The following technical discussion is part of an occasional series showcasing the ISA Mentor Program, authored by Greg McMillan, industry consultant, author of numerous process control books, 2010 ISA Life Achievement Award recipient and retired Senior Fellow from Solutia Inc. (now Eastman Chemical). Greg will be posting questions and responses from the ISA Mentor Program, with contributions from program participants.
In the ISA Mentor Program, I am providing guidance for extremely talented individuals from countries such as Argentina, Brazil, Malaysia, Mexico, Saudi Arabia, and the U.S. This question comes from Brian Hrankowsky.
The PID controller is an essential component of nearly all control loops in the process industry. We take for granted that a change in the PID controller mode or setpoint will not disturb the process. More needs to be known about bumpless transfer and how a new operating point can be achieved quickly and smoothly after the PID is switched to the automatic mode. The following question by Brian Hrankowsky, a resource in the ISA Mentor Program, helps us seek a good definition of PID bumpless transfer, how it is achieved in the PID and how options such as setpoint tracking, PID structure, setpoint dynamics and external reset feedback come into play.
In our plants, I have seen two definitions for PID bumpless transfer:
Note that the only difference in the two definitions is the removal of "the SP matches the PV and".
In reading on line, it seems that both ways of using the term are in use. The majority seems to be definition No. 1. However, I can imagine that configuring some systems to work like definition No. 2 suggests would be beneficial. In fact, I think the way some skid mount OEM equipment works is really like definition No. 2: The controller setpoint is fixed by the selected "format" or "recipe" and starting/stopping the machine just changes the controller mode. But generally in our DCS implementations, we configure the loop to behave as in definition No. 1.
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Good question. The transfer from manual or remote output to auto should be bumpless regardless of the current setpoint. This gives the most options. This is commonly achieved by biasing the contribution from the integral mode to counter act any contribution from the proportional mode. The ISA Dictionary 4th Edition says as much and even has a little equation that shows the bias (b) is set equal to the manual output (mo) minus the product of the gain and error (Kc e) to provide bumpless transfer. The simple equation does not show the control action sign or the effect of a beta setpoint weight factor. In real life it gets more complicated but the goal should be the same.
You may be able to simply check a box to enable a SP track PV option in a modern DCS. In chemical processes where we have seen benefit from the proportional step in the PID output on a setpoint change to get to the new setpoint sooner, we use a structure of PI on error and D on PV, enable the SP track PV option, and then have the batch or startup sequence automatically change the primary PID setpoint at the right time. A setpoint lead-lag or two degrees of freedom structure can minimize setpoint overshoot by optimizing the contribution from the proportional and derivative modes to the PID output.
This of course only works well if other systems are not upset by a sudden large change in the PID output. Tight pressure control of the source of the manipulated flow can reduce the upset to other users of the source (e.g., utility). However, operators may get concerned even if there is no detrimental effect. To prevent this, you can use setpoint rate limits on the analog output block or secondary PID setpoint and enable external reset feedback (dynamic reset limit) in the primary PID to slow down the change the in manipulated flow (now famously known as directional move suppression) and the consequential upset to others (including operators) without having to retune the primary PID.
In other words, "Bumpless Transfer” is a basic MUST for all loops regardless of setpoint value, and the “SP Track PV” option is chosen based on process and operator requirements. To achieve a new setpoint faster after a PID mode makes the transition from manual or remote output to auto, this track option is used and the setpoint is then changed to the desired operating point after the PID goes to auto to give a quick change in the contribution from the proportional and derivative modes as determined by the PID structure or setpoint dynamics. External reset feedback and setpoint rate limits of the manipulated flow can slow down the actual change in the PID output to reduce the upset to other loops and operators.
Any change that is to be made to a control system must be thoroughly functionally tested by realistic simulations of the process’s dynamic response. The ability of the control system improvement to deal with abnormal besides normal operating conditions must be verified. The commissioning and performance of improvements should be closely monitored to ensure they meet plant requirements.
See the ISA book 101 Tips for a Successful Automation Career that grew out of this Mentor Program to gain concise and practical advice. See the InTech magazine feature article Enabling new automation engineers for candid comments from some of the original program participants. See the Control Talk column How to effectively get engineering knowledge with the ISA Mentor Program protégée Keneisha Williams on the challenges faced by young engineers today, and the column How to succeed at career and project migration with protégé Bill Thomas on how to make the most out of yourself and your project. Providing discussion and answers besides Greg McMillan and co-founder of the program Hunter Vegas (project engineering manager at Wunderlich-Malec) are resources Mark Darby (principal consultant at CMiD Solutions), Brian Hrankowsky (consultant engineer at a major pharmaceutical company), Michel Ruel (executive director, engineering practice at BBA Inc.), Leah Ruder (director of global project engineering at the Midwest Engineering Center of Emerson Automation Solutions), Nick Sands (ISA Fellow and Manufacturing Technology Fellow at DuPont), Bart Propst (process control leader for the Ascend Performance Materials Chocolate Bayou plant), Angela Valdes (automation manager of the Toronto office for SNC-Lavalin), and Daniel Warren (senior instrumentation/electrical specialist at D.M.W. Instrumentation Consulting Services, Ltd.).
About the Author
Gregory K. McMillan, CAP, is a retired Senior Fellow from Solutia/Monsanto where he worked in engineering technology on process control improvement. Greg was also an affiliate professor for Washington University in Saint Louis. Greg is an ISA Fellow and received the ISA Kermit Fischer Environmental Award for pH control in 1991, the Control magazine Engineer of the Year award for the process industry in 1994, was inducted into the Control magazine Process Automation Hall of Fame in 2001, was honored by InTech magazine in 2003 as one of the most influential innovators in automation, and received the ISA Life Achievement Award in 2010. Greg is the author of numerous books on process control, including Advances in Reactor Measurement and Control and Essentials of Modern Measurements and Final Elements in the Process Industry. Greg has been the monthly "Control Talk" columnist for Control magazine since 2002. Presently, Greg is a part time modeling and control consultant in Technology for Process Simulation for Emerson Automation Solutions specializing in the use of the virtual plant for exploring new opportunities. He spends most of his time writing, teaching and leading the ISA Mentor Program he founded in 2011.
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