A new 80,000-ton sulfur project is being established and is set to begin construction – share your opinions!
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Our factory is constructing a new 80,000-ton sulfur recovery project, with commencement scheduled for next September. I would like to gather information on the points that need attention during the initial stages of project construction! You can bring up anything; I will consider it all! To be precise, our plant’s sulfuric acid production project consists of two units, each with a capacity of 40,000 tons, giving a total exhaust gas treatment capacity of 60,000 tons! Question: 1. The old factory has a capacity of 20,000 tons and uses blending valves ； For new projects, steam superheaters are being used instead; I have no experience in this area. Could those with experience please share the advantages and disadvantages of this approach? ； 2. The small plant for exhaust gas hydrogenation is not in operation; those with experience are requested to provide a systematic and comprehensive summary of exhaust gas hydrogenation! Thank you very much here!
The advantage of high-doping valves is that temperature regulation is relatively fast; the disadvantage is that it results in a certain loss of conversion efficiency, and moreover, such valves are prone to problems. The advantage of steam heaters is that there is no loss in conversion rate, operation is stable, and the equipment is less prone to problems. However, the downside is that temperature regulation is slow, especially under low load conditions. Additionally, sulfur tends to accumulate at low points, and problems can arise in the steam condensate system. For the exhaust gas hydrogenation system, as long as the temperature rise in the bed is well controlled, there are no major issues in other aspects. Additionally, I would like to ask: your Klaus units consist of two sets of 40,000 tons each, so why is the exhaust volume only 60,000 tons?
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It’s probably a matter of quantity; the factory can’t accurately assess the amount of acidic gas involved. The values obtained for residue hydrogenation are only theoretical, so they must have been cautious in their approach, I guess! Thank you for your reply. Do you have any materials on this topic? If so, please send them to me!
In sulfur and sulfurization units, high-temperature mixing valves are commonly used, while steam heaters are rarely employed. As far as I know, Huizhou Refinery does use steam heaters, with 3.5 Mpa steam being used as the heat source, and the results are quite good. For exhaust gas hydrogenation, a new process is recommended: the use of sulfur dioxide absorbents can reduce equipment costs, and no hydrogen is required, ensuring that exhaust emissions meet the new national standards.
Is the new process you mentioned one that uses ionic liquids to absorb sulfur dioxide? The question is, what to do with the absorbed sulfur dioxide?
Please note the following: 1. What type of lining is used in your sulfur production furnace (rammed or brick-lined), and the process of heating the lining must follow the requirements of the lining supplier. 2. Which product is used for the mixing valve – one with cooling or without cooling? (I personally think those with cooling are better.) 3. What are the advantages and disadvantages of including a wire mesh demister at the process gas outlet of the condensing cooler in the design? 4. The heat source used for the reheating in exhaust gas hydrogenation is medium-pressure steam, flue gas from incinerators, or an on-line furnace.
The liquid phase that has absorbed sulfur dioxide is regenerated; the sulfur dioxide obtained after regeneration is directly fed into the sulfur production furnace, which allows for reduced air supply to the sulfur production furnace and an increased processing capacity of the same.
Are there any practical application examples?