Is coking liquefied gas in gaseous or liquid form in the desulfurization tower?
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Is coking liquefied gas in gaseous or liquid form in the desulfurization tower? The liquefied gas desulfurization tower uses methyl diethanolamine; the operating pressure is 0.75, and the operating temperature is 50°C. How does the liquefied gas come into countercurrent contact with ethanolamine inside the tower? What is the principle?
Under this pressure, liquefied gas is in a liquid state; it flows from the bottom of the tower upward, while ethanolamine flows from the bottom downward. The two fluids come into contact within the tray or packing layer, where they react to release the hydrogen sulfide contained within them
Liquid; the desulfurization tower contains sieve pores or packing, and the densities of the two are different
Liquid! The desulfurization tower operates with a full liquid level; the density of the amine solution differs from that of the liquefied gas. What we control is the boundary level, not the liquid level!
Extraction works on the same principle as liquid-liquid extraction.
The liquefied gas is condensed to 30 degrees in the stabilizer top cooler, and then sent to the liquefied gas desulfurization tower. Upon contact with the liquid at 40 degrees, could some of the lighter components vaporize, resulting in overpressure in the desulfurization tower? (The liquefied gas after purification contains sulfur at levels of tens of thousands of PPM; the lean liquid fails to settle and remains in the sedimentation tank.) Here we have sieve pores, and I’m not sure whether the designed pore opening rate is too low.:
In liquid-phase desulfurization, what we control is the liquid level on the tray.
Does anyone here have the structural diagrams of the oil skimming tanks for the dry desulfurization tower and the circulating hydrogen desulfurization tower?