This invention relates to gas phase reactions wherein a finely divided solid catalyst is contacted with reacting gases at elevated temperature to effect an exothermic reaction, which reaction tends to increase the temperature sufficiently to interfere with the desired reaction and/or to damage...

This invention relates to an improved method, for hydrogenating carbon oxides to produce hy-\ drocarbons and oxygenated organic compounds. The carbon oxides treated include not only carbon monoxide and carbon dioxide but also other organic compounds which contain the carbonyl group, such as...

Chemical reaction with fluidized solids

Synthesis of organic compounds

A method for reducing catalyst attrition losses in hydrocarbon synthesis processes conducted in high agitation reaction systems; a method of producing an attrition-resistant catalyst; a catalyst produced by such method; a method of producing an attrition-resistant catalyst support; and a catalyst support produced by such method The inventive methods and catalysts have several aspects In one aspect, the catalyst preferably comprises a η-alumina support including an amount of titanium effective for increasing the attrition resistance of the catalyst In another aspect, the catalyst preferably comprises a η-alumina support which has been treated, after calcination, with an acidic, aqueous solution In another aspect, the catalyst preferably comprises cobalt on a η-alumina support wherein the cobalt has been applied to the η-alumina support by totally aqueous, incipient wetness-type impregnation In another aspect, the catalyst preferably comprises cobalt on a η-alumina support with an amount of a lanthana promoter effective for increasing the attrition resistance of the catalyst In another aspect, the catalyst preferably comprises a η-alumina support produced from boehmite having a crystallite size, in the 021 plane, in the range of from about 30 to about 55 angstroms Use of the catalysts in high agitation reaction systems results in reduced catalyst attrition losses

Reducing fischer-tropsch catalyst attrition losses in high agitation reaction systems

This invention relates to the calcination and nodulization of trade sludges or slurries that are lime-bearing, such as paper mill causticizing sludge, water softening sludge, sludge from first carbonation or other lime sludge producing stations in sugar factories, and so on. Such sludges are...

Calcining lime bearing sludges

Cobalt catalysts, and processes employing these inventive catalysts, for hydrocarbon synthesis. The inventive catalyst comprises cobalt on an alumina support and is not promoted with any noble or near noble metals. In one aspect of the invention, the alumina support preferably includes a dopant in an amount effective for increasing the activity of the inventive catalyst. The dopant is preferably a titanium dopant. In another aspect of the invention, the cobalt catalyst is preferably reduced in the presence of hydrogen at a water vapor partial pressure effective to increase the activity of the cobalt catalyst for hydrocarbon synthesis. The water vapor partial pressure is preferably in the range of from 0 to about 0.1 atmospheres.

Fischer-tropsch activity for non-promoted cobalt-on-alumina catalysts

The synthesis of hydrocarbons and oxygenated products from carbon monoxide and hydrogen is effected by contacting in a conversion zone with a suspension of finely-divided synthesis catalyst in a gas, the concentration of catalyst in said suspension being sufficiently low to permit conversion and resultant heat release to take place at a substantially uniform rate over an extended path of contact between reactants and catalyst, unreacted gases being withdrawn and contacted with a dense turbulent fluidized catalyst mass to effect substantial completion of the conversion. Deposition of carbon and disintegration of the catalyst, especially iron catalysts, is thereby reduced. The dilute phase conversion is preferably effected in successive stages, independently controlled as to catalyst supply, density, and temperature, up to a conversion of say 50-80 per cent, the catalyst entrained in the upward flow of gas then being carried to the final dense phase from which it may be recirculated to the dilute phase stages. Preferred catalysts contain iron obtained from oxides or sulphides and promoted with alkali oxides or halides, e.g. the reduction product of Fe2O3 95.4, Al2O3 2.6 K2O 2, and SiO2 1.4 parts by weight. Dilute phase densities of 0.5-10 lb./c. ft. may be established with superficial gas velocities of 1-20 ft./sec. with particle sizes of 5-150 m , and space velocities of 2,000-20,000 v./v./hr. of fresh feed. Dense phase densities of 20-150 lb./c. ft. are obtained with gas velocities of 0.1-3 ft./sec., and space velocities of less than 5,000 v./v./hr. Classification of particles may be effected in the dense phase and those of a narrow size range circulated to the dilute phase. Temperatures may vary for example from 500-650 DEG F. in the initial zone to 550-700 DEG F. in a subsequent zone, and 600-800 DEG F. in the final dense-phase zone. Fresh feed is supplied by lines 1 and 3 to reactor 10 and iron catalyst by stand-pipe 12 from reactor 50. Conditions are controlled to give a limited turbulence and slippage of catalyst particles, sufficient to permit efficient heat transfer to the cooling surfaces 18 while permitting carry-over of catalyst to reactor 30, to which additional catalyst may be fed by stand-pipe 32, and fresh feed gas by lines 21, 23. Product gases then pass to dense phase reactor 50 provided with conventional cooling means 48. Products pass through separator 58 and separated fines are returned by pipe 60 or lines 61, 63 as desired. Clarification of particles may be effected in packing 66 and those of desired size recycled.ALSO: The synthesis of hydrocarbons and oxygenated products from carbon monoxide and hydrogen is effected by contacting in a conversion zone with a suspension of finely divided synthesis catalyst in a gas, the concentration of catalyst in said suspension being sufficiently low to permit conversion and resultant heat release to take place at a substantially uniform rate over an extended path of contact between reactants and catalyst, unreacted gases being withdrawn and contacted with a dense turbulent fluidized catalyst mass to effect substantial completion of the conversion. Deposition of carbon and disintegration of the catalyst, especially iron catalysts, is thereby reduced. The dilute phase conversion is preferably effected in successive stages, independently controlled as to catalyst supply, density, and temperature, up to a conversion of say 50-80 per cent, the catalyst entrained in the upward flow of gas then being carried to the final dense phase from which it may be recirculated to the dilute phase stages. Preferred catalysts contain iron obtained from oxides or sulphides and promoted with alkali oxides or halides, e.g. the reduction product of Fe2O3 95.4, Al2O3 2.6, K2O, and SiO2 1.4 parts by weight. Dilute phase densities of 0.5-10 lb./c.ft. may be established with superficial gas velocities of 1-20 ft./sec. with particle sizes of 5-150m and space velocities of 2,000-20,000 v/v/hr. of fresh feed. Dense phase densities of 20-150 lb./c.ft. are obtained with gas velocities of 0.1-3 ft./sec. and space velocities of less than 5,000 v/v/hr. Classification of particles may be effected in the dense phase and those of a narrow size range circulated to the dilute phase. Temperatures may vary for example from 500-650 DEG F. in the initial zone to 550-700 DEG F. in a subsequent zone, and 600-800 DEG F. in the final dense phase zone. Fresh feed is supplied by lines 1 and 3 to reactor 10 and iron catalyst by standpipe 12 from reactor 50. Conditions are controlled to give a limited turbulence and slippage of catalyst particles, sufficient to permit efficient heat transfer to the cooling surfaces 18 while permitting carry-over of catalyst to reactor 30, to which additional catalyst may be fed by standpipe 32, and fresh feed gas by lines 21, 23. Product gases then pass to dense phase reactor 50 provided with conventional cooling means 48. Products pass through separator 58 and separated fines are returned by pipe 60 or lines 61, 63 as desired. Classification of particles may be effected in packing 66 and those of desired size recycled.

Chemical reaction with fluidized solids

Citations

Synthesis of organic compounds

Reducing fischer-tropsch catalyst attrition losses in high agitation reaction systems

Calcining lime bearing sludges

Fischer-tropsch activity for non-promoted cobalt-on-alumina catalysts

Synthesis of hydrocarbons

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