Matching tower temperatures in amine absorbers can be very challenging. it's a function of reaction chemistry, kinetics, interface, tray residence time, tray efficiency, foaming/froth, etc. You need to input the correct number of actual trays and then start adjusting efficiency values until...
Does anyone have any sizing guidelines for an iron sponge tower? I know there are a lot of alternatives including aqueous iron processes, triazine, bio, etc. I've been asked to check on the required size of an iron sponge system. I need mass pickup of H2S in lb/lb and a space velocity...
Honestly this is a new one. I've been running this software for decades and haven't seen this error - you need to contact their helpdesk to see what's going on.
Doing a blowdown on a LSHH in the KO drum is an incorrect action. The resulting flow will potentially carry significant amounts of KO drum liquids up the stack. If you're lucky, these fluids aren't flammable. The good news is that the LSHH will clear. :) Block and hold is the answer.
You really need to look at maximum heat flux, maximum bulk fluid temperature, superheat, pressure drop, and a bunch of other factors. The flow is determined by the duty of the unit including condensing (the majority), desuperheating, and subcooling. Ultimately the exchanger will reach a...
This should work reasonably well - as dcasto suggested, it will approach the equilibrium effect of a single theoretical stage. You could probaby simulate this at about 30% efficiency and see if this is enough for your application. The H2S reaction is instantaneous however, the spray nozzle and...
Is anyone aware of a code and/or published guideline that requires an auto-blowdown of a natural gas facility when a gas detection event is triggered? We often do this at 20 ppmv or 40% LEL but is this a code requirement or just common practice. The plant is 24 hour attended and the owner is...
Be careful using Panhandle for anything other than long single phase gas lines and even then, we often correct for sctual conditions or if we can reference back to real pressures. It can be horrifically wrong sometimes.
Hang on, I'll put this in excel format so you can copy/paste. Here it is in mole %http://files.engineering.com/getfile.aspx?folder=5de5fbf8-5b35-484c-98cb-b32f415ffef4&file=Tower_Feed.xlsx
ok, see below. Feed is at 109°F and 60 Psig and the reboiler will run at about 267°F to make a 12 RVP stable condensate. Tower will run at pretty much 60 Psig.http://files.engineering.com/getfile.aspx?folder=f2ac9d6a-1c30-4585-9d39-f84c0a1dec14&file=06-10-2013_1-43-29_PM.jpg
Yeesh, fast fingers but slow brain. I was trying to say that simple bubble point calc's don't seem to represent column performance because each stage is at a diferent temperature.
It doesn't seem to be that simple. I've tried just a straight forward JT valve with the outlet set at -30°C and the pressure drops into a vacuum. This is still with almost 5% methane in the stabilzier column feed mixture. It almost seems like I have to do a stage by stage flash where I...
