Recent content by Iradah

Thanks SeanB, can you please give a short example of what you mean by a high level. I also wish if more people put their views, this is an important discussion and having critical discussion in our plant currently.

Thanks Morten for your valuable input.

Thanks e43u8 and all for your inputs. This dicussion was useful.

OK, I will try to clarify it more. The flare header is already sized and installed. It was sized for a certain required load. the Flare header seems to be incorrectly sized as it shows locations of choked flow. some people mentioned that there should be no issue now because the required relief...

After three months, I am still not sure of the results I got. I worked the flare header pressure drop calculation from the stack backward to the PSV outlet. I divided the system into sections and used Weymouth equation for gas pressure drop calculations. However, I could find good way to...

Although the required flare volume is less, the PSV will still flow the initial flow, so how can I update the document for less flow?

I am sure that you have good views on this subject, looking forward to hearing them.

Thanks Latexman, This is what I think. At original inlet rates to the vessel and at blocked outlet case, the PSV will be continuously flowing the designed flow rate for its size. at lower inlet to the vessel than the original design, the PSV will be still flowing the same rate it was designed...

Hello, I was wondering how the PSV behaves when it reaches the set point and opens. for a PSV sized for a blocked outlet relief load, it will be sized for the flow rate into the vessel. After some years, the production might be less and the required relief load will be less, however, the PSV...

Hello all, I need to know what the practice is in oil and gas plants operation with respect to writing operating procedures. Who owns the operating procedures for the plant? Who writes them? Who approves them? what are the levels of approval the procedure go through? What is the exact role of...

Hello all, I just thought I can share with you an event happened at our site. We had a black out at which the ESD was initiated and all blow down valves open to flare. There are two flare stacks at the plant, one of the operators wanted to reduce the loss to flare so he isolated one of the...

To add to LittleInch question about the effect of lower plant capacity on the sizing of the flare header: This is because some relief scenarios are blockage scenarios where the plant inlet will be flared because of the blockage downstream and this is why the relief load is less and hence there...

Thanks all for your valuable feedback. I am afraid I have to re-calculate which is not a quick task as expected by my managers. My manager said that I can pick one of the cases mentioned in the report and do calculations in excel sheet. Just pressure drop calcs for several lines connected to...

Hello, I need your feedback about choked flow in flare headers. I am reading a study on our flare header system at the plant made in 2009. There is a PSV that has a 12” line going into a 16” pipe then into 24” header. The study says that there will be choked flow at the end of the 16” header...

Hi zdas04, LittleInch, The reason I want to do that is the old story of our stationary pig in C4 line that I discussed with you under: http://www.eng-tips.com/viewthread.cfm?qid=354614 The pig is still stuck, and we are preparing to divert C4 temporarily somewhere until the line is fixed. I...