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 USA. This question comes from Muhammad Al-Khalifah in Saudi Arabia. .
What is the proper back pressure control valve type used for high turndown ratio at the same given pressure drop (minimum and maximum flow conditions)? What will be the effect on the valve seat if the case valve is operating most of the time at minimum flow condition?
I have never seen a back pressure control valve that had the same upstream and downstream conditions regardless of flow…but I suppose it could occur. The short answer to your question would be:
If the valve is routinely operating nearly closed at high pressure drops then you’ll likely encounter cavitation/flashing and the seat and valve body will erode. If continuous operation will be required under these conditions, you’ll want to consult your valve manufacturer and make sure they understand the situation. They may go with a specialized valve body style or particularly hardened trim to provide the long life you need or you’ll be replacing control valves often.
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Equations and figures noted below are from the ISA book Essentials of Modern Measurements and Final Elements in the Process Industry.
For back pressure and feed valves, I would use an equal percentage characteristic with a ratio of valve pressure drop to system pressure drop greater than 0.25 so the installed characteristic is not too flat near the closed and near the open position (see figures 7-47a-c and equations 7-19a-d on pages 407-411 for the effect of this ratio on rangeability).
For the recycle valve discussed in the a previous a previous blog post, a linear characteristic might be better since the pressure drop across the valve is fixed and the ratio of valve drop to system drop approaches 1.0 yielding an installed characteristic that is close to the inherent characteristic and thus a nearly constant valve gain (constant slope of installed valve characteristic). For the back pressure valve to minimize stick-slip and backlash and thus oscillations near the seat,
I would use a rugged sliding stem double port globe valve as shown in Figure 7-4 on page 327 (e.g., Fisher E body) with a sensitive actuator (e.g., diaphragm) sized for at least twice the maximum expected pressure drop at shutoff, and a smart digital positioner. The valve should be installed in the flow-to-open direction to prevent the bathtub stopper effect at low flow. For the feed valves, I suggest a single port globe valve as shown in Figure 7-3 on page 326 with the same actuator and positioner design considerations. The trim is easier to replace in single port valves and the shutoff is tighter, which could be important for isolating downstream users.
A new high pressure design diaphragm actuator as shown in Figure 7-15c has been developed providing much greater thrust/torque. For very high pressure drops, you may need to go to a piston actuator. For large valves you may need to go to a v-notch ball valve as shown in Figure 7-9 or contoured butterfly valve as shown in Figure 7-11. You may need to add a volume booster as shown in Figures 7-29 and 7-30 on the positioner outlet(s) of the pressure control valve if the actuator volume is so big the pre-stroke time delay is greater than about 0.1 seconds.
To minimize interaction between a back pressure loop and a flow loop in series, the pressure drop should be much greater across the flow control valve. The pressure loop should be tuned for fast maximum disturbance rejection. The pressure controller module execution time (0.1 to 0.2 seconds) should be 5 times faster than the flow controller execution time (0.5 to 1.0 seconds). To save energy, a valve position controller (VPC) could be used to slowly reduce the pump pressure to keep the largest of the flow control valve positions at a maximum in the suggested throttle range of the valve.
A VPC can also be used to for the simultaneous throttling of a big and small valve in parallel. The VPC process variable is small valve position, the VPC setpoint is mid throttle position (e.g., 50%), and the VPC output is the big valve signal. For more details on VPC use, see my Control magazine article Don’t Over Look PID for APC. A field pressure regulator is faster than a pressure control loop but you lose visibility and adjustability of pressure.
A variable frequency drive (VFD) would be faster than a control valve if rate limiting is not excessively used in the setup of the speed control but rangeability is a problem if the system frictional pressure drop is low compared to the static head at minimum flow. The Chemical Processing article by Cecil L. Smith Watch out for variable speed pumping provides considerable insight as to the effect of static head on VFD rangeability. The deadband and slip in a VFD is small if properly designed and setup (deadband is often introduced in the drive setup to eliminate reaction to noise but this deadband may be too large causing poor control).
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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