Desulfurization of coking dry gas
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Desulfurization of coking dry gas: Dear experts, what is the typical hydrogen sulfide content in coking dry gas before desulfurization? Before treatment here, the concentration was 40,000 PPM; after treatment, the level was poor at 300 PPM. The ethanolamine concentration is 27%, with a hydrogen sulfide content of 0.6% in the lean solution and 0.2% in the rich solution. The circulation volume of ethanolamine is 40 tons. I would appreciate advice from experts. Thank you!
That’s too general! It’s hard to tell; from the apparent symptoms, it seems that the number of trays is insufficient (since the sulfur concentration in the rich liquid is quite low, and the ammonia concentration in the lean liquid should be sufficient). What is the processing capacity for the coker dry gas? Is the operating pressure and the temperature of the lean amine solution appropriate? You can take a look
I’m not sure if there are any calibration calculations for the desulfurization tower; if so, please provide them. Thank you
The hydrogen sulfide content in the lean solution is 0.6%, while it is 0.2% in the rich solution – that can’t be right, right?
If the sulfur content in the dry product is too high, it is recommended to use desulfurization alcohol again to ensure optimal results
40,000 is also okay; I’m not sure what the processing rate is. There is no problem with liquid-rich regeneration
Methanethiol has a low boiling point, which is closely related to the content of hydrocarbons with three or more carbon atoms in dry gas
According to what the poster said, there’s no need to regenerate the lean liquid; the rich liquid is already better than the lean liquid. Temperature? Dry gas volume?
Could you talk about the components of exhaust gas before it is treated?
300 left after treatment at a concentration of 40,000? The efficiency is really too low, isn’t it?