Abstract: In a process and apparatus for the production of gas containing hydrogen and carbon monoxide from a solid fuel in a fluidized bed, the solid particles contained in the product gas are separated off in a cyclone separator and recycled to the fluidized bed by way of a recycling conduit. The recycling conduit is provided with injection nozzles for introducing gas flows into the recycling conduit in a pulse-like manner in order to loosen up the particles therein. The gas flows may be introduced into the recycling conduit in displaced relationship in respect of time in such a way that, of two adjacent injection locations, gas is injected through the injection location which is arranged at a greater spacing from the reactor at a later time than at the injection location which is closer to the reactor.

Abstract: A process of catalytic coal gasification characterized by mixing an inexpensive, low rank coal with an aqueous solution of inexpensive, widely existing alkali metal or alkaline earth metal chlorides, such as Nacl, KCl, or the like; adding a pH adjustor such as ammonia to the resulting mixture to adjust pH to 5.about.12, whereby an ion exchange is effected between said metal and hydrogen in the coal, thereby loading only metals as a catalyst on the coal; washing the coal with water to remove chloride by-products; and running steam onto the catalyst-loaded coal at high temperatures and high pressures.

Abstract: A process for the partial combustion of finely-divided coal at high temperatures and pressures to make synthesis gas having entrained particles of fly ash which are separated from the gas at high pressure. The fly ash and a minor amount of entrained gas are handled in a batchwise manner to isolate a batch in a lock hopper, depressurize the batch, strip the synthesis gas from the fly ash and cool the fly ash prior to disposal.

Abstract: A process and apparatus for providing additional desulfurization of the hot gas produced in a fluid-bed coal gasifier, within the gasifier. A fluid-bed of iron oxide is located inside the gasifier above the gasification bed in a fluid-bed coal gasifier in which in-bed desulfurization by lime/limestone takes place. The product gases leave the gasification bed typically at 1600.degree. to 1800.degree. F. and are partially quenched with water to 1000.degree. to 1200.degree. F. before entering the iron oxide bed. The iron oxide bed provides additional desulfurization beyond that provided by the lime/limestone.

Abstract: Heterocyclic and O-substituted aromatic species, for example those obtained as a by product of coal gasification, may be gasified by reaction with steam in the presence of a nickel-alumina containing catalyst to produce methane-containing gases. The reforming reaction is carried out at temperatures of not greater than 500.degree. C.

Abstract: This invention relates to a gasification process for a coal gasification furnace in a coal gasification plant and to an apparatus therefor.

Abstract: A method of and apparatus for gasifying carbonaceous material in a circulating fluidized bed reactor having a lower reactor chamber and an upper reactor chamber interconnected by a throttled throat portion. Carbonaceous material is supplied to a first fluidized bed gasification zone maintained in the lower chamber and is gasified there by a gasifying agent and recycled hot particles separated from the product gas. The effluent from the first gasification zone is passed upwardly through the throttled throat portion to a second fluidized bed gasification zone of the spouting-bed type maintained in the upper chamber to complete gasification of unconverted carbon remaining in the particles entrained in the gaseous effluent from the first zone at a higher temperature than that of the first zone.

Abstract: A process for the partial oxidation of fuel using a multi-orifice burner comprising a central channel, and three concentric channels encircling the central channel, is disclosed, fuel being supplied through the second concentric channel at a specific velocity and oxygen being supplied through the other channels at specific mass flow distribution and velocities.

Abstract: The gasification of coal in the presence of steam and oxygen is significantly enhanced by introducing a thermochemical water-splitting agent such as sulfuric acid, into the gasifier for decomposing the steam to provide additional oxygen and hydrogen usable in the gasification process for the combustion of the coal and enrichment of the gaseous gasification products. The addition of the water-splitting agent into the gasifier also allows for the operation of the reactor at a lower temperature.

Abstract: Synthesis gas is produced by the partial oxidation of a feedstock comprising sulfur-containing petroleum coke and/or liquid hydrocarbonaceous fuel and having ashes that contain nickel and a comparatively low level of silicon. The production of toxic nickel subsulfide (Ni.sub.3 S.sub.2) in the slag is prevented, and there is substantially no increase in the mole ratio H.sub.2 S+COS/H.sub.2 +CO in the raw product gas stream by introducing an additive comprising about 2 to 100 wt. % of a sulfur-containing material and any remainder comprising a supplemental iron-containing material into the reaction zone along with the feed. The additive combines with substantially all of the nickel constituents and most of the iron constituents and sulfur found in the feedstock to produce molten slag substantially comprising a fluid sulfide phase and a relatively minor amount of an Fe, Ni alloy phase.

Abstract: In the partial oxidation of a sulfur- and metal-containing carbonaceous charge fuel to produce a sulfur-containing synthesis gas and metal-containing molten slag, an integrated method of charge fuel pretreatment and Claus unit tail gas sulfur removal is provided. The process of the instant invention is advantageous over other partial oxidation processes in that: (i) a fluid, molten slag which flows easily is produced, thereby improving reactor performance; and (ii) the overall removal of sulfur compounds from the synthesis gas is made simpler, more efficient, and less costly, as the need for a conventional Claus unit tail gas sulfur removal process is eliminated.

Abstract: Synthesis gas, fuel gas, or reducing gas is produced by the noncatalytic partial oxidation of a sulfur-containing liquid hydrocarbonaceous fuel or a slurry of sulfur-containing solid carbonaceous fuel with a free-oxygen containing gas in the first free-flow reaction zone located in a refractory lined gas generator at an autogenous temperature in the range of about 1900.degree. F. to 2900.degree. F. and above the ash-fusion temperature of the slag formed in the reaction zone. About 85 to 99 weight percent of the carbon in the fuel feed to the reaction zone is converted into carbon oxides. At least a portion of the hot effluent gas stream from the reaction zone is passed through a free-flow second reaction zone R.sub.2 in admixture with a second portion of sulfur-containing fuel and an iron-containing additive. In the second reaction zone the carbon in the second portion of fuel, unconverted fuel and particulate matter from R.sub.1 react with H.sub.2 O and/or CO.sub.2 to produce supplemental H.sub.

Abstract: Synthesis gas, fuel gas, or reducing gas is produced by the noncatalytic partial oxidation of a sulfur-containing liquid hydrocarbonaceous fuel or a slurry of sulfur-containing solid carbonaceous fuel with a free-oxygen containing gas in the free-flow reaction zone of a refractory lined gas generator at an autogenous temperature in the range of about 1900.degree. F. to 2900.degree. F. and above the ash-fusion temperature of the slag formed in the reaction zone, so that about 75 to 95 weight percent of the carbon in the fuel feed to the reaction zone is converted into carbon oxides. At least a portion of the hot effluent gas stream from the reaction zone is passed through a free-flow radiant cooler in admixture with an iron-containing additive. In the radiant cooler at least a portion of the sulfur-containing gases e.g. H.sub.2 S and COS react with the iron-containing additive to produce particulate matter comprising iron oxysulfide.

Abstract: Synthesis gas, fuel gas, or reducing gas is produced by the noncatalytic partial oxidation of a sulfur-containing liquid hydrocarbonaceous fuel or a slurry of sulfur-containing solid carbonaceous fuel with a free-oxygen containing gas in a first free-flow reaction zone R.sub.1 located in a refractory lined gas generator at an autogenous temperature in the range of about 190.degree. F. to 2900.degree. F. and above the ash-fusion temperature of the slag formed in the reaction zone. About 85 to 99 weight percent of the carbon in the fuel feed to the reaction zone is converted into carbon oxides. At least a portion of the hot effluent gas stream from the first reaction zone is passed through a free-flow second reaction zone R.sub.2 in admixture with a second portion of sulfur-containing fuel and a calcium-containing additive. An equilibrium oxygen concentration with a partial pressure which is less than about 10.sup.-12 atmosphere is provided in the gas phase in the first and second reaction zones.

Abstract: Gasification is performed under pressures in the range from 5 bars to 150 bars with oxygen, steam and/or carbon dioxide as gasifying agents. Pellets are fed to the top of a fixed bed in the gasification reactor. The gasifying agents are introduced into the fixed bed from below. Mineral constituents are withdrawn as solid ash or liquid slag from the lower end of the fixed bed. The pellets are made from fine-grained hard coal which has a particle size below 1 mm and contains 3 to 10 wt. % of fines having particle sizes not in excess of 2 micrometers and 70 to 80 wt. % of particles not in excess of a fraction not in excess of 63 micrometers. The fine-grained hard coal is mixed with bentonite to obtain a mixture which contains 1 to 8 wt. % bentonite. With an addition of water, the mixture is shaped to form pellets which contain 15 to 25 wt. % water. The pellets are fed in an undried, moist, plastically deformable state to the top of the fixed bed.

Abstract: The gasification of sulfur-bearing coal produces a synthesis gas which contains a considerable concentration of sulfur compounds especially hydrogen sulfide that renders the synthesis gas environmentally unacceptable unless the concentration of the sulfur compounds is significantly reduced. To provide for such a reduction in the sulfur compounds a calcium compound is added to the gasifier with the coal to provide some sulfur absorption. The synthesis gas from the gasifier contains sulfur compounds and is passed through an external bed of a regenerable solid absorbent, preferably zinc ferrite, for essentially completed desulfurizing the hot synthesis gas. This absorbent is, in turn, periodically or continuously regenerated by passing a mixture of steam and air or oxygen through the bed for converting absorbed hydrogen sulfide to sulfur dioxide.

Abstract: This invention relates to a two-fluid nozzle which is adjustable to provide a substantially constant mixing energy. Adjustment of the two-fluid nozzle is made in accordance with the pressure and mass flow values of the liquid and gas fed to the nozzle. A microprocessor calculates the mixing energy from these values and provides an output to the nozzle to adjust it should its mixing energy be in variance with a pre-selected mixing energy.

Abstract: The present invention describes a process for producing synthesis gas by partial oxidation of carbon-containing particles suspended in water with oxygen at elevated pressures and temperatures of 1000.degree. to 1600.degree. C. Three substance streams are added separately but simultaneously to the reactor. The inner substance stream consists of oxygen or a mixture of oxygen and synthesis gas. The middle substance stream forms a carbon-water suspension, and the outer substance stream carries oxygen or oxygen-containing gases. Due to the fact that these three substance streams intersect at an acute angle, an ideal distribution of the suspension with the gas streams is achieved and an optimum reaction course is ensured. In order to be able to compensate requirement fluctuations during continuous operation, the outlet opening for the carbon-water suspension and the outer gas stream can be correspondingly adapted in a continuous and independent manner.

Abstract: Coal is transported through a hot carbonizing furnace chamber successfully on two endless traveling chain grates, the first of which is higher than the second and the second being run at a slower speed than the first so as to form a thicker bed than the coal on the first grate. Air is fed through the coal on the first grate in sub-stoichiometric amounts at low velocity so as to drive off the volatiles while air and steam are fed to the coal in the second grate in amounts sufficient to burn the coal. Gaseous by-products are exhausted from the furnace chamber and ashes are discharged through a conventional take-off.

Abstract: In a process for the gasification of carbonaceous substances, exothermic and endothermic gasification agents are injected into the reaction area through at least one nozzle comprising at least two coaxial pipes, the outer pipe terminating short of the end of the inner pipe, at a distance such that the end face of the outer pipe is in a region of the pressurized interior of the reactor, in which the temperature is below the melting point of the ash of the solid particles to be gasified. The speed of flow of the endothermic agent out of the annular gap between the pipes is substantially higher than the speed of flow of the exothermic agent out of the inner pipe and the flow of endothermic gasification agent tends to be constricted around the flow from the inner pipe. The outer edge of the inner pipe is a sharp, right-angled edge so that in the region thereof eddies are formed which protect the region from the penetration of particles of ash therein.

Abstract: Solid fuels are gasified in a fixed bed under a pressure from 5 to 100 bars by a treatment with oxygen, water vapor and carbon dioxide. The raw gas from the gasifier is cooled so that an aqueous condensate is formed, at least part of which is burnt in a fluidized bed furnace at temperatures in the range from about 750.degree. to 1000.degree. C. The resulting combustion gas contains water vapor and is supplied to the gasifier. The condensate which becomes available as the raw gas is cooled may be treated in a separator to remove at least part of its dust and tar contents before the condensate is supplied to the fluidized bed furnace. A circulating fluidized bed is preferably maintained in the fluidized bed furnace.

Abstract: A system for reacting solid particles flowing under gravity through a thin walled enclosure has at least one fluid flowing through the enclosure in a counter-current to the flow of the solid particles. The feeding of the solid particles into the enclosure and the discharging therefrom of the converted ash particles may be adjusted. A particle bed is controlled by feeding the fluid into the enclosure so that it has to go through a substantial part of the bed thickness. The enclosure is vibrated to obtain a vibrated particle bed, with the vibrations being directed along a direction which lies at substantially a right angle to the vertical.

Abstract: A coal gasification method using coal powder introduced along with oxygen or air and steam, into a reaction chamber, supplies the char produced in the reaction chamber or the char and coal, along with oxygen or air and steam is introduced into a combustion chamber, formed in lower part of the reaction chamber and burns in the combustion chamber to maintain the temperature therein at about 1,600.degree. C., and forms the high temperature region of the reaction chamber into an agglomerated bed of fluidized coal having a temperature between 900.degree. and 1,300.degree. C.

Abstract: A process for gasifying a non-gaseous solid material wherein a portion of the gasification is accomplished in the presence of steam and another portion of the gasification is accomplished in the presence of hydrogen and in the substantial absence of carbon dioxide and steam. The gasification will be accomplished at an elevated temperature and pressure.

Abstract: An ash fusion temperature reducing agent principally comprising at least 50.0 wt. % of a manganese compound, such as MnO, and the remainder of the agent comprising a silicon compound, such as SiO.sub.2 is mixed with an ash-containing fuel comprising a pumpable liquid hydrocarbonaceous material and/or petroleum coke to produce Mixture A. In one embodiment, the ash fusion temperature reducing agent comprises a comminuted pyrolusite ore in which the following elements are present in weight percent basis ore: manganese in the range of about 50-75, calcium in the range of about 0-1.0, silicon in the range of about 0-3.0, magnesium in the range of about 0-1.0, and aluminum in the range of about 0-1.0. Mixture A is reacted with a free-oxygen containing gas in a free-flow refractory lined reaction zone of a partial oxidation gas generator. A hot raw effluent gas stream comprising H.sub.2 +CO along with molten ash having a reduced initial deformation temperature are produced at a lower temperature.

Abstract: An ash fusion temperature increasing agent principally comprising a silicon and/or titanium compound, such as SiO.sub.2 and/or TiO.sub.2 is mixed with an ash-containing fuel comprising a pumpable liquid hydrocarbonaceous material and/or petroleum coke to produce Mixture A. In one embodiment, the ash fusion temperature increasing agent comprises about 55-100 wt. % of silicon compound selected from the group consisting of fine silica or quartz, volcanic ash, and mixtures thereof; and the remainder, if any, of said ash fusion temperature increasing agent comprises a member of the group consisting of aluminum compound such as Al.sub.2 O.sub.3, magnesium compound such as MgO, and mixtures thereof. Mixture A is reacted with a free-oxygen containing gas in a free-flow refractory lined reaction zone of a partial oxidation gas generator. A hot raw effluent gas stream comprising H.sub.2 +CO along with fly-ash having an increased initial deformation temperature are produced at a higher temperature.

Abstract: Deposition of ash in the outlet conduit of a synthesis gas quench chamber is reduced or eliminated by providing a streamlined configuration at the mouth and throat of the outlet conduit.

Abstract: Separation of clarified water and rapid settling of the particulate solids e.g. ash, slag, char and mixtures thereof from aqueous dispersions of quench cooling and/or scrubbing water as produced in the partial oxidation process for ash-containing solid carbonaceous fuels is effected by mixing with said dispersion a sulfonated product of humic acids and their salts and adjusting the pH of the mixture to a value in the range of about 2 to 6.

Abstract: This process relates to the upgrading of at least one stream of condensate water by removing water soluble gaseous impurities from the group consisting of HCN, COS, HCOOH, and mixtures thereof as produced in a process for the production of synthesis gas by the partial oxidation of solid carbonaceous fuel and/or liquid hydrocarbonaceous fuel. In the process, at least one internally produced condensate stream of water containing the aforesaid water soluble gaseous impurities is mixed with and vaporized into a stream of synthesis gas. The vaporized mixture is then introduced into at least one bed of catalyst where the gaseous impurities are removed by hydrolysis. The upgraded water stream is then recycled in the process for use in cooling and/or scrubbing the hot raw effluent gas stream from a partial oxidation gas generator.

Abstract: In a coal or coal char gasification system using hot recycled inert heat transfer medium (IHTM) solids, the heat transfer medium and some of the unreacted or ungasified char are passed through a spouted-bed reactor. In the spouted-bed reactor, the unreacted char is burned in a way that more efficiently reheats the heat transfer medium and reduces fusion, agglomeration, plugging, fouling and erosion problems. These advantages are provided by the fact that only a central spout of solids is fluidized and the fact the solids undergo a systematic cyclic mechanism where there is greater contact between the hot char and IHTM solids. The spouted-bed produces a hydrodynamic system which is substantially different from conventional gas-solid combustor configurations, especially fluidized combustors.

Abstract: A method for the gasification of coal in a fluidized bed gasifier to improve gasification efficiency comprising the steps of introducing coal into the thermal cracking zone of a fluidized bed gasifier, thermally cracking and partially combusting the coal in said gasifier, recovering a fluid product gas containing fine particles therein from the fluidized bed gasifier, separating the fine particles as char from the first product gas, gasifying said recovered fine char particles at a temperature higher than its melting point in a high temperature gasifier to produce ash and a second product gas having H.sub.2 and CO as its main components, recovering the ash as a slag and feeding the second product gas containing H.sub.2 and CO to the coal feeding position of the fluidized bed gasifier in the thermal cracking zone.

Abstract: A method of generating a low-tar generator gas includes contacting the hot tar-containing generator gas in a contact zone with ballast bodies to cool the generator gas and capture tar and dust on the exposed surfaces of the ballast bodies, and admixing the thus heated ballast bodies to the wet solid fuel to be gasified to dry and pre-heat such fuel in preparation for the actual gasification which is performed in two separate gasification zones which are arranged one above the other by reacting the solid fuel with an oxygen-containing gasification medium that is introduced from above into the upper one, and from below into the lower one, of the gasification zones with attendant formation of two conflagration fronts in the gasification zones. The generator gas which is thus generated in the two gasification zones is discharged through a common discharge conduit which has the contact zone incorporated therein.

Abstract: Low sulfur, iron and calcium containing solid carbonaceous fuel having a high melting point ash is mixed with a sufficient amount of iron sulfide containing material or supplemental iron and sulfur containing reactant materials that react in the reaction zone to produce iron and sulfur containing compounds. The mixture of materials is reacted in a free-flow gasifier by partial oxidation to produce a raw gas stream of synthesis gas, reducing gas or fuel gas, containing entrained particulate matter including molten slag. By the process, sufficient iron and sulfur are in the reaction zone so that the melting point of the fuel ash is decreased, and the mole ratio H.sub.2 S/H.sub.2 +CO in the raw gas stream is greater than 0.01. Further, the amount of iron in the molten ash is greater than 10.0 wt. %, and preferably at least 14 wt. % of the molten ash. By this means, the fluid temperature of the molten ash entrained in the raw gas stream is reduced at least 100.degree. F.

Abstract: Method and installation for processing a material in a circulating fluidized bed, in which, in the filtration compartment (4) traversed by the fluidization gas at a speed which is so regulated as to put into suspension only the particles having dimensions smaller than a given limit, the unburnt largest particles (25) which are recovered and are directly recycled in the fluidized bed (21) and the fine particles (24) are subjected in an adjacent compartment (5) to a processing for agglomerating the ashes by forming in the processing compartment (5) a high temperature zone (96), the agglomerated ashes (26) being withdrawn at the base of the processing compartment (5) and the unburnt fine particles (27) being returned to fluidized bed (21) through a recycling circuit (54).

Abstract: A process for producing a synthesis gas containing methane and using a reactor having a fuel containing carbon comprises directing gasification gases in a circulation system through a bed of fuel containing carbon to form a synthesis gas containing methane and carbon dioxide. Thereafter, the synthesis gas is cooled in a regenerator and subjected to the gas separation wherein the syngas is subjected to a gas cleansing by means of a pressure change absorption in a gas scrubber to remove most of the methane and carbon dioxide and its water content is increased. The separated gas is then heated and subsequently the portion is returned into the system together with the waste gases and fuel containing carbon. The process includes a 4-pole heater which includes the first heat exchange passage for the syngas which is cooled and a second heat exchange passage for the recirculation of the syngas and is further cooled and passed through a scrubber.

Abstract: A method is provided for turning down from design conditions or below the output of raw product gas from a free-flow partial oxidation gas generator, or when operating below design conditions the output of raw product gas from the gas generator may be turned up while maintaining substantially constant the efficiency of the gas generation, or conversion of the fuel to gas, and the quality of the gas produced. The flow rates of the feedstreams to the burner are adjusted down or up a predetermined amount for each of the feedstreams to the burner to obtain a specified output of raw product gas while maintaining substantially constant in the reaction zone the levels of O/C atomic ratio and the H.sub.2 O/fuel weight ratio. Further, a pressure adjustment in the system is made which produces a corresponding adjustment to the pressure in the gas generator. The adjusted pressure is a direct function of the adjusted flow rate for the adjusted fuel or oxidant feedstream.

Abstract: Process for producing synthesis gas, reducing gas, or fuel gas substantially free-from volatile metal hydride impurities e.g. a hydride of arsenic, germanium, antimony, lead, tin, silicon, and mixtures thereof starting with the partial oxidation of liquid hydrocarbon fuel and/or solid carbonaceous fuel containing at least one mtal impurity from Group IV A and V A of the Periodic Table of Elements. At least one intermetallic reaction product of said metal impurity from Group IV A and V A leaves the gas generator in admixture with the hot raw process gas stream. A metal hydride forms when the gas stream is quench cooled and scrubbed with water. The metal hydride is then decomposed into its elements e.g. H.sub.2 and a Group IV A aor V A metal when the cooled and scrubbed gas stream contacts a solid sorbent material having a minimum surface area of 10 square meters per gram in a gas-solids contacting zone at a temperature in the range of about 0.degree. C. to 350.degree. C.

Abstract: Synthesis gas is produced by the partial oxidation of a fuel feedstock comprising sulfur-containing petroleum coke and/or heavy liquid hydrocarbonaceous fuel and having a nickel and iron-containing ash in a free-flow refractory lined partial oxidation reaction zone. The production of toxic nickel subsulfide (Ni.sub.3 S.sub.2) in said slag is prevented, and there is a substantial reduction in the concentration of H.sub.2 S+COS in the raw product gas stream by introducing an iron-containing additive into the reaction zone along with the feed. The weight ratio of iron-containing additive to ash in the fuel feedstock is in the range of about 0.5 to 10.0. The weight ratio of iron to nickel in said mixture of iron-containing additive and fuel feedstock is greater than 0.33. The additive combines with at least a portion of the nickel and iron constituents and sulfur found in the feedstock to produce a very fluid sulfide phase of iron and nickel, and an Fe, Ni alloy phase.

Abstract: Control process for producing an aqueous slurry of solid carbonaceous fuel having a desired solids concentration for feed to a partial oxidation gas generator by grinding together in a size reduction zone a recycle aqueous slurry stream comprising carbon-containing particulate solids, a stream of solid carbonaceous fuel, and a specific amount of make-up water. No valves are in the line or path between the size reduction zone and the feed tanks for the solid carbonaceous fuel and recycle aqueous slurry. A system control unit automatically calculates the amount of make-up water and provides a corresponding signal to control the flow rate. Input signals that are provided to the system control unit include those corresponding to the weigh belt feeder speed and moisture content for the solid carbonaceous fuel; and pump speed, weight fraction, temperature, and density of the solids for the slurry of recycle particulate solids.

Abstract: An ash fusion temperature reducing agent comprising a comminuted ore mixture of the silicates of iron, calcium, magnesium and aluminum is mixed with an ash containing pumpable liquid hydrocarbonaceous material to produce Mixture A. Mixture A is reacted with a free-oxygen containing gas in a partial oxidation gas generator. A hot raw effluent gas stream comprising H.sub.2 +CO along with molten ash having a reduced ash fusion temperature are produced at a lower temperature. Alternatively, Mixture A may be first introduced into a coking zone and converted into petroleum coke in which the ash fusion temperature reducing agent is dispersed throughout. The petroleum coke is then introduced into the partial oxidation gas generator where the hot raw effluent gas stream comprising H.sub.2 +CO is produced along with molten petroleum coke ash having a reduced ash fusion temperature.

Abstract: A partial oxidation process for the production of a stream of mixed gases comprising H.sub.2 and CO. An aqueous particulate solid carbonaceous fuel slurry feedstream is preheated by indirect heat exchange with a process-derived stream of skimmed gases substantially comprising H.sub.2 O. The aqueous carrier of the slurry is vaporized by introducing superheated steam directly into the slurry pipeline. A suspension of particulate solid carbonaceous fuel entrained in a gaseous mixture substantially comprising steam e.g. about 90 to 99.9 wt. % H.sub.2 O and about 0.1 to 10 wt. % of a CO.sub.2 -containing gas mixture is produced. The suspension of solid fuel in the gaseous mixture is then separated in a skimming operation into an overhead gas stream substantially comprising steam, as previously described, and a bottom stream comprising particulate solid carbonaceous fuel with the remainder of said gaseous mixture.

Abstract: A blowdown pot is provided with an inlet pressure control valve through which the pot receives unwanted residue e.g., ash from a high pressure chemical reactor, and this reactor residue can thereby be continuously or semi-continuously blown out from the high pressure, high temperature chemical reactor into the relatively low pressure blowdown pot which includes means maintaining a liquid level therein minimizing steam flashing and vessel wear. At the same time the reactor residue is removed from the pot with a liquid overflow.

Abstract: The fuel constitutes a fixed bed in the reactor, which is provided in its lower portion with a rotating grate, which is adapted to be speed-controlled. The gasifying agents consisting of oxygen, steam and/or carbon dioxide are introduced through the rotating grate into the fixed bed. Under the action of the rotating grate the incombustible mineral constituents are delivered as solid ash to a lock chamber container. The speed of the rotating grate is controlled in dependence on the temperature in the lock chamber container. The speed will be decreased when the temperature in the lock chamber container exceeds a desired value, and increased when the temperature is too low. The desired temperature in the lock chamber container is taken into account as a range, which varies with time. The speed can be controlled by hand or can be automatically controlled with the aid of a computer. The rate at which oxygen as a gasifying agent is supplied to the reactor is also taken into account in the speed control.

Abstract: A process for the gasification of carbonaceous agglomerates in a reactor at a pressure of the range of 5 to 150 bar. The agglomerates are fed into said reactor from a storage zone located above the reactor and form a fixed bed in the reactor, in which they slowly descend when gasified. At least two gasification agents selected from the group consisting of oxygen, air, steam and carbon dioxide are introduced into said reactor through the bottom and rise through said fixed bed. Solid ash or liquid slag is discharged below said fixed bed and a steam-containing product gas is tapped from the reactor above said fixed bed. In order to minimize or prevent the condensation of steam on the agglomerates in the storage zone, the invention provides for a controlled atmosphere almost entirely free of oxygen and steam which is introduced into the storage zone at a pressure approximately equal to the pressure of the product gas.

Abstract: An improved process for producing a methane-enriched gas wherein a hydrogen-deficient carbonaceous material is treated with a hydrogen-containing pyrolysis gas at an elevated temperature and pressure to produce a product gas mixture including methane, carbon monoxide and hydrogen. The improvement comprises passing the product gas mixture sequentially through a water-gas shift reaction zone and a gas separation zone to provide separate gas streams of methane and of a recycle gas comprising hydrogen, carbon monoxide and methane for recycle to the process. A controlled amount of steam also is provided which when combined with the recycle gas provides a pyrolysis gas for treatment of additional hydrogen-deficient carbonaceous material.

Abstract: In a partial oxidation process the gaseous effluent from a reactor is contacted with water to cool and remove solid particulates, i.e., ash and soot. The water from this operation is then mixed with an organic extractant, e.g., naphtha, and fed into a decanter to form aqueous and organic phases. The aqueous phase from the decanter is fed to a water flash separator to remove dissolved gases. The solids in a portion of the water flash separator bottoms are further concentrated in a hydrocyclone and thereafter purged. The remaining water is recycled for recontact with the gaseous effluent.

Abstract: Deposition of ash in the outlet conduit of a synthesis gas quench chamber is reduced or eliminated by providing a wetted-wall at the mouth and throat of the outlet conduit.

Abstract: A fluidized bed gasifier and a method for operating for the gasification of carbonaceous material comprising a vertically disposed elongated vessel comprising an upper section of a first diameter, a lower section of a second diameter and a transition section disposed therebetween wherein the first diameter is greater than the second diameter; a tubular manifold disposed generally horizontally and within the vessel; gas supply means penetrating said vessel and fluidly connected with said manifold and a plurality of tubes each having an inlet and an outlet, said inlet attached to, in fluid communication with, and distributed about the manifold and said outlets directed downwardly towards the interior of the vessel adjacent the transition section.

Abstract: A cyclic char gasifier process and apparatus are described wherein reactant gases are first compressed into the pores of a char fuel to react and then the reacted gases are expanded out of the char fuel pores. This cycle of compression and expansion is repeated with fresh reactant gases supplied for each compression and with reacted gases removed at each expansion. Air and steam are preferred reactant gases when the char fuel is to be gasified by oxidation. Reacted gases from such an oxidation gasifier plant are preferred reactant gases when the char fuel is to be partially gasified by devolatilization. Rapid reaction to a rich product gas can occur over the large surface area inside the char pores and the undesirable Neumann reversion reaction is suppressed by the strongly reducing conditions prevailing therein. The gases of devolatilization gasification can be used to enrichen the gases of oxidation gasification by using two cyclic char gasifier plants in a combination system.

Abstract: Coarse-grained fuels are gasified in a moving bed under a pressure of 5 to 150 bars with oxygen, water vapor and, if desired, carbon dioxide. The resulting product gas is at temperatures of 250.degree. to 700.degree. C. and is cooled to temperatures in the range from 120.degree. to 220.degree. C. to form an aqueous condensate, which contains distillation products and is known as gas liquor. The gas liquor obtained by the gasification in a moving bed is pressure-relieved to atmospheric or a higher pressure and the flashed-off vapor is supplied to the fluidized bed gasifier. In the fluidized bed gasifier, fine-grained solid fuels are gasified under a pressure which is lower than that in the moving bed.The flashed-off vapor supplied to the fluidized bed supplies at least one-half of the water vapor required for the gasification in the fluidized bed.