Thanks mike, that helps. I guess my problem is sometimes I spend too much time describing what happened, rather than what I did or what I would like my b2b to do. I find it hard to work without background information, but it makes the notes very very long (we handle a very wide range and very...
I couldn't find anything on this topic, so I was wondering if anyone here could share experience or tips on how to stay organized and aligned working an extended on/off schedule.
My specific situation is working 28 days on/28 days off at a fairly remote upstream oil and gas facility. When I'm...
Another difference is in the inspection and testing requirements. Some key differences that frequently come up for the work I'm involved with are that 31.3 requires 5% x-ray for the circumferential welds, whereas 31.8 I beleive has different requirements for x-ray depending on what %of SMYS the...
I ran into almost the same problem, except our issue was that the air flow switch had to clear to allow the unit to start, and the fan just couldn't make enough pressure to trip the DP switch into showing air flow, and the startup sequence would abort. The operators would go out and pull the low...
Thanks for your input, I have a few questions and clarifications:
" I doubt you have velocities high enough to develop a true froth of homogenous gas / liquid in the vessel (but you can check that)" - how do I check this? I have looked at drag effects for liquid droplets in this stream to see...
Hello all,
We have a remote gas sales facility that utilizes a caustic wash system, and apparently, intermittently the entire liquid content of the caustic wash vessels are carried out to the sales pipeline.
The system is configured as shown in the attached drawing, basically 2 vertical...
Why is the separator so large? For slug volume or for separation? If for separation, there are a number of ways to potentially reduce the size.
For enough money, you can put anything offshore.
I think Chance17 gave you the correct answer, and then went from there and gave you some extra things to consider.
Consider the system from the perspective of just the PSV - when the PSV inlet side reaches the set pressure, the PSV will go fully open, and the flow rate will be governed by the...
What are the overpressure scenarios? If you can mitigate those, do you need a PSV?
In a heated water loop, your overpressure source may not be the pumps, but rather heat input from the heater, or blocked flow and thermal expansion, or fire case on a vessel.
Same for the chilled side - what if...
The attachment didn't take - here it is:http://files.engineering.com/getfile.aspx?folder=24d22abf-7472-4a4e-9fe8-362f7e68532c&file=Demethanizer_pump_troubleshoot_sketch.pdf
Basic P&ID attached
I work in a small gas plant, and a while back one of our two demethanizer bottoms pumps went out (only 1 normally runs at a time), and we have been running on just one ever since. The two pumps were multi-stage vertical can pumps from 1948, and we couldn't find anybody that...
I am having problems similar to the second post by vinya in this old thread: http://www.eng-tips.com/viewthread.cfm?qid=45357&page=53
Basically, our lean TEG surge tank is collecting a layer of hydrocarbon on top of it, filling up to the skimming level, and continuously dumping (why it doesn't...
Snorgy is correct, sometimes LMTD does not work, as described as a 'special case' at this website: http://www.cheresources.com/heat_transfer_basics.shtml
I believe the correct temperature difference to use in this case is 30F.
