Tuning A Control Loop - The Knowledge Board
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- Опубліковано 16 чер 2024
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DESCRIPTION
Tuning a loop by trial and error is no longer a viable long-term solution for loop stability. In this video we show a proven process for tuning a self-regulating process. This technique is used on 1000’s of control loops and is now available to you in this video.
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I could tell within the first minute that this guy is a natural teacher.
Kevin, you are a great teacher and engineer, THANKS!!
Thanks for taking the time to share your knowledge. You have a knack for explaining a complicated process and breaking it down in a fashion that even a noob can grasp. Cheers!
Your a genius man. Great explanation. You truly know exactly what your talking about. I would love to work on automation projects with you.
Simply an amazing video. It was well summarized and yet extremely informative, specially being just the tip of the iceberg. I am leaning on doing my senior project on PID systems based on what I just learned from you.
Thank you
Kevin, You are brilliant. You teach control as it is in real world. thanks.
One of the best explanations I have watched about a close control loop tuning. A master.
Thank you for sharing with all of us.
Fabulous Sir!
Thanks a lot ABB service!🙌
Hope to get more informative videos at here!
Very practical and honest explanation from his dedicated experience! Received an realistic insight into the topic! Salute to you! ....Love from India!
Thank you for the info, it has definitely helped me understand the basic concept of tuning. Awesome video, thanks for sharing to the Automation world. By the way, i do love your VFD products. I have changed about 95% of our drives over to yours.
I'm now closer to understanding PiD settings ,before I had always guessed.Thank you.
An absolutely brilliant video, very well explained!
Thanks for the very informative and practical explanation.
Thank you for taking out time for this wonderful explanation.
Wow....That's the best explanation I've ever got about PID loops... Thanks a lot....
Confident and Concise session. This knowledge is greatly appreciated. Good thing you had 5 boards at your disposal.
that amazing :) so much important things explained in such easy way.
Thank you. That was incredibly helpful.
Great video ! Extremely Informative ! Thanks for sharing.
Thank you for share this with us. Excellent explanation. 👏👏👏👏😃
Very nice and informative, great work!
Great video. Thanks for sharing.
Really great video on Tuning Fundamentals,,
Your first point is so RIGHT the number if times I have gone to breakdowns "Due to the controller" that is something physical not functioning correctly in the big bad world. The worst was the wrong sensor been installed from construction and after a lot of engineers looking at the controler over 3 years, then I go to site, doing your first thing and look at all the sensors and find they all were getting reading from a pressure tranducer that was the wrong type. Remember there is no such thing as a desk engineer. Very Good Video
SIR, YOU ARE A GENIUS! A very practical way on physically implementing control loops. I have to say that I used to struggle a lot with such concepts in college. This video is gold.
You prolly dont care but does someone know of a method to get back into an instagram account?
I was dumb lost my account password. I would appreciate any help you can give me
Thanks Kevin. Great stuff.
That was really clear, practical and helpful. Thanks a lot.
9:15 - Wow! I've been to engineering school and I never made that connection! Approximating τ as Δ/4 will be extremely useful to me into the foreseeable future! Thanks.
This is the best PID video I’ve seen yet.
Great video! Very concise and no nonsense :-) It might be worth mentioning that when deriving a model from a step-response (I call this a data-driven model), the step used for the response should be in the linear region of the plant/process. Take for instance a motor that can run between 0-1000rpm. To derive a linear model for this motor, the step should not be close to the lower (0 rpm) and upper (1000rpm) operating regions of the motor, due to non-linearities from e.g. inertial mass (shaft, gearbox, load). I would recommend performing an initial step of say 200rpm, followed by a step from 200 to 800rpm. This last step is used for the linear model. The low and upper regions for a motor tend to be non-linear and would not produce an accurate linear model.
For validation I tend to check my stability margins by evaluating the gain and phase margins of the system (yes, I use a classic frequency analysis design approach). Typically I calculate these margins and measure them using an analyzer. In most cases all checks out, but you could risk running into instability due to resonances that are not apparent in the 1st order model. Cheers from Denmark :-)
Good facilitator,very informative.
Thanks for sharing this lesson. best regards
very good explanation, Thanks
Excellent and most practical.
Good video and well explained!!
Excellent video, thanks !
Very, very nice. Bravo and big thank you.
thanks for this lucid explanation
Great explanation, I’ll have to watch again. Only thing I’m not understanding is changing of set point as it relates to time. For example using temperature as units if changing from 72 to 78 vs 84. The function of time changes but I’m not sure how. Any ideas? Will watch again...I love how many whiteboards you have btw 😆
Crystal clear explanation.
Great video. I just need to find a process to tune now.
Very good teaching... Please also make a more video tutorial specs of PLC of what is about is in the marking .
wooow , no word can describe my thankness
Excellent, very good explanation, my respects teacher ............... BRAVO ... !!!
Thanks. I felt like I was back in college learning stuff!
Although some people are very good at it: trial and error tuning should be avoided as much as possible. This is a very nice example to extract information out of process data for tuning loops with simple dynamics ..... However if you follow this instructions to the letter your proportional gain (Kc) will be most of the times not correct and you will not get the intended closed loop behavior. The proportional gain(Kc) should be based on the scaled process gain. So if you use in the calculations Kp*(Output_sf/PV_sf) then your result will be fine. If you use tool for this you have to give in the scale factors and the software takes care of everything. If you plan to do the calculations manually (which is not bad at all) then never forget to include the scaling.....Wrong (or no) scalings = Wrong tuning
so where and what value did you set the the P, the I, The D?
Nicely Explained!
This guy is a world class educator.
thanks! though it is the tip of the iceberg, it is much helpful to my knowledge at work.
ABB is the Best
Very informative video, thanks a lot. :D
This is a very good class
Super helpful thank you!
I love this Videos! UFB Job!
My man. Thank you!
can u give lecture on differential pressure to steam flow cascade in distillation column . or suggest me any good book
Exeptional explication, could you teach us how to tune a second order closed loopr response?, I love you man!!!!!
superb . very informative..thanks for the video:)
Excellent video! :)
amazing! thank you.
thank you very much, it works
Similar to the way I do it, but on some occasions unable to perform even a manual step so watching the response adjust accordingly plotting values to see how the gain changes with various output settings. What about showing when to use a feed-forward and looking at the plant to determine the best way to control not as individual PIDs plus combing more than one process variable into a single control valve.
This is really a nice video
I get it now! Thank you.
Great video Kevin! It did leave me with a few questions. At 5:00 and again at 7:50 you describe bump testing and write out a change in the process variable based on the change in the output. My question pertains to what is "output". I keep thinking that we should be watching for a change in output based on a change of input... So I'm interpreting you to mean that the change in the output, is the output controller (presumably in milliamps from 4 mA to 20 mA), which serves as input to the control valve or the pump speed that would create a change in flowrate (to pick an arbitrary, hypothetical process variable). Presumably this output (my input) is a number that you can get from the control system historian (DeltaV/Foxboro/Siemens PLC/DCS) or taking a measurement with a multimeter across the two wires to the control element. Is that correct?The process variable is undoubtedly measured and also available from the HMI or historian.
My next question pertains to the equations for Standard, Parallel, and Classical PID algorithms. You showed to solve for Kp and Tp and how some of the other parameters (Kc, Ti, Td) could be solved for if one assumes a 1st order model. However you present these 3 equations for standard/parallel/classical with variable S, and never define what S is. Are those expressions supposed to be equal to something? Are you supposed to set these expressions equal to zero to find S?
You're (or you are) a genius.
I suppose you'd have to be a control nerd, as I am, to realize this, but excellent presentation.
Hello sir. I want to start with control systems design and PID so I can do advanced projects, can you recommend me a course or a book to start with ?
thank man! You are genius man!
Really helpful
well done...Thankyou
Man..... you are my hero ;---;
Sir how we can design a PID controller for controlling the position of shaft which is supported by active magnetic bearing ?
How do you do! Please! Could you present video's ABB lst300. How to calibrate it!
thanks so much sir...
Sp validation is good. Also good to validate by load changing to see how fast pv return to sp.
Very Good ; Thanks
Brilliant man
thanks a ton !!!
@14:22 We will do change the setpoint in closed loop. But what the initial value of the PID parameters
I knew I was watching a genius at work when he converted a delta symbol to a 4 on the fly at 9:15 😉
Nice sir, we need more real time problen
thanks a lot sir
Amazing
amazing
Where did you "go back to get a master's degree"? And what background did you have prior yo that, if you don't mind my asking.
Hi Kevin. I work for ABB New Zealand and I am interested in the training course single Loop tuning. Kindly, coud you please send me the training code or the link for apply the training?. thanks
That's a very good video. The main reason, it starts from zero, lol. I'm tired of books that hit you with nuclear-physics looking stuff on page one! Talk to me like I'm stupid cause I am! 😂
I'm going to need more whiteboards.
Please create video for gain scheduling and also Feed forward
Thanks ！！！
Great ! But you didn't mention about the delay (dead time) potential issues, with a long delay, this tuning rule is much less efficient, but ok it works great in many cases.
Laurent Porre
Dead time is included in the process variable response. If it’s too long (compared to actual response) it means the valve is sticking (called stiction) in his first order example. Repairs would have to be made first and then perform new bump tests.
Awesome.....
@14:47 could you please explain why the ratio is 1. What if the ratio is different than 1.
I am confused, isn't the measured Process variable (PV) the same of the output value at (ua-cam.com/video/3viD5ij60EI/v-deo.html)? according to this reference en.wikipedia.org/wiki/PID_controller
GREAT
Kevin, You remaked that is extremenly important to know the PID type (Standard, Parallel or Classical). However, in video I cannot see where this information is relevant. The fact you said to use standard, where it is used for calculation?
How do you adjust your method if the focus is on disturbance rejection and not a setpoint change (i.e. setpoint is fixed all of the time)?
This is not only the exact question why I (master in control engineering plus 30 years of field experience in power plant control loops) disliked this video but the first question you have to ask yourself when theoretically approaching a control loop. Of course first you have to identify that measuring equipment and actuator are doing what they are supposed to do. This is correctly mentioned at the beginning of the video. But then it gets confusing. Most controls are optimized for disturbance and not for setpoint changes. If setpoint changes are part of the process you add in the setpoint path a setpoint control/guidance , e.g. a ramp or a time delay, to smoothen setpoint changes. But the controller itself should be optimized for what you call disurbance rejection. And the integral time is not set according to dominant process time constant like in the example which is in most cases way to slow, but to the parasitary delay times in the process plus the measuring delays. If you want to allow a fast control with a certain amount of overshoot you select about 2-3 times the sum of the delays, if you want a rather slow control without any overshoot you make that factor higher. Kp you select in a way, that your control is fast enough. You have to be aware that the control is more sensitive to noise (can also come from the measurement) when the gain is bigger.
Whereas the video contains a lot of information in a relatively short time the content is in my opinion not totally correct.
how do you tune with two interacting loops? i do not want to decouple. say for instance the interaction exists between the ratio controller which is (feed in/ flow out) and the pressure (which depends on feed in)
tandem313
In this instance you would make the inner loop 10 times faster than the outer loop, using the same bump testing and tuning rules.
123445687359324876234 videos, 6476354812364129876491386 research articles summarized in to just under 22 minutes! Great video, Great explanation. Thanks ABB