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Forum Post: AMS Device Manager connection through T+H to Stahl RIO

September 12, 2014, 6:50 am
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Hi

I hope to use a Network designed AMS Device Manager system using a server plus station and one client.  The system will connect to HART devices through Stahl remote IO, onto Delta V profibus DP and then into a T+H profibus to Ethernet module. The ethernet network is then connected to my client and server + stations.  My question is below.

Does anyone know the maximum number of T+H profibus DP to Ethernet modules you can connect to a single networked AMS Device Manager server plus station?  I need to connect more than 30 so if the limit is less than that does anyone know how to get round the problem without introducing a second Device Manager system?

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File: ACS6000: RADIUS Authentication, Authorization, and Accounting

September 12, 2014, 8:23 am
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ACS 6000 Advanced Console Server | IT Console | RADIUS Authentication, Authorization, and Accounting

Background:

Remote Authentication Dial-In User Service (RADIUS) is a client/server protocol and software that enables remote access servers to communicate with a central server to authenticate dial-in users and authorize their access to the requested system or service.

Environment/ Setup:

  • Operational FreeRadius Server version 2.2.3 or higher.
  • Authentication Server and Accounting Server are configured on a single machine.
  • Cyclades ACS6000 Advance Console Server Firmware 2.5.0.7 or higher.
  • Privilege access to both Radius Server and ACS6000 Advance Console Server as root user.

Objectives:

  • To configure Cyclades ACS6000 Advance Console Server external authentication using RADIUS protocol
  • To limit/allow all access to serial port(s) using a group authorization 

Charkkrit Wattananusit

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Blog Post: Regulatory and Model Predictive Control Difference?

September 12, 2014, 11:47 am
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Over in LinkedIn’s Process Control group, a question was asked:

What is the difference between regulatory and model predictive control. Is it possible that MPC work as stand alone without regulatory control?

Emerson’s Chowyang Neo offered:

Chowyang Neo Sales & Marketing Manager

Chowyang Neo
Sales & Marketing Manager

Regulatory Control generally refers to good old PID loop control. Gaps between the SP and PV known as errors are being fed to a PID controller so that Process Variables (PV) is then being steered closer towards the setpoint (SP) based on the magnitude of the error. There can be more advanced variants of this simple PID – cascade, ratio, feedforward etc. But all of these are generally considered as Regulatory or Adv Regulatory Control.

The use of model based technique is driven more by the complex, multi-variable nature of some of the processes we see in this industry. The level control of boiler is a classic example with many factors playing a part….Have a read to get more

Emerson’s Lou Heavner added:

Lou Heavner Systems/Project Engineering Consultant

Lou Heavner
Systems/Project Engineering Consultant

There is a hierarchy of process control starting with open loop, where the operator is the controller. He makes manual adjustments to valves and other final control elements to keep the process at operating targets or within operating constraints. This represents the absence of automation. Next up the hierarchy there are feedback controllers that take the place of the operator automatically closing the loop, with PID being the most prevalent by far. This basic level of feedback control is inherently single loop in nature.

There is one measured variable that is controlled and one manipulated variable (usually a control valve) that is the process input. A control panel or DCS may have hundreds of single-input-single-output feedback control loops for the operator to manage. The next level up the hierarchy involves a branch. Up one path, there is supervisory control that is used to sequence the process or manage a batch process. That is not the realm of MPC, although MPC may be seen in batch and sequential processes.

The other branch includes multivariable regulatory control. One approach to multivariable control is advanced regulatory control in which single control loops may be cascaded, ratioed, or included as part of complex strategies with feed forward inputs to cancel measured disturbances and override controls to handle constraints. Special features in digital systems also make it easy to handle nonlinearity with characterization, create inferential calculations, and a host of other functions to improve control. Modified PID controllers such as Smith Predictor or “Error Squared” or other controller algorithms can be used to deal with deadtime, nonlinearity, and other challenges.

Occasionally you may see a feedback controller that is not PID per se, but uses something like fuzzy logic. A specific type of advanced control is model predictive control. This type of controller uses dynamic process models and is computationally intensive, compared to PID. But because it has process dynamic models and is projecting where the process will be in the future, it doesn’t have to execute as frequently as PID. In the early days, there were not the tools for process identification that are available today nor the computational power to execute the controls without a host computer. But like many things, the technology has improved and become more accessible to process plants.

Now DCS systems can execute MPC and have their own process identification tools. MPC is perhaps the best means for handling deadtime dominant processes, which tend to be slow due to the deadtime anyway, and which are the most difficult for feedback controllers. It is ideal for interactive processes because it can easily model and accommodate multivariable interactions. It is perhaps the best approach for constraint optimization at the controller level, because it won’t stop seeking a better solution once it hits the first constraint. It will continue to move toward a better position while honoring constraint limits until it uses up all of its degrees of freedom.

However, it is not without its limitations. It can be limited by model accuracy and by process nonlinearity. One common area of process nonlinearity is valve response. So while it is possible to use MPC to manipulate valves directly, it is usually better to have the MPC send a setpoint to a flow loop and let the flow loop manipulate the valve. I would make the same argument for cascade control in many processes, especially level control, where too often, performance is limited by the failure to cascade the level controller to a flow controller. Very fast processes (like flow loops that are easy to control with PID) put quite computational load on controllers executing MPC. While some embedded MPC controllers can execute at a high frequency, like once per second, this generally isn’t the best approach for high speed processes.

MPC has a feedback mechanism, which is usually a model correction factor. As noted in my previous response, there is always going to be some model mismatch and the feedback handles that. But the difference between MPC and PID is that PID controls the present while MPC controls the future. This gives the MPC control the chance to be as robust as PID control. But increasing robustness of either PID or MPC will lead to some degradation of performance. I would recommend in most cases that you don’t limit yourself to just one approach, be that PID or MPC. Use them both where they are the best choice. To do otherwise would be akin to taking your screw driver out of your tool box and limiting yourself to only your hammer.

You can connect and interact with Chowyang, Lou, and other process control specialists in the DeltaV and Ovation tracks of the Emerson Exchange 365 community. If you join us in Orlando for the Emerson Exchange conference, you can find them and many more experts too!

Related Posts:

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File: UMIQ lost communication to Universal Management Gateway Appliance

September 12, 2014, 2:41 pm
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File: Symbols Portal will Fail with errors on some Non English Languages IE browsers

September 12, 2014, 2:46 pm
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The solution is to set the Language of IE to English.    There are some Languages which prevent one from logging into the portal.     Some Languages will give an error when requesting symbols. 

This Tech note explains the problem and what the current workaround is.

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Forum Post: Corrosion, erosion or something else?

September 12, 2014, 10:05 pm
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We face problem with, one of the valve was installed in our plant. After two or three years, the valve body and trim corroded and need to be replaced, we replace it two times, but did not find exact reason to solve it. The valve specification as below:

Body size: 12” trim:8”

Material: monel

Service: sea water

Pressure:15 Bar

Trim type: anticavitation, cavitrol III   

body and cage photos            o                                                                                                                                                                                                                                                                                                                                                                                                                     

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Forum Post: AMS and Eaton c441 relay

September 13, 2014, 9:33 am
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We are running AMS version 12. when I look at our profibus network within device explorer, our Eaton c441 relays show up as unknown device. Does any one if the required files exist so that I can add the device type and have these relays show up properly in AMS?

Thanks

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Forum Post: RE: AMS Device Manager connection through T+H to Stahl RIO

September 12, 2014, 8:11 am
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Ian,  I was curious, what are you trying to accomplish?  Are you trying to get the HART devices to AMS or all  of your Profibus devices?

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Forum Post: RE: “ARC insights” on On-Off valve controllers

September 12, 2014, 10:01 am
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This article is now available in an easier to read HTML page format:

www.ceasiamag.com/.../10661

"how intelligent on-off valves, in conjunction with asset management software, can help reduce unnecessary valve inspection, speed up valve overhaul, and enable shorter turnarounds to be planned in plants."

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Forum Post: RE: Connect two Sun serial ports with Avocent Sun adapter

September 12, 2014, 11:29 am
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or is it saying pin 1 on the RJ45 is RTS, pin 2 is DTR, etc.?  in that case i would just use a straight-through cable, it seems....

i guess the ordering in the diagram is throwing me off but it was just presented in a way so the ASCII wires do not have to cross.....


so i guess pin 1 on the adapter goes to pin 1 on the X2250, pin 2 to pin 2, 3-3, and 4-4, but 5-8, 6-6, and then i get confused again because pin 7 on the adapter is DCD but there is no DCD on the X2250, and then finally pin 8 on the adapter goes to pin 7 on the X2250.  i guess i can put pin 7 on the adapter to pin 5 (GND) on the X2250?  thats the only pin left and apparently Sun doesn't use DCD so makes sense, i think.  guess i will try it pending any response and hope i dont cause an explosion ;)

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Forum Post: RE: Writing a Start Command to a DC1 Block?

September 12, 2014, 4:21 pm
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Matt,

Thank you very much for your Valuable time and input.  I already discussed with Customer regarding the TPXX and the reply is VFD itself has that functionality.

Customer have following concern on the faceplate display of MVS and CMT modules.

Scenario is as below.

Speed control Master module :  CMT type and the PV is  740 RPM (tag number HC- VS09) 

Slave is VFD : MVS type HS-09

If it is in CAS MVS module will get the Speed set point from master modules HC-VS09.

 If operator wants to set the Speed manually, then he can set the value from MVS faceplate by clicking the Speed Popup. 

By considering this I have set the ranges as below 

CMT Module : 

PID/PV - 0 -740 RPM

SP_HI_LIM : 740

OUT_SCALE : 0- 740 RPM

 In MVS  module

AO1/SP_HI_LIM : 740

AO1/PV_SCALE : 0-740 RPM.

 But when MVS (HS-09) is controlled by CMT HC-VS09 in CAS mode. Seeing different speed values in different places leads a bit confusion. 

Could you please guide me , is this ranges setting are proper? 

Please find the attachment from having the same configuration from Simulation system. 

Your guidance and your time is much helpful  here..

Thanks,

Manik

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Forum Post: RE: DeltaV on Windows 7 Enterprise

September 13, 2014, 12:12 am
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Maybe it was necessary to use Enterprise for 2-and 4-screen VIRTUAL operator stations, because Windows 7 Pro does not have true multimonitor support over RDP (en.wikipedia.org/.../Windows_7_editions).

Licensing is also different, that could also play a role. Anyway, it seems to be supported for virtual stations only. But I think technically you can install DeltaV. I vaguely remember trying to install 11.3.1 on Windows 7 Enterprise and it gave an error saying that this edition is not supported. I think version 12 would not have anything against it, even though apparently it won't be supported.

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Forum Post: RE: AMS and Eaton c441 relay

September 13, 2014, 2:10 pm
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The reason that AMS display the eaton device as unknown because AMS does have a device description(dd). You need to see request/ask if they have one available.
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Forum Post: Fan Less DSR Models

September 13, 2014, 2:11 pm
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What Avocent DSR models are fan less?

Thank you.

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Forum Post: RE: Corrosion, erosion or something else?

September 13, 2014, 7:02 pm
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Forum Post: Refinery Automates beyond the P&ID using Wireless Pervasive Sensing

September 14, 2014, 7:49 am
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If you are planning to visit the Emerson Exchange you may wish to attend the “Refinery Automates beyond the P&ID using Wireless Pervasive Sensing” (session ID 2-1762).

https://www.emersonexchangeregistration.org/2014/connect/sessionDetail.ww?SESSION_ID=1762

 If you have not yet decided to go Emerson Exchange, this workshop is just one of many good reasons to go.

 The Reliance Industries refinery complex in India needed visibility to improve reliability, energy efficiency, and to reduce HS&E risk, which requires new measurements. Wireless systems were commissioned in two refineries in October 2012 starting with monitoring on steam traps on medium and low pressure lines as well as flare monitoring on pressure relief valves. The reliability requirements were met and what started as a trial has since become permanent and is expanding with vibration measurements

 The plants faced challenges such as not knowing which of many possible hydrogen process lines is flaring thus making the root cause hard to identify. Plants had no visibility of which steam traps have failed, several of which are critical. A solution had to be deployed while the refineries are running as the process could not be stopped. Huge metal reformer furnaces block line of sight

 A second layer of automation for pervasive sensing of missing measurements beyond the P&ID using about 100 WirelessHART acoustic transmitters was deployed requiring no signal or power cables to be run. The non-intrusive sensors strap onto the outside of the pipe requiring no additional process penetrations. The data is integrated requiring no DCS I/O cards.

 Solution was deployed without stopping production achieving >> 99% reliability despite of huge obstacles. Greater visibility for maintenance, reliability, energy efficiency, and HS&E officers without visiting the field was achieved. Reliance will deploy more wireless devices, next eying vibration transmitters.

 

Here’s a letter to help you seek approval from your supervisor to attend this important event:

http://www.emersonexchange.org/americas/wp-content/uploads/sites/2/2014/05/Justification-Letter-Emerson-Exchange-2014.docx

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Forum Post: RE: Beyond the control room

September 14, 2014, 7:59 am
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The HTML version of the "beyond the control room" article about the data which is sent not to the operators at the DCS console in the control room, but about the data for improving reliability, maintenance productivity, energy efficiency, and reducing HS&E risk - data sent to the asset management system and plant historian for display to maintenance and reliability engineers, energy managers, and HS&E officers is now available:

www.ceasiamag.com/.../10658

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Forum Post: RE: DeltaV on Windows 7 Enterprise

September 14, 2014, 4:33 pm
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DeltaV will still not install on a Windows 7 Enterprise OS version in v12.3 or 12.3.1 unless it is a virtual workstation.  In addition we only support installation on our Windows Embedded licensed computers and this in Windows 7 professional. And yes we support Enterprise on virtual workstations only to get the multi-monitor support.

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Blog Post: 에머슨 그룹, 2014 년도 3/4 분기 실적 결과 보고

September 14, 2014, 5:45 pm
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에머슨 그룹, 2014 년도 3/4 분기 실적 결과 보고 전체 매출 63억 달러로 소폭 감소, 기초 매출(underlying sales: 인수, 처분 사업, 매각 대기 중 사업, 중단 대상 브랜드 및 상표를 제외한 매출 내용) 3% 증가 총 이익률(GPM) 130 BP 확대로, 강력한 수익성 향상 제시 1.03 달러의 주당 순이익 6% 상승, 전년도 처리 비용 제외 역대 최대 수주 잔고, 당해 초부터 현재까지 20% 이상 증가, 매각 내역 제외 에머슨 그룹은 2014년 6월 30일 자로 마감된 3사분기 매출액이 Artesyn 사업 부문 매각으로 인한 5% 감소, 인수를 통한 1% 추가와 더불어 총 1% 하락을 기록했다고 발표했습니다. 해당 분기 시장과 지역에 따라 고르.......
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Forum Post: RE: Writing a Start Command to a DC1 Block?

September 15, 2014, 12:19 am
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HI,

having hard time understanding the idea behind everything.. but that´s normal for me Yes

Why do you have to change manipulate the anaalog output directly?

Normally the control schemes I have seen you do not have to do that, you just simply change the PID control to manual and change the value from there...?

You could add a control to the pump, when it starts the PID goes into CAS, Auto or what ever and you set somekind of setpoint (if you want to) to the controller.

You can do the same the other way around, when the pump stops you put the PID in Man mode and setpoint or tracking value and so on to 0.

Regrading the ranges, you have to check the VFD settings, it will run something at 100% speed-input...

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