Transcribed Text
Problem 1:
(a) Figure 1 shows a feedback control scheme for blending process that is subject to significant
disturbances. It is desired to augment this scheme with feedforward control. Of the four potential
locations for the feedforward measurement indicated in the diagram, A, B, C, or D, which would
be the best? (The A values noted in the diagram correspond to the average residence time in the
indicated hollow pipes). Justify your answer briefly.
Composition
Controller
CC
CA
Composition
Analyzer
D
C
B
A
o3 sec
05 sec
Figure 1: Blending process.
(b) Figure 2 shows a schematic diagram for a heat exchanger exit temperature control problem.
The exit temperature of the process stream is influenced by the steam flowrate into the hea
exchanger shell, and by the erratically varying inlet temperature of the process stream. The
steam flowrate itselfis also subject to erratic fluctuations induced by unsteady, unpredictable,
and unmeasured steam supply pressure.
Temperature measurements are provided by two temperature sensors and accompanying
transmitters indicated as TT1 and TT2 in the diagram; and steam flow measurements are
provided by a flowmeter and the accompanying flow transmitter, FT, also indicated in the
diagram.
A flow controller, FC, a temperature controller, TC, and a feedforward controller, FFC (which
can configured any way you wish), have been made available to you. You are requiredto place
these controllers such that the heat exchanger system is configured for:
1. Feedforward control only,
2. Feedback control with cascade control,
3. Feedforward control augmented with feedback,
4. Feedforward, feedback, and cascade control.
For each case, draw a process diagram similar to that given in Figure P2.2, showing clearly the
connections between each of the controllers in question and the sensor/transmitter from which
it gets its information
FFC
TC
FC
Steam
TT2
TT
FT
Process
Stream
Condensate
Figure 2: Heat exchanger.
Problem 2
The objective in the water heating tank process shown in Figure 3 is to maintain the outlet
temperature at some desired setpoint Td by adjustingq, the quantity of heat sent to the tank vi a steam
heating. The steam delivery pressureis P, and it experiences variations over which we have no control, but
which affect 9.
The following deviation variables are given:
Ti  Ti = d1; p  p' = d2; T  T* = y; Td  T2 = Ya, a  a = u
The relevant transfer functions for the components of the closedloop system are also given as
follows: 91(s), process; @d1(s), disturbance (inlet stream temperature), h(s), thermocouple; 8c (s),
feedback controller, go(s), control valve; 9dz (s), disturbance (steam pressure).
(a) Develop a block diagram for the closedloop system showing all the components, and obtain
the closedloop transfer function equation.
(b) For the specific situation in which the following transfer function are given:
0.5
= 1
2
= 0.5s +
0.15
9az(s)=1557 =
1
h(s)=00251
+
Under PI control with T1 = 0.2, find the range K€ values for which the system remains
stable.
(c) If a cascade control strategy is to be implemented, how should the second control loop be
configured (i.e., what will it manipulate, and what measurement will it accept)? Draw the
block diagram for the process under this strategy. If the new controller is specified as a
proportional controller with gain Ke2 = 5.0, with the primary controller as givenir part (b), find
the range of K€ values for which the cascade control system will be stable.
T1
P
Set point
T
11
TT
TC

T&
Figure 3: Water heating tank process.
Problem 3:
For the blending process (Continuing Problem), the transfer functions for this process are given
as:
F1(s) 2.5s+1'FF(s) 5s+1
The plant transfer function matrix now becomes:
e0.1s
e0.1s
5s+1
=
0.1e
O.1e
2.5s+1
2.5s+1_
1. Perform an interaction analysis using RGA
2. Choose the optimal pair of control and manipulated variables to minimize interactions and
compare with the base case discussed in Chapter 15.
3. Design and implement a multiloop PI controller, with parameters based on ZN tuning for
both level and composition loops (take into account that the level controller is the same as
designed before since the corresponding transfer functions have not changed).
4. Design and implement a decoupling controller for the process and compare the
performance with conventional multiloop control.
Problem 4
The "lowboiler column" in a distillation train used to separate the products of an industrial chemical
reactor has the following experimentally determined approximate transfer function model
y(s) = g(s)u(s) + ga(s)d(s)
Where.
0.012
0.011
0.00175e0.1:
0.004s + 1
0.055s + 1
0.00525s + 1
0.013
0.075

0.00012e0.25:
g(s) =
0.00325s + 1
0.015s + 1
0.0141s + 1
0.0043
0.04
0.000086
S
S
S
0.0041
0.185
0.0041s + 1
0.37s + 1
ga(s) =
0.001
0.16
0.000225s + 1
0.4s + 1
The variables are defined in terms of deviation variables
y1= T36 temperature of tray 36 (C)
y2= Bottom Temperature (°C)
y3=Reflux receiver level (ft)
mi= Reflux Flow Rate (lb/hr)
mz= Reboiler Heat Duty (NHDU)
m3= Condenser Cooling Water Flowrate (lb/hr))
d1 = Feed Flow Rate
d2= Feed Temperature
a) Assuming that it has been predetermined that the bottom temperature is to be controlled with the reboiler
heat duty, use the RGA to determine how the remaining variables should be paired.
b) Using the yim3; y2m2; y3m1 pairing and using the following controller parameters
Loop 1: (T36 loop) Kc=80; 1/t1=3.5
Loop 2: (Bottom Temperature loop) K.=2.0; 1/t1=6.0
Loop 3: (Reflux level loop) Kc=500; 1/t1=2.0
Obtain the simulation of the overall column response to a 600 lb/hr step increase in the feed flowrate
Now, using the yimi; y2m2; y3m3 along with the following controller parameters
Loop 1: (T36 loop) Kc=500; 1/tr=1.0
Loop 2: (Bottom Temperature loop) Kc=4.5; l/tr=2.0
Loop 3: (Reflux level loop) Kc=12000; 1/t1=0.8
Obtain the simulation of the overall column response to a 600 lb/hr step increase in the feed
flowrate.
Compare the results under both the old and new configurations
c) Givennow that for economic and environmental reasons the temperature T36 is the most critical of
all
the
low
boiler columns variables, and that very tight control is therefore required for this
variable, which of the two configurations investigated in part b) is preferable. Discuss your answer
in the light of the RGA results obtained in part a)
Given that Tray 36 is close to the top of the column and that the reflux receiver is a 3ft diameter
cylindrical drum into which empties all the material from the (essentially total) condenser. From a
consideration of the physics of the problem, which would you expect to be
more
effective
manipulated variable to use in controlling this temperature: the reflux flow rate or the condenser
cooling temperature, Support your answer adequately. Offer an explanation for the results given
by
the RGA.
d)
Repeat part b) for a step input disturbance of 5°C in the feed temperature. Once again, comment on
which configuration provides tighter control of the critical T36 variable.
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