TITLE MULTI VESSEL BATCH DISTILLATION
#
# Plant consists of 3 column sections, 2 intermediate vessels,
# reboiler, total condenser and accumulator (trays are numbered
# from the top and down).
# Vapor bypassing the intermediate vessels
#
# There are 4 components. The lightest product is accumulated
# in the condenser, the second lightest in the upper vessel,
# the third lightest in the lower vessel and the heaviest in
# the reboiler.
#
# The mathematical model assumes constant relative volatility
# (relative to the heaviest component) and linear tray
# hydraulics. Separation is taking place in the vessels too.
#
# Control algorithm: 3 PI-controllers which control the
# temperature in the middle of the column sections.
# Manipulated variable is the liquid flow from the vessel
# above. Set points for the controllers are average boiling
# temperature between the two separated components
#
# The termination criterion is based on approach to steady
# state; max[xt(t)-xt(t-0.01)] in the condenser, vessels and
# reboiler.
#
# Two report forms: Multi_vessel and Summary.
#
#---------------------------------------------------------------
#
# Dummy variable XT in most models. Reason: Can not use derivative
# variable (xt) in input/output streams (use xo instead).
#
# Composition changes as separate variables in condenser,
# vessels and reboiler. Reason: Can not use arrays in connections.
#
#---------------------------------------------------------------
#
# Author: Bernd Wittgens, based on E. Sorensen
# Date: 10.10.95
#
****
OPTIONS
ROUTINES DAE
EXECUTION
PRINTLEVEL = 2 # level of output during solution
TARGET = terminal # device to which output is directed
REL_TOL = 1E-8 # relative tolerence
ABS_TOL = 1E-8 # absolute tolerence
EVENT_TOL = 1E-8 # event tolerance
INTERVALS = 100 # number of time steps for dynamic solution
TIME_STEP = 0.1 # length of time step for storing data
DEBUG = OFF # switch for additional information
****
DECLARE
TYPE
FLOWRATE = 10.0 : 0 : 50 Unit = "kmol/hr"
MOLE_FRACTION = 0.5 : 0 : 1 Unit = "-------"
MOLAR_HOLDUP = 3.0 : 0 : 25 Unit = "kmol"
REFLUX_RATIO = 1 : 0 :1.0E10 Unit = "-------"
EQ_CONST = 1 : 0.01 : 100 Unit = "-------"
NOTYPE = 1 : -100 : 250 Unit = "-------"
TEMPERATURE = 90 : 50 : 130 UNIT = "deg. C "
STREAM MAINSTREAM
SET NC = 4
TYPE FLOWRATE, MOLE_FRACTION(NC)
****
MODEL CONDENSER # Condenser model #
SET NC
TYPE
LO,VI,L_CNTR AS FLOWRATE
XO,YI,XD,XT AS ARRAY(NC) OF MOLE_FRACTION
HT,HC AS MOLAR_HOLDUP
R AS REFLUX_RATIO
T AS TEMPERATURE
TB AS ARRAY(NC) OF TEMPERATURE
SS_XT_1,SS_XT_2 AS NOTYPE
SS_XT_3,SS_XT_4 AS NOTYPE
MINUS AS NOTYPE
STREAM
INPUT 1 VI,YI
OUTPUT 1 LO,XO
CONNECTION 1 L_CNTR # From controller #
CONNECTION 2 SS_XT_1 # Approach to steady_state #
CONNECTION 3 SS_XT_2 # Approach to steady_state #
CONNECTION 4 SS_XT_3 # Approach to steady_state #
CONNECTION 5 SS_XT_4 # Approach to steady_state #
CONNECTION 6 T
EQUATION
# Material balance #
$HT = VI - LO ;
HC * $XT + XT * $HT = VI * YI - LO * XD ;
HT = HC ;
XT = XO = XD ;
# Reflux ratio #
R * VI = LO ;
# Controller #
LO = L_CNTR ;
# Temperature #
T = Tb(1)*xt(1)+Tb(2)*xt(2)+Tb(3)*xt(3)+Tb(4)*xt(4);
# Steady state measure = xt(t)-xt(t-minus) #
SS_XT_1 = XT(1) - (DELAY XT(1) BY MINUS) ;
SS_XT_2 = XT(2) - (DELAY XT(2) BY MINUS) ;
SS_XT_3 = XT(3) - (DELAY XT(3) BY MINUS) ;
SS_XT_4 = XT(4) - (DELAY XT(4) BY MINUS) ;
****
MODEL PI_CONTROLLER # Proportional controller
SET CLIP = 1
TYPE
MEASURE, SET_POINT AS NOTYPE
BIAS,GAIN, reset AS NOTYPE
ERROR, I_error, eps AS NOTYPE
CALC_VALUE,CONT AS NOTYPE
CONTROL_ACTION AS NOTYPE
MAX,MIN AS NOTYPE
CNTR_FLAG,SET_FLOW AS NOTYPE
STREAM
CONNECTION 1 MEASURE
CONNECTION 2 CONTROL_ACTION
EQUATION
ERROR = SET_POINT - MEASURE ;
$I_error = eps ;
CALC_VALUE = BIAS + GAIN * (error + I_error/reset) ;
# Clip if required #
IF CLIP = 1 THEN
IF CALC_VALUE > MAX THEN
CONT = MAX
ELSE IF CALC_VALUE < MIN THEN
CONT = MIN
ELSE
CONT = CALC_VALUE
ENDIF
ENDIF
ELSE
CONT = CALC_VALUE
ENDIF ;
IF CNTR_FLAG = 1 THEN
CONTROL_ACTION = CONT
ELSE
CONTROL_ACTION = SET_FLOW
ENDIF ;
# antiwindup
IF < <calc_value <= min> OR <calc_value => max> > then
eps = 0.0
else
eps = error
endif;
****
MODEL P_CONTROLLER # Proportional controller
SET CLIP = 1
TYPE
MEASURE, SET_POINT AS NOTYPE
BIAS,GAIN,ERROR AS NOTYPE
CALC_VALUE,CONT AS NOTYPE
CONTROL_ACTION AS NOTYPE
MAX,MIN AS NOTYPE
CNTR_FLAG,SET_FLOW AS NOTYPE
STREAM
CONNECTION 1 MEASURE
CONNECTION 2 CONTROL_ACTION
EQUATION
ERROR = SET_POINT - MEASURE ;
CALC_VALUE = BIAS + GAIN * ERROR ;
# Clip if required #
IF CLIP = 1 THEN
IF CALC_VALUE > MAX THEN
CONT = MAX
ELSE IF CALC_VALUE < MIN THEN
CONT = MIN
ELSE
CONT = CALC_VALUE
ENDIF
ENDIF
ELSE
CONT = CALC_VALUE
ENDIF ;
IF CNTR_FLAG = 1 THEN
CONTROL_ACTION = CONT
ELSE
CONTROL_ACTION = SET_FLOW
ENDIF ;
****
MODEL REBOILER # Reboiler model #
SET NC
TYPE
LI,VO AS FLOWRATE
XI,YO,XN,XT AS ARRAY(NC) OF MOLE_FRACTION
HT,HN AS MOLAR_HOLDUP
K AS ARRAY(NC) OF EQ_CONST
SS_XT_1,SS_XT_2 AS NOTYPE
SS_XT_3,SS_XT_4 AS NOTYPE
MINUS AS NOTYPE
T AS TEMPERATURE
TB AS ARRAY(NC) OF TEMPERATURE
STREAM
INPUT 1 LI,XI
OUTPUT 1 VO,YO
CONNECTION 1 SS_XT_1 # Approach to steady_state #
CONNECTION 2 SS_XT_2 # Approach to steady_state #
CONNECTION 3 SS_XT_3 # Approach to steady_state #
CONNECTION 4 SS_XT_4 # Approach to steady_state #
CONNECTION 5 T
EQUATION
# Material balance #
$HT = LI - VO ;
HT * $XT + XT * $HT = LI * XI - VO * YO ;
HT = HN ;
XT = XN ;
# Phase equilibrium #
YO(2:NC) * XN(1) = K(2:NC)/K(1) * XN(2:NC) * YO(1) ;
SIGMA(YO) = 1.0 ;
# Temperature #
T = Tb(1)*xt(1)+Tb(2)*xt(2)+Tb(3)*xt(3)+Tb(4)*xt(4);
# Steady state measure = xt(t)-xt(t-minus) #
SS_XT_1 = XT(1) - (DELAY XT(1) BY MINUS) ;
SS_XT_2 = XT(2) - (DELAY XT(2) BY MINUS) ;
SS_XT_3 = XT(3) - (DELAY XT(3) BY MINUS) ;
SS_XT_4 = XT(4) - (DELAY XT(4) BY MINUS) ;
****
MODEL STEADY_STATE # Returns maximum change in composition over time interval #
SET NNC=16
TYPE
COND_SS_XT_1,COND_SS_XT_2 AS NOTYPE
COND_SS_XT_3,COND_SS_XT_4 AS NOTYPE
V_A_SS_XT_1,V_A_SS_XT_2 AS NOTYPE
V_A_SS_XT_3,V_A_SS_XT_4 AS NOTYPE
V_B_SS_XT_1,V_B_SS_XT_2 AS NOTYPE
V_B_SS_XT_3,V_B_SS_XT_4 AS NOTYPE
REB_SS_XT_1,REB_SS_XT_2 AS NOTYPE
REB_SS_XT_3,REB_SS_XT_4 AS NOTYPE
SS AS ARRAY(NNC) OF NOTYPE
MAX_SS AS NOTYPE
STREAM
CONNECTION 1 COND_SS_XT_1 # From condenser #
CONNECTION 2 COND_SS_XT_2
CONNECTION 3 COND_SS_XT_3
CONNECTION 4 COND_SS_XT_4
CONNECTION 5 V_A_SS_XT_1 # From vessel_A #
CONNECTION 6 V_A_SS_XT_2
CONNECTION 7 V_A_SS_XT_3
CONNECTION 8 V_A_SS_XT_4
CONNECTION 9 V_B_SS_XT_1 # From vessel_B #
CONNECTION 10 V_B_SS_XT_2
CONNECTION 11 V_B_SS_XT_3
CONNECTION 12 V_B_SS_XT_4
CONNECTION 13 REB_SS_XT_1 # From reboiler #
CONNECTION 14 REB_SS_XT_2
CONNECTION 15 REB_SS_XT_3
CONNECTION 16 REB_SS_XT_4
EQUATION
# All composition changes in an array #
SS(1) = COND_SS_XT_1 ; SS(2) = COND_SS_XT_2 ;
SS(3) = COND_SS_XT_3 ; SS(4) = COND_SS_XT_4 ;
SS(5) = V_A_SS_XT_1 ; SS(6) = V_A_SS_XT_2 ;
SS(7) = V_A_SS_XT_3 ; SS(8) = V_A_SS_XT_4 ;
SS(9) = V_B_SS_XT_1 ; SS(10) = V_B_SS_XT_2 ;
SS(11) = V_B_SS_XT_3 ; SS(12) = V_B_SS_XT_4 ;
SS(13) = REB_SS_XT_1 ; SS(14) = REB_SS_XT_2 ;
SS(15) = REB_SS_XT_1 ; SS(16) = REB_SS_XT_2 ;
# Largest steady state deviation #
MAX_SS = SMAX(SS) ;
****
MODEL TRAY # Column tray model #
SET NC
TYPE
LO_INIT,LI,VO,VI,LO AS FLOWRATE
XI,XO,YO,YI,XT AS ARRAY(NC) OF MOLE_FRACTION
X1,X2,X3,X4 AS MOLE_FRACTION
HI_INIT,HI,HT AS MOLAR_HOLDUP
K AS ARRAY(NC) OF EQ_CONST
TAU AS NOTYPE
T AS TEMPERATURE
TB AS ARRAY(NC) OF TEMPERATURE
STREAM
INPUT 1 LI,XI
INPUT 2 VI,YI
OUTPUT 1 LO,XO
OUTPUT 2 VO,YO
CONNECTION 1 X1 # Composition of component 1 #
CONNECTION 2 X2 # Composition of component 2 #
CONNECTION 3 X3 # Composition of component 3 #
CONNECTION 4 X4 # Composition of component 4 #
CONNECTION 5 T
EQUATION
# Material balance #
$HT = LI + VI - LO - VO ;
HT * $XT + XT * $HT = LI * XI + VI * YI - LO * XO - VO * YO ;
HT = HI ;
XT = XO ;
# Constant molar flows #
VI = VO ;
# Phase equilibrium #
YO(2:NC) * XO(1) = K(2:NC)/K(1) * XO(2:NC) * YO(1) ;
SIGMA(YO) = 1.0 ;
# Temperature #
T = Tb(1)*xt(1)+Tb(2)*xt(2)+Tb(3)*xt(3)+Tb(4)*xt(4);
# Tray hydraulics #
(LO - LO_INIT) * TAU = HI - HI_INIT ;
TAU = 2/3 * HI/LO ;
# Measurements used by controllers #
X1 = XO(1) ;
X2 = XO(2) ;
X3 = XO(3) ;
X4 = XO(4) ;
****
MODEL VESSEL # Intermediate storage vessel model #
SET NC
TYPE
LI,LO,L_CNTR AS FLOWRATE
XI,XO,XT AS ARRAY(NC) OF MOLE_FRACTION
HT,HI AS MOLAR_HOLDUP
SS_XT_1,SS_XT_2 AS NOTYPE
SS_XT_3,SS_XT_4 AS NOTYPE
MINUS AS NOTYPE
T AS TEMPERATURE
TB AS ARRAY(NC) OF TEMPERATURE
STREAM
INPUT 1 LI,XI
OUTPUT 1 LO,XO
CONNECTION 1 L_CNTR # From controller #
CONNECTION 2 SS_XT_1 # Approach to steady_state #
CONNECTION 3 SS_XT_2 # Approach to steady_state #
CONNECTION 4 SS_XT_3 # Approach to steady_state #
CONNECTION 5 SS_XT_4 # Approach to steady_state #
CONNECTION 6 T
EQUATION
# Material balance #
$HT = LI - LO ;
HT * $XT + XT * $HT = LI * XI - LO * XO ;
HT = HI ;
XT = XO ;
# Controller #
LO = L_CNTR ;
# Temperature #
T = Tb(1)*xt(1)+Tb(2)*xt(2)+Tb(3)*xt(3)+Tb(4)*xt(4);
# Steady state measure = xt(t)-xt(t-minus) #
SS_XT_1 = XT(1) - (DELAY XT(1) BY MINUS) ;
SS_XT_2 = XT(2) - (DELAY XT(2) BY MINUS) ;
SS_XT_3 = XT(3) - (DELAY XT(3) BY MINUS) ;
SS_XT_4 = XT(4) - (DELAY XT(4) BY MINUS) ;
****
FLOWSHEET
# Liquid flows (top and down)..
# reflux to column section A
STREAM L1_FEED OUTPUT 1 OF cond IS INPUT 1 OF TRAY_A1
STREAM L2_FEED OUTPUT 1 OF TRAY_A1 IS INPUT 1 OF TRAY_A2
STREAM L3_FEED OUTPUT 1 OF TRAY_A2 IS INPUT 1 OF TRAY_A3
STREAM L4_FEED OUTPUT 1 OF TRAY_A3 IS INPUT 1 OF TRAY_A4
STREAM L5_FEED OUTPUT 1 OF TRAY_A4 IS INPUT 1 OF TRAY_A5
STREAM L6_FEED OUTPUT 1 OF TRAY_A5 IS INPUT 1 OF TRAY_A6
STREAM L7_FEED OUTPUT 1 OF TRAY_A6 IS INPUT 1 OF TRAY_A7
STREAM L8_FEED OUTPUT 1 OF TRAY_A7 IS INPUT 1 OF TRAY_A8
STREAM L9_FEED OUTPUT 1 OF TRAY_A8 IS INPUT 1 OF TRAY_A9
STREAM L10_FEED OUTPUT 1 OF TRAY_A9 IS INPUT 1 OF TRAY_A10
STREAM L11_FEED OUTPUT 1 OF TRAY_A10 IS INPUT 1 OF TRAY_A11
STREAM L12_FEED OUTPUT 1 OF TRAY_A11 IS INPUT 1 OF VESSEL_A
STREAM L13_FEED OUTPUT 1 OF VESSEL_A IS INPUT 1 OF TRAY_B1
STREAM L14_FEED OUTPUT 1 OF TRAY_B1 IS INPUT 1 OF TRAY_B2
STREAM L15_FEED OUTPUT 1 OF TRAY_B2 IS INPUT 1 OF TRAY_B3
STREAM L16_FEED OUTPUT 1 OF TRAY_B3 IS INPUT 1 OF TRAY_B4
STREAM L17_FEED OUTPUT 1 OF TRAY_B4 IS INPUT 1 OF TRAY_B5
STREAM L18_FEED OUTPUT 1 OF TRAY_B5 IS INPUT 1 OF TRAY_B6
STREAM L19_FEED OUTPUT 1 OF TRAY_B6 IS INPUT 1 OF TRAY_B7
STREAM L20_FEED OUTPUT 1 OF TRAY_B7 IS INPUT 1 OF TRAY_B8
STREAM L21_FEED OUTPUT 1 OF TRAY_B8 IS INPUT 1 OF TRAY_B9
STREAM L22_FEED OUTPUT 1 OF TRAY_B9 IS INPUT 1 OF TRAY_B10
STREAM L23_FEED OUTPUT 1 OF TRAY_B10 IS INPUT 1 OF TRAY_B11
STREAM L24_FEED OUTPUT 1 OF TRAY_B11 IS INPUT 1 OF VESSEL_B
STREAM L25_FEED OUTPUT 1 OF VESSEL_B IS INPUT 1 OF TRAY_C1
STREAM L26_FEED OUTPUT 1 OF TRAY_C1 IS INPUT 1 OF TRAY_C2
STREAM L27_FEED OUTPUT 1 OF TRAY_C2 IS INPUT 1 OF TRAY_C3
STREAM L28_FEED OUTPUT 1 OF TRAY_C3 IS INPUT 1 OF TRAY_C4
STREAM L29_FEED OUTPUT 1 OF TRAY_C4 IS INPUT 1 OF TRAY_C5
STREAM L30_FEED OUTPUT 1 OF TRAY_C5 IS INPUT 1 OF TRAY_C6
STREAM L31_FEED OUTPUT 1 OF TRAY_C6 IS INPUT 1 OF TRAY_C7
STREAM L32_FEED OUTPUT 1 OF TRAY_C7 IS INPUT 1 OF TRAY_C8
STREAM L33_FEED OUTPUT 1 OF TRAY_C8 IS INPUT 1 OF TRAY_C9
STREAM L34_FEED OUTPUT 1 OF TRAY_C9 IS INPUT 1 OF TRAY_C10
STREAM L35_FEED OUTPUT 1 OF TRAY_C10 IS INPUT 1 OF TRAY_C11
STREAM L36_FEED OUTPUT 1 OF TRAY_C11 IS INPUT 1 OF REB
# Vapour flows (bottom and up)..
STREAM V1_FEED OUTPUT 1 OF REB IS INPUT 2 OF TRAY_C11
STREAM V2_FEED OUTPUT 2 OF TRAY_C11 IS INPUT 2 OF TRAY_C10
STREAM V3_FEED OUTPUT 2 OF TRAY_C10 IS INPUT 2 OF TRAY_C9
STREAM V4_FEED OUTPUT 2 OF TRAY_C9 IS INPUT 2 OF TRAY_C8
STREAM V5_FEED OUTPUT 2 OF TRAY_C8 IS INPUT 2 OF TRAY_C7
STREAM V6_FEED OUTPUT 2 OF TRAY_C7 IS INPUT 2 OF TRAY_C6
STREAM V7_FEED OUTPUT 2 OF TRAY_C6 IS INPUT 2 OF TRAY_C5
STREAM V8_FEED OUTPUT 2 OF TRAY_C5 IS INPUT 2 OF TRAY_C4
STREAM V9_FEED OUTPUT 2 OF TRAY_C4 IS INPUT 2 OF TRAY_C3
STREAM V10_FEED OUTPUT 2 OF TRAY_C3 IS INPUT 2 OF TRAY_C2
STREAM V11_FEED OUTPUT 2 OF TRAY_C2 IS INPUT 2 OF TRAY_C1
STREAM V12_FEED OUTPUT 2 OF TRAY_C1 IS INPUT 2 OF TRAY_B11
STREAM V13_FEED OUTPUT 2 OF TRAY_B11 IS INPUT 2 OF TRAY_B10
STREAM V14_FEED OUTPUT 2 OF TRAY_B10 IS INPUT 2 OF TRAY_B9
STREAM V15_FEED OUTPUT 2 OF TRAY_B9 IS INPUT 2 OF TRAY_B8
STREAM V16_FEED OUTPUT 2 OF TRAY_B8 IS INPUT 2 OF TRAY_B7
STREAM V17_FEED OUTPUT 2 OF TRAY_B7 IS INPUT 2 OF TRAY_B6
STREAM V18_FEED OUTPUT 2 OF TRAY_B6 IS INPUT 2 OF TRAY_B5
STREAM V19_FEED OUTPUT 2 OF TRAY_B5 IS INPUT 2 OF TRAY_B4
STREAM V20_FEED OUTPUT 2 OF TRAY_B4 IS INPUT 2 OF TRAY_B3
STREAM V21_FEED OUTPUT 2 OF TRAY_B3 IS INPUT 2 OF TRAY_B2
STREAM V22_FEED OUTPUT 2 OF TRAY_B2 IS INPUT 2 OF TRAY_B1
STREAM V23_FEED OUTPUT 2 OF TRAY_B1 IS INPUT 2 OF TRAY_A11
STREAM V24_FEED OUTPUT 2 OF TRAY_A11 IS INPUT 2 OF TRAY_A10
STREAM V25_FEED OUTPUT 2 OF TRAY_A10 IS INPUT 2 OF TRAY_A9
STREAM V26_FEED OUTPUT 2 OF TRAY_A9 IS INPUT 2 OF TRAY_A8
STREAM V27_FEED OUTPUT 2 OF TRAY_A8 IS INPUT 2 OF TRAY_A7
STREAM V28_FEED OUTPUT 2 OF TRAY_A7 IS INPUT 2 OF TRAY_A6
STREAM V29_FEED OUTPUT 2 OF TRAY_A6 IS INPUT 2 OF TRAY_A5
STREAM V30_FEED OUTPUT 2 OF TRAY_A5 IS INPUT 2 OF TRAY_A4
STREAM V31_FEED OUTPUT 2 OF TRAY_A4 IS INPUT 2 OF TRAY_A3
STREAM V32_FEED OUTPUT 2 OF TRAY_A3 IS INPUT 2 OF TRAY_A2
STREAM V33_FEED OUTPUT 2 OF TRAY_A2 IS INPUT 2 OF TRAY_A1
STREAM V34_FEED OUTPUT 2 OF TRAY_A1 IS INPUT 1 OF COND
# Controlling composition 1 in Condenser..
CONNECTION 1 OF CNTR_1 IS CONNECTION 5 OF TRAY_A6
CONNECTION 2 OF CNTR_1 IS CONNECTION 1 OF COND
# Controlling composition 2 in Vessel A..
CONNECTION 1 OF CNTR_2 IS CONNECTION 5 OF TRAY_B6
CONNECTION 2 OF CNTR_2 IS CONNECTION 1 OF VESSEL_A
# Controlling composition 3 in Vessel B..
CONNECTION 1 OF CNTR_3 IS CONNECTION 5 OF TRAY_C6
CONNECTION 2 OF CNTR_3 IS CONNECTION 1 OF VESSEL_B
# Connections for composition change measure #
CONNECTION 1 OF ST_STATE IS CONNECTION 2 OF COND
CONNECTION 2 OF ST_STATE IS CONNECTION 3 OF COND
CONNECTION 3 OF ST_STATE IS CONNECTION 4 OF COND
CONNECTION 4 OF ST_STATE IS CONNECTION 5 OF COND
CONNECTION 5 OF ST_STATE IS CONNECTION 2 OF VESSEL_A
CONNECTION 6 OF ST_STATE IS CONNECTION 3 OF VESSEL_A
CONNECTION 7 OF ST_STATE IS CONNECTION 4 OF VESSEL_A
CONNECTION 8 OF ST_STATE IS CONNECTION 5 OF VESSEL_A
CONNECTION 9 OF ST_STATE IS CONNECTION 2 OF VESSEL_B
CONNECTION 10 OF ST_STATE IS CONNECTION 3 OF VESSEL_B
CONNECTION 11 OF ST_STATE IS CONNECTION 4 OF VESSEL_B
CONNECTION 12 OF ST_STATE IS CONNECTION 5 OF VESSEL_B
CONNECTION 13 OF ST_STATE IS CONNECTION 1 OF REB
CONNECTION 14 OF ST_STATE IS CONNECTION 2 OF REB
CONNECTION 15 OF ST_STATE IS CONNECTION 3 OF REB
CONNECTION 16 OF ST_STATE IS CONNECTION 4 OF REB
****
UNIT ACC IS AN ACCUMULATOR
****
UNIT CNTR_1 IS A PI_CONTROLLER
****
UNIT CNTR_2 IS A PI_CONTROLLER
****
UNIT CNTR_3 IS A PI_CONTROLLER
****
UNIT COND IS A CONDENSER
****
UNIT REB IS A REBOILER
****
UNIT ST_STATE IS A STEADY_STATE
****
UNIT TRAY_A1 IS A TRAY
****
UNIT TRAY_A10 IS A TRAY
****
UNIT TRAY_A11 IS A TRAY
****
UNIT TRAY_A2 IS A TRAY
****
UNIT TRAY_A3 IS A TRAY
****
UNIT TRAY_A4 IS A TRAY
****
UNIT TRAY_A5 IS A TRAY
****
UNIT TRAY_A6 IS A TRAY
****
UNIT TRAY_A7 IS A TRAY
****
UNIT TRAY_A8 IS A TRAY
****
UNIT TRAY_A9 IS A TRAY
****
UNIT TRAY_B1 IS A TRAY
****
UNIT TRAY_B10 IS A TRAY
****
UNIT TRAY_B11 IS A TRAY
****
UNIT TRAY_B2 IS A TRAY
****
UNIT TRAY_B3 IS A TRAY
****
UNIT TRAY_B4 IS A TRAY
****
UNIT TRAY_B5 IS A TRAY
****
UNIT TRAY_B6 IS A TRAY
****
UNIT TRAY_B7 IS A TRAY
****
UNIT TRAY_B8 IS A TRAY
****
UNIT TRAY_B9 IS A TRAY
****
UNIT TRAY_C1 IS A TRAY
****
UNIT TRAY_C10 IS A TRAY
****
UNIT TRAY_C11 IS A TRAY
****
UNIT TRAY_C2 IS A TRAY
****
UNIT TRAY_C3 IS A TRAY
****
UNIT TRAY_C4 IS A TRAY
****
UNIT TRAY_C5 IS A TRAY
****
UNIT TRAY_C6 IS A TRAY
****
UNIT TRAY_C7 IS A TRAY
****
UNIT TRAY_C8 IS A TRAY
****
UNIT TRAY_C9 IS A TRAY
****
UNIT VESSEL_A IS A VESSEL
****
UNIT VESSEL_B IS A VESSEL
****
OPERATION
SET
WITHIN COND
MINUS=0.1 , TB=<64.7,78.3,97.2,117.7>
WITHIN CNTR_1
SET_POINT=71.5, BIAS=10.0, GAIN=-.25, reset = 250, MIN=0.0, MAX=20.0,
CNTR_FLAG=1, SET_FLOW=10.0
# CNTR_FLAG = 1 for automatic
WITHIN TRAY_A1 #K=<10.2,4.5,2.3,1.0>
LO_INIT=10.0, HI_INIT=0.01, K=<10.2,4.5,2.3,1.0>
TB=<64.7,78.3,97.2,117.7>
WITHIN TRAY_A2
LO_INIT=10.0, HI_INIT=0.01, K=<10.2,4.5,2.3,1.0>
TB=<64.7,78.3,97.2,117.7>
WITHIN TRAY_A3
LO_INIT=10.0, HI_INIT=0.01, K=<10.2,4.5,2.3,1.0>
TB=<64.7,78.3,97.2,117.7>
WITHIN TRAY_A4
LO_INIT=10.0, HI_INIT=0.01, K=<10.2,4.5,2.3,1.0>
TB=<64.7,78.3,97.2,117.7>
WITHIN TRAY_A5
LO_INIT=10.0, HI_INIT=0.01, K=<10.2,4.5,2.3,1.0>
TB=<64.7,78.3,97.2,117.7>
WITHIN TRAY_A6
LO_INIT=10.0, HI_INIT=0.01, K=<10.2,4.5,2.3,1.0>
TB=<64.7,78.3,97.2,117.7>
WITHIN TRAY_A7
LO_INIT=10.0, HI_INIT=0.01, K=<10.2,4.5,2.3,1.0>
TB=<64.7,78.3,97.2,117.7>
WITHIN TRAY_A8
LO_INIT=10.0, HI_INIT=0.01, K=<10.2,4.5,2.3,1.0>
TB=<64.7,78.3,97.2,117.7>
WITHIN TRAY_A9
LO_INIT=10.0, HI_INIT=0.01, K=<10.2,4.5,2.3,1.0>
TB=<64.7,78.3,97.2,117.7>
WITHIN TRAY_A10
LO_INIT=10.0, HI_INIT=0.01, K=<10.2,4.5,2.3,1.0>
TB=<64.7,78.3,97.2,117.7>
WITHIN TRAY_A11
LO_INIT=10.0, HI_INIT=0.01, K=<10.2,4.5,2.3,1.0>
TB=<64.7,78.3,97.2,117.7>
WITHIN VESSEL_A
MINUS=0.1
TB =<64.7,78.3,97.2,117.7>
WITHIN CNTR_2
SET_POINT=87.75, BIAS=10.0, GAIN=-.25, reset = 250, MIN=0.0, MAX=20.0,
CNTR_FLAG=1, SET_FLOW=10.0
WITHIN TRAY_B1
LO_INIT=10.0, HI_INIT=0.01, K=<10.2,4.5,2.3,1.0>
TB=<64.7,78.3,97.2,117.7>
WITHIN TRAY_B2
LO_INIT=10.0, HI_INIT=0.01, K=<10.2,4.5,2.3,1.0>
TB=<64.7,78.3,97.2,117.7>
WITHIN TRAY_B3
LO_INIT=10.0, HI_INIT=0.01, K=<10.2,4.5,2.3,1.0>
TB=<64.7,78.3,97.2,117.7>
WITHIN TRAY_B4
LO_INIT=10.0, HI_INIT=0.01, K=<10.2,4.5,2.3,1.0>
TB=<64.7,78.3,97.2,117.7>
WITHIN TRAY_B5
LO_INIT=10.0, HI_INIT=0.01, K=<10.2,4.5,2.3,1.0>
TB=<64.7,78.3,97.2,117.7>
WITHIN TRAY_B6
LO_INIT=10.0, HI_INIT=0.01, K=<10.2,4.5,2.3,1.0>
TB=<64.7,78.3,97.2,117.7>
WITHIN TRAY_B7
LO_INIT=10.0, HI_INIT=0.01, K=<10.2,4.5,2.3,1.0>
TB=<64.7,78.3,97.2,117.7>
WITHIN TRAY_B8
LO_INIT=10.0, HI_INIT=0.01, K=<10.2,4.5,2.3,1.0>
TB=<64.7,78.3,97.2,117.7>
WITHIN TRAY_B9
LO_INIT=10.0, HI_INIT=0.01, K=<10.2,4.5,2.3,1.0>
TB=<64.7,78.3,97.2,117.7>
WITHIN TRAY_B10
LO_INIT=10.0, HI_INIT=0.01, K=<10.2,4.5,2.3,1.0>
TB=<64.7,78.3,97.2,117.7>
WITHIN TRAY_B11
LO_INIT=10.0, HI_INIT=0.01, K=<10.2,4.5,2.3,1.0>
TB=<64.7,78.3,97.2,117.7>
WITHIN VESSEL_B
MINUS=0.1 , TB=<64.7,78.3,97.2,117.7>
WITHIN CNTR_3
SET_POINT=107.2, BIAS=10.0, GAIN=-.25, reset = 250, MIN=0.0, MAX=20.0,
CNTR_FLAG=1, SET_FLOW=10.0
WITHIN TRAY_C1
LO_INIT=10.0, HI_INIT=0.01, K=<10.2,4.5,2.3,1.0>
TB=<64.7,78.3,97.2,117.7>
WITHIN TRAY_C2
LO_INIT=10.0, HI_INIT=0.01, K=<10.2,4.5,2.3,1.0>
TB=<64.7,78.3,97.2,117.7>
WITHIN TRAY_C3
LO_INIT=10.0, HI_INIT=0.01, K=<10.2,4.5,2.3,1.0>
TB=<64.7,78.3,97.2,117.7>
WITHIN TRAY_C4
LO_INIT=10.0, HI_INIT=0.01, K=<10.2,4.5,2.3,1.0>
TB=<64.7,78.3,97.2,117.7>
WITHIN TRAY_C5
LO_INIT=10.0, HI_INIT=0.01, K=<10.2,4.5,2.3,1.0>
TB=<64.7,78.3,97.2,117.7>
WITHIN TRAY_C6
LO_INIT=10.0, HI_INIT=0.01, K=<10.2,4.5,2.3,1.0>
TB=<64.7,78.3,97.2,117.7>
WITHIN TRAY_C7
LO_INIT=10.0, HI_INIT=0.01, K=<10.2,4.5,2.3,1.0>
TB=<64.7,78.3,97.2,117.7>
WITHIN TRAY_C8
LO_INIT=10.0, HI_INIT=0.01, K=<10.2,4.5,2.3,1.0>
TB=<64.7,78.3,97.2,117.7>
WITHIN TRAY_C9
LO_INIT=10.0, HI_INIT=0.01, K=<10.2,4.5,2.3,1.0>
TB=<64.7,78.3,97.2,117.7>
WITHIN TRAY_C10
LO_INIT=10.0, HI_INIT=0.01, K=<10.2,4.5,2.3,1.0>
TB=<64.7,78.3,97.2,117.7>
WITHIN TRAY_C11
LO_INIT=10.0, HI_INIT=0.01, K=<10.2,4.5,2.3,1.0>
TB=<64.7,78.3,97.2,117.7>
WITHIN REB
K=<10.2,4.5,2.3,1.0>, MINUS=0.1, VO=10.0
TB=<64.7,78.3,97.2,117.7>
# base case XT=<0.25,0.25,0.25,0.25>,
# XT=<0.25,0.23,0.27,0.25>,
# XT=<0.3,0.1,0.4,0.2>
INITIAL
WITHIN COND
XT=<0.3,0.1,0.4,0.2>, HT=2.5
within cntr_1
I_error = 0.0
WITHIN TRAY_A1
XT=<0.3,0.1,0.4,0.2>, HT=1.0E-2
WITHIN TRAY_A2
XT=<0.3,0.1,0.4,0.2>, HT=1.0E-2
WITHIN TRAY_A3
XT=<0.3,0.1,0.4,0.2>, HT=1.0E-2
WITHIN TRAY_A4
XT=<0.3,0.1,0.4,0.2>, HT=1.0E-2
WITHIN TRAY_A5
XT=<0.3,0.1,0.4,0.2>, HT=1.0E-2
WITHIN TRAY_A6
XT=<0.3,0.1,0.4,0.2>, HT=1.0E-2
WITHIN TRAY_A7
XT=<0.3,0.1,0.4,0.2>, HT=1.0E-2
WITHIN TRAY_A8
XT=<0.3,0.1,0.4,0.2>, HT=1.0E-2
WITHIN TRAY_A9
XT=<0.3,0.1,0.4,0.2>, HT=1.0E-2
WITHIN TRAY_A10
XT=<0.3,0.1,0.4,0.2>, HT=1.0E-2
WITHIN TRAY_A11
XT=<0.3,0.1,0.4,0.2>, HT=1.0E-2
WITHIN VESSEL_A
XT=<0.3,0.1,0.4,0.2>, HT=2.5
within cntr_2
I_error = 0.0
WITHIN TRAY_B1
XT=<0.3,0.1,0.4,0.2>, HT=1.0E-2
WITHIN TRAY_B2
XT=<0.3,0.1,0.4,0.2>, HT=1.0E-2
WITHIN TRAY_B3
XT=<0.3,0.1,0.4,0.2>, HT=1.0E-2
WITHIN TRAY_B4
XT=<0.3,0.1,0.4,0.2>, HT=1.0E-2
WITHIN TRAY_B5
XT=<0.3,0.1,0.4,0.2>, HT=1.0E-2
WITHIN TRAY_B6
XT=<0.3,0.1,0.4,0.2>, HT=1.0E-2
WITHIN TRAY_B7
XT=<0.3,0.1,0.4,0.2>, HT=1.0E-2
WITHIN TRAY_B8
XT=<0.3,0.1,0.4,0.2>, HT=1.0E-2
WITHIN TRAY_B9
XT=<0.3,0.1,0.4,0.2>, HT=1.0E-2
WITHIN TRAY_B10
XT=<0.3,0.1,0.4,0.2>, HT=1.0E-2
WITHIN TRAY_B11
XT=<0.3,0.1,0.4,0.2>, HT=1.0E-2
WITHIN VESSEL_B
XT=<0.3,0.1,0.4,0.2>, HT=2.5
within cntr_3
I_error = 0.0
WITHIN TRAY_C1
XT=<0.3,0.1,0.4,0.2>, HT=1.0E-2
WITHIN TRAY_C2
XT=<0.3,0.1,0.4,0.2>, HT=1.0E-2
WITHIN TRAY_C3
XT=<0.3,0.1,0.4,0.2>, HT=1.0E-2
WITHIN TRAY_C4
XT=<0.3,0.1,0.4,0.2>, HT=1.0E-2
WITHIN TRAY_C5
XT=<0.3,0.1,0.4,0.2>, HT=1.0E-2
WITHIN TRAY_C6
XT=<0.3,0.1,0.4,0.2>, HT=1.0E-2
WITHIN TRAY_C7
XT=<0.3,0.1,0.4,0.2>, HT=1.0E-2
WITHIN TRAY_C8
XT=<0.3,0.1,0.4,0.2>, HT=1.0E-2
WITHIN TRAY_C9
XT=<0.3,0.1,0.4,0.2>, HT=1.0E-2
WITHIN TRAY_C10
XT=<0.3,0.1,0.4,0.2>, HT=1.0E-2
WITHIN TRAY_C11
XT=<0.3,0.1,0.4,0.2>, HT=1.0E-2
WITHIN REB
XT=<0.3,0.1,0.4,0.2>, HT = 2.5
#HT =10.0-33*1.0E-2 - 3*2.5
# account for tray holdup when
# start from empty column
****
CONDITIONS
IF ST_STATE.MAX_SS < 1.0E-6
Then Stop 1000 ST_STATE.MAX_SS
Code
1000 FORMAT (1H,'Steady state reached! Maximum deviation=',G14.5)
$Endcode # has to be in the first column!!
****
REPORT MULTI_VESSEL
FIELDS
LOWLIMIT = 1.0E-6
ZERO = 1.0E-8
DECIMALS = 1
&6 = CNTR_1.SET_POINT ;
&7 = CNTR_1.MEASURE ;
&8 = CNTR_1.GAIN ;
&13 = CNTR_2.SET_POINT ;
&14 = CNTR_2.MEASURE ;
&15 = CNTR_2.GAIN ;
&20 = CNTR_3.SET_POINT ;
&21 = CNTR_3.MEASURE ;
&22 = CNTR_3.GAIN ;
DECIMALS = 2
&1 = T ;
&2 = TRAY_A1.VO ;
&5 = COND.LO ;
&9 = TRAY_A11.LO ;
&12 = VESSEL_A.LO ;
&16 = TRAY_B11.LO ;
&19 = VESSEL_B.LO ;
&23 = TRAY_C11.LO ;
&25 = REB.VO ;
DECIMALS = 3
&3 = COND.HT ;
&4 = COND.XT(1) ;
&10 = VESSEL_A.HT ;
&11 = VESSEL_A.XT(2) ;
&17 = VESSEL_B.HT ;
&18 = VESSEL_B.XT(3) ;
&24 = REB.HT ;
&26 = REB.XT(4) ;
DECIMALS = 2
&27 = REB.K(1) ;
&28 = REB.K(2) ;
&29 = REB.K(3) ;
&30 = REB.K(4) ;
DISPLAY
********************************************************************
* MULTI VESSEL BATCH DISTILLATION TIME = %%%%%%%% hr *
********************************************************************
* *
* FLOW = %%%%% KMOL/HR /----------------\ *
* --------------| HT = %%%%% KMOL| CONDENSER *
* /|\ | XT = %%%%% | *
* | \----------------/ *
* | | FLOW = %%%%% KMOL/HR *
* ------------ \|/ *
* | |---------------- *
* | TRAYS_A | /|\ *
* | | | | X_S = %%%%% *
* | |-------| X_M = %%%%% *
* ------------ KP = %%%% *
* /|\ | *
* | | FLOW = %%%%% KMOL/HR *
* | \|/ *
* /-----------------\ *
* | HT = %%%%% KMOL | *
* | XT = %%%%% | VESSEL_A *
* \-----------------/ *
* /|\ | FLOW = %%%%% KMOL/HR *
* | |---------- *
* | \|/ /|\ *
* ------------ | | X_S = %%%%% *
* | | | X_M = %%%%% *
* | TRAYS_B |------- KP = %%%% *
* | | *
* | | *
* ------------ *
* /|\ | *
* | | FLOW = %%%%% KMOL/HR *
* | \|/ *
* /-----------------\ *
* | HT = %%%%% KMOL | *
* | XT = %%%%% | VESSEL_B *
* \-----------------/ *
* /|\ | FLOW = %%%%% KMOL/HR *
* | |---------- *
* | \|/ /|\ *
* ------------ | | X_S = %%%%% *
* | | | X_M = %%%%% *
* | TRAYS_C |------- KP = %%%% *
* | | *
* | | *
* ------------ *
* /|\ | *
* | | FLOW = %%%%% KMOL/HR *
* | \|/ *
* /-----------------\ REBOILER *
* | |_______\ *
* | HT = %%%%% KMOL | / VAPOUR = %%%%% KMOL/HR *
* | XT = %%%%% |/_______ *
* | |\ *
* \-----------------/ *
* *
* 4 COMPONENT MIXTURE - K = %%%%%, %%%%%, %%%%%, %%%%% *
* *
********************************************************************
****
REPORT SUMMARY
FIELDS
LOWLIMIT = 1.0E-6
ZERO = 1.0E-8
DECIMALS = 2
&1 Left = T ;
DECIMALS = 3
&2 Left = COND.HT ;
&3 Left = VESSEL_A.HT ;
&4 Left = VESSEL_B.HT ;
&5 Left = REB.HT ;
DECIMALS = 4
&6 Left = COND.XT(1) ;
&7 Left = VESSEL_A.XT(1) ;
&8 Left = VESSEL_B.XT(1) ;
&9 Left = REB.XT(1) ;
&10 Left = COND.XT(2) ;
&11 Left = VESSEL_A.XT(2) ;
&12 Left = VESSEL_B.XT(2) ;
&13 Left = REB.XT(2) ;
&14 Left = COND.XT(3) ;
&15 Left = VESSEL_A.XT(3) ;
&16 Left = VESSEL_B.XT(3) ;
&17 Left = REB.XT(3) ;
&18 Left = COND.XT(4) ;
&19 Left = VESSEL_A.XT(4) ;
&20 Left = VESSEL_B.XT(4) ;
&21 Left = REB.XT(4) ;
DISPLAY
********************************************************************
* SUMMARY MULTI VESSEL BATCH DISTILLATION TIME = %%%%%% hr *
********************************************************************
* *
* CONDENSER: VESSEL_A: VESSEL_B: REBOILER: *
* *
* HT(KMOL) %%%%% %%%%% %%%%% %%%%% *
* *
* XT(1) %%%%%%%% %%%%%%%% %%%%%%%% %%%%%%%% *
* XT(2) %%%%%%%% %%%%%%%% %%%%%%%% %%%%%%%% *
* XT(3) %%%%%%%% %%%%%%%% %%%%%%%% %%%%%%%% *
* XT(4) %%%%%%%% %%%%%%%% %%%%%%%% %%%%%%%% *
* *
********************************************************************
****