Calculos Equilibrio Líquido Vapor Método NTRL Mezcla Ternaria

7/25/2019 Calculos Equilibrio Lquido Vapor Mtodo NTRL Mezcla Ternaria

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FIQ-UNCP "Termodinmica de los Procesos Quimicos II - VI Semestre" J

T(C) = 60

T(K) = 333.15

Parmetros de Van Laar: Clculo del coe !c!ente de act!"!dad:

T #1 #$0.%$6$ 333.15 0.001 0.&&& 0.4262 0.%3&% 1.530161&555

333.15 0.1 0.& 0.%$6$ 0.%3&% 1.%15$%&0'0'0.%3&% 333.15 0.$ 0.' 0.%$6$ 0.%3&% 1.31 &% 31 1

333.15 0.3 0. 0.%$6$ 0.%3&% 1.$36&56$%61

333.15 0.% 0.6 0.%$6$ 0.%3&% 1.1 0$1%35% 333.15 0.5 0.5 0.%$6$ 0.%3&% 1.1160'$1301333.15 0.6 0.% 0.%$6$ 0.%3&% 1.0 3$ '&0 $333.15 0. 0.3 0.%$6$ 0.%3&% 1.0%0'353$%5333.15 0.' 0.$ 0.%$6$ 0.%3&% 1.01'05&06%6 333.15 0.& 0.1 0.%$6$ 0.%3&% 1.00%51$30 %333.15 0.&&& 0.001 0.%$6$ 0.%3&% 1.000000%53

C LC*L+ ,- L P/- + - ,- V P+/:

METIL ACETATO METANOLVP_A= -8.05406 VP_A= -8.54796 VP_B= 2.56375 VP_B= 0.76982 VP_C= -5.12994 VP_C= -3.1085 VP_D= 0.16125 VP_D= 1.54481

Pc= 46.9 Pc= 80.9Tc= 506.8 Tc= 512.6 T= 333.15 T= 333.15

x= 0.34264009 x= 0.350078034

DIAGONAL

#$% & Van %aar

Sistema Isot'rmico!etil (cetato )*+ - !etanol

$CU(CI N #$ (.N$/

0.20.30.40.50.60.70.80.9

1

Y1

)+1(

=ln2

212

121

121

A x

A x

A

1(

=ln 2

)+1(

1

2

212

121

12

= A x

A x

A

e(

2 = e

=12 A

=21 A

=1=12 A =21 A


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0 0 0.2 0.2 0.4 0.40.6 0.6 0.8 0.8 1 1

0 0.1 0.0

.


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seph Christian Cruz uanca

P !1 P !2 P "1 "2 "1#"2 1.00000041 1.1259659 0.846540765 0.84741748 0.00203313 0.99796687 11.00416758 1.1259659 0.846540765 0.92441413 0.17238185 0.82761815 11.01687721 1.1259659 0.846540765 0.98545515 0.30117327 0.69882673 11.03861229 1.1259659 0.846540765 1.03329051 0.4043695 0.5956305 1

1.07011078 1.1259659 0.846540765 1.07058402 0.49230006 0.50769994 11.11240598 1.1259659 0.846540765 1.09918372 0.57163803 0.42836197 11.16688325 1.1259659 0.846540765 1.12021097 0.64727564 0.35272436 11.23535711 1.1259659 0.846540765 1.1340956 0.72336191 0.27663809 11.32017492 1.1259659 0.846540765 1.14055621 0.80402862 0.19597138 11.4243557 1.1259659 0.846540765 1.13851946 0.8940927 0.1059073 1

1.55037134 1.1259659 0.846540765 1.1261529 0.99883457 0.00116543 1

,+

Metil Acetato (1) - Metanl (2)

VAN LAAR

DIAGONAL

0.2

0.4

0.6

0.8

1

1.2

Metil

P

)+ 2121

212

21

A x

A x

A

)+1 2

1 21

212

2 1

A x

A x

A

=2


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0.3 0.4 0.5 0.6 0.7 0.8 0.9 1

X1

0 0.1 0.2 0.3

-1.66533453693773E-016


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cetato (1) - Metanl (2)

Xvs P

Y vs P


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0.4 0.5 0.6 0.7 0 .8 0.9 1

X-Y


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2 4* CP Termod!nm!ca de los Procesos u!m!cos 4 V emestre ose78 C8r!st!an Cru9

P (;ar) = 1

Parmetros de Van Laar: Clculo del coe !c!ente de act!"!dad:

Pres!on T #1 #$0.%$6$ 1 33 .$'&1&'11 0.001 0.&&& 0.%$6$

1 31&.060' 3 ' 0.1 0.& 0.%$6$0.%3&% 1 315. ''61%16 0.$ 0.' 0.%$6$

1 316. $61 51 0.3 0. 0.%$6$

1 31 . &'&5% 0.% 0.6 0.%$6$1 31'.'&5 6%%% 0.5 0.5 0.%$6$1 3$0.0'5'6$ & 0.6 0.% 0.%$6$1 3$1.31$01156 0. 0.3 0.%$6$1 3$$.6$'&6 6% 0.' 0.$ 0.%$6$1 3$%.06351 '$ 0.& 0.1 0.%$6$1 3$5.6330'5&& 0.&&& 0.001 0.%$6$

C LC*L+ ,- L P/- + - ,- V P+/:

= 0. 6&'$VP C= 45.1$&&% VP C= 43.10'5VP ,= 0.161$5 VP ,= 1.5%%'1

Pc= %6.& Pc= '0.&Tc= 506.' Tc= 51$.6

VP VP > VP C VP , Pc Tc #

#$% & Van %aar

$CU(CI N #$ (.N$/

Sistema Iso0rico!etil (cetato )*+ - !etanol ),+

00

0.10.20.30.40.50.60.70.80.9

1

y

)+1(

=ln2

212

121

121

A x

A x

A

1(

=ln 2

)+1(

1

2

2 12

121

12

= A x

A x

A

e(

2 = e

=12 A

=21 A

=12 A


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4'.05%06 $.563 5 45.1$&&% 0.161$5 %6.& 506.' 0.33%% $ %4'.05%06 $.563 5 45.1$&&% 0.161$5 %6.& 506.' 0.3 0%%0$6%'4'.05%06 $.563 5 43.10'5 0.161$5 %6.& 506.' 0.3 6'&6& $&4'.05%06 $.563 5 43.10'5 0.161$5 %6.& 506.' 0.3 50% 005 4'.05%06 $.563 5 43.10'5 0.161$5 %6.& 506.' 0.3 $&30$%0

4'.05%06 $.563 5 43.10'5 0.161$5 %6.& 506.' 0.3 0 6605$'4'.05%06 $.563 5 43.10'5 0.161$5 %6.& 506.' 0.36'%1 &$54'.05%06 $.563 5 43.10'5 0.161$5 %6.& 506.' 0.365&&'3&'6 4'.05%06 $.563 5 43.10'5 0.161$5 %6.& 506.' 0.3633&&'$ 14'.05%06 $.563 5 43.10'5 0.161$5 %6.& 506.' 0.36056&$$$&4'.05%06 $.563 5 43.10'5 0.161$5 %6.& 506.' 0.35 % $$06


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uanca , ?+ L:

00.$0.%

0.6 0.'1

P"71 P"7$ @1 @$0.%3&% 1.530161&555 1.000000%13% 1.$&35%0'355 0.&&&065$&$& 0.001& &3$ 0.&&'0666%030.%3&% 1.%15$%&0'0' 1.00%16 5 5 0.6 &%3&665% 0.&&&065$&$& 0.0&615 636$ 0.&0$&060 5&0.%3&% 1.31 &% 31 1 1.016' $05 0. 13$160&%3 0.&&&065$&$& 0.1' &&6$% 6 0.'1$ %13 ' 0.%3&% 1.$36&56$%61 1.03'61$$'5 0. 3 $%30$6$ 0.&&&065$&$& 0.$ 35'1$0&' 0. $63%&0%1$

0.%3&% 1.1 0$1%35% 1.0 0110 &1 0. 655$6 $5 0.&&&065$&$& 0.35'33$1%53 0.6%1%663$3%0.%3&% 1.1160'$1301 1.11$%05&'3$ 0. &53361 0& 0.&&&065$&$& 0.%%3'30$%3& 0.5556'310% 0.%3&% 1.0 3$ '&0 $ 1.166''3$51 0.'$' $%5'06 0.&&&065$&$& 0.5336 156 % 0.%6631 0$310.%3&% 1.0%0'353$%5 1.$3535 10&5 0.'6%$' 15%5 0.&&&065$&$& 0.6$& 06%$0 0.3 0$60 $3 0.%3&% 1.01'05&06%6 1.3$01 %&$%3 0.&03'30%&16 0.&&&065$&$& 0. 361$$$5&' 0.$63 ''1'&50.%3&% 1.00%51$30 % 1.%$%3556&&5 0.&%'533 '$5 0.&&&065$&$& 0.'5 53$% $6 0.1%$30$%3%%0.%3&% 1.000000%53 1.5503 13%15 0.&&&%%50 % 0.&&&065$&$& 0.&&'%%60'1& 0.0015%'&$$$

VP VP > VP C VP , Pc Tc #

0.1 0.2 0.3 0.4 0.5 0.6 0.7 0.8 0.9 1

METIL ACETATO (1) - METANOL (2)

VANLAAR

x

-0.8 0.2305

310

315

320

325

330

335

340

METIL ACETATO (1) - M

X-Y

T

)+ 2121

212

21

A x

A x

A

)+ 2

1 21

212

2 1

A x

A x

A

=1 =2=21 A


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4'.5% &6 0. 6&'$ 43.10'5 1.5%%'1 '0.& 51$.6 0.3%$0031$54'.5% &6 0. 6&'$ 43.10'5 1.5%%'1 '0.& 51$.6 0.3 5636%'54'.5% &6 0. 6&'$ 43.10'5 1.5%%'1 '0.& 51$.6 0.3'3&% $&& 4'.5% &6 0. 6&'$ 43.10'5 1.5%%'1 '0.& 51$.6 0.3'$11'$6% 4'.5% &6 0. 6&'$ 43.10'5 1.5%%'1 '0.& 51$.6 0.3'00$5%506

4'.5% &6 0. 6&'$ 43.10'5 1.5%%'1 '0.& 51$.6 0.3 ''5 50$4'.5% &6 0. 6&'$ 43.10'5 1.5%%'1 '0.& 51$.6 0.3 556%06014'.5% &6 0. 6&'$ 43.10'5 1.5%%'1 '0.& 51$.6 0.3 31 $0%1%4'.5% &6 0. 6&'$ 43.10'5 1.5%%'1 '0.& 51$.6 0.3 060$' $34'.5% &6 0. 6&'$ 43.10'5 1.5%%'1 '0.& 51$.6 0.36 '0%$&614'.5% &6 0. 6&'$ 43.10'5 1.5%%'1 '0.& 51$.6 0.36% %$3$15


11/24

11.$1.%

1.6 1.'$

@1A@$1.0000%5&6 $0.&&&063 1$11.000 3 6$630.&&&&30$51

0.&&& &'%6' 0.&&&5133%'6 0.&&&&''5&050.&&&&6 1%%%0.&&&&10%%&30.&&&'3%&0 10.&&&&&500%1

1.2

TANOL (2)

X vsT


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Sistema IsobricoMetil Acetato (1) - Metanol (2)

! #$% & N/T%

, T+ +>T- ,+ ,-L , T > K Com7onentes T T> TC

1 et8anol 1'.&11& 3'03.&' 4%1.6'$ Bater 1'.3036 3'16.%% 4%6.133 n 7ro7anol 1 .5%3& 3166.3' 4'0.15

Parametos de !nteracc!on del c8emcad >! > !

1 $ 455.15'1 6 0.%%11 3 41.$' &% $'.300 $ 3 1005.$3 $$3.5&6

Clculo del coe !c!ente de act!"!dad:

/ Pres!on T (K) #1 #$ #3 T1$1.&' 60 3%6. & %'%'3 0 0.56 0.%% 40.0'00%5$36%1.&' 60 35$. 305'&&6 0.0& 0.51 0.% 40.0 '6&''3551.&' 60 356.'&5&&50% 0.1' 0.%6 0.36 40.0 '03$551.&' 60 356.13%5&'&1 0.$ 0.%1 0.3$ 40.0 &%661551.&' 60 35%.5&50$ 61 0.36 0.36 0.$' 40.0 '$'50%$1

1.&' 60 35$.0 5&111' 0.%5 0.31 0.$% 40.0 ''%51 %51.&' 60 3%&.$13653$ 0.5% 0.$6 0.$ 40.0 &%&1%1$'1.&' 60 3%6.$331'353 0.63 0.$1 0.16 40.0'01 56&66 1.&' 60 3%3.1'1'3536 0. $ 0.16 0.1$ 40.0'0'''566%1.&' 60 33&.5%$61'5 0.'1 0.11 0.0' 40.0'1 555$&'

0.60.7

0.8

0.

1


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0 0.1 0.2 0.3 0.4 0.5 0.6 0.7 0.8 0. 10

0.1

0.2

0.3

0.4

0.5et

"ol

fraccion molar etanol

fraccion molar agua


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LP 1 0.30310.300 0.%'5

T$1 T13 T31 T$3 T3$ ?1$ ?$10.& $&%156'& 40.001'6&053& 0.0%106&' %1 1.%5' '616$1 0.3$%%'1 11% 1.0$%55'%$1$ 0. %%60 0&%6 0.&565 6$0%6 40.001'3 6155 0.0%03 &05'3 1.%3%$%'6%'5 0.31&0$3 665 1.0$%1%03&0$ 0. %'30& 610.&%5%11'10& 40.001'1616'3 0.03&&0 '61 1.%1 50&$%3% 0.3153003 5' 1.0$3'5530'' 0. 50'%6$&150.&% %330%&$ 40.001'$0051$ 0.03&&&3106' 1.%$053&' 0.315& %% 06 1.0$3&06&15 0. 503'6%35&0.&515%65''& 40.001'$ &53% 0.0%0166 % ' 1.%$6 0 %6$1 0.31 3%6360$ 1.0$%011&%&' 0. %&%51%$6

0.&5'35%&%0 40.001'%103$5 0.0%0%5%1%$% 1.%36&1560 ' 0.31&616&'5% 1.0$%1'5'1 3 0. % &06%%%&0.&66$0&&001 40.001'561$$1 0.0%0 '5 16% 1.%%'6&$&&15 0.3$$$36660% 1.0$%3'6%%&$ 0. %61$ &1' 0.& %5$ $&'% 40.001' $1001 0.0%1136'11 1.%61163 35' 0.3$5010561% 1.0$%5&'&355 0. %%$%&$&66 0.&'31&$15 1 40.001''' %56 0.0%150$5 $6 1.% %155%% 0.3$ &003%$5 1.0$%'$03%5% 0. %$$& $$530.&&3 3000 & 40.001&0'&'&$ 0.0%1&% 3& 1 1.%'&&55%%11 0.331%1% 5 1.0$50'&6 &6 0. 3&&300&36


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anol

l#mn AM


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,!aDonal

# @

0 00.1 0.1

0.$ 0.$0.3 0.30.% 0.%0.5 0.50.6 0.6 0. 0. 0.' 0.'0.& 0.&

1

?13 ?31 ?$3 ?3$1.00056$1'$5 0.&' $6$336 0.%&$'6&$'1' 0.'5%3'% 5% 0.%& 365$&56 40.%01 1'%$$& 4$.$613%$3$351.00055$ $3 0.&' &31%336 0.%&' 6&'0'& 0.'566%&%161 0.%&0%&6051' 40.$6'1%%30&' 41.1'33&0 536 1.0005%6$ 1 0.&''0 1%%%' 0.50$'3560&$ 0.'5'1& '&% 0.%'5&& 6 35 40.1 &&%&'5 ' 40.66$13 '&1$

1.0005% %3&$ 0.&''0%60&53 0.50$0& 0 %$ 0.'5 &1 $5&5 0.%' 51&0'13 40.1$1%%301%' 40.3'56$'136'1.0005%&'16 0.&' &&%506& 0.5005& 3' 3 0.'5 3%66$ 0.%&01560111 40.0'063&6%'5 40.$$51&00$15

1.000553 51 0.&' &0&1$'6 0.%&'1$50 &5 0.'56%0$&'% 0.%&%$6&$$ 6 40.05$1$ &6'6 40.1$&1$000%1.00055'$&1 0.&' '1063% 0.%&5$' ''%% 0.'553155 ' 0.%&&$'03 5' 40.03$$3663 & 40.0 0 %603%51.0005630&& 0.&' 0635$& 0.%&$301$ 03 0.'5%165660% 0.505$% 6 40.01'5&%0501 40.0355&$'36'

1.00056'10 1 0.&' 5& $65 0.%'&$0&0%$1 0.'5$&6&3%'3 0.51$'5501'5 40.00&5665%56 40.015$$35636 1.0005 %1& ' 0.&' %656355 0.%'5% %5616 0.'515166&&6 0.5$%&%50 5 40.003&&31'0 40.00%%'16&%1


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20.11%6 015&% 0.3$%%'1 11% 0 0 1.3'331350%5 1.%5' '616$10.3'$%&5$6$5 0.$3% 1 3&& 0.0%0%0'1&1& 0.$1 %&061%1 1.6365&$$'% 1.05' '1 16&0. 00%0&5$ 0.16'%31%$' 0.0''56$ 35% 0.$ 33&$05 % 1.6&&5''5&&5 0. &61 610&10.&'063 '31 0.11'3$ 10&$ 0.1%&36 5'1 0.$ $% 1330' 1. 16$&$0'$& 0.613310$ 36 1.$0$%0'15%$ 0.0 %$3''& 0.$$ '0&30$' 0.$%6&603 % 1. 3 61$536& 0.% %5551053

1.36 5505&'1 0.0%%0%'1%0$ 0.33306 %556 0.$11'1%65'$ 1.'0$05&63 & 0.3655'5% %%1.%'6311 31 0.0153&6516' 0.%'0%6' &$1 0.1 3%$$30&1 1.&5$'%565$& 0.$ 3$61%$ 1.56&& 65& 3 40.00&3 '01 0. 000$13& % 0.13%&3011%% $.$'31'&'033 0.$0%$6''11%1.6$&1605&%3 40.0310'&&636 1.05&3&&551 0.0& '6015'% 3.0'3'$$0$ ' 0.1%$ 6'3$$51.6 6100'&5$ 40.050%$'353 1. 51 5%55%5 0.06$&$5%1$5 5.'3 $0$$%$' 0.0&031%%'6

1


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3 P"71 P"7$ P"73 @10 0 %.300 35&6$% 6$&.31'0% 05 $ 3.$%6 1'$0$' $'&. &655$$ 5 0

40.0515$0%%%6 0.0 0%$6 &'' $.&3 ' &5$% &'.$66%$$315 3%&.3$5 6$56$3 3 5.$%&&%%$5%6 0.03615 ' 40.113163%&5$ 0.10$6305&03 $.1&3'1 55&6 &3'.$ &5%$ % %1$. 5$5&530%& %%6.&%%136 3 0.1556% ' '5

40.1&13 %% 0.11%%'%5$&1 1. 0&' 00316 &11.$5&5%%5 3 %00.%'''$3'06 %33.0566$$&33% 0.31 %6'6&%340.$&$'& 6 51 0.113'5035'& 1.3%3'0'556& '5'.6050%0'5& 3 6.6$16'5$3$3 %06.06$6 1 53% 0.%'&0$'5&5'

40.%30$1$1301 0.105 551''$ 1.0%1&'60$6 .&3&1'&563 3%0.1%3&%66'6% 36%.&00 $%%&0 0.6$&&$3 3&$40.6$%60&%$& 0.0&$&'0%501 0. 5%56&$&5 6&%.0 &' % $6 30$.3%3'35506' 3$$.3' '% 5&5& 0. 3$&&$%&0%40.&1' '0'% 0.0 31311 1 0.5$' $&%%6 61%.&% 1'&1 $ $66.'0$13%6 %$ $'$.5 306$ 33% 0.'0030&% 13

41.%1$53$ 3% 0.05&&$$5&6 0.$&'$%%%53% 5%1.&$505%31 $3%.1$&' %5&$& $%6.13 $&35'&5 0.'36%15%$0$4$.%0'66$51$5 0.0%16$'$105 0.10$6$0$6' %6%.50'05%5%% 1&&.6%1'033'0 $0 .'' &1$&&$5 0.'$& '35 %3


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Dia !"a# @$ @3 E # @

0.$ '515&0'1 0. $15$$$&6$ 1.00003'$0%% 0 10.3'36%33 16 0.5'0$3111&& 1.00003$3616 0.1 0.&0.%$%5& &1& 0.%6%%53&505 1.0%%6&& %' 0.$ 0.'

0.3 0'1036%5 0.311 0 01 1.0000561$'& 0.3 0. 0.30&&'&63%6 0.$01036%& % 1.00005% $ ' 0.% 0.6

0.$500$30$63 0.1$006&&33% 1.0000166&'& 0.5 0.50.$01&'&%&&5 0.065 ''&1'5 1.000 0&0'5 0.6 0.%0.16'3$050$% 0.031%56$0'5 1.0000'61'$$ 0. 0.30.15$0031$&% 0.0115&0&0 ' 1.00000&%5 % 0.' 0.$0.16'66&01'5 0.00$$%5633 1.0006&'$$5' 0.& 0.1

1 0


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Calculos Equilibrio Líquido Vapor Método NTRL Mezcla Ternaria

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Transcript of Calculos Equilibrio Líquido Vapor Método NTRL Mezcla Ternaria