A Process Engineering magazine article, Level best, poses a question:
Has the deployment of level measurement devices changed in the wake of the Buncefield [UK] disaster?
The article’s author connects with several instrumentation suppliers including Emerson’s Christoffer Widahl and Andreas Hessel for their thoughts on the progression and use of level measurement technology since this 2005 incident.
Christoffer noted that the newer generation of engineers want a simpler configuration process for level measurement devices. He added: Continue Reading ▶
Equipment failure is the leading cause of unplanned loss of production for most process manufacturers and producers. Critical equipment is typically continuously monitored but often other equipment has been too difficult or cost prohibitive to monitor.
Here is short 1:42 video, Emerson Essential Asset Monitoring, Reliability Solutions, which highlights how this second-tier equipment, also known as essential assets, includes pumps, heat exchangers, blowers, non-critical compressors, pipes and vessels, cooling towers, and air cooled heat exchangers. While these assets may not have been originally classified as “critical”, an outage or failure can cause a serious process disturbance or shutdown, resulting in lost production, potential reportable safety or environmental incidents and fines. Continue Reading ▶
Going back to 1980s when I worked on offshore oil & gas production projects, it seemed that well test measurements could be a tricky business. Even with today’s technologies, the increase in unconventional oil & gas production continues to make well test measurements a challenge.
In an E&P magazine article, Benefits of best practice maximize production and profits
, Emerson’s Michael Machuca
explores some of the measurement technologies and associated diagnostics to help drive sound decisions in well optimization, reservoir life sustainability and long-term profitability.
Michael highlights these unconventional oil & gas production challenges:
Operators are moving toward larger well pads with longer laterals that may have multiple lease holders per pad and tank. Larger facilities are now requiring commingling of production into a single tank or pipeline. As a result, it is necessary to measure production at the separator or heater treater to ensure proper allocation of royalties to the land owner and to fully understand how each well is producing.
Specifically, a separator and a heater treater are: Continue Reading ▶
Knowledge sharing need not be limited to one week conferences like the recent Emerson Exchange conference. I mention this to highlight an excellent discussion thread in Emerson Experts Forum in the Emerson Exchange 365 community. The thread, MPC [Model Predictive Control Penalties opens with this question:
What should I understand for “Penalty on Move” and “Penalty on Error”? Is there a way to calculate these?
Emerson’s Lou Heavner, whom you may recall from numerous advanced control-related posts responded:
The Penalty on Move is calculated based on the dynamics of the problem and is usually a good first guess. The Penalty on Error is initially set to a default value of 1. They both work to improve the performance of the controller, especially in the face of imperfect models.
Increasing the POM of an MV will make the action of that MV less aggressive. If an MV seems to be cycling or moving to aggressively, then increase the POM. I find that it is best to make changes larger or smaller by a factor of 2. Occasionally the POM will be too large and the MV seems almost dead. In that case reduce the POM, always observe after making a change.
I have rarely seen the need to adjust the POE of a Process Output. My colleague and fellow contributor to this forum James Beall has seen some benefits with changing POE. It works on a single Process Output rather than an MV. Increasing the POE will make it try harder to reach its constraint target. Decreasing POE will allow it to give up more easily. Think in terms of relative importance and increase the POE on variables that are not achieving the control objective and reduce it on those that are not as important such as level in a surge tank. For Process Outputs that are not being optimized, it doesn’t make much sense to me to worry about it.
Before MPC Plus, POM and POE required a download to change. In MPC Plus they can be modified on-line.
Let me know if this is not what you were seeking.
Seeing the thread, Emerson’s James Beall, also highlighted here on the blog numerous times, added [hyperlinks inserted by Jim]: Continue Reading ▶