ejercicios DTR resueltos.docx

7/26/2019 ejercicios DTR resueltos.docx

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TABLA 1:

tConcen

trationtm Cn C F Cn t

tmCn

t

tm2Cn

tE(t)

((t

tm)^

2)*E(t

)/s

XA(t) XAs

0 0 75 0 0 0 0 0 0 0 0 0 0 0.511832

34

0.577894

5150 0 162.

5

0 0 0 0 0 0 0 0 0.8218

3

0 0.732749

42

0.845683

56175 0.001 187.

5

0.001

01

0.0010

1

0.0253 0.0253 4.7444

5

889.58

5

0.0010

2

7.643

54

0.8663

5

0.0008

8

0.768443

67

0.884241

6200 0.003 212.

5

0.003

04

0.0030

4

0.1012

2

0.0759

1

16.131

1

3427.8

6

0.0030

6

11.60

39

0.8997

4

0.0027

5

0.797436

7

0.913165

39225 0.0074 232.

5

0.007

49

0.0074

9

0.2135

6

0.1498 34.827

9

8097.5 0.0075

4

10.10

78

0.9247

9

0.0069

7

0.816882

84

0.931006

98240 0.0094 245 0.009

51

0.0095

1

0.3087 0.1189

3

29.137

1

7138.6 0.0095

8

4.474

48

0.9367

1

0.0089

7

0.827647

91

0.940244

86250 0.0097 255 0.009

82

0.0098

2

0.4068

8

0.0981

8

25.035

4

6384.0

3

0.0098

8

1.332

5

0.9435

8

0.0093

3

0.835590

92

0.946736

29260 0.0094 267.

5

0.009

51

0.0095

1

0.5496 0.1189

3

31.813 8509.9

8

0.0095

8

0.024

98

0.9497

1

0.0091 0.844770

6

0.953868

07275 0.0082 287.

5

0.008

3

0.0083 0.7570

9

0.1659

9

47.722

7

13720.

3

0.0083

5

1.496

82

0.9576

8

0.008 0.857935

82

0.963346

63300 0.005 312.

5

0.005

06

0.0050

6

0.8836 0.1265

2

39.537 12355.

3

0.0050

9

7.505

95

0.9682

5

0.0049

3

0.872163

79

0.972504

97325 0.0025 337.

5

0.002

53

0.0025

3

0.9468

6

0.0632

6

21.349

9

7205.6 0.0025

5

10.23

35

0.9761

9

0.0024

9

0.884356

64

0.979374

97350 0.0012 362.

5

0.001

21

0.0012

1

0.9772

3

0.0303

6

11.007 3990.0

5

0.0012

2

9.551

01

0.9821

4

0.0012 0.894884

77

0.984528

41


2/16

375 0.0005 387.

5

0.000

51

0.0005

1

0.9898

8

0.0126

5

4.9025

8

1899.7

5

0.0005

1

6.549

23

0.9866 0.0005 0.904037

99

0.988394

2400 0.0002 425 0.000

2

0.0002 1 0.0075

9

3.2262

1

1371.1

4

0.0002 3.902

28

0.9899

5

0.0002 0.915678

8

0.992459

75450 0 0 --- --- --- --- --- --- 0 0.9943

4

0 --- 0

0.9934

2


3/16

Curves parametersArea under concentration vs. time curve

=

0.988

Residence time V/Q = 32.4 seconds

Residence time ! t"e curve #se$undos%

=

269.43445

Variance o& t s2= 1903.36

Variance o& t"eta = 0.0253027

1. 'ra(car )a curva *#t% para estos datos.

0 50 100 150 200 250 300 350 400 450 500

0

2

4

6

8

10

12

*#t% vs t#s%

E(t) vs t(s)

2. +Qu, &racci-n de materia) reside entre 23 s ! 2 s en

e) reactor0

&racci-n de materia) reside entre 23 s ! 2

s en e) reactor=

3

3. 'ra(car )a curva #t% para estos datos.


4/16

0 50 100 150 200 250 300 350 400 450

0

0.5

1

1.5

#t% vs t#s%

F(t) vs t(s)

4. +Qu, &racci-n de materia) reside menos de 2 s en e)

reactor0

&racci-n de materia) reside menos de 2 sen e) reactor

.44325

. Ca)cu)ar e) tiempo de residencia medio tm.

Ca)cu)ar e) tiempo de residencia

medio tm

25.43

44

5. 'ra(car #t 6 tm%2*#t% como &unci-n de) tiempo.

0 50 100 150 200 250 300 350 400 450 500

02

4

6

8

10

12

14

##t 6 tm%72%8*#t% vs t#s%

((t tm)^2)*E(t)/s vs

t(s)

. Ca)cu)ar )a varian9a 72

Ca)cu)ar )a varian9a

72.

13.3

5

s2


5/16

;. 11 s61> +Qu, conversiones predicen )osmode)os de se$re$aci-n ! tan?ues en serie0

Para una rea!"n #e $r!mer %r#en& 'a %nvers!"n a 'a sa'!#a #e'tanue n est #a#a $%r 'a e$res!"n

. Ca)cu)ar )a conversi-n idea)> si se asume @uo pist-n.

**RCCD< ETR

Ejercicio 1:

Un anlisis de la DTR se efectu en un reactor de fase lquida. Se obtuvieronlos siguientes datos:

t Concentration

0 0

15

0

0

1

5

0.001

!0

0

0.00"

!!

5

0.00#

!#

0

0.00$#

!5

0

0.00$

!%

0

0.00$#

!

5

0.00&!

"00

0.005

FAn .15;;

.24


6/16

"!

5

0.00!5

"5

0

0.001!

"

5

0.0005

#00

0.000!

#5

0

0

1. 'raficar la curva ()t* +ara estos datos.!. ,-u fraccin de /aterial reside entre !"0 s !0 s en el reactor". 'raficar la curva 2)t* +ara estos datos.

#. ,-u fraccin de /aterial reside /enos de !50 s en el reactor5. 3alcular el tie/+o de residencia /edio t/.%. 'raficar )t 4 t/*!()t* co/o funcin del tie/+o.. 3alcular la variana 6!.&. Si se efectu en el reactor una reaccin de +ri/er orden con 7 8 090115

s419 ,-u conversiones +redicen los /odelos de segregacin tanquesen serie

9. 3alcular la conversin ideal9 si se asu/e fluo +istn.

Ejercicio 2:

;as concentraciones de traador9 en un e


7/16

2 0.322.5 0.37

3 0.43.5 0.43

4 0.454.5 0.48

5 0.485.5 0.496 0.5

6.5 0.57 0.51

7.5 0.518 0.51

8.5 0.519 0.51

9.5 0.52

10 0.52

3alcular graficar las curvas ()t* 2)t*9 calcular el tie/+o de residencia /ediot/ la variana =>!

t/mint/se

g

Concentratio

ntm Cn C F Cn t tm

0 0 15 0 0 0 0. 30 0.11 45 0.00045

436

0.000454

36

0.01363

07

0.01363

074

0.6

1 60 0.2 75 0.00082

611

0.000826

11

0.03841

39

0.02478

315

1.8

1. 90 0.27 105 0.00111

524

0.001115

24

0.07187

11

0.03345

72

3.5

2 120 0.32 135 0.00132177 0.00132177 0.111524 0.0396531 5.3

2. 150 0.37 165 0.00152

829

0.001528

29

0.15737

3

0.04584

87

7.5

3 180 0.4 195 0.00165

221

0.001652

21

0.20693

9

0.04956

63

9.6

3. 210 0.43 225 0.00177

613

0.001776

13

0.26022

3

0.05328

39

11.

4 240 0.45 255 0.00185

874

0.001858

74

0.31598

5

0.05576

22

14.

4. 270 0.48 285 0.00198

265

0.001982

65

0.37546

5

0.05947

95

16.

300 0.48 315 0.00198 0.001982 0.43494 0.05947 18.


8/16

265 65 4 95

. 330 0.49 345 0.00202

396

0.002023

96

0.49566

3

0.06071

88

20.

5 360 0.5 375 0.00206

526

0.002065

26

0.55762

1

0.06195

78

23.

5. 390 0.5 405 0.00206

526

0.002065

26

0.61957

9

0.06195

78

25.

420 0.51 435 0.00210657

0.00210657

0.682776

0.0631971

27.

. 450 0.51 465 0.00210

657

0.002106

57

0.74597

3

0.06319

71

29.

; 480 0.51 495 0.00210

657

0.002106

57

0.80917 0.06319

71

31.

;. 510 0.51 525 0.00210

657

0.002106

57

0.87236

7

0.06319

71

33.

540 0.51 555 0.00210

657

0.002106

57

0.93556

4

0.06319

71

35.

. 570 0.52 585 0.00214787

0.00214787

1 0.0644361

37.

1 600 0.52 0 0 0 0 0

1.00000

029

353

TABLA 1:


9/16

TABLA 2:

*#

% #

% #

% Ln #

%

0.04239

11

0 0 1 0 0

0.12717

3

0.16077

3

0.01363

07

0.98636

9

-

0.013724

5

0.162995

0.21195

6

0.29231

5

0.03841

39

0.96158

6

-

0.039171

1

0.303993

0.29673

8

0.39462

6

0.07187

11

0.92812

9

-

0.074584

7

0.425184

0.38152 0.467704

0.111524

0.888476

-0.118248

0.526412

0.46630

2

0.54078

3

0.15737

3

0.84262

7

-

0.171231

0.641782

0.55108

5

0.58463 0.20693

9

0.79306

1

-

0.231855

0.737182

0.63586

7

0.62847

8

0.26022

3

0.73977

7

-

0.301407

0.84955

0.72064

9

0.65770

9

0.31598

5

0.68401

5

-

0.379776

0.961542

0.80543

2

0.70155

7

0.37546

5

0.62453

5

-

0.470747

1.12333

0.89021

4

0.70155

7

0.43494

4

0.56505

6

-

0.570831

1.24157

0.97499

6

0.71617

2

0.49566

3

0.50433

7

-0.68451 1.42003

1.05978 0.73078

8

0.55762

1

0.44237

9

-

0.815588

1.65195

1.14456 0.73078

8

0.61957

9

0.38042

1

-

0.966476

1.921

1.22934 0.74540

4

0.68277

6

0.31722

4

-1.14815 2.34977

1.31413 0.74540

4

0.74597

3

0.25402

7

-1.37031 2.93435

1.39891 0.74540

4

0.80917 0.19083 -1.65637 3.90611

1.48369 0.74540

4

0.87236

7

0.12763

3

-2.05859 5.8402

1.56847 0.74540

4

0.93556

4

0.06443

62

-2.74208 11.5681

1.65325 0.76002 1 2.22E-

16

- 3.42E+15


10/16

a) GAF!C" E(t):

0 100 200 300 400 500 600 700

0

2

4

6

8

10

12

*#t% vs t#se$.%

E(t) vs t(m!n)

#) GAF!C" F(t):

0 100 200 300 400 500 600 700

0

0.2

0.4

0.6

0.8

1

1.2

#t% vs t#se$.%

F(t) vs t(se,un#%s)


11/16

Ejercicio $%

;a /asa de reaccin en un tanque agitado continuo ocu+a un volu/en de? 8 195/". (l fluo volu/trico es @?0 8 "0 ;A/in. Bara /edir la DTR9 seintroduo en el reactor un traador inerte en for/a de escaln. ;a curva 2)t*9 ala salida del reactor9 est re+resentada +or los siguientes datos:

t/min F(t)

5 0.!$

10 0."

15 0.##

!0 0.51

!5 0.5%

"0 0.%1

"5 0.%5

#0 0.%$

#5 0."

50 0.%

%0 0.&1

0 0.&5

&0 0.&&

$0 0.$1

100 0.$"


12/16

Una re+resentacin de 2 co/o funcin de /uestra clara/ente unadesviacin del co/+orta/iento ideal. Una concentracin elevada de traador9/edida a la salida del reactor9 al inicio del e


13/16

Tabla I

T(s) Concentration tm Cn C F Cnt tmCnt tm2Cnt

300 0.00058 450 7.2846e-005 7.2846e-005 0 0.0218538 9.83421 4425.4

600 0.00074 750 9.29415e-005 9.29415e-005 0.0278824 0.0278824 20.9118 15683.9

900 0.00088 1050 0.000110525 0.000110525 0.0610399 0.0331575 34.8154 36556.1

1200 0.00102 1350 0.000128109 0.000128109 0.0994725 0.0384326 51.8839 70043.3

1500 0.00112 1650 0.000140668 0.000140668 0.141673 0.0422005 69.6307 114891

1800 0.00122 1950 0.000153228 0.000153228 0.187641 0.0459683 89.6383 174795

2100 0.0013 2250 0.000163276 0.000163276 0.236624 0.0489827 110.211 247975

2400 0.00138 2550 0.000173323 0.000173323 0.288621 0.051997 132.592 338110

2700 0.00146 2850 0.000183371 0.000183371 0.343632 0.0550113 156.782 446829

3000 0.00152 3300 0.000190907 0.000190907 0.458176 0.114544 377.995 1.24739e+006

3600 0.00162 3900 0.000203466 0.000203466 0.580256 0.12208 476.112 1.85683e+006

4200 0.0017 4500 0.000213514 0.000213514 0.708365 0.128109 576.488 2.5942e+0064800 0.00176 5100 0.00022105 0.00022105 0.840995 0.13263 676.413 3.44971e+006

5400 0.00182 5700 0.000228586 0.000228586 0.978146 0.137151 781.763 4.45605e+006

6000 0.00186 --- --- --- --- --- --- ---


14/16

Tabla II

E() F() I() n I()

0.126225 0.259701 0 1 0 0.259701

0.210374 0.331343 0.0278824 0.972118 -0.0282785 0.340847

0.294524 0.39403 0.0610399 0.93896 -0.0629823 0.419645

0.378674 0.456716 0.0994725 0.900528 -0.104775 0.507165

0.462824 0.501492 0.141673 0.858327 -0.15277 0.584267

0.631123 0.582089 0.236624 0.763376 -0.270005 0.762519

0.715273 0.61791 0.288621 0.711379 -0.34055 0.868609

0.799423 0.653731 0.343632 0.656368 -0.421034 0.995982

0.925648 0.680596 0.458176 0.541824 -0.612815 1.25612

1.09395 0.725373 0.580256 0.419744 -0.868111 1.72813

1.26225 0.761193 0.708365 0.291635 -1.23225 2.61009

1.43055 0.788059 0.840995 0.159005 -1.83882 4.95618

1.59885 0.814925 0.978146 0.0218538 -3.82338 37.2898


15/16

C!r"es #arameters

Area under concentration vs. time curve = 7.962

Residence time V! = 30000 secondsResidence time "# t$e curve = 3565.07 seconds

Variance o% t = 2.34375e+006 s2

Variance o% t$eta =0.184406

First or$er con"ersions

&onversion = 0.984822

'(u) %(o* conversion = 0.999906e(( mi,ed conversion = 0.90268

A,ia( disersion mode( conversion = 0.997416

an/s in serires conversion = 0.995516

&$o(ette-&(outier conversion = 0.98475

evensie( conversion = 0.984753

%o$els #arameters

A,ia( disersion mode( u( = 0.102806

um"er o% tan/s in series = 5.42283

&$o(ette and &(outier mode(

nut %(o* to t$e *e(( mi,ed reactor = 1800 ($

#ass %(o* = 0 ($

e(( mi,ed vo(ume = 1.24101e+007 cm3

eat$ vo(ume = 2.58992e+006 cm3

evensie( mode(

e(( mi,ed vo(ume = 1.24101e+007 cm3

eat$ vo(ume = 2.58992e+006 cm3

'(u) %(o* vo(ume26.9341 cm3

&orre(ation coe%%icient com"ined mode(s = 0.856884

Result:


16/16

;a fraccin de este circuito corto )*

Variance o% t$eta =0.184406

(ventual fraccin de volu/en /uerto )G*.

eat$ vo(ume = 2.58992e+006 cm3

3alcular la conversin que se es+era en este reactor.&onversion = 0.984822

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ejercicios DTR resueltos.docx