For double-tower stripping, what should the control parameters be after hydrogen sulfide removal? Severity of corrosion
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With the current double-tower stripping process, the hydrogen sulfide level in the desulfurization tower is 1200 ml/l, which is below the designed level of 26 ppm; as a result, the hydrogen sulfide level in the ammonia removal tower rises sharply, causing corrosion of the heat exchangers and the impellers of the pumps. I had previously posted about the corrosion issues affecting the heat exchangers and pumps, and now the impellers of the corrosion-resistant pumps are also showing signs of corrosion, becoming thinner and developing holes. The questions I would like to ask are: what are the parameters at the bottom of the desulfurization tower? What is the hydrogen sulfide content at the top of the ammonia removal tower? Also, I’m interested in the material selection for the equipment, as well as the criteria for determining whether the purified water meets the required standards. Photos are included.
It should not be achievable; a result of 1200 ml/l is considered good.
This post was last edited by pm9521 on 2017-9-6 at 14:48. However, the cost of the reflux tank can exceed 230,000; the corrosion of the pumps is severe. For a flow rate of 1200 ml/l, bottom blowing is used, while a reboiler should be employed under normal circumstances, with costs ranging from 5000 to 7000. Temperature 60-70 degrees.
Why does hydrogen sulfide cause such severe corrosion when combined with ammonia?
I guess it’s because of the neutralization that produces salt
There is a problem with the deacidification tower that requires renovation; we can handle it. For inquiries, please contact Engineer Wang at 13702159086. Thank you!