I have a reactor that is insulated with 2" of OC Foam Glass 1. It protected by 304 stainless. Can I take credit for the foam glass when calculating the required relief rate?
George, good question. I will need to look at this. Because L/D is ~2, I don't think detonation is likely a problem in the reactor itself, but i suspect it needs to be looked at in the piping to/from, where lengths are long.
I have a reactor consuming hydrogen. The MAWP is 90 psig. The NFPA Pmax ~ 87 psig and Pred ~136 psig. Because the Pmax is lower than the MAWP, does this mean that the vessel will contain a deflagration - i.e. that we do not need to install rupture discs for this scenario?
Thanks for the great input.
Littleinch - your general comment about looking at conditions after the steam is cut off is what is really needed, but I don't have the software to model this. Btw, the steam is fed to a reboiler, which in turns vaporizes a mix of water, MeOH and other...
I have a Client with a distillation column. I am designing for vacuum protection. The column has a reboiler. A portion of the OH vapor is fed downstream to a process and a portion is condensed. Assuming the steam to the reboiler stops and the condenser still operates. The default in the...
George, I had not thought through the possibility of the flow path pack through the tube chamber and back through the tubes. I do think that is valid.
This helped. Thank you both.
Yep, We normally assume a 1/8" tube leak for this case. However, a Client has opted to take a much more conservative case for situations wherein the upstream pressure exceeds the lower pressure, protected, system MAWP by 2X. That has caused us to look at the full tube rupture case. As you...
Latexman, that was also my thought, but have never seen both sides of the tubes being protected (i.e. RV on both inlet and outlet of (in this case) cooling water. Thank you
For "normal" tube rupture case (tube side is high pressure, shell low pressure) the standard approach is to assume 2 orifice or 1 orifice / 1 pipe - i.e. from both sides. However, for case where tube side is low pressure, protected side, I am not sure how dual source would apply. Anyone had...
George, Thanks for the very useful approach. Could you clarify what you define as the "internal recycle lines" in (a)? If this refers to the recycle line through the cooler back to the suction KO drum, then I believe I will run into a complication. Since the compressor is sized 10X the...
Appreciate your comments...
Entire system, including the suction drum, is designed for 900 psig. George, I am trying to determine if the system can be over pressured (and ultimately the relief rate). So at relief the flow to the system will stop since the upstream pressure < 900 psig...
I am a bit stumped about handling this system. See attached. At blocked in relief (900 psig), the flow to the system will cease, but before that happens the loop pressure will increase substantially. This will cause the suction pressure to the compressor to increase, ultimately causing the RV...
To follow up on your comments...
The max temperature of the oil sees is 130°F.
As indicated above, its flash point is 204°.
There are no "baddies" or volatiles in the oil.
There are no other sources of high temp in the building.
I am clarifying the electrical Code, but I believe it is...
pb, I am literally in the middle of putting together an analysis sheet using an old journal article from Larry Simpson. I wonder if you have the article from Forrest and Fisher that you could share, or at least let me know the date of the article. It may be a more recent article than...
I have a recycled oil stream, Flash Point 204°F, being fed through indoor ASME filters designed for 150 psig. There is no source of temperature exceeding the flash point. I am questioning whether I need to consider a fire case. Thoughts?
