Looking forward to the new software .... Any news on the release date ?
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Forum Post: RE: New MHM software platform
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Forum Post: CSI2140 battery
Just out of interest I had issues with a battery not showing all green while charging . Disconnecting the battery from the attached circuit and reconnecting seems to have resolved the problem . The battery returned to nomal operation .
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Blog Post: Magnetrol Model R96 Rev 1 DeltaV and AMS Interoperability Tests
In Emerson’s continuing commitment to open and interoperable standards, the Magnetrol Model R96 Rev 1 has passed the rigorous and comprehensive testing of the DeltaV Stress Test labs. Using the Device Installation Kits for Emerson Products website at http://www2.emersonprocess.com/en-US/documentation/deviceinstallkits/Pages/deviceinstallkitsearch.aspx , these fieldbus device files are now available for use.
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Forum Post: CSI 2130 Relative Phase Convention
Please could someone clarify for me what convention the CSI 2130 uses for relative phase. Is it phase lag or lead and what's the minus all about. -90 for example means the same as 270?? Thanks
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Blog Post: The Most Disturbing Disturbances are Self-Inflicted
The post, The Most Disturbing Disturbances are Self-Inflicted , first appeared on ControlGlobal.com's Control Talk blog. The most disturbing disturbances, the ones that are frequent, fast and furious (FFF), are self-inflicted either in the design, installation, maintenance or operation of the process control system. The good news is that through better application of advances in technologies and the better education of everyone responsible for the implementation, maintenance, operation and technical support of the plant's systems, we can eliminate most of these disturbances. This is an opportunity for the synergy between modeling and control to identify, prototype, test, install and continuously improve solutions not forgetting that training plant people is the key for long term effectiveness. We can revitalize the automation profession by finding and implementing process control improvements that goes beyond a simple migration project. Keep in mind as we go through the sources of these most disturbing disturbances that this dialog is not meant as criticism. It is intended to open minds and provide insights as to opportunities. Disturbances most often originate from the Advanced Process Control (APC), Basic Process Control Systems (BPCS), Sequential Operations, Safety Instrumented Systems (SIS), maintenance and operators. The disturbances from outside influences (e.g., raw materials and weather) and internally (fouling of surfaces and deactivation of catalysts) tend to be slower, smaller and less often. The disturbances originating from people, valves, and PID controllers tend to be FFF. Cyclic disturbances are the epitome of frequent disturbances. Cyclic disturbances pose additional problems in terms of the disturbance frequency being much faster than a loop’s natural frequency becoming effectively noise or even worse, the disturbance frequency being around the loop frequency causing resonance. Cyclic disturbances tend to originate from PID controllers due to poor tuning or poor choice of structure, throttle valves due to backlash, stiction, and positive feedback from recycle steams, on-off valves due to sequential operations, regeneration of catalysts, defrosting of crystal coated surfaces and cleaning of fouled surfaces. Cycles can appear that coincide with shift changes due to operators moving the process to their preferential operating points. SIS actions, shutdown and startup are extremely disruptive and can appear to be cyclic if there are many parallel unit operations that are going up and down. If you go a little deeper, you realize nearly all the disturbances begin with valve movement and speed changes since these are ultimately what are manipulated to affect the process. If the valve positions and speeds were not changed, the process would not be at the right operating conditions and possibly unsafe but there would be few cyclic disturbances. We should not lose sight of this fundamental when trying to track down and eliminate a disturbance. We should always seek to find out what valve moved first and what happens if the valve does not move (loop momentarily in manual). Finally, we should ask does that valve need to move and can the movement be slower? For a short term disturbance whose amplitude is not going to cause a trip or damage equipment, the best correction may be no correction. Any feedback correction may be late creating a second disturbance. We will focus in this blog on the BPCS and Sequential Operations since they are the primary source of the above cyclic disturbances. Well-designed Model Predictive Control (MPC) takes into account interactions and dynamics and tends to move the process slowly through proper adjustment of penalty on move (move suppression) and penalty on error. However, if the MPC in the process of pushing the process closer to constraints causes an activation of the SIS, the consequences are severe. MPC by nature is pushing the limits so there needs to be caution exercised. Valve Position Control (VPC) also pushes the limits with the added risk of a VPC not providing decoupling and the PID being tuned improperly. We will address minimizing the disruption by a VPC as part of the discussion of PID control. The overuse of integral action is the primary culprit since it is has no sense of direction and is never satisfied continually moving the process. Integral action is often used in lieu of proportional action. Before we even go any further, let’s make sure that any concern about excessively abrupt changes by proportional action for setpoint changes is alleviated by the use of PID options such as structure or a setpoint filter as noted in the ISA Mentor Program 1/26/2106 post “ Equivalent Methods to Eliminate proportional Step and Derivative Kick ”. For all types of changes, external reset feedback along with up or down rate limits on setpoints can provide directional move suppression, even more flexible than what we get from an MPC. This move suppression prevents upsets to other loops from more proportional action, whether a speed or valve is being manipulated. Simply turning on external reset feedback suspends integral action that would cause the manipulated loop, valve or speed setpoint to change faster than the loop, compressor, fan, pump or valve can respond. This eliminates the confusing burst of oscillations for large disturbances or setpoint changes that occurs from violation of the cascade rule. External reset feedback eliminates the limit cycle from valves that have excessive backlash, a slow response of a large actuator or an insensitive poor positioner design. External reset feedback also enables a VPC to more effectively do its job to give a gradual optimization but a fast recovery for upsets. External reset feedback is also the key feature of an enhanced PID that suppresses oscillations from the excessive dead time of analyzers as discussed in the 7/6/2015 Control Talk Blog “ Batch and Continuous Control with At-Line and Offline Analyzers Tips ”. I could go on and on about all the benefits I have found. Simply turning on external reset feedback and making sure the feedback signal is fast and representative of the response of what is manipulated can prevent oscillations. The PID gain can be increased eliminating the slow oscillations from too low of a PID gain in counterintuitive situations where oscillations get worse as we decrease the PID gain. We are taught that a high PID gain causes oscillations not realizing there many important situations where too low of a PID gain causes even more disruptive oscillations because the amplitude is larger and the cycling is perpetual. We have the counterintuitive situation where for composition, gas pressure, level, pH and temperature control loops on vessels and columns, we have oscillations that get worse as we decrease the PID gain. The process response in these loops is near-integrating, true integrating or runaway. Another common non-intuitive situation is where the limit cycle from backlash and stiction in these processes is reduced by increasing the PID gain. In self-regulating processes, external reset can stop an oscillation from stiction. The offset can be corrected by a setpoint change from an upper loop or the operator. The oscillations from insensitive positioners (e.g., most single stage and spool positioners from the last century) and from the slow response of large actuators (aggravated by low bleed positioners) can be eliminated in most cases by increasing the PID gain after turning on external reset feedback. Manual actions are abrupt, subjective, non-repeatable and usually late and are guesses at best. All manual actions by operators including those during startup, transitions, maintenance activities and abnormal operations should be automated preferably by the use of PID control. Feedforward control, principally ratio control, should be used to keep the process unit operations working together in unison. The scheduled addition of batch feed, reagent, substrate, air and utility flows, should be made more continuous by ratio control and by fed batch control of composition, dissolved oxygen, pH or temperature. The effect of batch operations on downstream equipment should be moderated by intervening tank volumes whose level control is tuned for maximum absorption of flow variability being careful the counterintuitive situation is not created by too small of a PID gain and reset time. The product of the PID gain and reset time should be larger than twice the inverse of integrating process gain. This can be assured by lambda tuning with the arrest time set to prevent the maximum rate of change of level from activating a low or high level alarm. Turning batch, manual, discrete, and sequential operations over to a PID loop intelligent options and tuning with move suppression provides better control and smoother more repeatable manipulation of flows leading to less FFF and better recognition and attainment of process control improvement. I have run out time here and I suspect we are bordering on overload , so let’s simply say that mitigating and even eliminating the FFF disturbances comes down to slowing down the movement of on-off valves for sequences and of throttle valves and speed setpoints in loops by the use of move suppression and external reset feedback. The stroking of on-off valves can be slowed down by needle valves in the actuator air lines but a more effective solution is a smart positioner to provide precise intelligent adjustment and monitoring of the stroking time. The installed flow characteristic curve of these valves can be used to set the valve signal rate of change to slow down and speed up on the steep and flat part of the curve, respectively to provide a more constant less disruptive rate of change of flow. For a concise presentation of the concepts and details on PID control see my ISA book Good Tuning: A Pocket Guide, 4th Edition. If you are up for a more comprehensive view, see my Momentum Press book Tuning and Control Loop Performance - 4th Edition.
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Blog Post: 오래된, 노후한 발전소의 현대화를 위한 과제 – 1부
어느덧 국내에서 발전소가 증설되기 시작한지 40여년이 지나면서, 발전소 노후화에 대한 우려가 점차 커지고 있습니다. 과거에 비해 여유로운 전력 공급이 가능해지기는 했지만 여전히 가동 중단에 대한 부담감은 크기만 합니다. 에머슨 프로세스 매니지먼트는 그간 수 많은 플랜트 마이그레이션 및 현대화 프로젝트를 수행하면서 다양한 경험을 쌓아왔는데요. 본 포스팅에서는 현 플랜트 업계의 고민이라 볼 수 있는 노후한 발전소를 현대화 함에 있어, 고려하고 타개해야 할 어려움들에 대해 논의해보려고 합니다. 과거에 비해 현재의 기술은 얼마나 발전해 있는지, 과거의 시설에 현재의 기술을 도입하는데는 무리가 없는지, 에머슨이 직접 수.......
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Blog Post: Krohne MFC400 Rev 1 DDRev 3 DeltaV and AMS Interoperability Test
In Emerson’s continuing commitment to open and interoperable standards, the Krohne MFC400 Rev 1 DDRev 3 has passed the rigorous and comprehensive testing of the DeltaV Stress Test labs. Using the Device Installation Kits for Emerson Products website at http://www2.emersonprocess.com/en-US/documentation/deviceinstallkits/Pages/deviceinstallkitsearch.aspx , these fieldbus device files are now available for use.
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Blog Post: Toto, I’ve a Feeling We’re Not in Kansas Anymore
When I was little, Wizard of Oz was one of my favorite movies and by far the one that I watched the most. Though I’m a little disappointed in myself that I had that classic movie quote wrong in my head for so long but Google says that’s common so I must be in good company. It’s such a magical moment in that movie when Dorothy takes her first step from the black and white world of Kansas into the beautiful, colorful Land of Oz. It’s such a dramatic change and rather amazing to a little viewer. I’ve been thinking a lot lately on dramatic changes like this. This past weekend, my husband and I went to see my 103 year old grandmother and introduce her to our 8 month old son. It was a beautiful moment to see her reach out and hold his hand for a while and great to bring her some joy in what little time she has left. And can we just take a minute to think about this: 103 years old! How the world has changed in that time and how dramatically for women, including women in STEM. My Grandma Polly at 102 with the baby blanket that she made for my son My grandmother was born on January 3 rd , 1913. She lived through both World Wars, the Great Depression, the moon landing, and too many technological innovations to count. Her last phone was a cell phone which would have been an absurd concept when she was a child. For women, the path was quite limited when she grew up. Women didn’t even have the right to vote until she was 6 years old. My grandmother was only allowed an eight grade education as she was pulled from school to help raise her younger siblings. She was the oldest child and the only girl with seven younger brothers. Good grief, that’s a lot of testosterone! As a counter, my grandmother ended up having three girls. Things were a little different in the world when my mother was born though some viewpoints hadn’t changed too much. My grandfather refused to allow my mom to go to law school because why would you pay for law school when you’ll end up married and home with kids. I was quite shocked when she first told me that story. This didn’t quite mesh with my Type A, “I can do anything” mom. As a result, she stayed in town and got a music degree, playing in the typically male dominant percussion section no less. She ended up going in teaching, specifically English (hopefully my grammar is correct in this blog post!) and later into district level roles around career education. Though it seems a surprise that I ended up being the only engineer in my entire family and extended family, looking back it probably shouldn’t have been that surprising. With my mom being focused on career education, she was very aware of the variety of roles and opportunities out there. Since I was good at math and science, of course she was going to help me find possibilities in that arena. Add in a fantastic high school chemistry teacher plus an awesome and incredibly patient pre-calculus and AP calculus teacher (I missed a lot of class due to golf and she was always willing to help me get caught up), chemical engineering was not that far away. Many of the studies out there show that girls get involved in STEM careers because someone along the way pointed out that option to them. Often that role model in their life directed them a STEM role that the girl didn’t even know existed such as engineering for me. There are lots of options out there for both men and women to get involved and teach kids about the wide variety of STEM careers out there. One of my personal favorites is the program for Women in Science and Engineering at Iowa State University. I’ve been a longtime advisory board member for the program which reaches 9000 K-12 students ever year. They also do a tremendous amount of undergraduate support and these students that I meet through their events always amaze me. If you’re not already doing so, I encourage you to get involved in outreach or mentoring and help bring someone into a Technicolor world of the career possibilities out there, especially those in STEM. Someday soon, I know that my grandmother will be traveling somewhere over the rainbow and she’ll be at peace. The world changed a lot while she was here and I hope that we will continue to see positive change related to women during my lifetime.
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Blog Post: Innovations in Increasing Project Successes
Emerson’s innovations in process control magazine provides insights into many of the latest technology and service innovations occurring. The latest edition opens with an operating training simulator (OTS) successful implementation at Iberian Lube Base Oils Company (ILBOC) in Cartagena, Spain. The article highlights some of the key benefits: Emerson’s OTS provided ILBOC with a number of benefits including reduced operating costs, due to the ability to identify potential issues during initial start-up, shutdown and normal operations. Having well-trained operators reduced plant start-up and shutdown time and the production of off-specification product. Energy consumption is a significant issue at process plants. The experience and understanding of the process gained through the training is enabling operators to identify potential problems such as loss of power failure, or cooling water, that would reduce the energy efficiency of the plant. Roel Van Doren Emerson Process Management Europe president Roel Van Doren then described the issue the process manufacturing and production industries face in executing large capital projects: …65% of projects greater than $1bn fail, meaning that companies exceed their budgets by more than 25% or miss their schedules by more than 50%. He describes how Project Certainty helps to address this challenge. Project Certainty is: …a transformational approach to project execution, which will cut costs, reduce complexity and significantly improve the ability to accommodate changes throughout the lifecycle of the project. In practice this means that project performance will improve by eliminating unnecessary work and materials by automating the steps in the process and using standardised technologies. Other articles in the magazine feature: Emerson Process Management group vice president Jim Nyquist on Increasing Project Certainty Vice president projects and services John Nita on Adopting Main Automation Contractor services earlier Director of global industry consulting Chris Hamlin on Securing the return on your investment Director of strategic services Europe Michel Da Silva on Distributed project engineering Dynamic simulation and process optimisation business manager Ronnie Bains on Dynamic simulation supports successful startups Other short articles including configure-to-order cabinets, smart commissioning and specification process streamlining. Check out these articles and join these folks April 12-14 at the Emerson Exchange conference in Brussels . Related Posts Building a Problem Solving Reputation on Three Pillars Developing High-Level Operator Skills Prior to Startup Improving Data Management, Analytics and Flexibility in Life Sciences Remote Automation Solutions Roadmap Planning and Integrating Reliability for Top Performance Emerson Secure Remote Access Strengthens Security for Customers Remotely Accessing their Control Systems The post Innovations in Increasing Project Successes appeared first on the Emerson Process Experts blog.
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Forum Post: DMDS Detection
Hi, I am looking into a Gas Detector that is capable of detecting DMDS (Dimethyl Disulfide) with an alarm limit of .5PPM. Any suggestions? FYI, the application is for a Sulfur Injection skid. I have contacted several gas detection vendors and the only recommendation I seem to get is an H2S detector. Thanks in Advance! Brandon
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Blog Post: 한국 에머슨, 가로세로 낱말 퀴즈 당첨자 발표
참여해주신 여러분 모두 감사드리고요.기다리실까봐, 하루 먼저 발표했습니다-당첨되신 분들은 잊지 말고 쪽지 보내주세요!
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Forum Post: DeltaV Hotfix or compatibility issue between M-Series and S-Series Controllers
Current Situation: I have a site that has both M-Series and S-Series controllers working together to support a DeltaV system currently running. We installed a Charm panel (of course S-Series Controllers/CIOCs) and did not know if I need to implement another hotfix or flash the controllers/CIOCs to migrate them into the system? Please let me know if there is anymore information you need. Thanks
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Forum Post: RE: DeltaV Hotfix or compatibility issue between M-Series and S-Series Controllers
There are separate controller firmwares for SQ and SX controller that differ form the MD/MX/MQ/SD+ firmwares. We just upgraded to V13 and are on CTRL_P4 and CTRL_Q6 firmwares. What version of DeltaV are you on?
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Forum Post: RE: DeltaV Hotfix or compatibility issue between M-Series and S-Series Controllers
This is V11.3.1
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Forum Post: RE: DeltaV Hotfix or compatibility issue between M-Series and S-Series Controllers
You should flash the controller and CIOCs to match your current DeltaV hotfix level. To do this run the DeltaV Controller Upgrade Utility (Start > DeltaV > Installation > Controller Upgrade Utility) it will automatically bring you equipment to the correct flash, refer to KBA NA-0800-0048 for more information on preforming this upgrade. Before you do this you probably want to bring you DeltaV system to the latest hotfixs as there are some recent hot fixes that may apply to your configuration, refer to KBA NK-1100-1062 for the latest DeltaV 11.3.1 Hotfixes and what they fix.
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Forum Post: RE: DMDS Detection
Brandon, Solid state gas detectors can be used to detect dimethyl disulfide in the parts per million. To my knowledge, they don’t have the sensitivity to support alarm setting at 0.5 ppm. A typical range for a solid state sensor configured for dimethyl sulfide is 0 – 10 ppm. Irvine, CA-based International Sensor Technology offers a solid state gas detector for dimethyl disulfide. You may call or write IST to learn more about the limits of applicability of its product. Besides solid state sensors, another technology available to detect dimethyl disulfide is gas detector tubes. Nonetheless, these tubes are portable, single use devices, unsuitable for continuous gas monitoring. Dräger (Lübeck, Germany) makes a model for DMDS detection.
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Forum Post: RE: DMDS Detection
Thank you Scott!
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Blog Post: Optimizing Operations with Correct O2 Probe Placement in Coal-Fired Stoker Boilers
Hi and welcome to Analytic Expert. I’m Neil Widmer. Recently on our Emerson Exchange 365 site, I’ve fielded some interesting questions from customers and I thought the answers could be useful to you. So here are some application solutions that may save you money and improve your boiler operations. An engineer from JANSEN, a combustion and boiler engineering service company in the Western U.S., recently asked a question regarding a Rosemount O 2 probe application. Their client operates several stoker coal-fired boilers. On each boiler they use a single 6888 O 2 probe located downstream of the ID fan for fuel-air control. The service company encouraged the client to move the probe closer to the furnace due to air infiltration in the back passes. The concern is that air in-leakage can lead to inaccurate furnace excess oxygen measurement and boiler performance issues. The boiler operator said they tried the probes in locations closer to the furnace, but it “fouled” within months and they feel a clean stream downstream of the ID fan is a better option. The engineering service company asked if we are aware of conditions in a stoker coal fired application having a negative impact on the functionality of an oxygen instrument. Rosemount 6888 O2 Transmitter Probe and 6888Xi Local Operator Interface I responded that Rosemount agrees with the service company’s recommendation to move the probe to reduce boiler performance issues. In our experience, the probe should work very well upstream of the ID fan. Assuming that the fuel is typical bituminous stoker coal, there is no reason that our probe should not work perfectly when installed closer to the combustion process. Our probe can be located close to the boiler furnace exit and is often installed immediately downstream of the economizer convective pass. We have dozens of our probes in these exact stoker applications and they work very well. For most of these stoker applications, the snubber diffuser works fine without ash fouling issues. If the flue gas chemistry plugs the snubber diffuser too quickly, then a ceramic or Hastelloy diffuser would be another option. Click HERE to learn more about the different diffuser options. I also mentioned that our latest model 6888A O 2 system has a plugged diffuser diagnostic option which could help with predictive maintenance. Another question came in asking about particulate or erosion due to ash content as a result of moving the probe closer to the point of combustion. There is more coal fly ash upstream and the fly ash will abrade the stainless steel probe over time. Rosemount offers two options to increase probe life: an abrasion resistant probe, or an abrasive shield which covers and protects the probe. Customers can also provide their own abrasion protection. The cost of abrasion protection and replacing probes is typically minor compared to damaging the boiler from operating at improper air-fuel ratios. Therefore we would not recommend installing the probes downstream of the ID fan to reduce abrasion. An accurate measurement of furnace exhaust excess O 2 level is critical to understanding the furnace air-fuel ratio. Some of the potential boiler losses associated with operating the furnace too fuel-rich include delayed heat release, high furnace exit gas temperatures (FEGT), and fuel-rich corrosive gases which can cause generator tubes erosion, corrosion, and excessive fouling and slagging. These impacts can result in lost availability due to tube leaks or slag and clinker build-up, lower efficiency, and increased emissions like opacity, CO, and hazardous air pollutants (HAPs). On the other hand operating too fuel-lean (i.e., with excessive combustion air) reduces efficiency and can increase emissions of oxides of nitrogen (NO x ) and carry-over of particulate fly ash, as well as increase fan auxiliary power consumption and air pollution control device throughput, and last but not least, it can limit boiler output. One advantage of stoker boilers is that the coal is relatively large; typically 50% between ¼” and 2” mesh size. The coal burns on the grate and results in lower ash carry-over than pulverized coal-fired boilers where coal is predominantly burned in suspension. We have thousands of probes and decades of experience in pulverized coal boiler applications too. For these applications, the Hastelloy or ceramic diffuser is always recommended to increase time between filter maintenance. 6888 O 2 probes with these diffuser options have proven to be highly accurate and reliable in these harsh gas environments. Ultimately, the value of an accurate furnace O 2 measurement far outweighs the lifetime cost of probe maintenance, repair, and operation. Now it’s your turn. Do you have any questions on boiler operation I can help with?
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Blog Post: Overcoming Pharmaceutical Continuous Manufacturing Challenges
Why is there a movement in the pharmaceutical and biotech manufacturing industries to consider continuous manufacturing over traditional batch manufacturing processes? A 2012 U.S. Food & Drug Administration presentation, FDA Perspective on Continuous Manufacturing , captured some of the reasons why. Author Dr. Sharmista Chatterjee listed some advantages: Integrated processing with fewer steps No manual handling, increased safety Shorter processing times Increased efficiency Smaller equipment and facilities More flexible operation Reduced inventory Lower capital costs, less work-in-progress materials Smaller ecological footprint On-line monitoring and control for increased product quality assurance in real-time Amenable to Real Time Release Testing approaches Consistent quality Together, these open of the possibility to significantly reduce costs and improve quality. In a Pharmaceutical Processing magazine article, Continuous Progress in Continuous Manufacturing , Emerson’s Jonathan Lustri and co-authors Doug Hausner with C-SOPS and Paul Brodbeck with QbD Process Technologies describe process design, measurement, and control for enabling continuous processing. While the cost benefits are clear, the challenges to implement are as well. These challenges include: …process design, measurement, material traceability, and control. To address these challenges: Manufacturers, suppliers, and research institutions are collaborating to solve these challenges at projects across the globe, including the Engineering Research Center for Structured Organic Particulate Systems (C-SOPS) [hyperlink added], based at Rutgers, the State University of New Jersey. A large question is how to ensure quality and regulatory compliance when there are no breakpoints as batch production features. The answer: …is to monitor critical process parameters (CPP) and critical quality attributes (CQA) at a frequency that allows for sufficient monitoring of the process and product quality. In addition, the real-time application of Process Analytical Technology (PAT) for continuous processes is essential to quality control and must be integrated into the process control strategies. Another question for continuous processes is material traceability, which is critical for regulatory compliance, safety and efficacy. Rather than physically discrete batches, traceability in continuous processes: …relies on statistical probabilities. … It may only be possible to predict, for example, that there is a 90 percent chance that the material in a particular tablet came from Lot #1, a 9 percent chance that it came for Lot #2, and a 0.9 percent chance it came from Lot #3. The probability distribution depends on a concept called Residence Time Distribution (RTD)—a function that describes the amount of time a particle could spend inside the vessel. C-SOPS: …has developed models for unit operations to predict the RTDs under different process situations. These models have the advantage of: …being able to predict RTDs dynamically based on process parameters including flow rate, mixing speeds, and density. If a PAT application using an NIR analyzer to predict a CPP after the blender is out of specification, the RTD models can be used to predict when and which tablets need to be rejected. By integrating these models into the process control system, traceability is synchronized in real-time. Read the article for examples of how advanced controls for feedforward and feedback controls have been developed and implemented by C-SOPS in applications such as API concentration and how these RTD models help optimize plant design and production unit operations. You can connect and interact with other pharmaceutical and biotech manufacturing experts in the Life Sciences group in the Emerson Exchange 365 community. Related Posts What Do You Do for a Living? Improving Technology Transfer by Earlier Adoption of Standards and Software Platforms Continuous Manufacturing for Solid Dose Form Pharmaceuticals Advancing Process Intelligence and Analytics in Life Sciences Managing Asset Performance and Collaborating in the Life Science Industry Collaborating for End-to-End Supply Chain Improvements The post Overcoming Pharmaceutical Continuous Manufacturing Challenges appeared first on the Emerson Process Experts blog.
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Forum Post: RE: CSI 2130 Relative Phase Convention
John, the CSI 2130 uses the phase lag methodology. The range that is used is -180 to 180 degrees. In your example, -90 degrees would be equivalent to 270 degrees.
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