Abstract: Carbon is gasified with steam in the presence of a catalytic metal such as nickel by forming a dispersion of the metal on graphite wherein the average particle size of the dispersed metal is below about 100 A and preferably below 25 A in diameter and contacting the dispersed metal/graphite composite with steam at about 800.degree. C. or higher to gasify the graphite. This process will also gasify mixtures of graphite and amorphous carbon.

Abstract: In the preparation of the gaseous reactant feed to undergo a chemical reaction requiring the presence of steam, the efficiency of overall power utilization is improved by premixing the gaseous reactant feed with water and then heating to evaporate the water in the presence of the gaseous reactant feed, the heating fluid utilized being at a temperature below the boiling point of water at the pressure in the volume where the evaporation occurs.

Abstract: Disclosed is a method for recovering oil and gas from carbonaceous materials utilizing two molten baths. In the first molten bath reaction vessel, the carbonaceous material is thermally devolatilized. Part of the first melt from the first reaction vessel containing non-volatile constituents is passed to the second molten bath reaction vesel which contains a different melt at a higher temperature. The two melts are only partially soluble in each other so that they can be easily separated. Oxygen, air or oxides are charged to the second reaction vessel for gasifying residual quantities of carbon by oxidation. The first melt is returned to the first reaction vessel from the second reaction vessel. The melt in the first reaction vessel may comprise lead or zinc and be maintained at a temperature of 500.degree. C., while the melt in the second reaction vessel may comprise raw iron and be maintained at a temperature of 1200.degree. C.

Abstract: A three stage hydrogen generator (10), comprises a low BTU, carbon monoxide and hydrogen containing gas generation stage, a first reactor stage (12) for exothermically reducing ferric oxide with the low BTU gas and for generating superheated steam and a second reactor stage (14) for endothermically reacting steam and iron to produce substantially pure hydrogen gas. The hydrogen gas together with unreacted steam from the third stage (16) is directed to a condenser (18), preferably an air cooled unit, wherein the steam is condensed and the hydrogen gas recovered. The condensate (20) is cycled back to the second reactor (14) as the feed water for generating superheated steam and the heated cooling air (22) is directed to the first stage (12) for use in the generation of the low BTU gas. At least one, and preferably all, of the stages utilize a rotating fluidized bed. Desirably the condenser (18) is a rotating fluidized bed heat exchanger.

Abstract: The present invention is directed to a coal-water slurry atomizer for use a high-pressure dryer employed in a pumping system utilized to feed coal into a pressurized coal gasifier. The slurry atomizer is provided with a venturi, constant area slurry injection conduit, and a plurality of tangentially disposed steam injection ports. Superheated steam is injected into the atomizer through these ports to provide a vortical flow of the steam, which, in turn, shears slurry emerging from the slurry injection conduit. The droplets of slurry are rapidly dispersed in the dryer through the venturi where the water is vaporized from the slurry by the steam prior to deleterious heating of the coal.

Abstract: A process for the partial oxidation of pumpable slurries of solid carbonaceous fuels in which the pumpable slurry of solid carbonaceous fuel in a liquid carrier is passed in liquid phase through one passage of a burner comprising a retracted central coaxial conduit, an outer coaxial conduit with a converging orifice at the downstream tip of the burner and, optionally, an intermediate coaxial conduit. The downstream tips of the central conduit and the intermediate conduit, if any, are retracted upstream from the burner face a distance of respectively two or more say 3 to 10 for the central conduit, and about 0 to 12 say 1 to 5 for the intermediate conduit times the minimum diameter of the converging orifice of the outer conduit at the burner tip. A pre-mix zone is thereby provided comprising one or more, say 2 to 5 coaxial pre-mix chambers in series.

Abstract: Apparatus for thermally decomposing and gasifying either liquid or solid combustible material in a single reactor filled with working medium in a high active fluidization, said reactor being provided with two partitions, one of which is extended downwards up to the lower portion of the reactor, while the other is vertically extended at the lower and middle portions thereof substantially at a right angle to the first partition, whereby the reactor is divided into two sections, that is, thermal decomposition and gasification section and combustion and heating section, so that thermal decomposing and gasifying are performed by way of supplying the combustible raw material into the downwardly travelling working medium and at the same time supplying steam thereinto for generating and maintaining the high active fluidization of the working medium in the thermal decomposition and gasification section, while burning and heating are performed by way of supplying air or steam mixture gas of oxygen and steam into the up

Abstract: Method for generating methane or synthesis gas from carbon-containing materials, e.g. coal, by reacting part of the carbon with hydrogen in a hydrogenating gasifier to produce a methane containing gas, and reacting the residual carbon with steam in a steam gasifier to produce a raw gas containing synthesis gas. Features are:(a) The steam gasifier is heated with the raw gas leaving the hydrogenating gasifier.(b) The hydrogen gas entering the hydrogenating gasifier is heated with the raw gas leaving the steam gasifier.(c) The output stage of the steam gasifier is heated electrically.(d) The entire nuclear heat is given off to a steam loop.In addition a methane cracking furnace may be provided with the following features:(a) The methane cracking furnace is heated electrically in the upper temperature range.(b) The raw gas leaving the methane cracking furnace serves for heating the entering methane.

Abstract: Carbonaceous solids are contacted in the presence of water with potassium sulfate and a calcium compound selected from the group consisting of calcium oxide, calcium hydroxide, and calcium carbonate thereby producing treated carbonaceous solids which are then gasified. The calcium compound apparently activates the relatively noncatalytic potassium sulfate thereby producing a substantial catalytic effect on the gasification reactions.

Abstract: In a coal gasification operation or similar conversion process carried out in the presence of an alkali metal-containing catalyst wherein solid particles containing alkali metal residues are produced, alkali metal constituents are recovered from the particles primarily in the form of water-soluble alkali metal sulphites and bisulphites by treating the particles with a solution of sulfurous acid. During the treating process the water-insoluble alkali metal compounds in the alkali metal residues are converted into water-soluble alkali metal sulphites and bisulphites, which have been found to be catalytically active.

Abstract: A water jacket for coal gasification in which the gas producer is provided with an inwardly directed collar spaced from the water jacket and a plurality of apertures through the collar formation such that the collar can assist in supporting the refractory material of the wall of the gas producer.

Abstract: In a process for producing synthesis gas by reacting a solid carbonaceous fuel with water in the presence of a carbon dioxide acceptor to produce a synthesis gas rich in hydrogen with at least a portion of the carbon dioxide so produced being reacted with the carbon dioxide acceptor to produce calcium carbonate and to provide sufficient heat to maintain a desired reaction temperature, an improvement comprising; the use of finely-divided wood as the solid carbonaceous fuel.

Abstract: An automatic arrangement in which the intermittent tapping of liquid molten slag from the hearth of a slagging coal gasifier vessel (30) through a tap orifice (32) into a slag quench chamber (31) is selectively controlled by a system of timers (T1, T2, T3), the differential pressure between the gasifier vessel (30) and the quench chamber (31) being measured (22) and deviations from the expected measurements caused by malfunctions being used to override the timer system until the malfunctions have been corrected.

Abstract: The novel gasification reactor comprises a vertically oriented chamber with an upper pyrolysis section, a lower feed opening, and a primary combustion section. A lateral passage on each side and near the top of said primary combustion section each communicates with a separate secondary reaction chamber where a partially reacted feed is further reacted to form the product gas. In each passageway is a venturi nozzle or preferably a plurality of nozzles which accelerates the gas carrying entrained carbonaceous materials to produce a swirling curvilinear motion in the secondary reaction chambers.The reactor is fed by means of a plurality of hoppers and screw conveyors whereby the flow is regulated and positively fed both by gravity and the screw conveyors into rotary valve cavities in which counter rotating valves travel. The valves feed a piston which charges the reactor.

Abstract: An integrated fluid coking and gasification process is provided in which a portion of the coke is gasified in a first gasification zone in the presence of an oxygen-containing gas to produce a hot gas and hot coke. A portion of the resulting hot coke is gasified in a second gasification zone in the presence of steam to produce a gas comprising hydrogen and carbon monoxide, which is suitable, after conventional shift and clean up, for use as synthesis gas.

Abstract: The digestion of the cellulose-containing material is performed with a digestion liquor containing sulphur and sodium followed by recovery and regeneration of said digestion liquor and bleaching of the cellulose-containing material with chlorine dioxide. The SO.sub.2 -containing and possibly chloride-containing gas from the recovery boiler (11) of the process and from combustion of evil-smelling gases (20) is absorbed in an absorption liquor containing and alkali metal salt solution free of sulphur or sulphur compounds such as sulphide or thiosulphate, in a scrubber (27). The resulting scrubber liquor is mixed with acid residual solution (26) from the manufacture of chlorine dioxide, whereby sulphur dioxide (32) in gaseous state is returned to the process, whereafter the residual solution (34) free from SO.sub.

Abstract: Generating methane or synthesis gas from carbon-containing materials, e.g. coal, by reacting part of the carbon with hydrogen in a hydrogenating gasifier to produce a methane containing gas, and reacting the residual carbon with steam in a steam gasifier to produce a raw gas containing synthesis gas, which latter may be converted to hydrogen and directed to the hydrogenation gasifier or may at least in part be used as a product. The steam gasifier is heated with raw gas leaving the hydrogenating gasifier. The hydrogen gas entering the hydrogenation gasifier is heated with the raw gas leaving the steam gasifier. At least part of the methane is reacted with steam to synthesis gas while heat is being supplied.

Abstract: The invention concerns a method for the operation of gasification plants for pulverized fuels, wherein the pulverized fuel is reacted in a flame reaction with a gasifying agent containing free oxygen, into a combustible gas containing CO and H.sub.2. The task consists in precluding upon malfunctions in the supply of fuel, an oxygen discharge into the cooling and treatment plants, taking into consideration delays in the emergency shut-off systems and the controls for the oxygen supply.As per invention, a well-flowing additional fuel is stored in a reservoir at a pressure higher than the operating pressure of the gasification reactor. Upon malfunctions in the fuel supply, the additionally stored fuel will be transferred, within a short time, into the reaction chamber of the gasification plant. As additional well-flowing fuel combustible gas, liquid fuel or a pulverized solid fuel, also well-flowing, can be used.

Abstract: A hot raw gas stream, as produced by the partial oxidation of a solid carbonaceous fuel such as coal, is partially cooled and cleaned to remove entrained solid matter and slag. A novel gas--gas quench cooling and solids separation apparatus is employed. The apparatus comprises a closed cylindrical insulated vertical pressure vessel containing a lower quench chamber in communication with an upper solids separation chamber. The hot raw gas stream is cooled in the lower chamber to a temperature below the initial deformation temperature of the entrained slag by impingement and direct heat exchange with an oppositely directed coaxial stream of cooled, cleaned, and compressed recycle quench gas. The stream of cooled gas leaving the turbulent lower chamber passes up through a choke-ring into the comparatively calmer upper chamber counter-currently with solid slag droplets which separate out by gravity.

Abstract: A process for improved gas production and accelerated stabilization of landfills by accelerated in situ bioleaching of organic wastes by acid forming bacteria in substantially sealed landfills, passing the leachate of hydrolysis and liquefaction products of microbial action of the microorganisms with the organic material to an acid phase digester to regenerate the activated culture of acid forming microorganisms for recirculation to the landfill, passing the supernatant from the acid phase digester to a methane phase digester operated under conditions to produce methane rich gas. The supernatant from the methane phase digester containing nutrients for the acid forming microorganisms and added sewage sludge or other desired nutrient materials are circulated through the landfill. Low Btu gas is withdrawn from the acid phase digester while high Btu gas is withdrawn from the methane phase digester and may be upgraded for use as SNG.