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: A process is disclosed for gasifying solid coal particles in a rotary kiln that produces simultaneously and continuously two distinctly different fuel gas streams from the opposite ends of a single kiln. A relatively low temperature gas is discharged from the solids inlet end of the kiln, which contains substantially all tars produced by the process. A second of the gas streams is discharged from the solids discharge end of the kiln at approximately 1,900.degree. F. and substantially tar-free. Heat is recovered from this tar-free gas after only a simple cleaning of particulate matter, as may be provided by a cyclone separator.

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 partial oxidation process using a swirl burner for producing synthesis gas, fuel gas or reducing gas from slurries of solid carbonaceous fuel and/or liquid or gaseous hydrocarbon fuel. The swirl burner may have pre-mix and/or high turndown features. By means of the burner a first reactant stream is split into a plurality of swirling streams by being passed down through a central bundle of helical tubes. Simultaneously a second reactant stream is split into a plurality of swirling streams by being passed down through a plurality of related passages formed in the cylindrical space that surrounds said central bundle of helical tubes and/or the interstices between the helical tubes. When the two swirling reactant feed streams impinge, either upstream from the face of the burner in a pre-mix zone or downstream from the face of the burner, in the gas generator, they are intimately mixed together. The combustion efficiency of the burner is thereby improved.

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 method for starting up a partial oxidation gas generator without a separate preheat burner is described. The burner used includes central and annular bunches of parallel tubes that extend through central and annular passages formed by concentric conduits.

Abstract: Disclosed is a partial oxidation process for producing synthesis gas, fuel gas or reducing gas from slurries of solid carbonaceous fuel and/or liquid or gaseous hydrocarbon fuel. The burner has a high turndown feature and comprises a central conduit; a central bunch of parallel tubes that extend longitudinally through said central conduit; an outer conduit coaxial with said central conduit and forming an annular passage therewith; and an annular bunch of parallel tubes that extend longitudinally through said annular passage; and wherein the downstream ends of said central and annular bunches of parallel tubes are respectively retracted upstream from the burner face a distance of about 0 to 12 i.e. 3 to 10 times the minimum diameter of the central exit orifice and the minimum width of the annular exit orifice. Three ranges of flow through the burner may be obtained by using one or both bunches of tubes and their surrounding conduits.

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: 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: 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 hot raw synthesis gas stream leaving the reaction zone of a free flow partial oxidation gas generator at a temperature in the range of about 1800.degree. to 3000.degree. F. is passed through a first gas diversion and residue separation zone where the velocity of the gas stream is reduced and its direction is diverted into a side transfer line. Solid material and molten slag separate by gravity from the gas stream. The hot gas stream is then introduced into a second gas diversion and residue separation zone where the direction and velocity is changed and additional residue is separated. About 0.5 to 20 vol. % of the hot gas stream may be passed through bottom outlets in said first and second gas diversion zones in order to prevent bridging. The hot gas stream from the second gas diversion zone is passed upwardly through a radiant cooler where additional solid matter is removed by gravity and the gas temperature is reduced to a temperature in the range of about 900.degree. to 1800.degree. F.

Abstract: The hot raw synthesis gas stream leaving the reaction zone of a free flow partial oxidation gas generator at a temperature in the range of about 1800.degree. to 3000.degree. F. is passed through a first gas diversion and residue separation chamber where the velocity of the gas stream is reduced and its direction is diverted into a side transfer line. Solid material and molten slag separate by gravity from the gas stream. The hot gas stream is then introduced into second gas diversion and residue separation zone comprising at least one thermally insulated gas-solids impingement separation means were additional solid matter and slag is separated. For example, from about 2 to 8 thermally insulated gas-solids impingement separators may be employed which are connected in parallel and/or series. In one embodiment, about 0 to 20 vol. % of the hot gas stream may be passed through bottom outlets in said first and second gas diversion zones in order to prevent bridging.

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 pyrolyzing apparatus having a pyrolysis fluidized bed chamber and an incineration fluidized bed chamber or chambers each directly adjacent and communicated with the pyrolysis fluidized bed chamber through an opening or openings in a partition wall above a common perforated bottom plate, the respective levels of the fluidized beds being controlled by regulating the pressure(s) in free board(s) of the fluidized bed chambers.

Abstract: A multiple-zone fluidized bed coal conversion process for producing fuel gas and distillate liquid products. The coal is fed into an upper fluidized bed maintained at 950.degree.-1500.degree. F. for devolatilization. The resulting coke and some tars are deposited on a particulate carrier material, which descends along with the larger particles of unreacted coal through a stripping zone into a lower fluidized bed gasification zone, which is maintained at 1700.degree.-2000.degree. F. by steam and O.sub.2 -containing gas introduced therein to gasify the coke and char. Fine particles of unreacted coal and carrier are passed with gas and distillate vapor through a cyclone gas-solids separation step located in the devolatilization zone, from which the solids are returned to the lower bed for further gasification. Ash produced in the lower bed along with the clean hot particulate carrier is transferred through an up-transport tube to the upper bed.

Abstract: The invention concerns a process for the purification of a hydrogen-containing gas mixture comprising up to 45% by volume of hydrogen, together with carbon oxides, hydrogen cyanide and impurities including nitrogen oxides and/or oxygen. The process comprises passing the gas over a sulphur-resistant hydrogenation catalyst at a temperature of from 120.degree. C. to 250.degree. C. and at a pressure of from 0.5 to 250 bar to remove the nitrogen oxides and/or oxygen therefrom while substantially avoiding hydrogen cyanide removal. The gas may be obtained from a Koppers-Totzek gasifier and may be used for the production of ammonia after further purification. The sulphur-resistant catalyst may be a nickel molybdate or cobalt molybdate catalyst or a metal from Group VI and/or Group VIII of the Periodic Table.

Abstract: An improved apparatus and process for the conversion of hydrocarbonaceous materials, such as coal, to more valuable gaseous products in a fluidized bed gasification reaction and efficient withdrawal of agglomerated ash from the fluidized bed is disclosed. The improvements are obtained by introducing an oxygen containing gas into the bottom of the fluidized bed through a separate conduit positioned within the center of a nozzle adapted to agglomerate and withdraw the ash from the bottom of the fluidized bed. The conduit extends above the constricted center portion of the nozzle and preferably terminates within and does not extend from the nozzle. In addition to improving ash agglomeration and withdrawal, the present invention prevents sintering and clinkering of the ash in the fluidized bed and permits the efficient recycle of fine material recovered from the product gases by contacting the fines in the fluidized bed with the oxygen as it emanates from the conduit positioned within the withdrawal nozzle.

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: Coal is gasified, to yield a fuel gas having a medium-B.T.U. heating value, in the presence of air and steam in a plurality of reaction stages having different reaction temperatures. Reaction heat is principally supplied directly by recycle of char particles from a separate combustion zone to higher-temperature reaction zones and indirectly by combustion flue gas to lower-temperature reaction zones. Hydrogen sulfide, from product fuel gas, and flue gas are directly contacted to provide elemental sulfur. The only other product is a substantially non-combustible ash.

Abstract: A method for the continuous production of synthesis gas comprising carbon monoxide and hydrogen through the autothermal gasification of solid combustibles in a pressure reactor which comprises:introducing into a screw machine containing two parallely ordered shafts, a finely divided solid combustible, moistening and intimately mixing the solid combustible with 2 to 30% by weight of water, degasing and compressing the moist solid combustible to a pressure higher than that of the reactor, adding the gas-tight compressed and moist solid combustible to a reaction chamber-through a burner where the combustible is brought into contact with the gasification medium, thereby evaporating the water in the compressed and moist solid combustible and producing a comminuted dispersion of the solid combustible in the mixture of the gasification medium and water vapor;reacting the combustible dispersion to give a raw synthesis gas and removing the raw synthesis gas from the reactor.

Abstract: An integral gasifier including a pretreater section and a gasifier section separated by a distribution grid is defined by a single vessel. The pretreater section pretreats coal or other carbon-containing material to be gasified to prevent caking and agglomeration of the coal in the gasifier. The level of the coal bed of the pretreater section and thus the holding or residence time in said bed is selectively regulated by the amount of pretreated coal which is lifted up a lift pipe into the gasifier section. Thus, the holding time in the pretreater section can be varied according to the amount of pretreat necessary for the particular coal to be gasified.

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: In an integrated coking and gasification process wherein a stream of fluidized solids is passed from a fluidized bed coking zone to a second fluidized bed and wherein entrained solid fines are recovered by a scrubbing process and wherein the resulting solids-liquid slurry is stripped with a stripping gas to remove acidic gases, at least a portion of the stripping gas comprises a gas comprising hydrogen, nitrogen and methane separated from the coker products.

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 and apparatus for gasification of carbonaceous matter, preferably coal, is disclosed. In one embodiment, a stream of previously produced char, preferably produced from coal or other fuel, together with an oxidizer and steam is introduced into a combustion stage. The combustion gas produced by the combustion passes into a mixing zone and thence with high turbulence into a gasification zone or stage at subsonic velocity. Pulverized carbonaceous matter, preferably coal, is introduced and dispersed in the combustion gas in the mixing zone. The temperature, velocity and velocity changes principally of the gas in the gasification zone or stage are controlled to provide a heating rate for the particles of pulverized carbonaceous matter of at least about 10.sup.5 degrees Kelvin per second, and to effect rapid removal of volatile components from the immediate vicinity of the particles.

Abstract: A process and apparatus for gasification of carbonaceous matter, preferably coal, is disclosed. A stream of previously produced char, preferably produced from coal, or other fuel together with an oxidizer and steam is introduced into a first or combustion stage. The combustion gas produced by the combustion passes into a second or gasification stage and through a nozzle at at least sonic velocity. Pulverized carbonaceous matter, preferably coal, is introduced and dispersed in the combustion gas in the gasification stage. The temperature, velocity and velocity changes principally of the gas in the gasification stage are controlled to provide a heating rate for the particles of pulverized carbonaceous matter of at least about 10.sup.5 degrees Kelvin per second, and to effect rapid removal of volatile components from the immediate vicinity of the particles.

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 improvement in the fixed-bed pressure gasification of coal is described. The improvement includes removing at least a portion of the hydrocarbon (e.g., tar) from the raw gaseous fuel produced in the gasification process and introducing the the removed hydrocarbon directly into the interior of the coal bed below the devolatilization zone and at or above the maximum-temperature location in the bed.

Abstract: The hot raw synthesis gas stream leaving the reaction zone of a free flow partial oxidation gas generator at a temperature in the range of about 1800.degree. to 3000.degree. F. is passed through a first gas diversion and residue separation zone where the velocity of the gas stream is reduced and its direction is diverted into a side transfer line. Solid material and molten slag separate by gravity from the gas stream. The hot gas stream is then introduced into a second gas diversion and residue separation zone where additional residue is separated. About 0.5 to 20 vol. % of the hot gas stream may be passed through bottom outlets in said first and second gas diversion zones in order to prevent bridging. The hot gas stream from the second gas diversion zone is passed upwardly through a radiant cooler where additional solid matter is removed by gravity and the gas temperature is reduced to a temperature in the range of about 900.degree. to 1800.degree. F.

Abstract: Coal or other high ash containing carbonaceous solid fuel is reacted with a free-oxygen containing gas, with or without a temperature moderator, in a down-flow partial oxidation gas generator to produce a stream of raw synthesis gas, fuel gas, or reducing gas. A large portion of the combustion residue, i.e., molten slag and/or particulate solids that is entrained in the down-flowing generated gas stream is removed by gravity when the gas stream is passed through a diversion chamber where the velocity of the gas stream is reduced and its direction is diverted. The main gas stream leaving the diversion chamber through the side outlet passes upward through a solids separation zone, optionally including gas-gas quench cooling, cyclones, filters, impingement separators, or combinations thereof, where additional entrained solids are removed and where some cooling of the gas stream may be effected by impingement with a cooled cleaned recycle portion of the gas stream.

Abstract: Coal or other high ash containing carbonaceous solid fuel is reacted with a free-oxygen containing gas, with or without a temperature moderator, in a down-flow partial oxidation gas generator to produce a stream of raw synthesis gas, fuel gas, or reducing gas. A large portion of the combustion residue, i.e. molten slag and/or particulate solids that is entrained in the down-flowing generated gas stream is removed by gravity when the gas stream is passed through a diversion chamber. The main gas stream leaving the diversion chamber through the side outlet passes upward through a solids separation zone, optionally including gas-gas quench cooling, cyclones, filters, impingement separators, or combinations thereof. Next, most of the sensible heat in the gas stream is recovered by indirect heat exchange with boiler feed water and steam. Saturated and superheated steam are produced.

Abstract: Coal or other carbonaceous material is gasified by reaction with steam and oxygen in a manner to minimize the problems of effluent water stream disposal. The condensate water from the product gas is recycled to slurry the coal feed and the amount of additional water or steam added for cooling or heating is minimized and preferably kept to a level of about that required to react with the carbonaceous material in the gasification reaction. The gasification is performed in a pressurized fluidized bed with the coal fed in a water slurry and preheated or vaporized by indirect heat exchange contact with product gas and recycled steam. The carbonaceous material is conveyed in a gas-solid mixture from bottom to top of the pressurized fluidized bed gasifier with the solids removed from the product gas and recycled steam in a supported moving bed filter of the resulting carbonaceous char. Steam is condensed from the product gas and the condensate recycled to form a slurry with the feed coal carbonaceous particles.

Abstract: A method of producing hydrogen and carbon-oxide-containing gases for use for reducing ores and synthesizing hydrocarbons and oxygen-containing organic substances, comprises, directing a suspension of finely ground coal and oxygen through a burner into a pressure reactor to convert the coal into gases and partly burning the gases, separating the gases from non-converted coal and ash, directing the separated gases into a quenching water so that their heat content is converted into pressure steam and the gases are precooled. The precooled gases are further purified and further cooled. During quenching, the gases are cooled from temperatures in the range of from 1300.degree. C. to 1500.degree. C. down to 200.degree. C. to 300.degree. C., depending on the gasification pressure. The ash-free gases then become highly loaded with steam to a steam-to-gas ratio of 2 as they are cooled down to a temperature of from between 100.degree. C. to 200.degree. C., and to also form a condensate.

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: An apparatus and process for conduct of fluidized bed reactions having an improved grate wherein at least one substantially continuous open slot sufficiently wide for passage of heavy solid particles is provided for preferential removal of heavy particles from the fluidizing chamber. The apparatus and process is particularly useful in coal gasification applications.

Abstract: Briquettes of specified geometry and composition are produced to serve as feed material or "burden" in a moving-burden gasifier for the production of a synthesis or fuel gas from organic solid waste materials and coal, including especially, the so-called "caking" coals, as in the process of copending application number 675,918. The briquettes are formed from a well-blended mixture of shredded organic solid wastes, including especially, municipal solid waste (MSW) or biomass, and crushed caking coal, including coal fines. A binder material may or may not be required, depending on the coal/MSW ratio and the compaction pressure employed. The briquettes may be extruded, stamped, or pressed, employing compaction pressures in excess of 1000 psi, and preferably in the range of 2000 to 10,000 psi. The briquettes may be circular, polygonal, or irregular in cross-section; they may be solid, or concentrically perforated to form a hollow cylinder or polygon; they may be formed into saddles, pillows or doughnuts.

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: In an integrated fluid coking and gasification process wherein a stream of fluidized solids is passed from a fluidized bed coking zone to a second fluidized bed and wherein entrained solid fines are recovered by a wet scrubbing process and wherein the resulting solids-liquid slurry is stripped to remove acidic gases, the stripped vapors of the stripping zone are sent to the gas cleanup stage of the gasification product gas. The improved stripping integration is particularly useful in the combination coal liquefaction process, fluid coking of bottoms of the coal liquefaction zone and gasification of the product coke.

Abstract: In a coupled coal solvent liquefaction-gasification system wherein a recycle mineral residue-containing slurry is mixed with the raw coal feed slurry for the liquefaction zone, the resulting feed slurry is under a pumpability total solids level constraint. Where a coupled system is operating under such a total solids level contraint for the feed slurry, any increase in the mineral residue recycle rate relative to the coal feed rate advantageously provides a catalytic activity and selectivity advantage in favor of liquid coal product at the expense of higher and lower boiling products. It is shown herein that this activity and selectivity effect is enhanced with decreasing liquefaction zone residence times. In accordance with the present invention, the ratio of recycle mineral residue to feed coal is enhanced by recycling a second mineral residue-containing slurry to the liquefaction zone independently of the raw coal feed slurry.

Abstract: A process of producing a gas of high calorific value and low dust content comprising contacting coal with water vapor and free oxygen at a pressure of about 5 to 150 bars and a temperature sufficient to produce a gas containing hydrogen and carbon monoxide, containing at least about 10 grams of dust per standard cubic meter and having a temperature of about 350.degree. to 800.degree. C., subjecting the gas to a coarse purification to reduce the solids content thereof, then scrubbing the gas at about 200.degree. to 300.degree. C. with a liquid predominantly comprising hydrocarbons and including less than about 5% of water by weight, and withdrawing a purified gas substantially free of solids and having an enhanced calorific value. In accordance with preferred features, the coarse purification stage includes at least one cyclone separator, the gas leaves the coarse purification stage at a temperature above about 350.degree. C. and is cooled by spraying with water to below 350.degree. C.

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: Bitumen-containing material is processed by distillation with a solid heat-carrier with subsequent gasification of the distillation residue and combustion of the gasification residue in an aerofountain furnace. During gasification, the formed flue gas and ash are heated and part of ash is used as the heat-carrier. The flue gas and ash are withdrawn from the process simultaneously in the form of their suspension in air, from which the heat-carrier is isolated for the distillation process, the consumption of the heat-carrier being controlled by withdrawing part of the suspension containing fine fraction of ash before the heat-carrier is isolated.

Abstract: An improvement in the production of a natural gas substitute comprising at least about 80% of methane by volume by multi-stage methanation of a synthesis gas containing hydrogen and oxides of carbon over fixed-bed nickel-containing catalysts under a pressure of about 5 to 100 bars. The starting synthesis gas, preferably produced by oxygen and water gasification of coal, has about 8 to 25% by volume of methane on a dry basis. It is methanated in a first stage at an inlet temperature of about 230.degree.-400.degree. C. and an outlet temperature of about 550.degree. to 750.degree. C. and then in a second stage at about 230.degree. to 500.degree. C. The process is economical with respect to heat consumption and equipment cost.

Abstract: A low density particulate vanadium-containing metallic ash concentrate, at least 50 percent of the articles of said concentrate having a diameter not greater than about 1 micron, is produced from a partially gasified coke comprising metallic components including vanadium components by heating the partially gasified coke in an oxidizing atmosphere at a temperataure below the fusion point of the metallic components.

Abstract: Solid fuel is acted on by a gasifying medium in a fluidized bed W. The resulting gas enters a cyclone 20 having an outlet for solid particles connected to a gasification chamber 30 in which the particles are gasified by a separate stream of gasifying medium supplied by an injector 25.

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: Clean HCN-free synthesis gas is produced from raw synthesis gas leaving a partial-oxidation gas generator by a continuous process comprising the steps of partial cooling, scrubbing with condensate, cooling below the dew point by indirect heat exchange preferably with a rich liquid absorbent from a downstream acid-gas-removal zone, and scrubbing with cold aqueous absorbent. The rich HCN-containing aqueous absorbent is then safely processed, without polluting the environment. For example, the HCN-containing aqueous absorbent may be stripped or reacted in the gas generator. Optionally, other acid gases, if present, may be removed from the synthesis gas in said acid-gas-removal zone.

Abstract: In the production of gas from a solid fuel comprising effecting gasification by contacting the solid fuel with oxygen and water under pressure to form raw gas containing tar, solids and water, cooling the raw gas to effect condensation of the tar and water, the condensate containing the solids, separating from the solids-containing condensate a fraction enriched in solids, and disposing of said fraction, the improvement which comprises effecting said disposition by feeding at least part of said fraction to a solids disintegrator wherein the solids are reduced in size, and recycling at least part of the condensate containing disintegrated solids to the gasification step. Disintegration serves to reduce substantially all the particles to below about 2 mm with the predominant part below about 0.5 mm. Part of the condensate may also be recycled to the separation stage and all the recycled condensate is kept above 50.degree. C. to prevent solidification of tars.