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Control de Un Reactor CSTR
Control de Un Reactor CSTR
Control de Un Reactor CSTR
SEMESTRE : X
SECCIÓN : A
HUANCAYO-PERÚ
2013
CONTROL DE PROCESOS
Fe, Te,
CA0
V, T0, Cp,
V, Ts, Cp, F, T, CA
VARIABLES:
VARIABLE A CONTROLAR
VARIABLE DE PERTURBACIÓN
VARIABLE A MANIPULAR
SET POINT
CONTROL FEEDBACK
Fe, Te,
CA0
T V, T0, Cp,
V, Ts, Cp, F, T, CA
CONTROL FEED-FORWARD
T Controlador
Fe, Te, Anticipativo
CA0
T V, T0, Cp,
V, Ts, Cp, F, T, CA
CONTROL DE PROCESOS
dr ( t )
q ρ c p T 0 (t ) − V r A (t ) ( ΔH r ) − U A (T ( t) − T s ) − q ρ c p T (t ) =V ρ cv
dt …(1)
dcA(t )
V =0
dt
q (c A0 − c A ) − V r A = 0
q (c A 0 − c A ) = V r A ...........................................................(2)
De la Ecuación. (1):
dT ( t)
Vρ c v =0
dt
q ρ c p T o( t) − V r A (t ) ( Δ Hr ) − UA (T ( t ) − T s ) − q ρ c p T ( t ) = 0 .. . ..(3 )
dT
qρC p T 0 −V ( Δ Hr ) r̄ A−V ( Δ Hr )c 1 T (t )−V ( Δ Hr )c 2 C A( t )−UA (T (t )−T s )−qρC p T ( t)=VρC v . .. .. .(4 )
(t ) dt
Llevando la ecuación (4) a variables de desviación:
−
dT
VρC V =qρ CpT 0 (t )−V ( ΔH r ) r A−V ( ΔH r )C 1 T ( t)−V ( ΔH r )C 2 CA (T )−UA ( T (t )−T S )−qρC p T ( t ) . . .. .( a )
dt
En estado estacionario:
CONTROL DE PROCESOS
dT
VρC V =qρCp T 0(t )−V ( ΔH r )r A−V ( ΔH r )C 1 T ( t )−V ( ΔH r )C 2 C A (T )−UA (T ( t )−T S )−qρC p T ( t) . .. .. (b)
dt
dT 1 1
VρC V =qρCpT 0 −V ( ΔH r )C1 T −V ( ΔH r )C 2 CA 1 −UAT 1 −qρC p T 1 . . .. .(5)
dt (t )
De la Ecuación (5)
dT
qρ CpT 0( T )−V ( ΔH r )C 1 T ( t )−V ( ΔH r )C2 CA ( t)−UAT ( t)−qρC p T ( t)=VρC V
dt
dT
qρ CpT 0( T )−T ( t ) [ V ( ΔH r ) C1 +UA +qρC p ]−V ( ΔH r )C 2 CA (t )=VρC V
dt
dT
VρC V + T (t ) [ V ( ΔH r ) C 1 + UA +qρC p ]=qρCpT 0( T )−V ( ΔH r ) C 2 CA ( t )
dt
VρC V dT qρ Cp V ( ΔH r ) C2
+T (t )= T − CA ( t ) . .. .. ( 6)
V ( ΔH r ) C 1 +UA +qρC p dt V ( ΔH r ) C1 +UA +qρC p 0( T ) V ( ΔH r ) C1 +UA + qρC p
VρC V
τ 2=
V ( ΔH r )C 1 +UA +qρC p
Ganancia Estática
qρC p
K 3=
V ( ΔH r )C 1 +UA +qρC p
V ( ΔH r )C 2
K 4=
V ( ΔH r )C 1 +UA+qρC p
Ecuación. (6)
dT ( t )
τ2. +T (t )=K 3 . T o ( t )−K 4 CA ( t )
dt
De la Ecuación. (6)
CONTROL DE PROCESOS
K3 K4
T ( s)= .T o( s)− .CA(s)......................................................(7)
(τ 2 s+1) ( τ 2 s+1)
De (7)
T (s ) K3
=
T o (s ) τ 2 s+1
T( s) K4
=
CA (s ) τ 2 s+1