More Fun with PID Controllers

Exploring Just How Flexible and Powerful the PID Controller Can Be

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Greg McMillan and Stan Weiner bring their wits and more than 66 years of process control experience to bear on your questions, comments, and problems. Write to them at controltalk@putman.net.

McMillan & WeinerBy Greg McMillan and Stan Weiner

Stan: We continue exploring just how flexible and powerful the PID controller can be. The concept of setpoint (SP), process variable (PV), controller output (CO) and mode have been used since the inception of the PID in the 1930s. The modern-day DCS has all the modes, such as manual (MAN), automatic (AUTO), cascade (CAS), remote cascade (RCAS) and remote output (ROUT), developed for the electronic analog controllers in the 1970s. The RCAS mode is used for supervisory or model-predictive control, and the ROUT mode is used to position outputs for batch operation, transitions, start-up, shutdown and abnormal conditions.

Greg: You want the operator to be able to set a target (setpoint), monitor the control error, put a control system in manual and position the valve to deal with unforeseen situations, and to check out valve operation. The PID provides this familiar and effective interface, and has the flexibility to do just about anything within its framework. In the future, the operator will also be able to see trajectories of the PID SP, PV and CO intelligently scaled and time spanned to show where the process has been and where the process is going. The use of smart PID trajectories can overcome the problems introduced by digital displays, and provide a better perception of loop dynamics and tuning as discussed in "Are We Misleading Our Operators" (http://tinyurl.com/6xd3buf). For example, the delay between a change in the SP or CO and a change in the PV can make the operator aware of dead time, which is the most important and difficult dynamic parameter to understand.

Stan: In this third of a four-part series, we continue our interview with Mark Congiundi of Sasol, who has done an incredible job of using the PID, so the operator is not intimidated or out of touch with advanced applications—a common problem with supervisory, model-predictive, batch and field control systems.

Greg: When we use a variable-frequency drive (VFD) we have the opportunity to use tachometer feedback for greater rangeability and precision of speed adjustment. The speed control is very fast, and is best done in the drive rather than the DCS to avoid introducing a delay and lag due to signal transmission and DCS execution. For fast process loops manipulating a speed loop, slowing down the speed loop by putting it in the DCS can cause a violation of the cascade rule, which stipulates the secondary loop (speed loop) should be five times faster than the primary loop (process loop). Also, the vendor has the knowledge of internal drive operation to make the speed loop do its job. Keeping the speed loop in the VFD avoids the transfer of the responsibility for speed loop tuning and performance from the manufacturer to the user. The downside is the loss of operator access and visibility. How do you address the lack of an operator interface for a speed loop in a VFD?

Mark: I use a pass-through speed controller. The operator sees a speed PID loop that he can monitor and select modes. If the speed loop is put in the cascade mode, the PID uses a setpoint that is the output of the process PID. The speed-indicating controller (SIC) PV is the actual speed. A zero-gain PID with an external feedback signal that is the speed setpoint is used, so there is no response to the speed PV; the SIC functions to provide the flexibility of a hand-indicating controller (HIC), even though it looks like a conventional SIC. The bumpless transition to cascade, process PID features and equipment coordination are provided as if the SIC was doing speed control in the DCS. For example, the speed setpoint is automatically set to a minimum when the motor is off, so the motor can start at minimum speed.

Stan: The tuning settings for best setpoint response and disturbance rejection are quite different. The settings for minimum integrated error from unmeasured disturbances will typically cause overshoot and excessive oscillation for a setpoint change. This problem is prevalent in batch loops and automated start-up and transitions of continuous loops. How do you get the best setpoint and load response?

Mark: I use proportional action on PV rather than on error, so the controller gain does not provide a kick from the setpoint change. I then add to the PID output a feed-forward signal that is simply the change in setpoint multiplied by a gain factor. I can control the size of the step change in controller output from the step change in setpoint without affecting the disturbance response.

Greg: Some control systems offer a PID structure with factors built in to allow tuning for setpoint response without affecting the load response. For example, in a "two degrees of freedom" structure, the user can specify beta and gamma factors for the response to setpoint changes of the proportional and integral mode. The beta and gamma factors do not affect the reaction to disturbances. For loops with low controller gains and little-to-no rate action due to excessive dead time or noise, setpoint feed-forward can still be useful for a standard PID, since these factors have a 1.0 high limit. For these cases, where you effectively have proportional action on setpoint changes limited by a gamma setting of 1.0 and a low controller gain setting, the setpoint feed-forward factor would be the inverse of the process gain minus the controller gain. For example, if the process gain was 1.25 and the controller gain was 0.2, the setpoint feed-forward factor would be 0.6, so that the sum of feed-forward and proportional action on setpoint immediately puts the output to its final resting value, corresponding to PV = SP (feedforward gain = 1/1.25 - 0.2 = 0.6). The enhanced PID developed for wireless operation allows the controller gain to be set equal to the inverse of the process gain for loops dominated by an analyzer cycle time or wireless measurement update time as discussed in "Wireless PID Benefits" (http://tinyurl.com/644pt82). This immediately puts the PID output at the final resting value for self-regulating loops.

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