The Control Talk Blog provides guidance from a user's viewpoint on the design of automation systems, equipment, and piping for process control improvement. Details are offered on the selection and installation of PID controllers, control valves, variable speed drives, and measurements to maximize loop performance. The blogs are often more intensive and extensive and less vendor specific than a white paper. The goal is an advancement of the profession by sharing conceptual principle based knowledge.
Greg McMillan is a retired Senior Fellow from Solutia/Monsanto and an ISA Fellow. At present, McMillan 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. He received the ISA Kermit Fischer Environmental Award for pH control in 1991, received 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.
Here are key relatively straightforward principles and practices not commonly known that can make a world of difference in the performance of feedforward and ratio control systems. Also, guidance is offered for the setup and automatic identification of the parameters needed by the use of software designed to tune PID...
Why do many process control technologies fail to make prime time being relegated to special applications that are few and far between? Here I give what I see as the keys to a technology being successful and widely used in plant applications.
If the total loop deadtime becomes larger than the open loop time constant, you have a deadtime dominant loop. There is a lot of misunderstanding posed by this difficult challenge including a lot of prevalent myths.
Here we finish up the extensive presentation of how to get the most out of your PID. We start with a look at the contribution of each mode and show how to estimate performance metrics from tuning settings and how excessive integral action and insufficient proportional action create oscillations.
The major types of process responses and the different worlds of process applications are presented. Additionally, the oversight of not including and understanding the contribution of automation dynamics is addressed. The discussion of the response of the PID is started.
The key aspects of good vessel temperature and pH control are often not recognized. Here we provide some simple guidance and overview of the benefits of a particular strategy and implementation guidelines that should be commonly used.
Here we provide the key points for the final Part 3 of the recordings of my recent AIChE course sponsored by MYNAH Technologies. The focus here is on improving the performance of reactors, fermenters, crystallizers, evaporators, distillation columns, dryers and neutralizers.
Here we provide the key points for Part 2 of my recent AIChE St. Louis Section course sponsored by MYNAH Technologies. The focus here is on improving the performance of compressors, jackets, heat exchangers and batch operations and the key role of valve position control (VPC).
Many simple additions to PID control loops are presented here that can increase the plant production rate, yield, product quality, and on-stream time. The improvements typically can be done by the selection of PID options, pairing of variables, and the addition of PID controllers and simple standard function blocks.
Specifying the best valve size can reduce loop variability and enable tighter control. A side benefit can be easier PID tuning and a smaller valve. By understanding key principles, you can become a valuable resource for getting the best automation component that directly affects the process, the control valve.