Abstract: Synthesis gas, reducing gas, or fuel gas is produced by the partial oxidation of ash-containing solid carbonaceous and/or liquid hydrocarbonaceous fuel at an autogenous temperature in the range of about 20.degree. F. to 200.degree. F. below the softening temperature of the ash in said fuel, and at a pressure in the range of about 17 to 100 atmospheres to produce a raw effluent gas stream containing entrained carbon-rich fly-ash which is separated from the effuent gas stream. A fuel mixture comprising about 20 to 100 wt. % of said carbon-rich fly-ash and about 0 to 80 wt. % of a supplemental fuel is reacted by partial oxidation at an autogenous temperature of about 100.degree. F. above the ash-fusion temperature, and at a reduced pressure e.g. in the range of about 1 to 16 atmospheres and at least 16 atmospheres below the pressure in the partial oxidation reaction used to produce said carbon-rich fly-ash.

Abstract: Synthesis gas, reducing gas, or fuel gas is produced by the partial oxidation of bituminous coal at an autogenous temperature in the range of about 2000.degree. F. to 2700.degree. F. and at a pressure in the range of about 17 to 100 atmospheres to produce a raw effluent gas stream containing entrained molten slag and carbon-rich particulate material. After cooling, course slag and carbon-rich particulate material are separated. A fuel mixture comprising about 20 to 100 wt. % of said carbon-rich particulate material and the remainder comprising a supplemental fuel is reacted by partial oxidation at an autogenous temperature of about 2000.degree. F. to 2700.degree. F. and at a reduced pressure e.g. in the range of about 1 to 16 atmospheres and at least 16 atmospheres below the pressure in the partial oxidation reaction used to produce said carbon-rich particulate material.

Abstract: Synthesis gas is produced by the partial oxidation of a feedstock comprising petroleum coke containing metal sulfide compounds and metal oxy-sulfide compounds and having an ash that contains nickel, vanadium and silicon. In the process, a petroleum coke addition agent, such as elemental iron and/or iron compounds, is introduced into the upper section of a delayed coker and above the level of the nickel and vanadium ash-containing heavy liquid hydrocarbonaceous fuel being simultaneously introduced upwardly from the bottom of said delayed coker. By this means the petroleum coke addition agent is distributed uniformly across the surface of liquid hydrocarbonaceous material being coked and then uniformly distributed throughout the liquid fuel. In the delayed coker, a portion of the petroleum coke addition agent is reacted with a portion of the sulfur in the heavy liquid hydrocarbonaceous fuel to produce metal oxy-sulfides and metal sulfides.

Abstract: Aqueous slurries of solid carbonaceous fuel having an increased reactivity of the solid material are produced by maintaining the solid carbonaceous fuel-water slurry at a temperature in the range of about 300.degree. to 650.degree. F. and a pressure in the range of about 100 to 3500 psia and sufficient to maintain the H.sub.2 O in the slurry in liquid phase; at substantially constant temperature depressurizing said slurry to a pressure in the range of about above atmospheric to 250 psia above that in the reaction zone of a partial oxidation gas generator, thereby partially vaporizing the water in the slurry and producing steam. After depressurizing, the slurry is cooled so that the solid particles drop in temperature about 2.degree. F. to 10.degree. F. and the water in the slurry drops in temperature about 100.degree. F. to about 200.degree. F.

Abstract: Outlet structure of a powdered coal gasification generator. The bottom of the generator has an outlet throat with cylindrical walls that extend beyond the base. And, the walls terminate in an oblique manner with a face shaped to promote flow of slag from the generator to a single point in order to minimize reentrainment of slag into the gasification products.

Abstract: Activated agglomerated carbon may be prepared by leaching with a hydrohalic acid followed by displacement of the residual halide with organic carboxylate during subsequent washing with a water-soluble organic carboxylic acid or a water-soluble ammonium salt of an organic carboxylic acid.

Abstract: Methane-rich gas is produced by reacting gas mixtures comprising CO and at least one member selected from the group consisting of H.sub.2 and H.sub.2 O, such as synthesis gas, in a reactor containing an improved unsupported catalyst comprising an alkali-metal promoted partially reduced mixture of at least one nickel uranate and at least one oxide of nickel. The weight percent uranium present in the activated catalyst, based on total weight of catalyst composition, is in the range of over 50 to about 90.

Abstract: Hydrogen-rich gas is produced by reacting gas mixtures comprising CO and H.sub.2 O in a reactor containing an improved unsupported catalyst comprising an alkali-metal promoted partially reduced mixture of at least one copper uranate and at least one oxide of copper. The weight percent uranium present in the activated catalyst, based on total weight of catalyst composition, is in the range of over 50 to about 90.

Abstract: A high temperature solids gasification generator which employs finely divided solids, e.g. powdered coal, has a down flow and discharges into a plenum chamber below the generator. The plenum chamber has a restricted outlet at the bottom so that a pool of liquid slag will form, and there is a lateral outlet above the slag pool for effluent gas. The lateral outlet has its throat located offset farther from the axis of the plenum chamber than the inside radius of the chamber.

Abstract: Methane-rich gas is produced by reacting gas mixtures comprising CO and at least one member selected from the group consisting of H.sub.2 and H.sub.2 O, such as synthesis gas, in a reactor containing an improved unsupported catalyst comprising an alkali-metal promoted partially reduced mixture of at least one nickel uranate and at least one oxide of nickel. The weight percent uranium present in the activated catalyst, based on total weight of catalyst composition, is in the range of over 50 to about 90.

Abstract: Disclosed are a catalyst composed of a hydride of a rare earth and a transition metal, such as LaNi.sub.5 or LaCo.sub.5, and a reaction of H.sub.2 and CO to produce oxygenated hydrocarbons catalyzed by this catalyst. The reaction takes place at room temperature and at relatively low pressure.

Abstract: Nitrated hydrocarbons, such as nitroparaffins, are reduced to amines by use of palladium on a carbon catalyst characterized by low ash and low halide.

Abstract: A process for converting mixtures of C.sub.6 to C.sub.30 n-paraffin and n-paraffin by-products to substantially pure n-paraffin which comprises catalytically hydrogenating the mixture at a temperature of from about 600.degree. to 750.degree. F. in the presence of a Group VIII metal on alumina catalyst where the catalyst contains from about 0.05 to 2.0 weight percent of an alkali metal oxide or alkaline earth metal oxide or thallous oxide. The catalyst can additionally contain a Group VIB or VIIB metal.

Abstract: A process for converting mixtures of C.sub.6 to C.sub.30 n-paraffin and n-paraffin by-products to substantially pure n-paraffin which comprises catalytically hydrogenating the mixture at a temperature of from about 600.degree. to 750.degree. F. in the presence of a Group VIII metal on alumina catalyst where the catalyst contains from about 0.05 to 2.0 weight percent of an alkali metal oxide or alkaline earth metal oxide or thallous oxide. The catalyst can additionally contain a Group VIB or VIIB metal.

Abstract: A process for producing secondary alcohols from n-paraffins wherein a portion of the n-paraffin is converted to a borate ester along with oxygenated by-products and the borate ester is separated and hydrolyzed to a secondary alcohol. The mixtures of C.sub.6 to C.sub.30 n-paraffin and n-paraffin by-products are converted to substantially pure n-paraffin by catalytically hydrogenating the mixture at a temperature of from about 600.degree. to 750.degree. F. in the presence of a Group VIII metal on alumina catalyst where the catalyst contains from about 0.05 to 2.0 weight percent of an alkali metal oxide or alkaline earth metal oxide or thallous oxide. The catalyst can additionally contain a Group VIB or VIIB metal.

Abstract: A process for converting mixtures of C.sub.6 to C.sub.30 n-paraffin and n-paraffin by-products to substantially pure n-paraffin which comprises catalytically hydrogenating the mixture at a temperature of from about 600.degree. to 750.degree. F. in the presence of a Group VIII metal on alumina catalyst where the catalyst contains from about 0.05 to 2.0 weight percent of an alkali metal oxide or alkaline earth metal oxide or thallous oxide. The catalyst can additionally contain a Group VIB or VIIB metal. The n-paraffin is photochemically reacted with a gaseous nitrosating agent to form paraffin oximes and by-products and the by-products are recycled for catalytic hydrogenation.

Abstract: A process for converting mixtures of C.sub.6 to C.sub.30 n-paraffin and n-paraffin by-products to substantially pure n-paraffin which comprises catalytically hydrogenating the mixture at a temperature of from about 600.degree. to 750.degree.F. in the presence of a Group VIII metal on alumina catalyst, and from about 10 to 5,000 parts per million of nitrogen present as ammonia or an organonitrogen compound. The catalyst can additionally contain a Group VIB or VIIB metal.

Abstract: A process for converting mixtures of C.sub.6 to C.sub.30 n-paraffin and n-paraffin by-products to substantially pure n-paraffin which comprises catalytically hydrogenating the mixture at a temperature of from about 600.degree. to 750.degree.F. in the presence of a Group VIII metal on alumina catalyst, and from about 10 to 5,000 parts per million of nitrogen present as ammonia or an organonitrogen compound. The catalyst can additionally contain a Group VIB or VIIB metal.

Abstract: A process for converting mixtures of C.sub.6 to C.sub.30 n-paraffin and n-paraffin by-products to substantially pure n-paraffin which comprises catalytically hydrogenating the mixture at a temperature of from about 600.degree. to 750.degree.F. in the presence of a Group VIII metal on alumina catalyst, and from about 10 to 5,000 parts per million of nitrogen present as ammonia or an organonitrogen compound. The catalyst can additionally contain a Group VIB or VIIB metal.

Abstract: A process for converting mixtures of C.sub.6 to C.sub.30 n-paraffin and n-paraffin by-products to substantially pure n-paraffin which comprises catalytically hydrogenating the mixture at a temperature of from about 600.degree. to 750.degree.F. in the presence of a Group VIII metal on alumina catalyst, and from about 10 to 5,000 parts per million of nitrogen present as ammonia or an organonitrogen compound. The catalyst can additionally contain a Group VIB or VIIB metal.