A PROCEDURE FOR THE SELF-HYDROGENATION OF REFINERY GASES, FROM CATALYTIC FLUIDS CRACKING FACILITIES AND DELAYED COKING FACILITIES

摘要

PT--81622 A Process comprises (a) sepg. liq. stream from a refinery gas stream (A) , the liq.-free gas stream being split into a stream (B) feeding a fuel gas system and a stream (C) making up an ammonia plant feed (b) passing stream C through a compressor suction drum and compressing, causing intermediate suction of satd. and cooled gas recycle and mixing of gas with feed and removing portion of reaction-generated heat from hydrogenation reactor (c) compressing gas from (b) at 100-713 psi (7-50 kg/sq.cm) or higher, pref. 385-713 psi (27-50 kg/sq. cm), forming stream (D), the compressor receiving low density gases with a high concn. of H2 from cracking of heavy gas oil and vacuum residue with high levels of Ni (d) heating stream recovering heat from the recycle, effluent from hydrogenation reactor, passing mixt. (E) feed-recycle gas through reactor, the feed-recycle gas ratio being controlled so that the temp. of reactor is kept at min. levels of coke deposits on the catalyst without reduction in the hydrogenation reaction rate, reactor being filled with a fixed bed catalyst of cobalt-molybdenum oxide or Ni-Mo, and designed so that the space velocity is such that the hydrogenated prod. stream (F) is practically olefin-free or ultimately contains below 0.3 wt.% olefins, the life-time of the catalyst being at least a year and at the same time S cpds. e.g. COS, being hydrogenated to sulphydric acid (e) passing a portion of hydrogenated gas, stream (G), through a ZnO fixed bed reactor to remove as ZnS the sulphydric acid in the refinery gas or produced is (d) followed by injection of the hydrogenated and S-free refinery gas, stream (K), in the water stream reformer (f) returning a portion of hydrogenated gas, stream (H), to heat exchanger, cooling the gas, stream (I), with water up to 140-170 (150) deg. C, sepg. liq. formed followed by injection of gas, stream (I), in intermediate stage of compressor. (First major country equivalent to PT--81622-A) GBAB- GB2183670 B Process comprises (a) sepg. liq. stream from a refinery gas stream (A) , the liq.-free gas stream being split into a stream (B) feeding a fuel gas system and a stream (C) making up an ammonia plant feed (b) passing stream C through a compressor suction drum and compressing, causing intermediate suction of satd. and cooled gas recycle and mixing of gas with feed and removing portion of reaction-generated heat from hydrogenation reactor (c) compressing gas from (b) at 100-713 psi (7-50 kg/sq.cm) or higher, pref. 385-713 psi (27-50 kg/sq. cm), forming stream (D), the compressor receiving low density gases with a high concn. of H2 from cracking of heavy gas oil and vacuum residue with high levels of Ni (d) heating stream recovering heat from the recycle, effluent from hydrogenation reactor, passing mixt. (E) feed-recycle gas through reactor, the feed-recycle gas ratio being controlled so that the temp. of reactor is kept at min. levels of coke deposits on the catalyst without reduction in the hydrogenation reaction rate, reactor being filled with a fixed bed catalyst of cobalt-molybdenum oxide or Ni-Mo, and designed so that the space velocity is such that the hydrogenated prod. stream (F) is practically olefin-free or ultimately contains below 0.3 wt.% olefins, the life-time of the catalyst being at least a year and at the same time S cpds. e.g. COS, being hydrogenated to sulphydric acid (e) passing a portion of hydrogenated gas, stream (G), through a ZnO fixed bed reactor to remove as ZnS the sulphydric acid in the refinery gas or produced is (d) followed by injection of the hydrogenated and S-free refinery gas, stream (K), in the water stream reformer (f) returning a portion of hydrogenated gas, stream (H), to heat exchanger, cooling the gas, stream (I), with water up to 140-170 (150) deg. C, sepg. liq. formed followed by injection of - gas, stream (I), in intermediate stage of compressor. (First major country equivalent to PT--81622-A)