Abstract: Coal is processed first through a moving bed reactor and then through a fixed bed reactor. Hot carbonized coal char is fed from the first stage reactor to the second stage reactor via a lock hopper and gas is taken off from the reactors either in separate streams or in a common stream.

Abstract: A process for withdrawing agglomerated solids, e.g. ash, from a fluidized bed of finely divided solid hydrocarbonaceous material, e.g. coal, is described. Agglomeration is effected by a high temperature reaction between the inorganic constituents of the hydrocarbonaceous material in the fluidized bed environment. A venturi is utilized to serve as a passage for withdrawing the agglomerated solids from the fluidized bed. Spiral or other descending ridges are positioned on the interior surface of the constricted cylindrical opening of the venturi to permit variable and increased rates of agglomerate discharge with improved separation and classification of the solid materials.

Abstract: A process of gasifying fine-grained solid fuels for the production of a product gas that contains hydrogen, carbon oxides and methane comprises a treatment with steam, oxygen and/or carbon dioxide in two interconnected gasifying stages under a pressure in the range from 2 to 150 bars and at temperatures of 500.degree. to 1500.degree. C. In the first gasifying stage, the fuel is gasified in a circulating fluidized bed by a treatment with gasifying stage. The residual solids which become available in the first gasifying stage are fed to the second gasifying stage and are virtually completely gasified therein, except for residual ash, by a treatment with a gasifying agent which includes oxygen. At least one-half of the product gas from the second gasifying stage is fed to the first gasifying stage and used as fluidizing fluid therein.

Abstract: Method for gasifying cellulosic material comprises feeding cellulosic material into the uphill end of an inclined rotary kiln; transporting a bed of cellulosic material through the kiln and continuously tumbling the bed; withdrawing fuel gas from the uphill end of the kiln so it flows countercurrent to the bed and removes moisture in the drying zone and thermally decompose volatiles in the devolatilization zone; admitting air overbed in the devolatilization zone and only underbed in the gasifying zone; and controlling the mass flow rate of air into the devolatilization and gasifying zones respectively as predetermined percentages of that rate of which is stoichiometric to the cellulosic material fed into the kiln to thereby limit temperature rise, prevent agglomeration and minimize entrainment of solid particles.

Abstract: Low BTU feed gas formed by gasification of carbonaceous materials with air is converted to high BTU gas by partial carbon monoxide separation and by using the reducing characteristic of the remaining feed gas in the iron reduction unit of a standard iron-steam process for manufacturing hydrogen. The hydrogen manufacturing stage also removes nitrogen which is a primary cause of low heat value in upgraded gases. The separated CO and the manufactured H.sub.2 are converted to a high quality methane. In the process, other undesirable impurities and diluents like hydrogen sulfide and carbon dioxide may be removed first.

Abstract: A process for gasifying coal and other carbonacaeous matter is disclosed which produces fuel gas containing low concentrations of polycyclic aromatic hydrocarbons. In this process the polycyclic aromatic hydrocarbons released by the coal during devolatilization and formed during pyrolysis of volatile matter are decomposed thermally in the presence of hydrogen, at a sufficiently high partial pressure (obtained by increasing the total pressure in the gasifier) to prevent polymerization of free radicals formed during pyrolysis. A relationship between the temperature, the gas residence time in the gasification reactor, the hydrogen partial pressure (i.e., total pressure in the gasifier), and the coal feed conditions are specified to achieve "clean" coal gasification.

Abstract: Method and apparatus for removing ash formed within, and accumulated at the lower portion of, a fluidized bed coal gasification reactor vessel. A supplemental fluidizing gas, at a temperature substantially less than the average fluidized bed combustion operating temperature, is injected into the vessel and upwardly through the ash so as to form a discrete thermal interface region between the fluidized bed and the ash. The elevation of the interface region, which rises with ash accumulation, is monitored by a thermocouple and interrelated with a motor controlled outlet valve. When the interface rises above the temperature indicator, the valve opens to allow removal of some of the ash, and the valve is closed, or positioned at a minimum setting, when the interface drops to an elevation below that of the thermocouple.

Abstract: A pressure container forms a shaft gasifier for receiving coarse coal in the form of a coal bed. A burner extends through the pressure container into a chamber therein and produces at least one primary gas jet directed against the coal bed, thereby gasifying the coal and generating a product gas and forming liquid slag. The liquid slag collects in a slag bath tank having an overflow weir over which the collected slag flows and falls freely toward a cooling water bath beneath the chamber. A water jet nozzle directs at least one water jet against the liquid slag as it falls freely between the weir and the cooling water bath. This atomizes the liquid slag, thereby cooling the slag and generating steam. At least a part of the steam is supplied as process steam to the coarse coal.

Abstract: A process is provided for the gasification of a carbonaceous fuel to produce a synthesis gas whereby a secondary stream of oxygen is indirectly heated from said synthesis gas and passed to the gasifier to augment the primary oxygen supply.

Abstract: An increased amount of carbon monoxide is produced in a process for the gasification of carbonaceous materials by employing a reverse water gas shift reaction in the process. Raw gas produced by the gasification of carbonaceous materials contains predominantly carbon monoxide and hydrogen along with hydrogen sulfide, carbon dioxide, water and methane. Carbon dioxide is separated from the raw gas as is the hydrogen sulfide. Thereafter, the carbon monoxide is separated from the raw gas to yield one portion of the carbon monoxide product gas. After the removal of carbon monoxide the raw gas consists of a hydrogen-rich gas. The hydrogen-rich gas which may be purified is mixed with the previously separated carbon dioxide along with any imported carbon dioxide and along with a recycle gas from a catalytic reaction loop. This mixed gas is conveyed to a heat exchanger in the catalytic reaction loop and passed through a heat exchanger located immediately after the gasifier through which the raw product gas passes.

Abstract: Disclosed is a process for converting crude carbon such as coal, carbonaceous wastes and the like into valuable chemical products and/or energy. A mass of solid crude carbonaceous fuel is fed into a high temperature liquid which acts as a solvent for carbon at a temperature sufficient to carbonize the mass and by which the carbon is separated from impurities. Volatile fractions are removed from the mass which acts as a distillation column. Air, or another oxygen source, is introduced into the reactor wherein it reacts with the carbon dissolved in the liquid therein, which may preferably be iron to form a hot fuel gas. The hot fuel gas is then used to produce useful energy, generally via a stepwise procedure.

Abstract: Gasification by reaction of carbon (e.g., in coal) with sulfur in the presence of steam, at 500.degree.-1500.degree. K., and controlled to favor production of carbon monoxide/-dioxide and hydrogen sulfide (further reactable to hydrogen and sulfur, which can be recycled). Heat generated by combustion of reaction products and/or through possible exothermic portions of the process can be utilized in the process for preheating reagents or reducing energy requirements of the main reaction.

Abstract: A process is disclosed for gasifying pelletized coal to produce a low Btu gas containing large amounts of hydrogen and carbon monoxide. Advantageously, the process is carried out on a circular traveling grate machine on a continuous basis. A horizontally moving, quiescent, gas-permeable bed of coal is formed by depositing at least one layer of a sized recycle charge of coal and at least one layer of fresh coal. To initiate an oxidizing reaction zone, the surface of one of the layers is ignited and the zone travels as a wave downwardly into the layer and upwardly into any superposed layer. Air and steam or air and carbon dioxide are either updrafted or downdrafted through the bed to control combustion. The coal is reduced in zones ahead of the advancing zone or zones of oxidation, and the reactions are terminated before the oxidation zone reaches both outermost surfaces of the bed to minimize the formation of carbon dioxide. Unreacted coal is separated from fine ash and is used as the recycle feed.

Abstract: An improved process is disclosed for the production of fuel gas such as synthetic natural gas from coal. A sized coal feed of larger particle size is gasified in a moving bed gasifier such as the British Gas/Lurgi slagging gasifier, and forms a methane rich synthesis gas containing heavy and light organics which is quenched to form a water phase containing dissolved phenolic and other compounds. The water phase is separated from the gas phase and insoluble organics and mixed with a second portion of the coal containing fine particles which are not suitable for moving bed gasification to form a slurry. This coal-phenolic water slurry is gasified in an entrained bed gasifier, for example, the Texaco partial oxidation process, and forms a methane lean synthesis gas. The phenol, ammonia and dissolved organics in the water phase are destroyed and converted to valuable product gas.

Abstract: An improved method for the generation of power in a combustion gas turbine utilizing fuel gas comprising hydrogen and carbon monoxide in which said fuel gas is subjected to a water gas shift reaction whereby said fuel gas is enriched in both hydrogen and carbon dioxide prior to combustion in said combustion gas turbine. Undesirable nickel compounds contained in said fuel gas are removed and undesirable carbonyl sulfide decomposed by said water gas shift reaction.

Abstract: Coarse, graded coal is fed to a pressurized relatively fixed bed, non-slagging gasifier from which crude gas is recovered. Fine coal is slurried in an aqueous mixture comprising the discharge from the relatively fixed bed gasifier, which discharge is composed of hydrocarbons, phenolic water and other liquids as major components and additional makeup water, if required, and the slurry is fed to a slagging, pressurized entrained flow gasifier from which additional crude gas is recovered. The two streams of gas are cleaned and then used to meet a variety of demands, including, but not limited to, gas turbine generation of electric power, manufacture of synthetic natural gas and manufacture of methanol.

Abstract: An improved method for feeding caking coal particles to a fluidized bed gasifier, without prior pretreatment, is disclosed. The coal particles are entrained in a gaseous stream and injected directly into the bottom of the fluidized bed around the outer perimeter thereof at a plurality of points and at a predetermined high velocity, such that the coal particles are shock heated and charred.

Abstract: Finely divided carbon is manufactured by a process including producing a gaseous stream containing carbon monoxide by reacting coal and air in a slagging ash gasifier, separating carbon monoxide from the gaseous mixture, and disproportionating the carbon monoxide to produce finely divided carbon and carbon dioxide, the latter of which is recycled to the gasifier.

Abstract: The present invention is directed to an improvement in the coal gasification process that effectively eliminates substantially all of the environmental pollutants contained in the producer gas. The raw producer gas is passed through a two-stage water scrubbing arrangement with the tars being condensed essentially water-free in the first stage and lower boiling condensables, including pollutant laden water, being removed in the second stage. The pollutant-laden water is introduced into an evaporator in which about 95 percent of the water is vaporized and introduced as steam into the gas producer. The condensed tars are combusted and the resulting products of combustion are admixed with the pollutant-containing water residue from the evaporator and introduced into the gas producer.

Abstract: A method of operating an entrained flow coal gasifier which comprises the steps of firing coal at two levels in a combustion zone with near stoichiometric air, removing molten ash from the combustion zone, conveying combustion products upwardly from the combustion zone through a reduction zone, injecting additional coal into the combustion products in the reduction zone and gasifying at least a portion of the coal to form low BTU gas, conveying the gas to a point of use, including also reducing gasifier output by modifying the ratio of air to coal supplied to the upper level of the combustion zone so that the ratio becomes increasingly substoichiometric thereby extending the gasification of coal from the reduction zone into the upper level of the combustion zone, and maintaining the lower level of coal in the combustion zone at near stoichiometric conditions so as to provide sufficient heat to maintain effective slagging conditions.

Abstract: An entrained flow coal gasifier wherein a high temperature product gas stream is essentially formed by burning char with air. Additional char, formed by partial gasification of coal, is added immediately thereafter to obtain the gasification reaction. Fresh coal is thereafter supplied in a lower temperature region thereby obtaining the volatile components driven off at a relatively low temperature.

Abstract: A method is described for the discharge of solids from a coal gasifier grate at different radial locations.

Abstract: This invention relates to a new and novel method and apparatus for reacting nongaseous material with a gaseous reactant comprising introducing a first stream containing a nongaseous material into a reaction zone; simultaneously introducing a second stream containing a gaseous reactant into the reaction zone such that the gaseous reactant immediately contacts and reacts with the first stream thereby producing a gaseous product; forming a spiralling vortex within the reaction zone to cause substantial separation of gases, including the gaseous product, from the nongaseous material; forming and removing a third stream from the reaction zone containing the gaseous product which is substantially free of the nongaseous material before a major portion of the gaseous product can react with the nongaseous material; and forming and removing a fourth stream containing the nongaseous material from the reaction zone.

Abstract: A single reactor is used for gasifying solid fuels of a wide range of particle sizes without first comminuting the particles to a common size. The larger particles are gasified on a fixed bed, and the smaller ones are gasified on a fluidized bed. In the reactor, the fluidized bed is arranged above the fixed bed and gases rising from the fixed bed help to fluidize the fluidized bed. In addition, a dust gasification region can be provided above the fluidized bed.

Abstract: A method of producing form coke that is coke having pieces of substantially identical form using a heated shaft furnace comprises mixing fine coke with a caking coal and pressing the mixture at temperatures at which the mixture is plastic in order to form briquettes. The briquettes are permitted to harden and degasify and thereafter they are exposed to a high temperature after hardening for example to a temperature of from 400.degree. to 900.degree. C from 60 to 120 minutes. Thereafter the briquettes are cooled. A first mixing substance is prepared by permitting a fine coal to fall in a non-compressed stream in the shaft furnace while heat is transferred thereto substantially by radiation.

Abstract: The high temperature gasification of solid fuel or mixtures of solid and liquid fuels is carried out by a method and apparatus wherein the gasified product from a high temperature gasification chamber having a slag bath therein is fed into a first dust collector. Gases, including vapors or aerosols, are fed from the dust collector into a waste heat boiler to reduce the temperature of the gases down to about 250.degree. C. The solids which essentially include flue coke are discharged from the dust collector into a separate heat exchanger wherein the temperature of the solids is reduced down to about 200.degree. C. The cooled solids and the cooled gases are fed into an absorption chamber wherein for a period of 1 to 10 seconds, the aerosols are absorbed into the flue coke. The absorption chamber is connected to a second dust collector that separates the gases from the flue coke having the absorbed aerosols.

Abstract: A process for the production of combustible gas from waste materials and other combustible materials, in which the charge is dried, its combustible parts are subjected to low-temperature carbonization and the low-temperature carbonization gases are converted to combustible gas in a hot reaction bed. The charge is subjected to low-temperature carbonization at a temperature of from 300.degree. to 600.degree. C with the exclusion of air, the resulting solid low-temperature carbonization residues are separated and the low-temperature carbonization gases are continuously drawn through a reaction bed at a temperature of from 1000.degree. to 1200.degree. C formed from a solid carbon vehicle and a preheated fresh-air supply, and are converted to high-energy combustible gas in said reaction bed.

Abstract: A process for the production of a synthesis gas, capable of being upgraded to a high BTU pipeline gas, by the partial oxidation and substantially complete gasification of a carbonaceous material under CO-promoting conditions wherein the carbonaceous material, oxygen, and recycled carbon dioxide from the process are introduced into a molten salt containing an alkali metal carbonate and a minor portion of an alkali metal sulfide, the system being operated at a selected temperature and pressure between 1400.degree. and 2000.degree. F and between 1 and 100 atmospheres. The molar ratio of carbon dioxide to oxygen employed is controlled at from about 0.6:1 to about 1.2:1 to control the CO production and also to maintain the molten salt at a desired operating temperature. Sulfur and ash introduced with the fuel are retained in the molten salt.

Abstract: Pulverized coal having a sulfur content of up to 2.5% is introduced into a gasification vessel together with air preheated to a temperature above 900.degree. F. The pulverized coal and preheated air react in the gasification vessel which is operated at temperatures in excess of 1800.degree. F. with a residence time of less than three seconds therein. The reaction between the concurrent downwardly flowing coal and air produces a product comprising partially gasified char entrained in a product gas comprising methane, hydrogen, hydrogen sulfide and oxides of carbon. The partially gasified low sulfur char entrained in the product gas is withdrawn from the gasifier and conducted to a waste heat boiler to provide steam as a source of energy for power generation. Thereafter, the low sulfur char is separated from the product gas and fed to a char storage hopper which maintains the char at a temperature above 900.degree. F. and preferably above 1100.degree. F.

Abstract: A combination process is provided for residua demetalation and desulfurization and resulting coke gasification which comprises contacting said residua with a porous refractory oxide in the absence of added hydrogen, at a temperature of from greater than 700.degree.F to about 1100.degree.F and a refractory oxide to oil weight ratio of from about 0.1 to about 5 to produce upgraded residua of cracking feed quality, and contacting said refractory oxide after an amount of coke has formed thereon with steam and a free oxygen containing gas in which the mole ratio of steam to oxygen is from about 3 to about 5, at a temperature of from about 1000.degree.F to about 1500.degree.F to produce producer gas and regenerated porous refractory oxide for further contacting with residua.

Abstract: A method and apparatus for gasifying coal wherein the gasification takes place in a spout fluid bed at a pressure of about 10 to 30 atmospheres and a temperature of about 1800.degree. to 2200.degree.F and wherein the configuration of the apparatus and the manner of introduction of gases for combustion and fluidization is such that agglomerated ash can be withdrawn from the bottom of the apparatus and gas containing very low dust loading is produced. The gasification reaction is self-sustaining through the burning of a stoichiometric amount of coal with air in the lower part of the apparatus to form the spout within the fluid bed. The method and apparatus are particularly suitable for gasifying coarse coal particles.

Abstract: A process for producing hot combustible gas free of sulfur, halogens and particulate matter. The process comprises passing oxygen, steam and/or carbon dioxide through a reaction zone containing an alkali or alkaline earth metal oxide, hydroxide, bicarbonate or carbonate and a carbonaceous fuel such as coal. The sulfur and halogen in the carbonaceous fuel are removed resulting in a combustible gas substantially free of sulfur, halogens and particulate matter.

Abstract: This is an improved continuous partial oxidation process for producing synthesis gas or fuel gas from a solid carbonaceous fuel. Liquid CO.sub.2 and a ground solid carbonaceous fuel such as coal are mixed together to produce a pumpable slurry feed. The CO.sub.2 serves as a carrier for the carbonaceous fuel and as a temperature moderator, and is preferably obtained by purifying the product gas.

Abstract: This is an improved continuous partial oxidation process for producing synthesis gas or fuel gas from gaseous CO.sub.2 -solid carbonaceous fuel feeds. A solid carbonaceous fuel such as finely ground coal from a pressurized lock hopper is passed directly into a high pressure high velocity CO.sub.2 -rich gas stream which carries the particles of coal into a free-flow noncatalytic gas generator where by the partial oxidation reaction with a free-oxygen containing gas, preferably in the absence of supplemental H.sub.2 O other than that normally present in the reactants, gaseous mixtures principally comprising H.sub.2, CO, CO.sub.2, and H.sub.2 O are produced. A CO.sub.2 -rich gas stream is recovered downstream in the process and recycled to the pressurized feed system. The CO.sub.2 -rich stream serves as a carrier for the carbonaceous fuel and as a reactant in the reaction zone.

Abstract: Substantially sulfur-free combustible fuel gas under superatmospheric pressure is produced by partial combustion or gasification under superatmospheric pressure of a sulfur-containing solid, liquid or gaseous fuel. The gasification is effected within a fluidized bed of particles containing alkaline earth metal compounds (e.g. the oxides) which are capable of reacting with, and of fixing, the fuel sulfur as sulfides under reducing conditions. Sulfide-containing particles are exposed to an oxidizing atmosphere and the sulfides are thereby converted to oxides with the liberation of SO.sub.2 in useful concentrations, and with the liberation of heat. Particles containing regenerated oxides are re-used for fixing more sulfur during fuel gasification. Expedients are described by which it is ensured that the sulfur-fixing activity of the particles is substantially maintained and that the temperatures of the particles during sulfur-fixing and regeneration are maintained within predetermined ranges.

Abstract: The gaseous product obtained by the partial oxidation of a fuel such as coal and/or oil is desulfurized and then admitted into a packed gas-liquid contact column. Here, the gas comes into contact with water so as to become at least partially saturated with water vapor. The gas is next conveyed to a reactor wherein it undergoes a methane-forming reaction under isothermal conditions, the methane-forming reaction taking place without previously subjecting the gas to a conversion reaction. The methane-forming reaction is carried out catalytically with a nickel-containing catalyst and deposition of carbon from the gas onto the catalyst is prevented by virtue of the water vapor present during the reaction. The quantity of water vapor present during the reaction is adjusted so as to lie between predetermined limits. After completion of the reaction, the gas is admitted into another packed gas-liquid column wherein it is cooled by contact with cooling water at which time residual water vapor in the gas condenses.

Abstract: Granulated coals or cokes derived from coal, in sizes up to about 3/4 inch and containing ash matter with an initial deformation temperature below about 2,300.degree.F, are fed to a slow fluidized bed comprising relatively large particles of coke intermingled with roughly spherical ash agglomerates, maintained at about 1,900.degree.F to about 2,450.degree.F, and supplied with a gasification medium, for example, steam mixed with oxygen or air. A fast fluidized bed of coke fines is superimposed above the slow bed and is contiguous therewith. Gasification products are discharged together with relatively fine particles of coke, which are collected and returned to the fast bed. Ash agglomerates are withdrawn from the bottom of the slow bed via a standpipe leading to a slagging grate. Combustion of coke fines in a forehearth beneath the slagging grate creates slagging temperatures therein and at the grate. Molten slag falls through a taphole and into a pool of water, from which slag frit and water are discharged.

Abstract: Granulated coals or cokes derived from coal, in sizes up to about 3/4 inch and containing ash matter with an initial deformation temperature above about 2,300.degree.F, are fed to a slow fluidized bed comprising relatively large particles of coke intermingled with roughly spherical ash agglomerates, maintained at about 2,050.degree.F to 2,650.degree.F, and supplied with a gasification medium, for example, steam mixed with oxygen or air. A fast fluidized bed of coke fines is superposed above the slow bed and is contiguous therewith. Gasification products are discharged together with relatively fine particles of coke, which are collected and returned to the fast bed. Ash agglomerates are withdrawn from the bottom of the slow bed via a standpipe leading to a mechanical grate. An oxidizing medium is introduced below the grate to consume coke particles that accompany the ash agglomerates entering the standpipe.