Low temperature, hydrogenation of crude benzene, key operating points for the stabilizer tower
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This post was last edited by shcw1976 on 2010-6-8 at 20:49. I’m a beginner in the field of naphtha hydrogenation; I would appreciate it if experienced colleagues could provide some guidance on the key aspects of operating a stabilizer. Thank you. For example, what should be the appropriate proportion of benzene in the overhead reflux? What factors influence the overhead temperature? What are the main control parameters for this type of tower?
Give it a push; I hope experts can offer some guidance
The stabilizer can be considered as an exhaust tower; its function is to remove H2S. The key point in its operation is to maintain the temperature after condensation at the top of the tower above 60 degrees. This tower operates in full reflux mode, with a steam flow rate of around 500–600 kg/h, and the hydrogenation feed amount is 10 t/h
This tower is primarily used to remove hydrogen sulfide; therefore, the reflux should be as low as possible, which also helps to reduce the load on the tower and lower energy consumption.
For example, what should be the appropriate content of benzene in the reflux from the tower top? It is around 2%. The tower top temperature is influenced by various factors: the tower top pressure, the reflux rate, the pressure in the pipeline for discharging hydrogen sulfide, the flow rate of steam added at the bottom of the tank, as well as the temperature and flow rate of the feed BTXS. What are the main control parameters for this tower? The top pressure is 400–450 Kpa, and the bottom temperature is around 178 degrees.
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