February 5, 2010

Exceptional Opportunities in Process Control - Middle Signal Selection

By Greg McMillan

This piece could have been titled "Exceptional Failures in Process Control." Despite my 25 years of explaining the importance of using middle signal selection, I don't see much evidence of what I have said has taken root outside of Monsanto and its spin-off Solutia, where it became a part of the culture and best practices to use middle signal of three pH electrodes for all important pH control loops. We ended up taking a view that all pH loops are important because if they are unimportant why should we go through the maintenance headaches and the risk of control system failure by installing a loop dependent upon the integrity of a single electrode. I think the main hurtle besides hardware and installation cost is the feeling that if one electrode requires so much effort, why should I add more? If the electrode life expectancy is too short, the feeling is right. We should not add more of a bad application or installation. Instead, we need to find a better design, technology, implementation, and location verified in testing via wireless pH or an alternate measurement (e.g. conductivity for concentrated acids or bases).

As an important side note, the use of three transmitters and middle signal selection on all of the important measurements (e.g. flow pressure, temperature, and level besides pH) used in the control system and safety system for a large intermediates plant has consistently eliminated false trips saving several million dollars per year.

What boggles my mind is that the risk of poor product quality and an environmental violation do not provide a wakeup call that the lifecycle cost of the measurement itself is insignificant in comparison to the risk. A simple quick ball park benefit versus cost analysis would show the absurdity of when the dollars of events likely to occur each year is more than 1000 times the dollars of the additional automation to prevent them. Unfortunately, we tend to get too focused on short term costs. Consider bioreactor batches worth millions of dollars each of a sold out pharmaceutical that are dependent pH upon control to within 0.02 pH. A second electrode is added but I am not sure it helps or just adds to the confusion. I find it almost bizarre how favorite electrodes are picked for the loop's PV and the stories that ensue about which one is best. It is a "fact of life" that electrodes will not agree in the short term due to non-ideal effects too numerous to get into here (check out my ISA book Advanced pH Measurement and Control for more info and previous blogs by searching for "pH"). The continual disagreement between two electrodes often leads to calibration adjustments chasing calibration adjustments. If left alone, the electrode that reads high today may in a couple of hours or at least by tomorrow read low. Electrodes can fail anywhere on the scale (including the most insidious failure of all type where the bad electrode signal is stuck at the pH set point). I maintain that the correct use of middle signal selection will actually reduce the long term maintenance cost by simple observation and the use of more intelligent practices eliminating unnecessary calibration and removal of electrodes.

A middle signal selection inherently ignores a single failure of any type and avoids the slowest electrode (e.g. coated electrode). This selection reduces noise and eliminates spikes without any addition of a signal lag like what you get from signal filtering. Middle signal selection also ignores an electrode with lower efficiency (shorter span) or that is drifting. Theoretically, electrodes of different "in service" time should be used to reduce the occurrence of concurrent failures. The middle electrode is the best signal on the average, but please don't use the average. I have seen some very smart attempts of computing average signals with built in intelligence on signal rejection that were out foxed by a single electrode failure scenario. You would think you could devise something smarter than the simple middle signal selection when in fact inherently it is impossible for a single failure. There can be additional intelligence for more than three electrodes or for protection against multiple concurrent failures.

To summarize, middle signal selection can improve process quality and on-stream time, reduce maintenance, and prevent environment violations by adding understanding and ignoring spurious signals, inaccurate measurements, and failures.

A prolonged deviation from the middle should be alarmed because if you don't fix the first failure or sustained error, middle signal section has a fifty-fifty chance of preventing the next failure or electrode inaccuracy. I could go on and on but I suspect you are pressed to move on. Before I go let's be frank with closing remarks in recognition of an engineer named Frank who was particularly astute at telling it the way it is.

There is an opportunity to use a statistical or first principle model based on titration curves to generate a third signal. Even if the model is wrong, it will be ignored by middle signal selection. There appears to be here mostly an upside where you will at least learn more about your process by developing a model.

I have no illusions as to whether this blog will change one person's mind enough to install middle signal selection even though it is a feature of a standard function block. I also have no expectations that enough users will see the need to take advantage of wireless measurements to eliminate the wiring installation and maintenance costs of going to three measurements. Even more unlikely is that users will end up using middle signal selection enough that it will be offered in a smart transmitter that inputs three electrodes even though electrodes are the weak link in regards to accuracy and reliability.




January 27, 2010

Exceptional Opportunities in Process Control - Smart Wireless pH and Conductivity

By Greg McMillan

As I look back over my experience with pH and conductivity measurements, the following opportunities stand out.

(1) Selecting the best sensor technology for a wide range of process conditions
(2) Eliminating measurement noise
(3) Predicting sensor demise
(4) Developing process temperature compensation
(5) Developing inferential measurements of process concentrations
(6) Finding the optimum sensor location

You really can't ship most chemicals to the electrode manufacturer and electrodes sent back after a problem often don't tell the whole story including handling, maintenance, and process conditions. The manufacturer's application support people are often at a loss as to what was really the problem. Then there are the insidious spikes that come and go with no sense of the source or the fix.

The biggest source of continual pH noise is fluctuations in acid and base concentration at the electrode. Operating points on the relatively steep portion of the titration curve require a degree of mixing that goes way beyond the norm. Electrodes are moved to a location that is the best compromise between noise and measurement delay and lag.

Users can install a test setup in the plant to compare the performance of various electrode technologies but this is time consuming and does not allow experimentation. Tests in the lab usually involve "dumb" lab meters with the data ending up in a spreadsheet oblivious to the historian and the tools in the DCS for neural networks and data analytics.

To see if the opportunities are more than a dream and if the problems can become just a bad memory, check out the InTech web exclusive article "Opportunities for Smart Wireless pH, Conductivity Measurements"




December 1, 2009

Exceptional Opportunities in Process Control - Control Valve Dynamics

By Greg McMillan

In the process industry, what a control loop eventually manipulates in nearly all applications is a flow via a final control element such as a control valve, damper, or variable speed prime mover (pump, fan, or compressor). Dampers and variable speed prime movers are commonly found in utility systems. Peristaltic pumps are used in labs and positive displacement pumps are used for extremely low additive flows in plants. In instances, mass flow controllers (thermal mass flow meters with an integrated PI controller and valve) and remotely set pressure regulators are used. However, in production units, control valves are used as the final element in 95% or more of the loops.

Do we know for a change in controller output, did the valve actually move and if so when? Do we know when the control valve is the source of process variability? Do we know what makes a valve "Good" or Bad" in terms of its ability to do its job?

In valve selection and specification, a lot of effort is put into making sure the valve passes the required flows, has minimal leakage, no plugging, and has materials of construction and packing that withstands process composition and conditions. The dynamic response is often neglected possibly because response criteria and requirements are not well understood. Since most loops are digital, the question comes down to whether the change in controller output in a given scan results in a change in position of the internal trim (closure component such as a plug, ball, or disc). Of course most valves will eventually re-position, but the internal trim may not move until the total accumulated change in the controller output is large enough to

(1) Exceed the sensitivity of the positioner and actuator
(2) Change the pressure in the actuator enough to move its shaft
(3) Work through the play in shaft/stem linkages or connections (backlash)
(4) Break free the internal trim from packing, seating, and sealing friction (sticktion).

The result is a delay and a jump followed by a slow transition to a new position. The jump from sticktion causes a limit cycle in any PI or PID control loop. The deadband from backlash causes a limit cycle in any PI or PID control loop on an integrating process (e.g. level or batch temperature). The delayed and slow response adds pure and effective deadtime, respectively, to the loop.

The ultimate question is what should a user specify in terms of valve response? The table ControlValveResponseCriteria.pdf provides a summary of the parameters that makes a valve rated "Great", "Good", "Fair", "Poor", and "Bad". For most loops where process variable deviations of 0.5% are tolerable, a "Fair" valve will suffice. For loops where tighter control is needed (e.g. column, crystallizer, evaporator, or reactor temperature), a "Good" valve is needed. For loops with high process gains (e.g. pH), a "Great" valve is required to prevent self-inflicted oscillations from limit cycles being larger than the allowable deviation around set point (pHControlValveSizeandResolution.pdf). For tight control in loops with extremely fast dynamics (e.g. polymer pressure and incinerator pressure) a "Great" valve or a special variable speed drive may be needed (see "Analog Control Holdouts" on this website).

The ISA-75.25.01-2000 (R2006) draft standard "The Test Procedure for Control Valve Response Measurement from Step Inputs" and ISA-TR75.25.02-2000 (R2006) draft technical report "Control Valve Response Measurement from Step Inputs", use the time to reach 86% of the final response as a major criteria. This assumes the step input size is larger than the valve resolution and deadband for steps in the same direction and reverse direction, respectively. This 86% response time for small steps can be estimated as the sum of the pre-stroke deadtime and secondary lag time plus twice the primary lag time. For example, the 86% response time of a "Good" valve would be about 1.3 seconds for a 0.5% step (0.2 sec + 0.1 sec + 2*0.5 sec). For large step sizes encountered in surge and vessel pressure control systems, the 86% response time can be estimated as the sum of the pre-stroke deadtime and secondary lag time plus the stroking time to reach 86% of the step size. For example, the 86% response time of a "Good" valve would be about 2.45 seconds for a 50% step (0.2 sec + 0.1 sec + 0.86*0.5*5 sec). Note that the actuator size, pneumatic connections, and accessory (e.g. booster, positioner, and solenoid valve) flow coefficient determines the pres-stroke deadtime and stroking time, The pre-stroke and stroking values are based solely on actuator shaft movement and are determined by the manufacturer for tests of an actuator not connected to a valve. The sensitivity of the actuator and positioner is the minimum change in signal that causes a change in shaft position within a reasonable time frame (e.g. 10 seconds). Diaphragm actuators and digital positioners have the best sensitivity. Rack and pinion actuators and spool positioners have the worst sensitivity. Pneumatic positioners and scotch-yoke actuators are also bad news. The deadband from backlash in stem and shaft connections and the resolution from friction in packing, seats, and seals are determined after the actuator shaft moves. For practical purposes, the sensitivity of the actuator and positioner can be combined with the resolution limit of the valve for a total resolution of the package.

I have been particularly sensitized to valve response due to working on pH, furnace pressure, and compressor control. To add insult to injury, a proliferation of piping valves with piston actuators and spool positioners developed as a result of the emphasis on tight shutoff and low cost rather than response. These on-off valves posing as throttling valves created a problem for all types of loops. The idea was if the on-off valve worked well for sequencing and safety systems and was already in the piping spec, why not slap on a positioner and make it a throttling valve. Often the process variability from valve limit cycles was attributed to unknown process disturbances since there was no readback of actual closure component position.

This blog is getting long so I will just close with some figures on valve dynamics (ControlValveDynamics.pdf) from my new book The Essentials of Modern Measurements and Final Elements - A Guide to Design, Configuration, Installation, and Maintenance.

In upcoming entries we will seek to sort fact from fiction and hopefully provide some insight on valve rangeability and variable speed drive dynamics and rangeability.




October 15, 2009

Exceptional Opportunities in Process Control - ISA Boston Presentation

By Greg McMillan

I will be doing the presentation McMillanISABostonExceptionalOpportunities.pdf next week at the Boston ISA section meeting. I will be giving out 10 free copies of my book The Funnier Side of Retirement for Engineers and People of the Technical Persuasion to balance out the serious stuff.

When?
Tuesday, October 20, 2009
6:00 - 7:00 Reception and registration
7:00 - 8:00 Dinner
8:00 - 9:00 Presentation

Where?
Best Western, Waltham, MA
380 Winter Street, Waltham, Massachusetts, 02451-8700, US
Phone: 781/890-7800 Fax: 781/890-4937




August 18, 2009

Post Retirement Key Points - Part 4 (2009 Articles)

By Greg McMillan

My articles in 2009 are focused on pH and wireless measurement and control. Not listed below is an article planned for later this year on the use of wireless pH for inferential measurement of solvent concentration at the University Texas Research Campus pilot plant for carbon dioxide capture.

"Virtual Plant Provides Real Insights", Chemical Processing, Jan, 2009
"ImprovingpHSystemDesignandPerformance.pdf"

(1) Modeling and control in a virtual plant showed that the size of the neutralization vessels could be reduced from 40,000 to 10,000 gallons reducing the project capital costs by more than $500K for a strong acid and base system. The virtual plant was also able to detail mixing, reagent injection, and valve requirements

(2) Translation of the controlled variable from pH to percent reagent demand (X axis of the titration curve), provided faster recovery from upsets.

(3) It was expected that the resolution of the reagent valves needed to be exceptional. It was surprising how important resolution was for the feed valves. What would be normally considered a good resolution for the feed valves caused excessive deviations in the vessel pH. Stick-slip in the feed valves showed up as short term deviation rather than a limit cycle in the pH because of the feedback correction by the pH loop

(4) Innovative Methods of continuous and semi-batch mode offered maximum operational flexibility.

"Is Wireless Process Control Ready for Prime Time", Control, May, 2009

My time in spent building and starting up chemical plants, working in process labs, and dealing with pH measurement noise gave me a greater appreciation for the significance of being able to eliminate instrument wiring. This article offers my take on the value wireless and shows incredibly tight wireless bioreactor pH control. Some biopharmaceutical processes require control within 0.02 pH of set point for optimum operation. The pH control demonstrated in this wireless pH test on a bioreactor with a disposable liner (single-use-bioreactor) was an order of magnitude better than required, the tightest pH control I have ever seen. Most of the credit goes to new wireless PID algorithm and the exceptional capability of the pH electrode and wireless pH transmitter. Finally, the wireless measurement did not have the spikes exhibited by the wired pH transmitter from ground noise, showing that wireless can eliminate a significant source of noise.

"The Essentials of pH Measurement Design, Installation, Maintenance, and Improvement", ISA 55th International Instrumentation Symposium, League City, 2009

This paper is a chapter out of "The Essential Book" scheduled to be published in time for ISA Expo 2009 in Houston.




August 10, 2009

Post Retirement Key Points - Part 3 (2007 - 2008 Articles)

By Greg McMillan

I am back from vacation. I am still feeling fine from a nice break from the heat of a book deadline and Austin's record temperatures. I was up north in Minnesota and Wisconsin where it was 25 degrees cooler. I happened across an exhibit of Cray computers in the Museum of Science and Technology in Chippewa Falls, the home of Cray Research, Inc. Samuel Cray attributed part of the company's success to a motto of "taking our jobs seriously but not taking ourselves seriously." Hopefully my Control Talk column is an example of this motto by combining a humorous look at ourselves with technical straight talk. A compilation of the column's comics was featured in the July issue of Control magazine in the online section "Out of Control Cartoons".

Then there are the outbursts of craziness designed to loosen us up such as The Funnier Side of Retirement for Engineers and People of the Technical Persuasion, which just won the ISA Raymond D Molloy Award as the best selling book in 2008. Since humor is derived from exaggeration of commonly recognizable traits, please don't buy this book if you want a detailed analytical realistic treatise. For this you can get any one of a dozen or more guides to retirement. If you like bizarre humor, this book may offer some laughs.

The following list of articles and associated papers in 2007 - 2008 are totally serious except for an occasional top ten list.

"Improve Control Loop Performance", Chemical Processing, Oct, 2007

(1) Nearly all control loops eventually affect the process by the manipulation of a flow via a control valve. Control loop performance depends upon valve performance.

(2) Valve specifications do not require a valve actually move in response to a change in signal. When valve performance has been considered, response time and rangeability are frequently the criteria. The real issues are valve resolution (sticktion) and deadband (backlash). If a properly selected and sized valve-actuator assembly has good resolution and sticktion, the valve will generally have good rangeability and response.

(3) Using a "state of the art" digital positioner can eliminate the positioner sensitivity problems prevalent in positioners for the last 50+ years but the positioner can be lying about valve performance if the feedback measurement is actuator shaft rather than ball or disk position in a rotary valve. Putting a digital positioner on a valve designed for on-off service and tight shutoff by a piping manufacturer is like putting makeup on a pig. On the other hand, putting a digital positioner on a valve designed by throttling service by a control valve manufacturer may be the best thing you can do for your loop.

(4) For pH control, the resolution of the control valve can determine the number of stages of neutralization needed.

"Virtual Control of Real pH", Control, Nov, 2007

"Advances in pH Modeling and Control", ISA 54th International Instrumentation Symposium, Pensacola, May, 2008

An online virtual plant can be adapted to match the actual plant by the simple innovative use of an integrated model predictive control (MPC). In this neutralization system, the influent acid concentration was quickly adapted to match the ratio of reagent to influent flow in the virtual plant to the actual plant. The virtual plant demonstrated of ability of model predictive control to replace fuzzy logic control for reagent optimization. An improvement in the kicker algorithm provided immediate savings of more than $100K per year in reagent cost.

"PAT Tools for Accelerated Process Development and Design", Bioprocess International, Process Design Supplement, Mar, 2008.

"Bioprocess Control: What the next 15 Years will Bring Part 2 - Process Modeling",
Pharmaceutical Manufacturing, June, 2008

Most process and control system improvements in bioreactors are set by biochemists and biochemical engineers in the research. A virtual plant running 500 times real time can complete a bioreactor batch in 15 minutes that would take several weeks in the lab or pilot plant. Virtual experimentation can accelerate process development and design. The integration of advanced control tools in the virtual plant can demonstrate the effectiveness of substrate and batch profile control. The results can justify additional online analytical measurements. The fast playback of virtual and actual plant batches in a minute or two offers incredible opportunities for online analysis via integrated data analytics and adaptive control tools. The potential benefits are faster commercialization, higher yields, and real time release.

"Unlocking the Secret Profiles of Batch Reactors", Control, July, 2008

The purpose of a batch reactor is to manufacture a product of a particular composition. The progression of the batch to the desired end point (the batch composition profile) is the most important indicator of batch performance. However, batch reactors rarely have any measurement of this profile. For chemical reactors, the main measurements indicative of the hidden profile of real interest are pressure, temperature, and feed flows. Multivariate statistical techniques such as Projection to Latent Structures (PLS) may be able to predict end points but the composition profile still remains a secret. If actual or inferential measurements of the profile are available, model predictive control can maximize the slope of the profile and hence the progression of the batch. The result is a faster batch for a given end point or a higher end point for a given cycle time. Also, the variability in batch profiles is transferred to feeds resulting in more repeatable batch profiles.

There is a misconception that biological processes are not as highly automated as chemical processes. Bioreactors generally have more control loops than a typical chemical reactor. Cell cultures have temperature, pressure, air flow, oxygen flow, inert flow, carbon dioxide flow, sodium bicarbonate flow, substrate flow, nutrient flow, pH, and dissolved oxygen control. Major advances in at-line composition measurements, such as the Nova Bioprofile Flex Analyzer combined with an auto sampler can provide measurements of substrates, nutrients, byproducts and cells every 4 to 12 hours depending upon the application. The Fogal Dielectric Spectroscopy probe can provide a measurement of the integrity of the cell membrane (cell viability). When combined with a turbidity measurement of cell density, the Fogale probe offers an online indication of live and dead cell concentrations.

One of the obstacles of online composition control is the time delay from the sample cycle time. The time in between samples for at-line analyzers can vary from an hour to a day. Fortunately, an unexpected side benefit of the enhanced wireless PID (developed to handle the larger and more variable time delays of wireless measurements) is exceptional control using measurements from at-line analyzers. The wireless enhanced PID has been shown to provide tight and stable control using at-line analyzers in specific studies for glucose control and in generic studies for continuous and batch processes. The results are documented in slides 29-34 of Interphex2009_Advances_In_Bioreactor_Modeling_and_Control.pdf. See the May 11, 2009 entry "What have I Learned - Cost and Source of Oscillations (Part 4)" for more details.

The new control algorithms (max slope MPC setting the enhanced wireless PID) coupled with new at-line and online analytical measurements will make bioreactor profile control common place leaving chemical reactor control even further behind. Are we going to let this happen?

Next week we conclude with the 2009 articles that include results of wireless control in a bioreactor with a disposable liner called a "Single Use Bioreactor" (SUB).




April 27, 2009

What Have I Learned? - Cost and Source of Oscillations (Part 2)

By Greg McMillan

The loops with the most severe oscillations listed in order from biggest amplitude to smallest amplitude are pH loops, level loops, flow loops, pressure loops, batch temperature loops, heat exchanger temperature loops, and column temperature loops.

The following is a list of the sources of product quality oscillations in the approximate descending order of frequency of occurrence based on my experience. I have even offered my best guess in parentheses as to the percentage of applications that can be tracked to these root causes for chemical and biochemical products. You may wonder why pH loops didn't make the top of the list since it has the most severe oscillations. The main reason pH loops are down the list is that most pH loops are in waste treatment (WT). Also, the pH loops in reactors and bioreactors tend to have much lower process gains than WT pH loops and some process regulation from reagent consumption. Interacting temperature loops on furnaces, reformers, and reactors are severe problems but are near the bottom of the list for applications for specialty chemicals and biochemical products because multi-zone or profile temperature control are more prevalent in the petroleum, petrochemical, and bulk chemical industries. The following list is for normal operation of loops with good valves and does not consider oscillations that originate from the startup and shutdown and failure of equipment. Next week we will see the implications of "not so good" valves.

(1) Too much reset action in level loops on surge and feed tanks (40%)
(2) Discontinuities at split range point for pH, pressure, and temperature loops (20%)
(3) Interacting pressure and flow loops on headers (10%)
(4) Too much reset action in overhead pressure loops on columns and vessels (10%)
(5) Set point response of batch temperature loops (5%)
(6) Interacting temperature loops for 2 point composition control of columns (5%)
(7) Interacting temperature loops on furnaces and reactors (5%)
(8) Set point response of batch pH loops (5%)




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The opinions expressed here are the personal opinions of Greg McMillan and Terry Blevins. Content published here is not read or approved by Emerson before it is posted and does not necessarily represent the views and opinions of Emerson. © 2006-2010 Greg McMillan and Terry Blevins. All rights reserved.