Patent GB-1006851-A (GB)
Title: Method of desulphurizing vapours and gases which contain organic sulphur compounds
IPC: C07C7/163
Filed: 1963-07-05
Abstract: <PICT:1006851/C4-C5/1> Gases containing organic sulphur compounds are desulphurized by catalytically hydrogenating at 280-400 DEG  C.; absorbing the H2S so produced at below 400 DEG  C. on granular material containing at least 5% Mn as MnO; and regenerating the absorber with air.  The hydrogenation catalyst may be Fe, Cr, Co, or Mo; the absorber may be pyrolisite (converted to MnO at the operating temperature) or a ceramic carrier, e.g. pumice grit, impregnated with a Mn salt, e.g. nitrate, and fired; catalyst and absorber may be mixed together.  The initial gases may be aliphatic hydrocarbons or aromatic mixtures of benzene, toluene and xylenes, and should boil below 200 DEG  C.; any olefins present will be hydrogenated to aliphatic hydrocarbons.  The H2S-free hydrocarbons produced may then be catalytically cracked to give a gas containing over 50% H2, part of which may be used in hydrogenation.  Hydrocarbon feed from 1 is evaporated wholly or partly in 2 at above 10 atm. pressure; higher boiling fractions may be withdrawn at 3 and used to heat cracker 12. H2 is fed in at 5, and the gases pass through heater 4, and hydrogenation stage 6; then either through absorber 9, while 9a is regenerated by air/50% CO2 from 16, or vice-versa. SO2 is withdrawn at 18, and the hydrocarbon stream passed through vertical catalyst-containing tubes in 12 where it is cracked with steam, and possibly air, from 13. CO is converted to CO2 at 21, and the gases, containing 3-5% CO, pass to pipe 5 or cooler 24.  The process may also be used to purify coal distillation gases and other industrial gases, e.g. water gas and synthesis gas.ALSO:<FORM:1006851/C1/1> A hydrogen-rich gas is obtained from hydro-carbon gases containing organic sulphur compounds by catalytically hydrogenating at 280-400 DEG  C.; absorbing the H2S so produced at below 400 DEG  C. in granular material containing at least 5% Mn as MnO, which is regenerated with air to produce SO2; and steam-cracking the H2S-free hydrocarbons.  The hydrogenation catalyst may be Fe, Cr, Co, or Mo; the absorber may be pyrolusite (converted to MnO at the operating temperature), or a ceramic carrier, e.g. pumice grit, impregnated with a Mn salt, e.g. nitrate, and fired; catalyst and absorber may be mixed together.  The initial gases may be aliphatic hydrocarbons, or aromatic mixtures of benzene, toluene, and xylenes, and should boil below 200 DEG  C., any olefins present are hydrogenated to aliphatic hydrocarbons.  Hydrocarbon feed from 1 is evaporated wholly or partly in 2 at above 10 atm. pressure; higher boiling fractions may be withdrawn at 3 and used to heat cracker 12. H2 is fed in at 5, and the gases pass through heater 4 and hydrogenation stage 6; thence either through absorber 9, while 9a is regenerated, by air/50% CO2 from 16, or vice versa. SO2 is withdrawn at 18, and the hydrocarbon stream passed through vertical tubes in 12 where it is catalytically cracked with steam and possibly air, from 13.  CO is converted to CO2 at 21, and the gases, containing 3-5% CO, pass to pipe 5 for use in the catalytic hydrogenation, or to cooler 24.