ChE / MET 433

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ChE / MET 433

18 Apr 12Cascade Control: Ch

09Ratio Control: Ch 10

Advanced control schemes

Tuning a Cascade System

• Both controllers in manual• Secondary controller set as P-only (could be PI, but this might slow

sys)• Tune secondary controller for set point tracking• Check secondary loop for satisfactory set point tracking

performance• Leave secondary controller in Auto• Tune primary controller for disturbance rejection (PI or PID)• Both controllers in Auto now• Verify acceptable performance

In-Class Exercise: Tuning Cascade Controllers

• Select Jacketed Reactor• Set T cooling inlet at 46 oC (normal operation temperature; sometimes it drops to 40 oC)• Set output of controller at 50%.• Desired Tout set point is 86 oC (this is steady state temperature)

• Tune the single loop PI control• Criteria: IMC aggressive tuning• Use doublet test with +/- 5 %CO• Test your tuning with disturbance from 46 oC to 40 oC

In-Class Exercise: Tuning Cascade Controllers• Select Cascade Jacketed Reactor• Set T cooling inlet at 46 oC (again)• Set output of controller (secondary) at 50%.• Desired Tout set point is 86 oC (as before)

• Note the secondary outlet temperature (69 oC) is the SP of the secondary controller

• Tune the secondary loop; use 5 %CO doublet open loop• Criteria: ITAE for set point tracking (P only)• Use doublet test with +/- 5 %CO• Test your tuning with 3 oC setpoint changes• Tune the primary loop for PI control; make 3 oC set point changes (2nd-dary controller)• Note: MV = sp signal; and PV = T out of reactor• Criteria: IAE for aggressive tuning (PI)• Implement and with both controllers in Auto… change disturbance from 46 to 40 oC.• How does response compare to single PI feedback loop?

Ratio Control• Special type of feed forward control

•Blending/Reaction/Flocculation

•A and B must be in certain ratio to each other

Ratio ControlPossible control system:

•What if one stream could not be controlled?

• i.e., suppose stream A was “wild”; or it came from an upstream process and couldn’t be controlled.

Ratio ControlPossible cascade control systems:

“wild” stream

Desired Ratio

Desired RatioThis unit multiplies A by the desired ratio; so output = A

“wild” stream

Ratio Control Uses:

• Constant ratio between feed flowrate and steam in reboiler of distillation column

• Constant reflux ratio

• Ratio of reactants entering reactor

• Ratio for blending two streams

• Flocculent addition dependent on feed stream

• Purge stream ratio

• Fuel/air ratio in burner

• Neutralization/pH

In-Class Exercise: Furnace Air/Fuel Ratio• Furnace Air/Fuel Ratio model• disturbance: liquid flowrate• “wild” stream: air flowrate• ratioed stream: fuel flowrate

• Minimum Air/Fuel Ratio 10/1• Fuel-rich undesired (enviro, econ, safety)• If air fails; fuel is shut down

Independent MV

Ratio set point

Dependent MV

Disturbance var.

TC output

Desired 2 – 5% excess O2

Check TC tuning to disturbance & SP changes.

ChE / MET 433

18 Apr 12Feed Forward Control: Ch

Advanced control schemes

Feed Forward ControlSuppose qi is primary disturbance

Heat Exchanger

TT)(tqi

? What is a drawback to this feedback control loop?? Is there a potentially better way?

Heat ExchangerTTFT

? What if Ti changes?

FF must be done with FB control!

Feed Forward and Feedback Control

Heat ExchangerTTFT

)(tTi)(tqi

steamTC

I)(tM FF )(tM

FFFF MtMtMtM )()()(

Block diagram:

sE sT++

FFCGFF

Feed Forward Control

No change; perfect compensation!

sE+ sR sT++

Response to MFF

Feed Forward Control

Examine FFC T.F.

sE+ sR sC++

)()( sQKFFCGsQGsC iTMiD D

For “perfect” FF control: 0sC

)()(0 sQKFFCGsQG iTMiD D

GKGFFCD

Feed Forward Control: FFC Identification

Set by traditional means:

GKGFFCD

Model fit to FOPDT equation: MD GG &

gpmTO%

gpmTOD%

D oMDo

KKKFFC

FF Gain

Lead/lag unit

Dead time compensator

{ FFC ss }steady state FF control

{ FFC dyn }dynamic FF control

Accounts for time differences in 2 legs

Often ignored; if set term to 1

oMo ttD

Eqn: 11-2.5 p 379

Feed Forward Control: FFC IdentificationHow to determine FOPDT models :

GKGFFCD

With Gc disconnected:• Step change COFB, say 5%• Fit C(s) response to FOPDT

MD GG &

gpmTO%

Still in open loop:• Step change Q, say 5 gpm• Fit C(s) response to FOPDT

KKKFFC

Ldm lead timeLgD lag time

Lead/Lag or Dynamic CompensatorLook at effect of these two to step change in input

Final Change from:• Magnitude of step change,• Initial response by the lead/lag, • Exponential decay from lag,

ld/ lg = ½

ld/ lg = 1

ld/ lg = 2

Output or response )(tc

Feed Forward ControlRule of Thumb: if lead-lag won’t help much; use FFCss

3.165.0 Lg

(p 389)

In text: pp 393-395, useful comments if implementing FFC

+ -1. Compensates for disturbances

before they affect the process1. Requires measurement or

estimation of the disturbance

2. Can improve the reliability of the feedback controller by reducing the deviation from set point

2. Does not compensate for unmeasured disturbances

3. Offers advantages for slow processes or processes with large deadtime.

3. Linear based correction; only as good as the models; performance decreases with nonlinear processes.

No improvement using FFC with set point changes.

In-Class PS Exercise: Feed Forward Control

What is the Gm, and what is the GD?Determine FCCTune PI controller to aggressive IMC

• Test PI Controller• Test PI + FFCss only• Test PI + FFC full

For disturbance: Tjacket in

50oC – 60oC – 50oC

In-Class PS Exercise: Feed Forward Control

PI only PI + FFCss only PI + full FFC

ChE / MET 433

ChE / MET 433

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