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Hello and thanks in advance for any help. I am trying to troubleshoot a small air stripping tower that removes dissolved chlorine from 75% sulfuric acid solution. The flowrate of sulfuric is 2.5GPM with ~1200 ppm Cl2. Only 700 ppm of Cl2 is being removed. The air flows at 5psig and 50SCFM. Tower...

do you have any amines in the C3 splitter? maybe injected upstream to control corrosion? i believe they are notorious for causing foam. the foam can also partially block your downcomers, causing the trays to flood.

In your case dont think id upset the C3 splitter. Just scan at normal conditions and make a judgement call after you see the first scan. You might consider scanning more than one pass in this tower. Just a thought but are you sure the instrumentation is correct? For the C2 splitter, is it...

I used to work at TruTec (which is now Tracerco) for several years. I would agree with both above...scan at your problem conditions. You dont know which tray the flooding originates, if it is total liquid flood, or jet flooding. The scan will be able to differentiate between jet and total flood...

Thank you all for your answers. Do any of you know the corrosion mechanism of NH4SH?

Thanks...im guessing those are also in order of increasing cost?

Temp is around 245F and conc is near 7557 ppm. NH3 in the water is 2520 ppm. I believe there is also NH4Cl. Not sure of any other impurities.

Hello, Does anyone know the corrosion mechanism associated with ammonium bisulfide? Is this mostly a corrosion/erosion issue? Also, is Inconel 625 an acceptable alloy to protect against it? Thanks in advance for any help. Jamie

Try downloading a copy of Koch Glitch's "KG Tower". I BELIEVE it has the ability to change the turndown% and see the results. Its pretty good about allowing you to input tray types, # of passes, etc.

The sulfide pitting is from Ammonium Bisulfide (aka hydrosulfide to some) and H2S. Conditions in the vessel are around 256F and <50psig. i believe its more a matter of the salt not staying in solution and erroding the metal.

Does anyone know of the benefit of post weld heat treating a carbon steel vessel (the entire vessel) with regards to sulfide corrosion? If treated, will the vessel be more resistant? Would cladding with inconel 625 be better? Thanks in advance, Jamie

is nuclear level detection out of the question? It seems to me that any fouling buildup on the walls would not effect its accuracy as the liquid it is "detecting" is a lot more dense.

During normal operation, 300 GPM discharged from pump. ~25 will be recycled via control valve or ARC to the pump suction. How will pump energy into fluid effect the scenario if the ARC knocks down the P to the suction P? Im a new engineer so this is a little hazy to me.

Thank you all for your help and advice

Hello all. Im looking for some opinions on the quality of auto recirc valves (Yarway, Schroedahl) vs control valves for pump protection at minimum flow. Are some auto recirc valves better than others? Just a little background...DP across pump during min flow is from 1000 to 140 psig and 320GPM...

According to simulation, the fluid will not flash (140F) as it goes from 1000psig to 280psig. ANybody know anything about pressure let-down valves?

Sean yes its for minimum flow protection. velocity is high but this is the extreme case and will rarely be encountered. Just looking for the best way to knock the pressure down so control valve doesnt see the brunt of it.

Thanks geordie87 that sounds like what i was looking for. Are there equations for sizing these in series?

Thanks Eltron, I am dealing with liquid however (35%wt amine in H2O). THe application is for minimum flow around a pump. THe FCV wont be able to take taht DP so im trying to find a good way of knocking it down before it gets there. Im reading things about venturis, anyone have any experience...