You should probably contact Mynah for help on this. https://www.mynah.com/support
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Forum Post: RE: Lost VIM configuration file(VIO) and completely forgot VIM IP address
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Blog Post: Emerson Exchange 2016 Abstract Preview: Chemical Injection Costs
Over the next couple of months we will be highlighting a few Emerson Exchange abstracts to help you decide what workshops and sessions you want to attend. One of the first abstracts we will cover is from Emerson’s Tim Drost and Laura Schafer. In their presentation, Reduce Chemical Injection Costs with Confidence in your Measurement , they will provide a critical examination of a chemical injection system and practices that may yield tremendous OPEX savings for an operator. Chemicals are a necessary expense – without preventive chemicals, scales and waxes could plug tubing, shutdown facilities, hydrates could block production, costing up to $1M/day in shut-in production as its dissociated. Without corrosion inhibitor, complete loss of well or infrastructure could occur over time. With such severe consequences, producers consistently inject more than the recommended quantity of chemical. A sampling of producers interviewed showed that chemical is typically over-injected by ~20%…… and the annual cost of over injection for a single chemical on a single platform run at 20% additional could be as high as $400,000! By improving chemical injection system reliability, operators can drop that excess spend without the risk of under-injection, immediately improving the bottom line. With Micro Motion technology, one major oil and gas operator reduced chemical spend over 40% with a more reliable chemical injection measurement system. To learn more about this case study and how this can help in your chemical injection application, make sure to register for Emerson Exchange 2016 . If you register before August 31st you can save $400! If you can’t make the conference, make sure to interact with flow measurement experts in the comment section below, or the Emerson Exchange 365 community. Related Stories Emerson Exchange 2016: The Power of PMO!!!
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Forum Post: RE: Lost VIM configuration file(VIO) and completely forgot VIM IP address
You should be able to determine the IP address with standard tools in your Windows PC. Connect your PC to the network for your VIM. From the command prompt run the command "arp -a". You should get a list of active addresses on the segment. You can also try "netstat -b" to get a list of ports and processes.
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Forum Post: Shattering the Glass Ceiling - Why this year's momentous election gives us ALL a reason to be inspired & invigorated
Women have made US history, once again. No matter what your political leanings it's time to stop, let it soak in and celebrate. For more inspiration, check out this Huff post article where women of all ages & from all walks of life, recall their own breakthroughs: Women Watching Clinton Make History Recall The Moment Their Own Glass Ceilings Shattered
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Forum Post: Emerson Exchange America’s 2016 Event – Recommended Modernization and Migration Related Sessions to Attend
Have you been wondering what Modernization and Migration related sessions our team recommends that you should attend at the upcoming 2016 America’s Emerson Exchange event in in Austin, TX (October 24 th - 28 th )? Well, we’ve made it easy for you, here’s a table of the workshops, short courses, Meet the Experts, and Technology Roadmap sessions that we are recommending be attended by anyone interested in DCS modernization and migration. These sessions can be easily added to your Personal Scheduler once it’s released.
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Forum Post: Emerson Exchange America’s 2016 Event – Recommended Modernization and Migration Related Sessions to Attend
Have you been wondering what Modernization and Migration related sessions our team recommends that you should attend at the upcoming 2016 America’s Emerson Exchange event in in Austin, TX (October 24 th - 28 th )? Well, we’ve made it easy for you, here’s a table of the workshops, short courses, Meet the Experts, and Technology Roadmap sessions that we are recommending be attended by anyone interested in DCS modernization and migration. These sessions can be easily added to your Personal Scheduler once it’s released. Please DOUBLE CLICK on the TABLE below for larger viewing.
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Forum Post: RE: Emerson Exchange America’s 2016 Event – Recommended Modernization and Migration Related Sessions to Attend
Hi Scott, This looks very interesting especially the mature/legacy system discussions . Where can we find further details on attending? We are a UK based company who specialize in legacy systems support. We design & manufacture the SCSIFLASH drive which is a plug and play Solid State SCSI legacy SCSI drive which provides further storage future-proofing for critical legacy computer applications that otherwise have plenty of life left in them - systems such as RS3, DCS, ABB, Emerson, Honeywell TDC3000 and MXOpen are all supported. We can replace both Tape & Disk. The SCSI-Flash drive provides an up-to-date, high-reliability, solid-state and low-cost solution to the problem its now also Network supported so you can back-up / restore directly from the disk, floppy or tape drive. For those who have these related issues I'd be happy to met you at the event to discuss your legacy problems. Look forward to hearing form you. Many thanks James Hilken - See www.cf2scsi.com for further details.
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Forum Post: RE: Lost VIM configuration file(VIO) and completely forgot VIM IP address
Get the latest version of VIMNet Explorer. There is a procedure called out in the help file for "Recover VIM Configuration." I would use fairchdm's suggestion on discovering the IP address of the VIM so that you can configure you laptop for the network. Once that is done, use the recovery procedure.
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Blog Post: 천연가스 산업-각 가스 배급망에 맞는 유량계 선택법
천연가스 산업-각 가스 배급망에 맞는 유량계 선택법 다양한 종류의 가스 배급망에서는 차압(DP), 초음파, 코리올리스(Coriolis) 유량계와 같이 각기 다른 계기를 필요로 합니다. Dan Hackett, Emerson Process Management 지난 몇 년간, 수압 파쇄법(프래킹, fracking)을 통한 미국 내 천연가스의 생산이 크게 증가했습니다. 연방 에너지 정보청(EIA)은 건성천연가스 출하량이 2000년 1조ft3에서 2010년 5조ft3 로 증가했다고 밝혔으며, 2035년에는 셰일가스가 미국 가스 생산량의 거의 절반을 차지할 것으로 예상하고 있습니다(그림 1 참조). 유량 측정은 공급망의 모든 부분에서 중요한 역할을 맡고 있습니다. 재정적 및 상거래용 측정은 두 가.......
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Forum Post: RE: Speed of Communication between I/O Card and the control module
Hi Mr. MC Chow, Thanks for your answer Sir. please correct me if i'm wrong, so DeltV ACN provided communication between Workstation and Controller. then if I want to know, how fast exactly speed or data transfer between controller and IO module, is it same with DeltaV ACN support Sir. Thanks
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Forum Post: MX Controller Cross Communications
Hi all, I wanted to ask about what to check, look out for and what the limiting factors are when implementing control strategies in separate controllers when the control strategies have a dependence on each other. Looking in Diagnostics, both controllers are MX and each have unsolicited parameters sent of 440 and 750, unsolicited parameters received of 26 and 52. One has a free processor time of 26 and the other 27. Given these values should I be considering doing the configuration in one controller alone, are there other considerations to take into account? Thanks,
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Blog Post: Flexible Operations for Changing Ethane Market Conditions
In an RBN Energy blog post, The Yellow Rose Of Texas: Battle Of Texas Ethane Begins As Cargo #1 Departs Morgan’s Point , it not only gives a great history lesson on the origins of the Yellow Rose of Texas, but also the market dynamics for ethane production. It highlights the challenge that shale gas production has created for midstream producers: That’s because the Shale Revolution led to huge increases in wet natural gas production and, with that, far more ethane than the U.S. petrochemical market was prepared to consume. That, in turn, resulted in massive ethane “rejection” – or leaving ethane in the gas stream and selling ethane at gas prices rather than selling it as a “purity” product for use as a cracker feedstock… I caught up with Emerson’s Lou Heavner on the control challenge in switching between ethane recovery and ethane rejection based on market prices for ethane. Lou noted that at the heart of the gas plant is the cryogenic turboexpander (TE) process and de-methanizer . A gas plant is a series of distillation column separation processes. The first column, the de-methanizer removes methane (C1) out of the top of and everything else—ethane (C2), propane (C3), butane (C4), etc. the natural gas liquids (NGLs)—out of the bottom. As with virtually any distillation process, there are quality limits on both the column overhead and bottom purities. Typically, the overhead product (residue gas) has a specification for BTU content or Wobbe index . There may be economically based specifications for C3 or other quality measures. The bottom specifications are typically C1 and C1/C2 ratio. The relative value of the overhead (distillate) product vs the bottom product sets the targets. When ethane is more valuable than methane, the separation process runs in ethane recovery mode . Its recovery is maximized by minimizing the amount of ethane that leaves the top of the de-methanizer. This is usually defined as a BTU lower limit on the residue (sales) gas, also known as methane, leaving the top. On the other side, when ethane prices approach methane prices, the separation process runs in ethane rejection mode . The control objective is to allow ethane to slip out the top of the de-methanizer, which reduces the amount of energy required to purify the residue gas stream and also unloads the next column, the de-ethanizer, if the gas plant has one. This is accomplished by maximizing the BTU content of the sales gas subject to a propane constraint, since propane and higher hydrocarbons may also slip into the residue gas stream. Since propane is always more valuable than methane, the objective is to keep propane slip to a minimum. Lou noted that there are two controlling specifications at the bottom of the de-methanizer—methane in the bottom and methane/ethane ratio in the bottom, which are always maximized to the spec limits. These objectives are achieved by configuring them in the embedded linear program (LP) optimizer that is part of DeltaV PredictPro . The MPCPro Operate window has a drop down where the operator can select the desired objective function, in this case ethane recovery or ethane rejection. Moving down the train of distillation columns in plants with a fractionation train—de-ethanizer, de-propanizer, de-butanizer, etc., similar pairs of objectives can be set, based on the economic value of the hydrocarbons being separated. For example, in the de-propanizer, propane is removed from the top and butane and heavier (C4+) leaves the bottom. If propane were more valuable than butane, we would want to let as much butane slip out with the propane as possible and minimize the propane lost in the bottom C4+ stream. If conditions were reversed with butane more valuable, we would maximize propane slip in the butane and minimize butane loss in the propane. The handles for any of these distillations are essentially the same, where reflux at the top and reboil heat at the bottom are used to control the compositions. They must be coordinated with each other and with pressure and level controls in the column and in the reflux accumulator. Lou noted that in most gas plants that do not use advanced control strategies that operators tend to overpurify and give up on recovery. Using advanced process control technologies, such as the model predictive control (MPC) technology in PredictPro, also generally improves the stability of the process and enhances the ability of the process to recover from a disturbance. It is important to remember that ethane prices are dynamic. Low prices today may turn into high prices tomorrow and back to low prices again in the future. Gas processors with the most flexibility to switch between ethane recovery and ethane rejection will have the advantage when ethane prices fluctuate. When optimized, typical project return on investments can be on the order of 6 months. Lou and the other advanced process control consultants can help scope and execute the project to provide your gas plant the flexibility to rapidly adapt to changing market conditions. You can also connect and interact with other control experts in the DeltaV and Improve & Modernize groups in the Emerson Exchange 365 community. Related Posts Assessing the Natural Gas Processing Market Condensing Wet Shale Gas for Natural Gas Liquids Optimizing Multi-well Gas Lift Operations Regulatory and Model Predictive Control Difference? Surge Relief for Oil and Gas Liquids Pipelines-Part 2 Natural Gas Liquids Mass Measurement The post Flexible Operations for Changing Ethane Market Conditions appeared first on the Emerson Process Experts blog.
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Blog Post: Flexible Operations for Changing Ethane Market Conditions
In an RBN Energy blog post, The Yellow Rose Of Texas: Battle Of Texas Ethane Begins As Cargo #1 Departs Morgan’s Point , it not only gives a great history lesson on the origins of the Yellow Rose of Texas, but also the market dynamics for ethane production. It highlights the challenge that shale gas production has created for midstream producers: That’s because the Shale Revolution led to huge increases in wet natural gas production and, with that, far more ethane than the U.S. petrochemical market was prepared to consume. That, in turn, resulted in massive ethane “rejection” – or leaving ethane in the gas stream and selling ethane at gas prices rather than selling it as a “purity” product for use as a cracker feedstock… I caught up with Emerson’s Lou Heavner on the control challenge in switching between ethane recovery and ethane rejection based on market prices for ethane. Lou noted that at the heart of the gas plant is the cryogenic turboexpander (TE) process and de-methanizer . A gas plant is a series of distillation column separation processes. The first column, the de-methanizer removes methane (C1) out of the top of and everything else—ethane (C2), propane (C3), butane (C4), etc. the natural gas liquids (NGLs)—out of the bottom. As with virtually any distillation process, there are quality limits on both the column overhead and bottom purities. Typically, the overhead product (residue gas) has a specification for BTU content or Wobbe index . There may be economically based specifications for C3 or other quality measures. The bottom specifications are typically C1 and C1/C2 ratio. The relative value of the overhead (distillate) product vs the bottom product sets the targets. When ethane is more valuable than methane, the separation process runs in ethane recovery mode . Its recovery is maximized by minimizing the amount of ethane that leaves the top of the de-methanizer. This is usually defined as a BTU lower limit on the residue (sales) gas, also known as methane, leaving the top. On the other side, when ethane prices approach methane prices, the separation process runs in ethane rejection mode . The control objective is to allow ethane to slip out the top of the de-methanizer, which reduces the amount of energy required to purify the residue gas stream and also unloads the next column, the de-ethanizer, if the gas plant has one. This is accomplished by maximizing the BTU content of the sales gas subject to a propane constraint, since propane and higher hydrocarbons may also slip into the residue gas stream. Since propane is always more valuable than methane, the objective is to keep propane slip to a minimum. Lou noted that there are two controlling specifications at the bottom of the de-methanizer—methane in the bottom and methane/ethane ratio in the bottom, which are always maximized to the spec limits. These objectives are achieved by configuring them in the embedded linear program (LP) optimizer that is part of DeltaV PredictPro . The MPCPro Operate window has a drop down where the operator can select the desired objective function, in this case ethane recovery or ethane rejection. Moving down the train of distillation columns in plants with a fractionation train—de-ethanizer, de-propanizer, de-butanizer, etc., similar pairs of objectives can be set, based on the economic value of the hydrocarbons being separated. For example, in the de-propanizer, propane is removed from the top and butane and heavier (C4+) leaves the bottom. If propane were more valuable than butane, we would want to let as much butane slip out with the propane as possible and minimize the propane lost in the bottom C4+ stream. If conditions were reversed with butane more valuable, we would maximize propane slip in the butane and minimize butane loss in the propane. The handles for any of these distillations are essentially the same, where reflux at the top and reboil heat at the bottom are used to control the compositions. They must be coordinated with each other and with pressure and level controls in the column and in the reflux accumulator. Lou noted that in most gas plants that do not use advanced control strategies that operators tend to overpurify and give up on recovery. Using advanced process control technologies, such as the model predictive control (MPC) technology in PredictPro, also generally improves the stability of the process and enhances the ability of the process to recover from a disturbance. It is important to remember that ethane prices are dynamic. Low prices today may turn into high prices tomorrow and back to low prices again in the future. Gas processors with the most flexibility to switch between ethane recovery and ethane rejection will have the advantage when ethane prices fluctuate. When optimized, typical project return on investments can be on the order of 6 months. Lou and the other advanced process control consultants can help scope and execute the project to provide your gas plant the flexibility to rapidly adapt to changing market conditions. You can also connect and interact with other control experts in the DeltaV and Improve & Modernize groups in the Emerson Exchange 365 community. Related Posts Assessing the Natural Gas Processing Market Condensing Wet Shale Gas for Natural Gas Liquids Optimizing Multi-well Gas Lift Operations Regulatory and Model Predictive Control Difference? Surge Relief for Oil and Gas Liquids Pipelines-Part 2 Natural Gas Liquids Mass Measurement The post Flexible Operations for Changing Ethane Market Conditions appeared first on the Emerson Process Experts blog.
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Forum Post: RE: Can you dynamically change DeltaV Operator Theme Color set?
That worked Matt, thank you for your help! Just to be clear for those that read this later, when using a PCSD graphics library the rectangle/button and corresponding code by Matt is all that's needed. I removed the code module and variable that the document "DeltaV Themes on the Fly" had me create. Please note I had to duplicate the Threshold tables (i.e. Theme_Colors_Dark_Blue, etc...) from SIGlobals into User to get this to work.
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Forum Post: RE: Can you dynamically change DeltaV Operator Theme Color set?
Chris, You shouldn't have needed to duplicate the table to user unless you were making custom changes to the colors. If no custom changes it should have loaded the Dark Blue theme from SIGlobals to be used by the graphics. So let me know why you needed to duplicate to User to get it to work. Matt
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Forum Post: RE: Emerson Exchange America’s 2016 Event – Recommended Modernization and Migration Related Sessions to Attend
Thanks for putting this together Scott.
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Blog Post: General Calibration Considerations for Contacting Conductivity Sensors
By J. Patrick Tiongson, Product Manager, Emerson At first glance, calibrating conductivity sensors may seem straightforward; however, many times, this is not the case. I’d like to share with you some of the various methods for calibrating contacting conductivity sensors and outline some of the potential issues that can accompany such procedures. There are three main methods for going about calibrating contacting conductivity sensors: 1) with a standard solution, 2) directly in process against a calibrated referee instrument and sensor, and 3) by grab sample analysis. Understanding the fundamentals of each method, and the issues associated with each, can help make the decision on how best to calibrate a sensor. Calibration with a standard solution consists of adjusting the transmitter reading to match the value of a solution of known conductivity at a specified temperature. This method is best when dealing with process conductivities greater than 100 µS/cm. Use of standard solutions less than 100 µS/cm can be problematic as you run into the issue of contaminating the standard with atmospheric carbon dioxide, thereby changing the actual conductivity value of the standard. For maximum accuracy, a calibrated thermometer should be used to measure the temperature of the standard solution. If dealing with low conductivity applications (less than 100 µS/cm), in-process calibration against a referee instrument is the preferred method. This method requires adjusting the transmitter reading to match the conductivity value read by a referee sensor and transmitter. The referee instrument should be installed close to the sensor being calibrated to ensure you are getting a representative sample. Best practices for attaining a representative sample across both the process and referee sensors include using short tubing runs between sensors and increasing sample flow. Though usually not as accurate as calibrating against a standard solution, this method eliminates the need to have to remove your sensor from process, and removes any risk associated with contamination from atmospheric carbon dioxide. The least preferred method of calibrating a contacting conductivity sensor is by analyzing a grab sample. This method entails collecting a sample from process and measuring its conductivity in a lab or shop using a referee instrument. Calibration via grab sample analysis is only ever recommended if calibration with a standard solution is not possible or if there are issues with installing a referee instrument directly in process. The collected grab sample is subject to contamination from atmospheric carbon dioxide and is also subject to changes in temperature when being transported. In other words, there are many potential sources for error in the final calibration results. More information regarding calibrating conductivity sensors can be found HERE . Have you been utilizing the best method for calibrating your sensors? Are there any challenges that you run into?
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Forum Post: Emerson Exchange America’s 2016 Event – Recommended Modernization and Migration Related Sessions to Attend
Have you been wondering what Modernization and Migration related sessions our team recommends that you should attend at the upcoming 2016 America’s Emerson Exchange event in in Austin, TX (October 24 th - 28 th )? Well, we’ve made it easy for you, here’s a table of the workshops, short courses, Meet the Experts, and Technology Roadmap sessions that we are recommending be attended by anyone interested in DCS modernization and migration. These sessions can be easily added to your Personal Scheduler once it’s released.
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Comment on I am a woman in STEM. But, it hasn’t always been easy.
Great story, Rosella! We miss you here. I have experienced a few similar things, but only once so openly. A coworker told me (many years ago and at a different company), "I hate engineers, I hate young professionals, and I hate women, so you have three strikes against you." It's hard to even know how to react to that.
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Comment on Balance - Lost & Found.
Thanks for the comments.
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