Practical plantwide process control: PID tuning Sigurd Skogestad, NTNU

Part 4: PID tuning Part 2 (4h). PID controller tuning: It pays off to be systematic!   1. Obtaining first-order plus delay models Open-loop step response From detailed model (half rule) From closed-loop setpoint response 2 . Derivation SIMC PID tuning rules Controller gain, Integral time, derivative time 3. Special topics Integrating processes (level control) Other special processes and examples When do we need derivative action? Near-optimality of SIMC PID tuning rules Non PID-control: Is there an advantage in using Smith Predictor? (No) Examples

Operation: Decision and control layers RTO Min J (economics); MV=y1s cs = y1s CV=y1; MV=y2s MPC y2s PID CV=y2; MV=u u (valves)

PID controller Time domain (“ideal” PID) Laplace domain (“ideal”/”parallel” form) For our purposes. Simpler with cascade form Usually τD=0. Then the two forms are identical. Only two parameters left (Kc and τI) How difficult can it be to tune??? Surprisingly difficult without systematic approach!

Disadvantages Ziegler-Nichols: Aggressive settings No tuning parameter Trans. ASME, 64, 759-768 (Nov. 1942). Comment: Similar to SIMC for integrating process with ¿c=0: Kc = 1/k’ 1/µ ¿I = 4 µ Disadvantages Ziegler-Nichols: Aggressive settings No tuning parameter Poor for processes with large time delay (µ)

Disadvantage IMC-PID (=Lambda tuning): Many rules Poor disturbance response for «slow» processes (with large ¿1/µ)

Motivation for developing SIMC PID tuning rules The tuning rules should be well motivated, and preferably be model-based and analytically derived. They should be simple and easy to memorize. They should work well on a wide range of processes.

SIMC PI tuning rule Approximate process as first-order with delay (e.g., use “half rule”) k = process gain ¿1 = process time constant µ = process delay Derive SIMC tuning rule*: Open-loop step response c ¸ - : Desired closed-loop response time (tuning parameter) Integral time rule combines well-known rules: IMC (Lamda-tuning): Same as SIMC for small ¿1 (¿I = ¿1) Ziegler-Nichols: Similar to SIMC for large ¿1 (if we choose ¿c= 0; aggressive!) Reference: S. Skogestad, “Simple analytic rules for model reduction and PID controller design”, J.Proc.Control, Vol. 13, 291-309, 2003 (*) “Probably the best simple PID tuning rules in the world”

MODEL Need a model for tuning Model: Dynamic effect of change in input u (MV) on output y (CV) First-order + delay model for PI-control Second-order model for PID-control Recommend: Use second-order model only if ¿2>µ

1. Step response experiment MODEL, Approach 1A 1. Step response experiment Make step change in one u (MV) at a time Record the output (s) y (CV)

First-order plus delay process MODEL, Approach 1A First-order plus delay process Step response experiment k’=k/1 STEP IN INPUT u (MV) RESULTING OUTPUT y (CV) : Delay - Time where output does not change 1: Time constant - Additional time to reach 63% of final change k : steady-state gain =  y(1)/ u k’ : slope after response “takes off” = k/1

MODEL, Approach 1A Δy(∞) RESULTING OUTPUT y STEP IN INPUT u Δu : Delay - Time where output does not change 1: Time constant - Additional time to reach 63% of final change k =  y(∞)/ u : Steady-state gain

Step response integrating process MODEL, Approach 1A Step response integrating process Δy Δt

MODEL, Approach 1B Shams’ method: Closed-loop setpoint response with P-controller with about 20-40% overshoot Kc0=1.5 Δys=1 Δy∞ OBTAIN DATA IN RED (first overshoot and undershoot), and then: tp=4.4, dyp=0.79; dyu=0.54, Kc0=1.5, dys=1 dyinf = 0.45*(dyp + dyu) Mo =(dyp -dyinf)/dyinf % Mo=overshoot (about 0.3) b=dyinf/dys A = 1.152*Mo^2 - 1.607*Mo + 1.0 r = 2*A*abs(b/(1-b)) %2. OBTAIN FIRST-ORDER MODEL: k = (1/Kc0) * abs(b/(1-b)) theta = tp*[0.309 + 0.209*exp(-0.61*r)] tau = theta*r 3. CAN THEN USE SIMC PI-rule Δyp=0.79 Δyu=0.54 tp=4.4 Example 2: Get k=0.99, theta =1.68, tau=3.03 Ref: Shamssuzzoha and Skogestad (JPC, 2010) + modification by C. Grimholt (Project, NTNU, 2010; see also PID-book 2012)

2. Model reduction of more complicated model MODEL, Approach 2 2. Model reduction of more complicated model Start with complicated stable model on the form Want to get a simplified model on the form Most important parameter is the “effective” delay 

MODEL, Approach 2

MODEL, Approach 2 Example 1 Half rule

MODEL, Approach 2 original 1st-order+delay

MODEL, Approach 2 2 half rule

MODEL, Approach 2 original 1st-order+delay 2nd-order+delay

Original 7th order, g0 1st-order, half rule, g1 2nd-order, half rule, g2 1st-order, closed loop, gcl

Approximation of zeros MODEL, Approach 2 Approximation of zeros To make these rules more general (and not only applicable to the choice c=): Replace  (time delay) by c (desired closed-loop response time). (6 places) c c c c c c Alternative and improved method forf approximating zeros: Simple Analytic PID Controller Tuning Rules Revisited J Lee, W Cho, TF Edgar - Industrial & Engineering Chemistry Research 2014, 53 (13), pp 5038–5047

Derivation of SIMC-PID tuning rules SIMC-tunings Derivation of SIMC-PID tuning rules PI-controller (based on first-order model) For second-order model add D-action. For our purposes, simplest with the “series” (cascade) PID-form:

Basis: Direct synthesis (IMC) SIMC-tunings Basis: Direct synthesis (IMC) Closed-loop response to setpoint change Idea: Specify desired response: and from this get the controller. ……. Algebra:

SIMC-tunings NOTE: Setting the steady-state gain = 1 in T will result in integral action in the controller!

IMC Tuning = Direct Synthesis SIMC-tunings IMC Tuning = Direct Synthesis Algebra:

SIMC-tunings Integral time Found: Integral time = dominant time constant (I = 1) (IMC-rule) Works well for setpoint changes Needs to be modified (reduced) for integrating disturbances Example. “Almost-integrating process” with disturbance at input: G(s) = e-s/(30s+1) Original integral time I = 30 gives poor disturbance response Try reducing it! g c d y u

Integral Time SIMC-tunings I = 1 Reduce I to this value: I = 4 (c+) = 8  Setpoint change at t=0 Input disturbance at t=20

SIMC-tunings Integral time Want to reduce the integral time for “integrating” processes, but to avoid “slow oscillations” we must require: Derivation: Setpoint response: Improve (get rid of overshoot) by “pre-filtering”, y’s = f(s) ys. Details: See www.nt.ntnu.no/users/skoge/publications/2003/tuningPID Remark 13 II

Conclusion: SIMC-PID Tuning Rules SIMC-tunings Conclusion: SIMC-PID Tuning Rules One tuning parameter: c

Some insights from tuning rules SIMC-tunings Some insights from tuning rules The effective delay θ (which limits the achievable closed-loop time constant τc) is independent of the dominant process time constant τ1! It depends on τ2/2 (PI) or τ3/2 (PID) Use (close to) P-control for integrating process Beware of large I-action (small τI) for level control Use (close to) I-control for fast process (with small time constant τ1) Parameter variations: For robustness tune at operating point with maximum value of k’ θ = (k/τ1)θ

Cascade PID -> Ideal PID

SIMC-tunings

Selection of tuning parameter c SIMC-tunings Selection of tuning parameter c Two main cases TIGHT CONTROL: Want “fastest possible control” subject to having good robustness Want tight control of active constraints (“squeeze and shift”) SMOOTH CONTROL: Want “slowest possible control” subject to acceptable disturbance rejection Want smooth control if fast setpoint tracking is not required, for example, levels and unconstrained (“self-optimizing”) variables THERE ARE ALSO OTHER ISSUES: Input saturation etc. TIGHT CONTROL: SMOOTH CONTROL:

TIGHT CONTROL

Typical closed-loop SIMC responses with the choice c= TIGHT CONTROL Typical closed-loop SIMC responses with the choice c=

Example. Integrating process with delay=1. G(s) = e-s/s. TIGHT CONTROL Example. Integrating process with delay=1. G(s) = e-s/s. Model: k’=1, =1, 1=1 SIMC-tunings with c with ==1: IMC has I=1 Ziegler-Nichols is usually a bit aggressive Setpoint change at t=0c Input disturbance at t=20

TIGHT CONTROL Approximate as first-order model with k=1, 1 = 1+0.1=1.1, =0.1+0.04+0.008 = 0.148 Get SIMC PI-tunings (c=): Kc = 1 ¢ 1.1/(2¢ 0.148) = 3.71, I=min(1.1,8¢ 0.148) = 1.1 2. Approximate as second-order model with k=1, 1 = 1, 2=0.2+0.02=0.22, =0.02+0.008 = 0.028 Get SIMC PID-tunings (c=): Kc = 1 ¢ 1/(2¢ 0.028) = 17.9, I=min(1,8¢ 0.028) = 0.224, D=0.22

Tuning for smooth control Tuning parameter: c = desired closed-loop response time Selecting c= (“tight control”) is reasonable for cases with a relatively large effective delay  Other cases: Select c >  for slower control smoother input usage less disturbing effect on rest of the plant less sensitivity to measurement noise better robustness Question: Given that we require some disturbance rejection. What is the largest possible value for c ? Or equivalently: The smallest possible value for Kc? Will derive Kc,min. From this we can get c,max using SIMC tuning rule S. Skogestad, ``Tuning for smooth PID control with acceptable disturbance rejection'', Ind.Eng.Chem.Res, 45 (23), 7817-7822 (2006).

Closed-loop disturbance rejection SMOOTH CONTROL Closed-loop disturbance rejection d0 -d0 ymax -ymax

u Kc SMOOTH CONTROL Minimum controller gain for PI-and PID-control: min |c(j)| = Kc

SMOOTH CONTROL Rule: Min. controller gain for acceptable disturbance rejection: Kc ¸ |ud|/|ymax| often ~1 (in span-scaled variables) |ymax| = allowed deviation for output (CV) |ud| = required change in input (MV) for disturbance rejection (steady state) = observed change (movement) in input from historical data

SMOOTH CONTROL Rule: Kc ¸ |ud|/|ymax| Exception to rule: Can have lower Kc if disturbances are handled by the integral action. Disturbances must occur at a frequency lower than 1/I Applies to: Process with short time constant (1 is small) and no delay ( ¼ 0). For example, flow control Then I = 1 is small so integral action is “large”

Summary: Tuning of easy loops SMOOTH CONTROL Summary: Tuning of easy loops Easy loops: Small effective delay ( ¼ 0), so closed-loop response time c (>> ) is selected for “smooth control” ASSUME VARIABLES HAVE BEEN SCALED WITH RESPECT TO THEIR SPAN SO THAT |u0/ymax| = 1 (approx.). Flow control: Kc=0.2, I = 1 = time constant valve (typically, 2 to 10s; close to pure integrating!) Level control: Kc=2 (and no integral action) Other easy loops (e.g. pressure): Kc = 2, I = min(4c, 1) Note: Often want a tight pressure control loop (so may have Kc=10 or larger)

Conclusion PID tuning 3. Derivative time: Only for dominant second-order processes

PID: More (Special topics) Integrating processes (level control) Other special processes and examples When do we need derivative action? Near-optimality of SIMC PID tuning rules Non PID-control: Is there an advantage in using Smith Predictor? (No) April 4-8, 2004 KFUPM-Distillation Control Course

1. Application of smooth control LEVEL CONTROL 1. Application of smooth control Averaging level control V q LC If you insist on integral action then this value avoids cycling Reason for having tank is to smoothen disturbances in concentration and flow. Tight level control is not desired: gives no “smoothening” of flow disturbances. Proof: 1. Let |u0| = |q0| – expected flow change [m3/s] (input disturbance) |ymax| = |Vmax| - largest allowed variation in level [m3] Minimum controller gain for acceptable disturbance rejection: Kc ¸ Kc,min = |u0|/|ymax| = |q0| / |Vmax| 2. From the material balance (dV/dt = q – qout), the model is g(s)=k’/s with k’=1. Select Kc=Kc,min. SIMC-Integral time for integrating process: I = 4 / (k’ Kc) = 4 |Vmax| / | q0| = 4 ¢ residence time provided tank is nominally half full and q0 is equal to the nominal flow.

More on level control Level control often causes problems Typical story: Level loop starts oscillating Operator detunes by decreasing controller gain Level loop oscillates even more ...... ??? Explanation: Level is by itself unstable and requires control.

Level control: Can have both fast and slow oscillations Slow oscillations (Kc too low): P > 3¿I Fast oscillations (Kc too high): P < 3¿I Here: Consider the less common slow oscillations

How avoid oscillating levels? LEVEL CONTROL How avoid oscillating levels? 0.1 ¼ 1/2

Case study oscillating level LEVEL CONTROL Case study oscillating level We were called upon to solve a problem with oscillations in a distillation column Closer analysis: Problem was oscillating reboiler level in upstream column Use of Sigurd’s rule solved the problem

LEVEL CONTROL

SIMC-tunings 2. Some special cases One tuning parameter: c

Another special case: IPZ process SIMC-tunings Another special case: IPZ process IPZ-process may represent response from steam flow to pressure Rule T2: SIMC-tunings These tunings turn out to be almost identical to the tunings given on page 104-106 in the Ph.D. thesis by O. Slatteke, Lund Univ., 2006 and K. Forsman, "Reglerteknik for processindustrien", Studentlitteratur, 2005.

3. Derivative action? Note: Derivative action is commonly used for temperature control loops. Select D equal to 2 = time constant of temperature sensor

Pure time delay process: “Minor” improvement by adding D-action* Optimal PI* = I-control θ=1 Time delay process: Setpoint and disturbance responses same + input response same * D-action (ID-control) is equivalent to PI-control (with ¿I >0)

Pure time delay process

) Two alternative “Improved SIMC”-rules Alt. 1. Improved PI-rule (iSIMC-PI): Add θ/3 to 1 Alt. 2. Improved PID-rule (iSIMC-PID): Add θ/3 to 2 iSIMC-PI and iSIMC-PID are identical for pure delay process (¿1=0) iSIMC-PID is better for integrating process

Integrating process

4. Optimality of SIMC rules How good are the SIMC-rules compared to optimal PI/PID? High controller gain (“tight control”) Low controller gain (“smooth control”) Multiobjective. Tradeoff between Output performance Robustness Input usage Noise sensitivity Our choice: Quantification Output performance: Rise time, overshoot, settling time IAE or ISE for setpoint/disturbance Robustness: Ms, Mt, GM, PM, Delay margin, … Input usage: ||KSGd||, TV(u) for step response Noise sensitivity: ||KS||, etc. J = avg. IAE for setpoint/disturbance Ms = peak sensitivity

Performance (J):

Robustness (Ms):

JIAE vs. Ms for optimal PI/PID (-) and SIMC (¢¢) for 4 processes CONCLUSION: SIMC almost «Pareto-optimal» Note: “PID” weightings used for JIAE

5. Better with IMC, Smith Predictor or MPC? Suprisingly, the answer is: NO, worse

The Smith Predictor IMC controller Where K is a “normal” controller Special case of Smith Predictor where K is a PI controller with the parameters ¿1 > 0 ¿1 = 0 Kc = ¿1/(k ¿c) ¿I = ¿1 Kc =0 Ki = Kc/¿I = 1/¿c (I-controller)

Comparison of J vs. Ms for optimal and SIMC for 4 processes CONCLUSION: i-SIMC is generally better than IMC & SP!

Step response, SP and PI y time time time Smith Predictor: Sensitive to both positive and negative delay error SP = Smith Predictor

In addition: SP & IMC usually have much lower (worse) delay margin than PI/PID

Reason: SP & IMC can have multiple GM, PM, DM

CONCLUSION Well-tuned PI or PID is better than Smith Predictor or IMC!! Especially for integrating processes