99
0.35274.38
0.40292.68
0.45305.66
0.50313.04
0.55314.59
0.60310.08
0.65299.26
0.70281.87
0.75257.54
0.85185.56
DHs =- 436.5958 x6 + 4003.4297 x5 - 5617.3018 x4 + 1994.4031 x3 + 1487.6691 x2 - 1430.9938 x - 0.49290.90135.83
0.9574.73
R2 =0.99990.9746.57
1.000.00
xDHs
0.000.00
0.05-68.11
0.10-127.24
0.15-177.48
0.20-218.96
0.25-252.24
0.30-278.14
0.35-297.66
0.40-311.82
0.45-321.54
0.50-327.57
0.55-330.32
0.60-329.80
0.65-325.52
0.70-316.37
0.75-300.56
0.80-275.50
0.85-237.77
0.90-183.01
0.95-105.85
1.000.00
Lquido
HL = CL . Mwprom (tL - tO) + DHs
T Cxy
80.600.000.0000
80.000.050.0630
79.500.100.1300
79.100.150.2006
78.300.200.2722
77.900.250.3427
77.100.300.4146
76.800.350.4848
75.900.400.5488
75.300.450.6052
74.700.500.6586
73.400.550.7102
72.900.600.7558
72.000.650.7966
71.000.700.8343
69.800.750.8707
68.800.800.9047
66.200.850.9329
64.100.900.9572
63.000.950.9794
61.401.001.0000
x =0.30to =18 C =291.15K
tL =25 C =298.15KDHs =-278.14KJ / Kmol
CL debe evaluarse a tprom y en funcin de la concentracin. Como no se tiene datos de CL, se calcular como una aproximacin CL . Mwprom
CL . Mwprom = CLA . MwA xA + CLB . MwB . xB
CLA y CLB se calcularn a la tprom
tprom = ( tL+tO ) / 2 =294.65K
CLA . MwA =1.35739E+05J / Kmol - K =135.73880KJ / Kmol - K
CLB . MwB =1.13351E+05J / Kmol - K =113.35138KJ / Kmol - K
CL . Mwprom =120.06760KJ / Kmol - K
HL =120.07660 * ( 25 - 18 ) - 278.14 =562.3312KJ / Kmol
T Cxy
80.600.000.0000
80.000.050.0630
79.500.100.1300
79.100.150.2006
78.300.200.2722
77.900.250.3427
77.100.300.4146
76.800.350.4848
75.900.400.5488
75.300.450.6052
74.700.500.6586
73.400.550.7102
72.900.600.7558
72.000.650.7966
71.000.700.8343
69.800.750.8707
68.800.800.9047
66.200.850.9329
64.100.900.9572
63.000.950.9794
61.401.001.0000
Vapor saturado
HV = y [ CLA . MwA (tv - tO) + lA . MwA ] + (1 - y) [ CLB . MwB (tv - tO) + lB . MwB ]
y =0.30
tv =68.8 C =341.95
to =25 C =298.15K
CLA y CLB se calcularn a la tprom
tprom =( tL + tO ) / 2 =320.05 K
CLA . MwA =1.29440E+05J / Kmol - K =129.44000KJ / Kmol - K
CLB . MwB =1.24850E+05J / Kmol - K =124.85000KJ / Kmol - K
lA y lB se calcularn a tvTrA =0.6195TrB=0.6146
lA . MwA =0.00000E+00J / Kmol =0.00000E+00KJ / Kmol
lB . MwB =0.00000E+00J / Kmol =0.00000E+00KJ / Kmol
Hv =2890.5983KJ / KmolHv =1242.9710797898BTU/lb mol
Pgina &P
Ejemplo
0
0
0
0
0
0
0
0
0
0
0
xA
DHS
Calor de Mezcla Cloroformo-Benceno 18 C
Construccin
00
00
00
00
00
00
00
00
00
00
00
00
00
00
00
00
00
00
00
00
00
Diagrama
Disulfuro de carbono ( A ) - Tetracloruro de Carbono ( B )
Datos de equilibrio del sistema a 1 atmsfera de presin
T Cxy
80.600.000.0000x =fraccin molar del CS2 en el lquido
80.000.050.0630y =fraccin molar del CS2 en el vapor
79.500.100.1300
79.100.150.2006
78.300.200.2722
77.900.250.3427
77.100.300.4146
76.800.350.4848
75.900.400.5488
75.300.450.6052
74.700.500.6586
73.400.550.7102
72.900.600.7558
72.000.650.7966
71.000.700.8343
69.800.750.8707
68.800.800.9047
66.200.850.9329
64.100.900.9572
63.000.950.9794
61.401.001.0000
a) Capacidad calorfica de solucinb) Calores latentes molares de vaporizacin
CLi . Mwi =(C1 + C2 . T + C3 . T2 + C4 . T3 + C5 . T4)/1000C2 + C3 . Tr + C4 . Tr2
li . Mwi =C1 (1 - Tr )/1000KJ / Kmol
KJ/Kmol - KT = K
CloroformoBencenoCloroformoBenceno
C11.2944E+051.2485E+05C14.1860E+074.7500E+07
C2-1.6950E+02-1.6634E+02C20.35840.45238Tc
C36.4781E-014.3209E-01C300.0534
C40.0000E+000.0000E+00C40-0.1181
C50.0000E+000.0000E+00
Tc K536.4562.16
c) Calores de mezcla a 25 C DHs
xBxAKJ/gmol mixKJ/Kmol
1.00000.00000.00000.000
0.81530.18470.1790179.000
0.66930.33070.2640264.000
0.53930.46070.3110311.000
0.40010.59990.3070307.000
0.28380.71620.2760276.000
0.14250.85750.1800180.000
0.09340.90660.1270127.000
0.00001.00000.00000.000
xDHs
0.000.00
0.0557.96
0.10107.92
0.15151.49
0.20189.59
0.25222.71
0.30250.99
0.35274.38
0.40292.68
0.45305.66
0.50313.04
0.55314.59
0.60310.08
0.65299.26
0.70281.87
0.75257.54
0.80225.72
0.85185.56
0.90135.83
0.9574.73
0.9746.57
1.000.00
DHs =- 1888.8191 x6 + 5483.3753 x5 - 6493.4512 x4 + 3684.4967 x3 - 2037.5618 x2 + 1251.6472 x + 0.0471
R2 =0.9997
Datos entalpa - concentracin
T CxCLA . MWACLB . MWBCL . MwpromDHsHLyCLA . MWACLB . MWBlAlBHv
80.600.000.000000.000000.000000.000.000.00000.000000.000000.000.000.00
80.000.050.000000.000000.0000057.960.000.06300.000000.000000.000.000.00
79.500.100.000000.000000.00000107.920.000.13000.000000.000000.000.000.00
79.100.150.000000.000000.00000151.490.000.20060.000000.000000.000.000.00
78.300.200.000000.000000.00000189.590.000.27220.000000.000000.000.000.00
77.900.250.000000.000000.00000222.710.000.34270.000000.000000.000.000.00
77.100.300.000000.000000.00000250.990.000.41460.000000.000000.000.000.00
76.800.350.000000.000000.00000274.380.000.48480.000000.000000.000.000.00
75.900.400.000000.000000.00000292.680.000.54880.000000.000000.000.000.00
75.300.450.000000.000000.00000305.660.000.60520.000000.000000.000.000.00
74.700.500.000000.000000.00000313.040.000.65860.000000.000000.000.000.00
73.400.550.000000.000000.00000314.590.000.71020.000000.000000.000.000.00
72.900.600.000000.000000.00000310.080.000.75580.000000.000000.000.000.00
72.000.650.000000.000000.00000299.260.000.79660.000000.000000.000.000.00
71.000.700.000000.000000.00000281.870.000.83430.000000.000000.000.000.00
69.800.750.000000.000000.00000257.540.000.87070.000000.000000.000.000.00
68.800.800.000000.000000.00000225.720.000.90470.000000.000000.000.000.00
66.200.850.000000.000000.00000185.560.000.93290.000000.000000.000.000.00
64.100.900.000000.000000.00000135.830.000.95720.000000.000000.000.000.00
63.000.950.000000.000000.0000074.730.000.97940.000000.000000.000.000.00
61.401.000.000000.000000.000000.000.001.00000.000000.000000.000.000.00
to =25 CMwA =76.13Kg/KmolHL =KJ / Kmol
MwB =153.84Kg/KmolHV =KJ / Kmol
Pgina &P
Diagrama
0
0
0
0
0
0
0
0
0
xA
DHS
Calor de Mezcla CS2 - CCl4 25 C
00
00
00
00
00
00
00
00
00
00
00
00
00
00
00
00
00
00
00
00
00
x , y
H
Diagrama Entalpa - Concentracin CS2 - CCl4
-
HL = CL . Mwprom (tL t0) + DHs
T CxCLA.MWACLB.MwBCL . MwpromDHSHL80.600.0080.000.0579.500.1079.100.1578.300.2077.900.2577.100.30
0.00-68.11-127.24-177.48-218.96-252.24-278.14
-
HV = yA [CLA . MwA (tV t0) + lA . MwA] +yB [CLB . MwB (tV t0) + lB . MwB]
T CyCLA.MWACLB.MwBlA.MWAlB.MwBHV
80.600.000080.000.063079.500.130079.100.200678.300.272277.900.342777.100.414676.800.4848
-
x , yHL vs xHV vs y
-
Ejemplos de clculo de entalpas
-
Calcular la entalpa molar de una mezcla lquida de cloroformo y benceno, que contiene 30 moles % de cloroformo, a la presin de 760 mm Hg y a una temperatura de 25 C.Ejemplo 1:xA = 0.30tL = 25 CLquido subenfriado
Grfico2
80.680.6
8080
79.579.5
79.179.1
78.378.3
77.977.9
77.177.1
76.876.8
75.975.9
75.375.3
74.774.7
73.473.4
72.972.9
7272
7171
69.869.8
68.868.8
66.266.2
64.164.1
6363
61.461.4
Ejemplo
Entalpa - concentracin para el sistema Cloroformo ( A ) - Benceno ( B ) a 1 atm.
a) Capacidad calorfica de solucin
CL . Mwprom = CLA . MwA . xA + CLB . MwB . xB
CLi . Mwi =C1 + C2 . T + C3 . T2 + C4 . T3 + C5 . T4J/Kmol - KT = K
C1C2C3C4C5
ACloroformo1.2944E+05-1.6950E+026.4781E-010.0000E+000.0000E+00
BBenceno1.2485E+05-1.6634E+024.3209E-010.0000E+000.0000E+00
b) Calores latentes molares de vaporizacin
C2 + C3 . Tr + C4 . Tr2
li =C1 (1 - Tr )J / Kmol
C1C2C3C4Tc
ACloroformo4.1860E+070.358400536.40
BBenceno4.7500E+070.452380.0534-0.1181562.16
c) Calores de mezcla a 18 C DHs
% peso AxAJ/g mezclaKJ/Kmol
00.00000.000.00
100.0678-1.13-91.43
200.1406-2.01-168.66
300.2190-2.64-230.08
400.3037-3.10-281.00
500.3955-3.31-312.58
600.4953-3.31-326.22
700.6042-3.18-327.70
800.7235-2.89-312.05
900.8548-2.05-232.46
1001.00000.000.00
xDHs
0.000.00
0.0557.96
0.10107.92
0.15151.49
0.20189.59
0.25222.71
0.30250.99
0.35274.38
0.40292.68
0.45305.66
0.50313.04
0.55314.59
0.60310.08
0.65299.26
0.70281.87
0.75257.54
0.85185.56
DHs =- 436.5958 x6 + 4003.4297 x5 - 5617.3018 x4 + 1994.4031 x3 + 1487.6691 x2 - 1430.9938 x - 0.49290.90135.83
0.9574.73
R2 =0.99990.9746.57
1.000.00
xDHs
0.000.00
0.05-68.11
0.10-127.24
0.15-177.48
0.20-218.96
0.25-252.24
0.30-278.14
0.35-297.66
0.40-311.82
0.45-321.54
0.50-327.57
0.55-330.32
0.60-329.80
0.65-325.52
0.70-316.37
0.75-300.56
0.80-275.50
0.85-237.77
0.90-183.01
0.95-105.85
1.000.00
Lquido
HL = CL . Mwprom (tL - tO) + DHs
T Cxy
80.600.000.0000
80.000.050.0630
79.500.100.1300
79.100.150.2006
78.300.200.2722
77.900.250.3427
77.100.300.4146
76.800.350.4848
75.900.400.5488
75.300.450.6052
74.700.500.6586
73.400.550.7102
72.900.600.7558
72.000.650.7966
71.000.700.8343
69.800.750.8707
68.800.800.9047
66.200.850.9329
64.100.900.9572
63.000.950.9794
61.401.001.0000
x =0.30to =18 C =291.15K
tL =25 C =298.15KDHs =-278.14KJ / Kmol
CL debe evaluarse a tprom y en funcin de la concentracin. Como no se tiene datos de CL, se calcular como una aproximacin CL . Mwprom
CL . Mwprom = CLA . MwA xA + CLB . MwB . xB
CLA y CLB se calcularn a la tprom
tprom = ( tL+tO ) / 2 =294.65K
CLA . MwA =1.35739E+05J / Kmol - K =135.73880KJ / Kmol - K
CLB . MwB =1.13351E+05J / Kmol - K =113.35138KJ / Kmol - K
CL . Mwprom =120.06760KJ / Kmol - K
HL =120.07660 * ( 25 - 18 ) - 278.14 =562.3312KJ / Kmol
T Cxy
80.600.000.0000
80.000.050.0630
79.500.100.1300
79.100.150.2006
78.300.200.2722
77.900.250.3427
77.100.300.4146
76.800.350.4848
75.900.400.5488
75.300.450.6052
74.700.500.6586
73.400.550.7102
72.900.600.7558
72.000.650.7966
71.000.700.8343
69.800.750.8707
68.800.800.9047
66.200.850.9329
64.100.900.9572
63.000.950.9794
61.401.001.0000
Vapor saturado
HV = y [ CLA . MwA (tv - tO) + lA . MwA ] + (1 - y) [ CLB . MwB (tv - tO) + lB . MwB ]
y =0.30
tv =68.8 C =341.95
to =25 C =298.15K
CLA y CLB se calcularn a la tprom
tprom =( tL + tO ) / 2 =320.05 K
CLA . MwA =1.29440E+05J / Kmol - K =129.44000KJ / Kmol - K
CLB . MwB =1.24850E+05J / Kmol - K =124.85000KJ / Kmol - K
lA y lB se calcularn a tvTrA =0.6195TrB=0.6146
lA . MwA =0.00000E+00J / Kmol =0.00000E+00KJ / Kmol
lB . MwB =0.00000E+00J / Kmol =0.00000E+00KJ / Kmol
Hv =2890.5983KJ / KmolHv =1242.9710797898BTU/lb mol
Pgina &P
Ejemplo
xA
DHS
Calor de Mezcla Cloroformo-Benceno 18 C
Construccin
Diagrama
Disulfuro de carbono ( A ) - Tetracloruro de Carbono ( B )
Datos de equilibrio del sistema a 1 atmsfera de presin
T Cxy
80.600.000.0000x =fraccin molar del CS2 en el lquido
80.000.050.0630y =fraccin molar del CS2 en el vapor
79.500.100.1300
79.100.150.2006
78.300.200.2722
77.900.250.3427
77.100.300.4146
76.800.350.4848
75.900.400.5488
75.300.450.6052
74.700.500.6586
73.400.550.7102
72.900.600.7558
72.000.650.7966
71.000.700.8343
69.800.750.8707
68.800.800.9047
66.200.850.9329
64.100.900.9572
63.000.950.9794
61.401.001.0000
a) Capacidad calorfica de solucinb) Calores latentes molares de vaporizacin
CLi . Mwi =(C1 + C2 . T + C3 . T2 + C4 . T3 + C5 . T4)/1000C2 + C3 . Tr + C4 . Tr2
li . Mwi =C1 (1 - Tr )/1000KJ / Kmol
KJ/Kmol - KT = K
CloroformoBencenoCloroformoBenceno
C11.2944E+051.2485E+05C14.1860E+074.7500E+07
C2-1.6950E+02-1.6634E+02C20.35840.45238Tc
C36.4781E-014.3209E-01C300.0534
C40.0000E+000.0000E+00C40-0.1181
C50.0000E+000.0000E+00
Tc K536.4562.16
c) Calores de mezcla a 25 C DHs
xBxAKJ/gmol mixKJ/Kmol
1.00000.00000.00000.000
0.81530.18470.1790179.000
0.66930.33070.2640264.000
0.53930.46070.3110311.000
0.40010.59990.3070307.000
0.28380.71620.2760276.000
0.14250.85750.1800180.000
0.09340.90660.1270127.000
0.00001.00000.00000.000
xDHs
0.000.00
0.0557.96
0.10107.92
0.15151.49
0.20189.59
0.25222.71
0.30250.99
0.35274.38
0.40292.68
0.45305.66
0.50313.04
0.55314.59
0.60310.08
0.65299.26
0.70281.87
0.75257.54
0.80225.72
0.85185.56
0.90135.83
0.9574.73
0.9746.57
1.000.00
DHs =- 1888.8191 x6 + 5483.3753 x5 - 6493.4512 x4 + 3684.4967 x3 - 2037.5618 x2 + 1251.6472 x + 0.0471
R2 =0.9997
Datos entalpa - concentracin
T CxCLA . MWACLB . MWBCL . MwpromDHsHLyCLA . MWACLB . MWBlAlBHv
80.600.000.000000.000000.000000.000.000.00000.000000.000000.000.000.00
80.000.050.000000.000000.0000057.960.000.06300.000000.000000.000.000.00
79.500.100.000000.000000.00000107.920.000.13000.000000.000000.000.000.00
79.100.150.000000.000000.00000151.490.000.20060.000000.000000.000.000.00
78.300.200.000000.000000.00000189.590.000.27220.000000.000000.000.000.00
77.900.250.000000.000000.00000222.710.000.34270.000000.000000.000.000.00
77.100.300.000000.000000.00000250.990.000.41460.000000.000000.000.000.00
76.800.350.000000.000000.00000274.380.000.48480.000000.000000.000.000.00
75.900.400.000000.000000.00000292.680.000.54880.000000.000000.000.000.00
75.300.450.000000.000000.00000305.660.000.60520.000000.000000.000.000.00
74.700.500.000000.000000.00000313.040.000.65860.000000.000000.000.000.00
73.400.550.000000.000000.00000314.590.000.71020.000000.000000.000.000.00
72.900.600.000000.000000.00000310.080.000.75580.000000.000000.000.000.00
72.000.650.000000.000000.00000299.260.000.79660.000000.000000.000.000.00
71.000.700.000000.000000.00000281.870.000.83430.000000.000000.000.000.00
69.800.750.000000.000000.00000257.540.000.87070.000000.000000.000.000.00
68.800.800.000000.000000.00000225.720.000.9