Improvements in or relating to hydrogenation of carbon oxides

摘要

Hydrocarbons and oxygenated derivatives are prepared by flowing a mixture comprising hydrogen and carbon monoxide or dioxide at a velocity of at least 5, preferably above 8 ft./sec. in contact with a finely divided hydrogenating catalyst of appropriate particle size such that it is moved in the direction of flow of said mixture in a condition more dilute than that of the catalyst in a conventional pseudo-liquid dense phase operation under comparable conditions. The catalyst may be a Group 8 metal or oxide, especially iron, with promoters and supports. The greater proportion preferably has a particle size less than 100m , and 25 per, cent by weight is less than 40m . With iron 450-750 DEG F. and 10-500 p.s.i.g. are suitable. Feed gas having an excess of hydrogen is preferred, part of the unconverted gas being recycled. The catalyst concentration is less than 18, e.g. 3-12 lbs./c. ft. The feed gas may be passed up conduit 8, Fig. 1, catalyst being introduced through standpipe 10, which has a jacket 11 for heat exchange medium. Catalyst separates in conical section 14 and returns to the standpipe, separation also being effected by filters 20, 21 in conduits 18, 19. Uncondensed products are recycled by line 44. The section 16 may be extended and adjusted in cross-section such that the gas velocity therethrough is appropriate for producing a dense pseudo-liquid catalyst phase. A modified form of reactor comprises a bundle of tubes in place of the conduit 8 and a central standpipe for return of catalyst. In Fig. 3, reaction tubes 107 are disposed in a shell 108 for circulation of heat-exchange fluid, and products pass by conduit 111 to chamber 120 where catalyst separates, and is returned by standpipe 129. In Fig. 4, the feed passes up conduit 211 and is mixed with catalyst from standpipe 249. The mixture passes to a first cooler 216 through a reducer 212 and pipe 213, the reaction time prior to the first cooler being less than 2 secs. Products pass to a second reactor 222, thence to a second cooler 224 before entering separator 232 where catalyst accumulates, is stripped in section 246 by gas introduced by pipe 247, and recycled by standpipe 249. In an example, a fused and reduced, promoted iron catalyst is used in the apparatus of Fig. 1. The oxygenated products include acids.ALSO:Hydrocarbons and oxygenated derivatives are prepared by flowing a mixture comprising hydrogen and carbon monoxide or dioxide at a velocity of at least 5, preferably above 8 ft./sec. in contact with a finely divided hydrogenating catalyst of appropriate particle size such that it is moved in the direction of flow of said mixture in a condition more dilute than that of the catalyst in a conventional pseudo-liquid dense phase operation under comparable conditions. The catalyst may be a group 8 metal or oxide, especially iron, with promoters and supports. The greater proportion preferably has a particle size less than 100 m , and 25 per cent by weight is less than 40 m . With iron, 450-750 DEG F. and 10-500 p.s.i.g. are suitable. Feed gas having an excess of hydrogen is preferred, part of the unconverted gas being recycled. The catalyst concentration is less than 18, e.g. 3-12 lbs./c. ft. The feed gas may be passed up conduit 8, Fig. 1, catalyst being introduced through stand-pipe 10 which has a jacket 11 for heat exchange medium. Catalyst separates in conical section 14 and returns to the stand-pipe, separation also being effected by filters 20, 21 in conduits 18, 19. Uncondensed products are recycled by line 44. The section 16 may be extended and adjusted in cross-section such that the gas velocity therethrough is appropriate for producing a dense pseudo-liquid catalyst phase. A modified form of reactor comprises a bundle of tubes in place of the conduit 8 and a central stand-pipe for return of catalyst. In Fig. 3, reaction tubes 107 are disposed in a shell 108 for circulation of heat-exchange fluid, and products pass by conduit 111 to chamber 120 where catalyst separates, and is returned by stand-pipe 129. In Fig. 4, the feed passes up conduit 211 and is mixed with catalyst from stand-pipe 249. The mixture passes to a first cooler 216 through a reducer 212 and pipe 213, the reaction time prior to the first cooler being less than 2 secs. Products pass to a second reactor 222, thence to a second cooler 224 before entering separator 232 where catalyst accumulates, is stripped in section 246 by gas introduced by pipe 247, and recycled by stand-pipe 249. In an example, a fused and reduced promoted iron catalyst is used in the apparatus of Fig. 1.