Copia De Guia N° 6 Reacciones.xlsx
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t [min] 0 1 2 3 4 5 6 7 8 9 10 11 12
C [mol/L] 0 1 5 8 10 8 6 4 3 2.2 1.5 0.6 0
k t(media) varianza σ2
Cmed 0.5 3 6.5 9 9 7 5 3.5 2.6 1.85 1.05 0.3 -
Δt Δt * Cmed 1 0.5 1 3 1 6.5 1 9 1 9 1 7 1 5 1 3.5 1 2.6 1 1.85 1 1.05 1 0.3 SUMATORIA 49.3
0.1 min-1 4.957 4.994
Flujo NO IDEAL, utilizo modelo de dispersión: varianza(θ) σ2
0.203
D/(u*L)
0.1148
varianza (θ) σ2 Control k*tm
0.2032 0.0000 0.4957
Dispersión grande
Utilizando el gráfico: 1-XA
0.55
XA
0.45 Calculando por cinética:
CA/CA0
0.624
1-XA
0.624
XA
0.376
E(t) 0.0000 0.0203 0.1014 0.1623 0.2028 0.1623 0.1217 0.0811 0.0609 0.0446 0.0304 0.0122 0 1
t * C * Δt 0 1 10 24 40 40 36 28 24 19.8 15 6.6 244.4
IMPULSO
C * Δt 0 1 5 8 10 8 6 4 3 2.2 1.5 0.6 49.3
(t-tm)^2*C*Δt EXP(kt)*E*Δt 0.0000 0.0000 15.6610 0.0184 43.7312 0.0830 30.6514 0.1202 9.1662 0.1360 0.0145 0.0984 6.5220 0.0668 16.6888 0.0403 27.7722 0.0273 35.9537 0.0181 38.1417 0.0112 21.9078 0.0041 246.211 0.624
C vs t 12 10 8 6 4 2 0
0
2
4
6
8
10
12
8
10
14
E(t) vs t 0.2500 0.2000 0.1500 0.1000 0.0500 0.0000
0
2
4
6
12
12
10
14
12
t [s] 0 150 175 200 225 240 250 260 275 300 325 350 375 400 450
Cx10-3 [g/L] Cmedx10-3 0 0 0 0.5 1 2 3 5.2 7.4 8.4 9.4 9.55 9.7 9.55 9.4 8.8 8.2 6.6 5 3.75 2.5 1.85 1.2 0.85 0.5 0.35 0.2 0.1 0 -
Δt 150 25 25 25 15 10 10 15 25 25 25 25 25 50 -
Δt * Cmed 0 12.5 50 130 126 95.5 95.5 132 165 93.75 46.25 21.25 8.75 5 981.5
E(t)x10-3 0 0 0.0010 0.0031 0.0075 0.0096 0.0099 0.0096 0.0084 0.0051 0.0025 0.0012 0.0005 0.0002 0.0000 0.0585838
E(t) 0 0 0.00000102 0.00000306 0.00000754 0.00000958 0.00000988 0.00000958 0.00000835 0.00000509 0.00000255 0.00000122 0.00000051 0.00000020 0.00000000 -
t * C * Δt 0 0 4.375 15 24.975 22.56 24.25 36.66 56.375 37.5 20.3125 10.5 4.6875 4 261.195
IMPULSO c) Varianza de la distribución σ2
1750.56137
d) Conversión k CA0
9.07421411 mol/l
σθ2
0.02504733
σθ
0.02507705 0.01269981 8.8327E-10
2
D/(uL) Control
0.0115 s-1
Utilizando el gráfico k*tm 1-XA XA
3.0402 0.09 0.91
el gráfico
C * Δt 0 0 0.025 0.075 0.111 0.094 0.097 0.141 0.205 0.125 0.0625 0.03 0.0125 0.01 0.988
(t-tm)^2*C*Δt EXP(kt)*E*Δt 0 0.000000 0 0.000000 199.6633 0.000191 310.7372 0.000762 172.0270 0.001504 55.8144 0.001513 20.0230 0.001752 2.6895 0.002857 23.1757 0.004935 158.7102 0.004012 229.7694 0.002674 219.9882 0.001711 152.9946 0.000950 183.9620 0.001014 1729.555 0.024
ρ PM
840 kg/m3 92.57 g/mol
a) Curva E(t)
E(t) vs t 0 0 0 0 0 0 0
0
50
100
150
200
250
300
b) Tiempo medio de residencia t(media)
264.367409 s
0.84 kg/l 0.09257 kg/mol
350
400
450
500
400
450
500
t [min] 0 2 4 6 8 9 10 11 12 13 14 15 16 18 20
C [mg/l] 0 0 0.8 2 4.4 9 12.6 20 30 34 36 38 39 40 40 SUMATORIA
k*CA0 V
ΔC 0 0.8 1.2 2.4 4.6 3.6 7.4 10 4 2 2 1 1 0 40
t*ΔC 0 1.6 4.8 14.4 36.8 32.4 74 110 48 26 28 15 16 0 407
F(t) 0 0 0.02 0.05 0.11 0.225 0.315 0.5 0.75 0.85 0.9 0.95 0.975 1 1 -
E(t) 2.44E-02 -1.43E-03 -1.41E-02 1.24E-02 6.85E-02 1.00E-01 1.30E-01 1.57E-01 1.80E-01 2.02E-01 2.27E-01 2.64E-01 3.27E-01 6.05E-01 1.28E+00 3.56E+00
E(t) -6.20E-03 5.48E-03 8.04E-03 1.88E-02 5.49E-02 8.79E-02 1.34E-01 1.95E-01 1.21E-01 9.82E-02 7.95E-02 6.50E-02 5.47E-02 4.67E-02 5.55E-02 1.02E+00
E(t)*t*Δt 0 0.02192 0.06432 0.22512 0.43936 0.79146 1.338 2.14126 1.4532 1.2766 1.113 0.975 1.7504 1.6812 13.27084
0.01 min-1 1 m3
a b c
9.00E-07 -4.00E-05 0.0006
a' b' c'
v0
0.01 m3/min
Cmáx
40 mg/l
d e f g
-0.0026 -0.0027 0.0244 -0.0055
d' e' f'
t(media) σ
13.27084 min
F(t) vs t
11.4821824
2
tm(nominal)
1.2
100 min
1 f(x) = 8.90220483431827E-07x^6 - 4.27267349539773E-05x^5 + 0.0006391486x^4 - 0.0026156342x^3 - 0.0026530592x^2 + 0.0244324912x - 0.0054824 R² = 0.9921857171
2.50E-01
0.8
2.00E-01 1.50E-01
0.6
1.00E-01
0.4
5.00E-02
0.2
0.00E+00 -5.00E-02
0
5
10
a) Aplicando el modelo de la dispersión
15
20
25
0
0
5
10
15
20
25
σθ2
0.065197
σθ
0.065201
2
D/(uL)
0.033739 Módulo de dispersión grande
Control
1.706313E-11
k*t*CA0
1
1-XA
0.5
XA
0.5
(t-tm)^2*E*Δt -2.1838284094 1.392268904 1.3820514668 1.9834990887 1.5257739465 1.6040321344 1.4314451581 1.0038060067 0.1955806544 0.0072033928 0.0422681073 0.1943496299 0.814845585 2.0888867321 11.4821823974
E*Δt -0.0124 0.01096 0.01608 0.03752 0.05492 0.08794 0.1338 0.19466 0.1211 0.0982 0.0795 0.065 0.1094 0.0934 1.09008
C vs t 45 40 35 30 25 20 15 10 5 0
0
5
10
15
20
25
ESCALÓN
5.40E-06 -2.00E-04 0.0024
a b c
9.00E-05 -0.0011 0.0055
a' b' c'
3.60E-04 -0.0033 0.011
a b c
-0.0078 -0.0054 0.0244
d e
-0.0062 -0.0005
d'
-0.0062
d
91486x^4 - 0.0026156342x^3 - 0.0026530592x^2 + 0.0244324912x - 0.0054824118
0.6
1.2
0.5 f(x) = 8.98713657916654E-05x^4 - 0.0010613353x^3 + 0.0054864684x^2 - 0.0061527134x - 0.0005122122 R² = 0.9965873158 0.4
1 f(x) = 0.0006558159x^3 - 0.0377117561x^ R² = 0.9976127046 0.8
0.3
0.6
0.2
0.4
0.1
0.2
0
0 0
2
4
6
8
10
12
b) Aplicando el modelo de tanques en serie
11
12
13
14
15
16
17
N
15.338129
1-XA
0.5
XA
0.5
7.00E-04 -0.0377 0.7235
a' b' c'
2.10E-03 -0.0754 0.7235
-3.632
= 0.0006558159x^3 - 0.0377117561x^2 + 0.7235425131x - 3.6320176559 0.9976127046
11
12
13
14
15
16
17
18
19
20
21
C [mol/L] 0 1 5 8 10 8 6 4 3 2.2 1.5 0.6 0
k t(media) varianza σ2
Cmed 0.5 3 6.5 9 9 7 5 3.5 2.6 1.85 1.05 0.3 -
Δt Δt * Cmed 1 0.5 1 3 1 6.5 1 9 1 9 1 7 1 5 1 3.5 1 2.6 1 1.85 1 1.05 1 0.3 SUMATORIA 49.3
0.1 min-1 4.957 4.994
Flujo NO IDEAL, utilizo modelo de dispersión: varianza(θ) σ2
0.203
D/(u*L)
0.1148
varianza (θ) σ2 Control k*tm
0.2032 0.0000 0.4957
Dispersión grande
Utilizando el gráfico: 1-XA
0.55
XA
0.45 Calculando por cinética:
CA/CA0
0.624
1-XA
0.624
XA
0.376
E(t) 0.0000 0.0203 0.1014 0.1623 0.2028 0.1623 0.1217 0.0811 0.0609 0.0446 0.0304 0.0122 0 1
t * C * Δt 0 1 10 24 40 40 36 28 24 19.8 15 6.6 244.4
IMPULSO
C * Δt 0 1 5 8 10 8 6 4 3 2.2 1.5 0.6 49.3
(t-tm)^2*C*Δt EXP(kt)*E*Δt 0.0000 0.0000 15.6610 0.0184 43.7312 0.0830 30.6514 0.1202 9.1662 0.1360 0.0145 0.0984 6.5220 0.0668 16.6888 0.0403 27.7722 0.0273 35.9537 0.0181 38.1417 0.0112 21.9078 0.0041 246.211 0.624
C vs t 12 10 8 6 4 2 0
0
2
4
6
8
10
12
8
10
14
E(t) vs t 0.2500 0.2000 0.1500 0.1000 0.0500 0.0000
0
2
4
6
12
12
10
14
12
t [s] 0 150 175 200 225 240 250 260 275 300 325 350 375 400 450
Cx10-3 [g/L] Cmedx10-3 0 0 0 0.5 1 2 3 5.2 7.4 8.4 9.4 9.55 9.7 9.55 9.4 8.8 8.2 6.6 5 3.75 2.5 1.85 1.2 0.85 0.5 0.35 0.2 0.1 0 -
Δt 150 25 25 25 15 10 10 15 25 25 25 25 25 50 -
Δt * Cmed 0 12.5 50 130 126 95.5 95.5 132 165 93.75 46.25 21.25 8.75 5 981.5
E(t)x10-3 0 0 0.0010 0.0031 0.0075 0.0096 0.0099 0.0096 0.0084 0.0051 0.0025 0.0012 0.0005 0.0002 0.0000 0.0585838
E(t) 0 0 0.00000102 0.00000306 0.00000754 0.00000958 0.00000988 0.00000958 0.00000835 0.00000509 0.00000255 0.00000122 0.00000051 0.00000020 0.00000000 -
t * C * Δt 0 0 4.375 15 24.975 22.56 24.25 36.66 56.375 37.5 20.3125 10.5 4.6875 4 261.195
IMPULSO c) Varianza de la distribución σ2
1750.56137
d) Conversión k CA0
9.07421411 mol/l
σθ2
0.02504733
σθ
0.02507705 0.01269981 8.8327E-10
2
D/(uL) Control
0.0115 s-1
Utilizando el gráfico k*tm 1-XA XA
3.0402 0.09 0.91
el gráfico
C * Δt 0 0 0.025 0.075 0.111 0.094 0.097 0.141 0.205 0.125 0.0625 0.03 0.0125 0.01 0.988
(t-tm)^2*C*Δt EXP(kt)*E*Δt 0 0.000000 0 0.000000 199.6633 0.000191 310.7372 0.000762 172.0270 0.001504 55.8144 0.001513 20.0230 0.001752 2.6895 0.002857 23.1757 0.004935 158.7102 0.004012 229.7694 0.002674 219.9882 0.001711 152.9946 0.000950 183.9620 0.001014 1729.555 0.024
ρ PM
840 kg/m3 92.57 g/mol
a) Curva E(t)
E(t) vs t 0 0 0 0 0 0 0
0
50
100
150
200
250
300
b) Tiempo medio de residencia t(media)
264.367409 s
0.84 kg/l 0.09257 kg/mol
350
400
450
500
400
450
500
t [min] 0 2 4 6 8 9 10 11 12 13 14 15 16 18 20
C [mg/l] 0 0 0.8 2 4.4 9 12.6 20 30 34 36 38 39 40 40 SUMATORIA
k*CA0 V
ΔC 0 0.8 1.2 2.4 4.6 3.6 7.4 10 4 2 2 1 1 0 40
t*ΔC 0 1.6 4.8 14.4 36.8 32.4 74 110 48 26 28 15 16 0 407
F(t) 0 0 0.02 0.05 0.11 0.225 0.315 0.5 0.75 0.85 0.9 0.95 0.975 1 1 -
E(t) 2.44E-02 -1.43E-03 -1.41E-02 1.24E-02 6.85E-02 1.00E-01 1.30E-01 1.57E-01 1.80E-01 2.02E-01 2.27E-01 2.64E-01 3.27E-01 6.05E-01 1.28E+00 3.56E+00
E(t) -6.20E-03 5.48E-03 8.04E-03 1.88E-02 5.49E-02 8.79E-02 1.34E-01 1.95E-01 1.21E-01 9.82E-02 7.95E-02 6.50E-02 5.47E-02 4.67E-02 5.55E-02 1.02E+00
E(t)*t*Δt 0 0.02192 0.06432 0.22512 0.43936 0.79146 1.338 2.14126 1.4532 1.2766 1.113 0.975 1.7504 1.6812 13.27084
0.01 min-1 1 m3
a b c
9.00E-07 -4.00E-05 0.0006
a' b' c'
v0
0.01 m3/min
Cmáx
40 mg/l
d e f g
-0.0026 -0.0027 0.0244 -0.0055
d' e' f'
t(media) σ
13.27084 min
F(t) vs t
11.4821824
2
tm(nominal)
1.2
100 min
1 f(x) = 8.90220483431827E-07x^6 - 4.27267349539773E-05x^5 + 0.0006391486x^4 - 0.0026156342x^3 - 0.0026530592x^2 + 0.0244324912x - 0.0054824 R² = 0.9921857171
2.50E-01
0.8
2.00E-01 1.50E-01
0.6
1.00E-01
0.4
5.00E-02
0.2
0.00E+00 -5.00E-02
0
5
10
a) Aplicando el modelo de la dispersión
15
20
25
0
0
5
10
15
20
25
σθ2
0.065197
σθ
0.065201
2
D/(uL)
0.033739 Módulo de dispersión grande
Control
1.706313E-11
k*t*CA0
1
1-XA
0.5
XA
0.5
(t-tm)^2*E*Δt -2.1838284094 1.392268904 1.3820514668 1.9834990887 1.5257739465 1.6040321344 1.4314451581 1.0038060067 0.1955806544 0.0072033928 0.0422681073 0.1943496299 0.814845585 2.0888867321 11.4821823974
E*Δt -0.0124 0.01096 0.01608 0.03752 0.05492 0.08794 0.1338 0.19466 0.1211 0.0982 0.0795 0.065 0.1094 0.0934 1.09008
C vs t 45 40 35 30 25 20 15 10 5 0
0
5
10
15
20
25
ESCALÓN
5.40E-06 -2.00E-04 0.0024
a b c
9.00E-05 -0.0011 0.0055
a' b' c'
3.60E-04 -0.0033 0.011
a b c
-0.0078 -0.0054 0.0244
d e
-0.0062 -0.0005
d'
-0.0062
d
91486x^4 - 0.0026156342x^3 - 0.0026530592x^2 + 0.0244324912x - 0.0054824118
0.6
1.2
0.5 f(x) = 8.98713657916654E-05x^4 - 0.0010613353x^3 + 0.0054864684x^2 - 0.0061527134x - 0.0005122122 R² = 0.9965873158 0.4
1 f(x) = 0.0006558159x^3 - 0.0377117561x^ R² = 0.9976127046 0.8
0.3
0.6
0.2
0.4
0.1
0.2
0
0 0
2
4
6
8
10
12
b) Aplicando el modelo de tanques en serie
11
12
13
14
15
16
17
N
15.338129
1-XA
0.5
XA
0.5
7.00E-04 -0.0377 0.7235
a' b' c'
2.10E-03 -0.0754 0.7235
-3.632
= 0.0006558159x^3 - 0.0377117561x^2 + 0.7235425131x - 3.6320176559 0.9976127046
11
12
13
14
15
16
17
18
19
20
21
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