I would like to model the amount of dissolved oxygen (DO) in water for the purpose of simulating a deoxygenation vacuum tower.
Can anyone tell me what the best fluid package to use for this?
Have you looked at this process...
http://www.grenlandgroup.com/minoxtm-deoxygenation-system/category365.html
Speaking with a rep from Grenland, I was told that 1:1 volume ration of N2 to Water will strip O2 down to 20 ppb or less. Not sure if it was a 1:1 volume ratio at operating conditions...
@ Jefka
I agree. It makes more sense to place the relief valve at the front end, closer to the source of the overpressure in the example I gave. I was just giving an example of when you would set the PSV set pressure below the MAWP. If the relief valve is placed at the front end, then you...
To expand on Jefka's example, if you have a string of equipment with the same MAWP (no rotating equipment or block valves in between them) and a single relief valve protecting all of them after the last piece of equipment (as is the case in some gas plants), you may want to set the relief valve...
In the case of an gas/liquid exchanger where the gas is the hot fluid and is on the tube side, and water is the cold fluid on the shell side, I am trying to calculate the relief rate when the water side is blocked in and the gas is still flowing. The gas is at a temperature where I would expect...
laliyo,
Are you considering using a rupture disk in place of the blinds that are on the vapor line of the exchanger whose shell side is not in service so that in the event of a ruptured tube, the shell side would then be open to the relief path to the PSV?
The problem with relieving from one...
cannondale,
Regarding your set pressure/operating pressure, API 520 Part 1 shows the maximum expected operating pressure at 90% of your set pressure. Typically if you operate above 90% of your set pressure, you want to use a pilot operated valve to avoid leaking by. Your max working pressure...
I realize now that in my original post I am comparing a vapor relief to a two phase relief, where in my response to CMA010 I am comparing one two phase relief to another.
When you compare the two-phase relief cases you get 4 times the area for 4 times the mass flow.
When you compare a single...
CMA010,
I'm sorry, I must not be explaining the scenario clearly enough.
The 1% volumetric flow is referring to the liquid phase of the two phase flow. We have 14,000 m3/h of flow, of that only 140 m3/h is liquid and 13,860 m3/h is vapor. Lots of vapor, very little liquid...VOLUME.
Now...
Thanks CJKruger, that's they type of confirmation that I'm looking for. Unfortunately there is no equipment between the exchanger and the PSV, but there is a significant amount of 20" pipe. The scenario is actually quite a bit more complicated, but not relevant here.
I'm comfortable with my...
I have a case where the high pressure side is BFW, on the shell, and flue gas in the tubes (low pressure side). If there is a tube rupture, high pressure BFW will go to the low pressure side and flash across the rupture. Using Hysys simulation, I calculated the percent flashing that occurs...
Thanks for all the input guys. A lot of good points.
In my case, the storage vessel is a horizontal drum that is actually rated for 50 psi and will get a code stamp, however it will be classified as an atmospheric storage drum because that's all that is required for it. It is in 10% caustic...
Yes, I meant a horizontal drum, not a cone roof tank.
Thanks for the input! I'm sure as soon as we make this change, the client will request that we use separate nozzles for vent and overflow!
I have designed an atmospheric storage drum with a vent and a separate overflow line. The client has requested that the vent and overflow lines be combined into a single nozzle.
We currently do not have an argument against this arrangement other than the cost of the engineering hours to modify...
What is the maximum operating pressure of the vessel?
I'm not sure I fully understand your process. Are you saying that you fill the vessel and start fermentation, which generates CO2 which mixes with the air that is already in the vessel, then you want to purge the vessel of that CO2/air...
Thanks Compositepro! I just needed to see where it was documented somewhere that having a mounded storage relaxed spacing standards in any way.
From NFPA 59A, Section 13.6, it looks like above ground and mounded storage are treated the same way as far as spacing goes. It looks like you need...
I am trying to find information on mounded storage. More specifically, mounded storage being used to reduce spacing requirements.
For example, if a LPG bullet is required to be 100 meters from a fence line, does having that same bullet in a mounded application reduce the spacing requirement...
All good advice, thanks!
This is in the troubleshooting stage. We are also controlling condensate in the reboiler by putting two steam traps in parallel (instead of just one) going to a condensate pot with level control.
