The document summarizes a presentation given by Gregory McMillan on process control improvements. It discusses PID controller forms and structures, ways to improve controller performance including PIDPlus algorithms, and best practices for control valves. Examples are given showing how PIDPlus can improve control loop performance under various conditions like wireless communication delays.
PID Control of Slow Valves and Secondary Loops Greg McMillan Deminar SeriesJim Cahill
Greg McMillan shares ways to address slow valves and different time constants between primary and secondary loops.
Recorded deminar (demo/seminar) available for viewing at: http://www.screencast.com/t/YWYxZGUw
PID Control Of Sampled Measurements - Greg McMillan Deminar SeriesJim Cahill
This presentation, PID Control of Sampled Measurements, is from the first in Greg McMillan's live seminar / demo (a.k.a. deminar) series.
You can watch a recorded version of this presentation at: http://www.screencast.com/t/ODhlOWY4M
For future events and background, visit: http://www.emersonprocessxperts.com/archives/2010/04/free_series_of.html
Greg teaches you about Auto Tuning and Adaptive Control of Nonlinear Processes that are self regulating. Recorded video available for viewing at: http://www.screencast.com/t/NDY1NTQx
PID Control of Runaway Processes - Greg McMillan DeminarJim Cahill
On-line demo / seminar presented by ModelingAndControl.com's Greg McMillan on August 25, 2010.
Recorded version of presentation will be available post live session at: http://www.screencast.com/users/JimCahill/folders/Deminars
PID Control of Valve Sticktion and Backlash - Greg McMillan Deminar SeriesJim Cahill
Greg McMillan shows the limit of PID control options to help with sticky valves and valves with excessive deadband in this live deminar (demo/seminar).
Recorded video at: http://www.screencast.com/t/OTJjYjE1Nz
PID Control of Slow Valves and Secondary Loops Greg McMillan Deminar SeriesJim Cahill
Greg McMillan shares ways to address slow valves and different time constants between primary and secondary loops.
Recorded deminar (demo/seminar) available for viewing at: http://www.screencast.com/t/YWYxZGUw
PID Control Of Sampled Measurements - Greg McMillan Deminar SeriesJim Cahill
This presentation, PID Control of Sampled Measurements, is from the first in Greg McMillan's live seminar / demo (a.k.a. deminar) series.
You can watch a recorded version of this presentation at: http://www.screencast.com/t/ODhlOWY4M
For future events and background, visit: http://www.emersonprocessxperts.com/archives/2010/04/free_series_of.html
Greg teaches you about Auto Tuning and Adaptive Control of Nonlinear Processes that are self regulating. Recorded video available for viewing at: http://www.screencast.com/t/NDY1NTQx
PID Control of Runaway Processes - Greg McMillan DeminarJim Cahill
On-line demo / seminar presented by ModelingAndControl.com's Greg McMillan on August 25, 2010.
Recorded version of presentation will be available post live session at: http://www.screencast.com/users/JimCahill/folders/Deminars
PID Control of Valve Sticktion and Backlash - Greg McMillan Deminar SeriesJim Cahill
Greg McMillan shows the limit of PID control options to help with sticky valves and valves with excessive deadband in this live deminar (demo/seminar).
Recorded video at: http://www.screencast.com/t/OTJjYjE1Nz
PID Control of True Integrating Processes - Greg McMillan DeminarJim Cahill
Presented August 11, 2010 by Greg McMillan as on-line demo/seminar. Video recording available at: http://www.screencast.com/users/JimCahill/folders/Public
On-line Process Control Lab Access and Use DeminarJim Cahill
Recorded demo/seminar of Greg McMillan presenting On-line Process Control Lab with Access and Use Instructions on May 27, 2010.
Screencast of presentation available at: http://www.screencast.com/t/Y2Q4NjM0Y
PID Tuning for Near Integrating Processes - Greg McMillan DeminarJim Cahill
Greg McMillan shares how to reduce tuning time for near integrating processes.
Recorded video version available for viewing at: http://www.screencast.com/t/NmUxZTBiNTg
To gain a basic understanding of the principles of PID Loop Optimisation.
To understand why “Loop Tuning” is often not the solution to achieving (or restoring) stability in a process control loop.
To understand how PROFIBUS PA instrumentation can assist in Loop Optimisation.
Foundation Fieldbus - Control in the FieldJim Cahill
Presented by Emerson's Travis Hesketh at the 2011 General Assembly in Mumbai, India on March 9-10.
Download the file to get the full effect of the slide builds.
Split Range Control - Greg McMillan DeminarJim Cahill
Presented March 9, 2011 by Greg McMillan as on-line demo/seminar. Video recording available at: http://www.screencast.com/users/JimCahill/folders/Public
A Unified PID Control Methodology to Meet Plant ObjectivesJim Cahill
Presented at the AIChE 2013 Spring Meeting and 9th Global Congress on Process Safety meeting by Greg McMillan, CDI Process & Industrial and Hector Torres, Eastman Chemical
Wireless Measurement and Control - AIChE New OrleansJim Cahill
Wireless Measurement and Control - Opportunities for Diagnostics Process Metrics Inferential Measurements and Eliminating Oscillations
Presented by Greg McMillan on March 15, 2011.
Natural gas operations considerations on process transients design and controlISA Interchange
This manuscript highlights tangible benefits deriving from the dynamic simulation and control of operational transients of natural gas processing plants. Relevant improvements in safety, controllability, operability, and flexibility are obtained not only within the traditional applications, i.e. plant start-up and shutdown, but also in certain fields apparently time-independent such as the feasibility studies of gas processing plant layout and the process design of processes. Specifically, this paper enhances the myopic steady-state approach and its main shortcomings with respect to the more detailed studies that take into consideration the non-steady state behaviors. A portion of a gas processing facility is considered as case study. Process transients, design, and control solutions apparently more appealing from a steady-state approach are compared to the corresponding dynamic simulation solutions.
Opportunity Assessment and Advanced ControlJim Cahill
Gregory K. McMillan ( http://www.modelingandcontrol.com ) presents the process of assessing opportunities to apply advanced process control (APC), their potential benefits, and exposes some common myths.
An optimal PID controller via LQR for standard second order plus time delay s...ISA Interchange
An improved tuning methodology of PID controller for standard second order plus time delay systems (SOPTD) is developed using the approach of Linear Quadratic Regulator (LQR) and pole placement technique to obtain the desired performance measures. The pole placement method together with LQR is ingeniously used for SOPTD systems where the time delay part is handled in the controller output equation instead of characteristic equation. The effectiveness of the proposed methodology has been demonstrated via simulation of stable open loop oscillatory, over damped, critical damped and unstable open loop systems. Results show improved closed loop time response over the existing LQR based PI/PID tuning methods with less control effort. The effect of non-dominant pole on the stability and robustness of the controller has also been discussed.
Control Loop Foundation - Batch And Continous ProcessesEmerson Exchange
This presentation, by Emerson's Terry Blevins and Mark Nixon, is a guide for engineers, managers, technicians, and others that are new to process control or experienced control engineers who are unfamiliar with multi-loop control techniques.
Their book is available in the ISA Bookstore at: http://emrsn.co/1E
This unit consists of a three part 1500 slide PowerPoint roadmap from sciencepowerpoint.com/ complete with a 14 page bundled homework package, modified version, 9 pages of unit notes, built-in hands-on activities with instructions and visuals, 25 video links, built-in quizzes, review games, answer keys, rubrics, worksheets that follow slideshow for classwork, complete student version of the unit, and much more.
Areas of Focus: -Locations of Water on the Planet, Importance of Water, Groundwater, Groundwater Pollution, The Water Molecule, Properties of Water, Polarity, Cohesion, Adhesion, Capillary Action, High Specific Heat, Water has a Neutral pH, lower density of ice, lake turnover, water cycle, three stares of matter, Water is the Universal Solvent, Mixtures, and much more.
I also sell all 20 Middle-Level Science Units as a curriculum package. This includes all 20 units (50,000 slides), in Life, Earth, and Physical Science for students in grades 5-10, This also includes 275 pages of bundled homework / assessment that chronologically follows each unit, 175 pages of modified assessments, 325 pages of answer keys, 260 pages of unit notes, 37 PowerPoint review games (5000+ slides), 315 videos, hundreds of pages of handouts, First Day PowerPoint, Guidebook, and Four Year Curriculum Guide and classroom license.
Thank you for time and if you have any questions please feel free to contact me at www.sciencepowerpoint@gmail.com. Best wishes.
Teaching Duration = 4+ Weeks
Sincerely,
Ryan Murphy M.Ed
http://sciencepowerpoint.com/
PID Control of True Integrating Processes - Greg McMillan DeminarJim Cahill
Presented August 11, 2010 by Greg McMillan as on-line demo/seminar. Video recording available at: http://www.screencast.com/users/JimCahill/folders/Public
On-line Process Control Lab Access and Use DeminarJim Cahill
Recorded demo/seminar of Greg McMillan presenting On-line Process Control Lab with Access and Use Instructions on May 27, 2010.
Screencast of presentation available at: http://www.screencast.com/t/Y2Q4NjM0Y
PID Tuning for Near Integrating Processes - Greg McMillan DeminarJim Cahill
Greg McMillan shares how to reduce tuning time for near integrating processes.
Recorded video version available for viewing at: http://www.screencast.com/t/NmUxZTBiNTg
To gain a basic understanding of the principles of PID Loop Optimisation.
To understand why “Loop Tuning” is often not the solution to achieving (or restoring) stability in a process control loop.
To understand how PROFIBUS PA instrumentation can assist in Loop Optimisation.
Foundation Fieldbus - Control in the FieldJim Cahill
Presented by Emerson's Travis Hesketh at the 2011 General Assembly in Mumbai, India on March 9-10.
Download the file to get the full effect of the slide builds.
Split Range Control - Greg McMillan DeminarJim Cahill
Presented March 9, 2011 by Greg McMillan as on-line demo/seminar. Video recording available at: http://www.screencast.com/users/JimCahill/folders/Public
A Unified PID Control Methodology to Meet Plant ObjectivesJim Cahill
Presented at the AIChE 2013 Spring Meeting and 9th Global Congress on Process Safety meeting by Greg McMillan, CDI Process & Industrial and Hector Torres, Eastman Chemical
Wireless Measurement and Control - AIChE New OrleansJim Cahill
Wireless Measurement and Control - Opportunities for Diagnostics Process Metrics Inferential Measurements and Eliminating Oscillations
Presented by Greg McMillan on March 15, 2011.
Natural gas operations considerations on process transients design and controlISA Interchange
This manuscript highlights tangible benefits deriving from the dynamic simulation and control of operational transients of natural gas processing plants. Relevant improvements in safety, controllability, operability, and flexibility are obtained not only within the traditional applications, i.e. plant start-up and shutdown, but also in certain fields apparently time-independent such as the feasibility studies of gas processing plant layout and the process design of processes. Specifically, this paper enhances the myopic steady-state approach and its main shortcomings with respect to the more detailed studies that take into consideration the non-steady state behaviors. A portion of a gas processing facility is considered as case study. Process transients, design, and control solutions apparently more appealing from a steady-state approach are compared to the corresponding dynamic simulation solutions.
Opportunity Assessment and Advanced ControlJim Cahill
Gregory K. McMillan ( http://www.modelingandcontrol.com ) presents the process of assessing opportunities to apply advanced process control (APC), their potential benefits, and exposes some common myths.
An optimal PID controller via LQR for standard second order plus time delay s...ISA Interchange
An improved tuning methodology of PID controller for standard second order plus time delay systems (SOPTD) is developed using the approach of Linear Quadratic Regulator (LQR) and pole placement technique to obtain the desired performance measures. The pole placement method together with LQR is ingeniously used for SOPTD systems where the time delay part is handled in the controller output equation instead of characteristic equation. The effectiveness of the proposed methodology has been demonstrated via simulation of stable open loop oscillatory, over damped, critical damped and unstable open loop systems. Results show improved closed loop time response over the existing LQR based PI/PID tuning methods with less control effort. The effect of non-dominant pole on the stability and robustness of the controller has also been discussed.
Control Loop Foundation - Batch And Continous ProcessesEmerson Exchange
This presentation, by Emerson's Terry Blevins and Mark Nixon, is a guide for engineers, managers, technicians, and others that are new to process control or experienced control engineers who are unfamiliar with multi-loop control techniques.
Their book is available in the ISA Bookstore at: http://emrsn.co/1E
This unit consists of a three part 1500 slide PowerPoint roadmap from sciencepowerpoint.com/ complete with a 14 page bundled homework package, modified version, 9 pages of unit notes, built-in hands-on activities with instructions and visuals, 25 video links, built-in quizzes, review games, answer keys, rubrics, worksheets that follow slideshow for classwork, complete student version of the unit, and much more.
Areas of Focus: -Locations of Water on the Planet, Importance of Water, Groundwater, Groundwater Pollution, The Water Molecule, Properties of Water, Polarity, Cohesion, Adhesion, Capillary Action, High Specific Heat, Water has a Neutral pH, lower density of ice, lake turnover, water cycle, three stares of matter, Water is the Universal Solvent, Mixtures, and much more.
I also sell all 20 Middle-Level Science Units as a curriculum package. This includes all 20 units (50,000 slides), in Life, Earth, and Physical Science for students in grades 5-10, This also includes 275 pages of bundled homework / assessment that chronologically follows each unit, 175 pages of modified assessments, 325 pages of answer keys, 260 pages of unit notes, 37 PowerPoint review games (5000+ slides), 315 videos, hundreds of pages of handouts, First Day PowerPoint, Guidebook, and Four Year Curriculum Guide and classroom license.
Thank you for time and if you have any questions please feel free to contact me at www.sciencepowerpoint@gmail.com. Best wishes.
Teaching Duration = 4+ Weeks
Sincerely,
Ryan Murphy M.Ed
http://sciencepowerpoint.com/
This presentation provides an overview of the book Control Loop Foundation. The book authors gave this presentation as a short course at Emerson Exchange 2010.
Slides giving an overview on pH and its measurement.
Contains information about pH meters, its calibration, maintenance , types of ph electrode and modern definition of pH
3 Things Every Sales Team Needs to Be Thinking About in 2017Drift
Thinking about your sales team's goals for 2017? Drift's VP of Sales shares 3 things you can do to improve conversion rates and drive more revenue.
Read the full story on the Drift blog here: http://blog.drift.com/sales-team-tips
Guidelines for Setting Filter and Module Execution RateEmerson Exchange
The is a recording of a presentation given at Emerson Exchange 2010. Basic guidelines are presented on how to set filtering to avoid aliasing. Also, information is provided on how to set control execution rate to achieve best performance.
Mechatronics is a multidisciplinary field that refers to the skill sets needed in the contemporary, advanced automated manufacturing industry. At the intersection of mechanics, electronics, and computing, mechatronics specialists create simpler, smarter systems.
In this paper, we propose a new technique for implementing optimum controller for a conical tank. The objective of the controller is to maintain the level inside the process tank in a desired value. Hence an attempt is made in this paper as Internal Model Based PID controller design for conical tank level control. For each stable operating point, a first order process model was identified using process reaction curve method. The real time implementation is done in Simulink using MATLAB. The experimental results shows that proposed control scheme have good set point tracking and disturbance rejection capability.
The ability to tune a PID loop manually is an art that is quickly becoming scarce, but, like driving a car with a stick shift, it can be very helpful in the right circumstance. In industrial processes automation, most modern control loops are equipped with an auto-tuning algorithm, but in spite of this, there are some loops these automated methods cannot tame.
Having knowledge of the different tuning elements and how to adjust them can help you bring these unruly loops under control. If you have the responsibility to keep the processes running at your plant or factory, this webinar will help you better understand the basics of PID control.
In this webinar you will learn:
The purpose of each of the PID tuning elements
How adjusting the individual PID elements will affect the process
General PID profiles for pressure / flow loops
General PID profiles for temperature loops
An explanation of some supporting parameters like cycle time, manual reset, and anti-reset windup
Utilizing DeltaV Advanced Control Innovations to Improve Control PerformanceEmerson Exchange
Many functions of the DeltaV system are unique in the process industry. In this presentation we explore and discuss innovative features of the DeltaV PID and embedded Advanced Control products that can be applied to improve control performance. In particular, PID options are addressed that enhance cascade and override applications and allow effective single loop control using a sampled or wireless measurement. Application examples are used to illustrate how MPC can be easily added and commissioned online with no changes in the existing control strategy. Also, continuous data analytics is used an example that illustrates how future tools will enable improvements to be made in plant operations.
New Kids on the I/O Block - Transferring Process Control Knowledge to Millenn...Jim Cahill
Presented at 2014 Emerson Exchange conference by Danaca Jordan and Jim Cahill.
As retirement rates accelerate in Western nations, efficiently transferring knowledge and lessons learned to new instrumentation and automation professionals grows in importance. Given generational differences in learning styles and limited spare time to develop training, what are some effective ways to accomplish this? A Boomer and a Millennial collaborate to share practical methods to take back with you.
Social Media and Collaboration in Automation and ManufacturingJim Cahill
Presented at the ARC Industry Forum in Orlando, Florida. The presentation highlights the important of surfacing expertise to make it findable and expanding your social network connections.
Social Media for Process Automation - Why?Jim Cahill
Some reasons process automation suppliers may want to consider the use of social media in their business efforts. Presented by Jim Cahill at the 2011 Valve Manufacturers Association Market Outlook Workshop (http://jimc.me/p5uOFC)
A presentation given to the ISA Executive Board on February 25, 2010. It describes opportunities for social media for businesses and institutions, the Emerson social media story, other companies successes, and pitfalls.
Process Profiling: Investigation And Prediction Of Process Upsets With Advanc...Jim Cahill
2009 HART Plant of the Year Award winner Mitsubishi Chemical Corporation Uses HART Technology to Detect Abnormal Situations and Failures before they Affect the Process
http://hartcomm.org/protocol/realworld/realworld_success_mitsubishi09.html
Advances In Digital Automation Within RefiningJim Cahill
Emerson's Tim Olsen presents to Argentinean refiners on the changes in automation technologies and how they are being applied to improve efficiency and reduce costs.
At Emerson Exchange 2009, Martin Berutti presents on the business benefits, requirements, and steps for building a Virtual DeltaV system with a virtual plant and I/O.
Isa saint-louis-exceptional-opportunities-short-course-day-2
1. ISA Saint Louis Short Course Dec 6-8, 2010 Exceptional Process Control Opportunities - An Interactive Exploration of Process Control Improvements - Day 2
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4. Block Diagram of “Series”, “Real”, or “Interacting” PID Form Nearly all analog controllers used the “Series” or “Real” Form SP proportional integral derivative Gain Reset (1 T i ) Rate CO filter filter CV filter Filter Time Rate Time Improving Controllers
5. Block Diagram of “Standard”, “Ideal”, or “Non-interacting” PID Form Nearly all digital controllers have the “standard” or “Ideal” form as the default Improving Controllers SP proportional integral derivative Gain Reset (1 T i ) Rate CO filter filter CV filter Filter Time Rate Time
6. Positive Feedback Implementation of Integral Mode Improving Controllers SP proportional derivative Gain Rate CO filter filter CV filter Filter Time Rate Time filter Filter Time = Reset Time ER is external reset (e.g. secondary PV) Dynamic Reset Limit ER Positive Feedback
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8. PID Controller Forms PB = 100% K c CO n = P n I n + D n + CO i CO i = controller output at transition to AUTO, CAS, or RCAS modes (%) CO n = controller output at execution n (%) CV n = controlled variable at execution n (%) D n = contribution from derivative mode for execution n (%) I n = contribution from integral mode for execution n (%) K c = controller gain (dimensionless) P n = contribution from proportional mode for execution n (%) R i = reset setting (repeats/minute) PB = controller proportional band (%) SP n = set point at execution n (%) T d = derivative (rate) time setting (seconds) T i = integral (reset) time setting (seconds/repeat) = rate time factor to set derivative filter time constant (1/8 to 1/10) = set point weight for proportional mode (0 to 1) = set point weight for derivative mode (0 to 1) R i = (60 T i ) Conversion of settings: Improving Controllers (K c T d ) SP n – SP n-1 ) – (CV n CV n-1 ) ] T d D n-1 D n = ------------------------------------------------------------------------------- T d t P n = K c SP n – CV n ) I n = (K c T i ) SP n – CV n ) t I n-1 Standard P n = K c SP n – D n ) I n = (K c T i ) SP n – D n ) t I n-1 Series
19. Control Valve Watch-outs dead band Deadband Stick-Slip is worse near closed position Signal (%) 0 Stroke (%) Digital positioner will force valve shut at 0% signal Pneumatic positioner requires a negative % signal to close valve The dead band and stick-slip is greatest near the closed position Deadband is 5% - 50% without a positioner ! Plugging and laminar flow can occur for low Cv requirements and throttling near the seat Consider going to reagent dilution. If this is not possible checkout out a laminar flow valve for an extremely low Cv and pulse width modulation for low lifts Improving Valves
20. Direct Connection Piston Actuator Less backlash but wear of piston O-ring seal from piston pitch is concern Improving Valves
21. Significant backlash from link pin points 1 and 2 Link-Arm Connection Piston Actuator Improving Valves
22. Stick-slip from rack and gear teeth - particularly bad for worn teeth Rack & Pinion Connection Piston Actuator Improving Valves
23. Lots of backlash from slot Scotch Yoke Connection Piston Actuator Improving Valves
24. Diaphragm Actuator with Solenoid Valves Improving Valves Port A Port B Supply ZZZZZZZ Control Signal Digital Valve Controller Must be functionally tested before commissioning! SV Terminal Box
25. Piston Actuator with Solenoid Valves Improving Valves Port A Port B Supply Digital Valve Controller SV SV Volume Tank Must be functionally tested before commissioning! Piston W Check Valve Air Supply Terminal Box
26. Size of Step Determines What you See Improving Valves Maintenance test of 25% or 50% steps will not detect dead band - all valves look good for 10% or larger steps
27. Effect of Step Size Due to Sensitivity Limit Improving Valves
28. Response to Small Steps (No Sensitivity Limit) Improving Valves Stroke (%) Time (sec)
29. Response to Large Steps (Small Actuator Volume) Improving Valves Time (sec) Stroke (%)
30. Installed Characteristic (Linear Trim) Improving Valves Valve pressure drop ratio ( P R ) for installed characteristic: Characteristic 1: P R 0.5 Characteristic 2: P R 0.25 Characteristic 3: P R 0.125 Characteristic 4: P R 0.0625
31. Installed Characteristic (Equal Percentage Trim) Improving Valves Valve pressure drop ratio ( P R ) for installed characteristic: Characteristic 1: P R 0.5 Characteristic 2: P R 0.25 Characteristic 3: P R 0.125 Characteristic 4: P R 0.0625
32. Improving Valves Installed Characteristic (Modified Parabolic Trim) Valve pressure drop ratio ( P R ) for installed characteristic: Characteristic 1: P R 0.5 Characteristic 2: P R 0.25 Characteristic 3: P R 0.125 Characteristic 4: P R 0.0625
33. Limit Cycle in Flow Loop from Valve Stick-Slip Improving Valves Controller Output (%) Saw Tooth Oscillation Process Variable (kpph) Square Wave Oscillation
35. Real Rangeability Improving Valves Minimum fractional flow coefficient for a linear trim and stick-slip: Minimum fractional flow coefficient for an equal percentage trim and stick-slip: Minimum controllable fractional flow for installed characteristic and stick-slip: C xmin minimum flow coefficient expressed as a fraction of maximum (dimensionless) P r valve pressure drop ratio (dimensionless) Q xmin minimum flow expressed as a fraction of the maximum (dimensionless) R v rangeability of control valve (dimensionless) R range of the equal percentage characteristic (e.g. 50) X vmin maximum valve stroke (%) S v stick-slip near closed position (%)
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37. Volume Booster with Integral Bypass (Furnace Pressure and Surge Control) Improving Valves Signal from Positioner Air Supply from Filter-Regulator Air Loading to Actuator Adjustable Bypass Needle Valve
38. Booster and Positioner Setup (Furnace Pressure and Surge Control) Improving Valves Port A Port B Supply ZZZZZZZ Control Signal Digital Valve Controller Must be functionally tested before commissioning! 1:1 Bypass Volume Booster Open bypass just enough to ensure a non-oscillatory fast response Air Supply High Capacity Filter Regulator Increase air line size Increase connection size Terminal Box
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44. Dynamic Response to Step Improving Measurements Time (seconds) Theoretical Transmitter Response Actual Transmitter Response True Process Variable m m deadtime measurement time constant Process Variable and Measurement
45. Dynamic Response to Ramp Improving Measurements Time (seconds) Actual Transmitter Response True Process Variable m m Process Variable and Measurement
46. Attenuation of Oscillation Amplitude by Transmitter Damping or Signal Filters: When a measurement or signal filter time ( f ) becomes the largest time constant in the loop, the above equation can be solved for (A o ) to get the Amplitude of the original process variability from the filtered amplitude (A f ) Improving Measurements Effect of Transmitter Damping and Signal Filters
47. Effect of Transmitter Damping or Filter for Surge Improving Measurements m m m m
56. Elimination of Ground Noise by Wireless pH Improving Measurements Wired pH ground noise spike Temperature compensated wireless pH controlling at 6.9 pH set point Incredibly tight pH control via 0.001 pH wireless resolution setting still reduced the number of communications by 60%
65. Effect of PZ Solvent on pH Improving Measurements
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67. Cascade Loop Block Diagram p1 p2 p2 K p2 p1 m2 m2 K m2 c2 f2 Primary Process K v v v K L2 L2 L2 Primary Load Upset CV p CO p MV PV p2 Delay Lag Delay Delay Delay Delay Delay Lag Lag Lag Lag Lag Gain Gain Gain Gain Local Set Point DV p2 % % % Delay <=> Dead Time Lag <=>Time Constant K L1 L1 L1 Delay Lag Gain DV p1 Secondary Load Upset CO s Secondary PID Cascade Set Point % % K p1 Gain CV s m2 m2 K m2 Delay Lag Gain c2 f2 Delay Lag Secondary Process Primary PID Primary: o2 v p1 p2 m2 c2 f2 v p1 Secondary: o1 v p1 m1 c1 f1 v Improving Loops - Part 1 K c2 T i2 T d2 K c1 T i1 T d1
68. Cascade Control Benefit (self-regulating process) Improving Loops - Part 1 i o i o i o i inner loop process time constant o outer loop process time constant i inner loop process deadtime o outer loop process deadtime
69. Cascade Control Benefit (integrating process) Improving Loops - Part 1 i inner loop process time constant o outer loop process time constant i inner loop process deadtime o outer loop process deadtime i o i o i o
70. Cascade Control Benefit (runaway process) Improving Loops - Part 1 i o i o i o i inner loop process time constant o outer loop process time constant i inner loop process deadtime o outer loop process deadtime
71. Secondary loop slowed down by a factor of 5 Secondary SP Secondary CO Primary PV Secondary SP Primary PV Secondary CO Effect of Slow Secondary Tuning (cascade control) Improving Loops - Part 1
72. Triple Cascade Loop Block Diagram Improving Loops - Part 1 Control Valve AO PID PID AI AI Flow Meter Process Process Sensor Secondary (Inner) Loop Feedback Primary (Outer) Loop Feedback Process SP Flow SP Out PV PV Relay PID * Position Loop Feedback DCS Valve Positioner Position (Valve Travel) I/P Drive Signal * most positioners use proportional only
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76. Bias Correction of Ratio Control For information on Ratio Control, see April 7, 2009 Post on website http://www.modelingandcontrol.com/2009/04/what_have_i_learned_-_ratio_co_1.html Improving Loops - Part 1
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Editor's Notes
The self-organizing network and automatic reporting of alerts makes it easy to maintain and revise a control system for flexibility and adaptability to changing experimental conditions and requirements in the dynamic environment of a process development lab.
Battery Life is extended by using exception reporting (signal is transmitted only when it exceeds the resolution setting) unless the elapsed time since the last transmission exceeds the refresh time, which can be set to large value.