Abstract: A hydrogen generation apparatus includes controls for delivering a feedstock to a reactor and a water gas step membrane reactor operating at a lower temperature than the reactor so as to efficiently produce purified hydrogen and manage heat within the apparatus. Catalytic combustion of feedstock in the presence of a combustible gas based on a computer controller facilitates operation. Flat plate heat exchangers in various configurations are contemplated as a reactor, water gas step membrane reactor, and purifier. Catalytic burning of feedstock in the presence of a combustible gas enhances apparatus efficiency.

Abstract: A hydrogen-rich reformate gas generator (36), such as a mini-CPO, POX, ATR or other hydrogen generator provides warm, dry, hydrogen-rich reformate gas to a hydrogen desulfurizer (17) which provides desulfurized feedstock gas to a major reformer (14) (such as a CPO) which, after processing in a water-gas shift reactor (26) and preferential CO oxidizer (27) produces hydrogen-containing reformate in a line (31) for use, for instance, as fuel for a fuel cell power plant. The expensive prior art hydrogen blower (30) is thereby eliminated, thus reducing parasitic power losses in the power plant. The drier reformate provided by the small hydrogen generator to the hydrogen desulfurizer favors hydrogen sulfide adsorption on zinc oxide and helps to reduce sulfur to the parts per billion level.

Abstract: A heat exchanger (60) for a fuel processing system (10) that produces a hydrogen reformate gas. The heat exchanger (60) includes a catalyst for converting carbon monoxide to carbon dioxide. The heat exchanger (60) can be any suitable heat exchanger, such as a tube and fin type heat exchanger, that is able to cool the reformate gas and includes a suitable surface on which the catalyst can be coated. In one embodiment, the heat exchanger (60) is part of a WGS reactor assembly (48). The WGS reactor assembly (48) includes a first stage WGS adiabatic reactor (52) followed by the catalyzed heat exchanger (60) and a second stage WGS adiabatic reactor (68). Also, in one embodiment, both the first stage and the second stage WGS reactors (52, 68) are medium temperature reactors. By catalyzing the heat exchanger (60) in the WGS reactor assembly (48), the assembly (48) can be smaller than what is currently known in the art.

Abstract: A partial oxidation fuel reformer in includes a torch assembly for generating a near-stoichiometric flame through which a relatively rich “primary” air/fuel mixture is advanced. The torch assembly includes a low-energy ignition source such as a conventional sparkplug. The flame has sufficient energy to ignite the primary mixture to facilitate a partial oxidation reaction. A method of operating a partial oxidation fuel reformer is also disclosed.

Abstract: An auto-thermal reformer assembly is provided having a plurality of self-contained reformer modules positioned within a pressure vessel. The reformer modules each contain catalyst for inducing reforming reactions to produce hydrogen rich gas. At least one heat exhanger is provided for transferring heat from the hydrogen rich gas to the reactants entering or inside of the pressure vessel.

Abstract: The invention relates to the method and device for plasmacatalytic conversion of liquid hydrocarbons, such as engine fuels, into a synthesis gas by employing a pulse-periodic pseudocorona streamer microwave discharge (or semi-continuous microwave discharge) in the presence of air, and in certain cases, water.

Abstract: A reactor vessel for the catalytic reforming of air and steam-fuel mix into a hydrogen rich output gas is designed to relevant pressure code requirements. The steam-fuel mix and/or air provided to the vessel may be internally pre-heated prior to contacting the catalyst. Reformate is selectively directed into a recuperator to accomplish such heating. A bypass valve to divert reformate around the recuperator is also provided to allow control of the reaction conditions. Notably, this control may be performed manually or by way of an automated system. The resulting vessel enhances the safety and performance of the vessel, and it is more easily integrated into a complete fuel processor system. A method for achieving these goals is also described.

Abstract: A hydrogen generating apparatus having a fuel feeding part, a water feeding part for fuel reforming, an oxidant gas feeding part, a reforming catalyst body, a heating part for the reforming catalyst, a CO shifting catalyst body and a CO purification catalyst body is provided wherein the reforming catalyst body, the CO shifting catalyst body and the CO purification catalyst body are sequentially ordered from the fuel feeding part toward the downstream side, and wherein a shifting catalyst of the shifting catalyst body contains as one component at least a platinum group-type catalyst.

Abstract: The invention relates to a system for converting fuel and air into reformate with a reformer (10) which has a reaction space (12), a nozzle (14) for supplying a fuel/air mixture to the reaction space (12), and a fuel feed (16) for supplying fuel to the nozzle (14). As claimed in the invention it is provided that in the air inlet area (18) of the nozzle (14) there are air guidance means (40) which impart a swirl to the inflowing air.

Abstract: A process for the production of synthesis gas from a hydrocarbon fuel and steam and/or oxygen gas wherein at least part of any steam requirement is provided by heat exchange against exhaust gas from a gas turbine driving an air separation unit supplying at least part of any oxygen requirement for the synthesis gas production. The process is particularly applicable when the synthesis gas is used to prepare a synfuel by methanol synthesis or a Fischer-Tropsch process.

Abstract: Improved method for recovering hydrogen and carbon monoxide from hydrocarbon conversion processes are disclosed. A monolith catalyst reactor means is utilized in treating the waste gas stream from the hydrocarbon conversion process to assist in recovering hydrogen and carbon monoxide from the waste gas stream. The present invention also provides a method for improving the yield of hydrogen and carbon monoxide from a hydrocarbon conversion process utilizing a monolith catalyst reactor means.

Abstract: An autothermal reformer according to the principles of the present invention comprises a first stage that selectively receives a fuel flow, a first oxidant flow, and a steam flow. The first stage has a first portion of a catalyst bed. The fluids within the first stage are routed through the first portion of the catalyst bed and react. There is a second stage downstream from and communicating with the first stage. The second stage receives the fluids from the first stage and also selectively receives a second oxidant flow. The second oxidant flow and the fluids received from the first stage flow through a second portion of a catalyst bed and further react.

Abstract: An evaporator device for generating a hydrocarbon-air mixture which can be decomposed in a reformer for producing hydrogen comprises a burner/evaporator area, which has a combustion/mixing chamber (14), into which air enters via an inlet opening device (16), a hydrocarbon evaporating means (24, 34), comprising a porous evaporator medium (24) and, associated with same, a first heating means (34) and a glow-type igniting member (28) for igniting the hydrocarbon-air mixture present in the combustion/mixing chamber (14).

Abstract: A method for generating a hydrogen-containing product gas from liquid or gaseous hydrocarbons includes providing a reformer installation having a combustion space, a mixing chamber and a reformer unit. Partial oxidation of a first hydrocarbon stream with a first oxygen-containing gas stream is performed and a first product-gas stream containing hydrogen is formed, in the combustion space. A second hydrocarbon stream is reformed with water and a second product gas stream containing hydrogen is formed, in the reformer unit. The first product-gas stream and the second product-gas stream are mixed in the mixing chamber to form a third product-gas stream. The reformer unit is heated with the third product-gas stream.

Abstract: The present invention relates to a method for oil gasification. In particular, the present invention relates to a method for oil gasification while reducing wastewater and costly purification systems. The method comprises providing feedstock and water to an oil gasification system; receiving flash gas from the oil gasification system at a flash gas condensing section; extracting vapor generated by the flash gas condensing section; returning water produced by the extracting step to the flash gas condensing section; outputting dry flash gas produced by the extracting step; receiving spent wash water at a syngas cooling section from a syngas washing section; and outputting washed syngas from the syngas washing section.

Abstract: The method for the reformation of fuels, in particular of heating oil (20′) and of another liquid fuel is carried out using an oxygen containing gas (5a, 5b, 21′, 22′).

Abstract: A process for the high-temperature gasification of possibly thermally pretreated heterogeneous wastes, in which oxygen is injected into the gasification bed with the aid of water-cooled oxygen lances. The oxygen is heated by an independent pilot flame and accelerated to speeds approaching the speed of sound. Accordingly, the oxygen lances cannot be plugged by melted charge components not susceptible to gasification because the pilot flame is driven independently of the oxygen-lance flow. A pulsing, phase-shifted impact from several oxygen lances arranged in a ring produces a circulating flow of material in the gasification zone, compensating the heterogeneity of the charge in the case of a waste gasification.

Abstract: A method and nickel-containing catalyst are disclosed for preparing synthesis gas by the reforming of a hydrocarbyl compound using an oxygen-containing compound.

Abstract: A method and nickel-containing catalyst are disclosed for preparing synthesis gas by the reforming of a hydrocarbyl compound using an oxygen-containing compound.

Abstract: The progress and completion of slag removal from the quench chamber of a partial oxidation reactor during controlled oxidation can be monitored by measuring such quench water parameters as pH, conductivity, total dissolved solids, and sulfate concentration.

Abstract: A process for the partial oxidation of bituminous oil emulsions to produce a raw gas containing CO and H.sub.2, the process including heating the bituminous oil emulsion to destabilize the emulsion and separating the bituminous oil from the emulsion water, concentrating the emulsion water by evaporation, and reacting in a gasification unit the bituminous oil, the concentrated emulsion water and oxygen or air to produce the raw gas containing mainly CO and H.sub.2.

Abstract: The invention is a process for quenching a first synthesis gas mixture containing synthesis gas, molten flyash, water, and carbon dioxide and producing additional synthesis gas consisting of (a) passing the first synthesis gas mixture into a first quench zone; (b) introducing into the quench zone a mixture of a liquid carbonaceous quenching medium in a nitrogen or carbon dioxide carrier gas; (c) endothermically reacting the liquid carbonaceous quenching medium with the water and the carbon dioxide in the synthesis gas mixture, thus producing additional synthesis gas consisting of hydrogen and carbon dioxide, and wherein the additional synthesis gas is admixed with the first synthesis gas mixture to form a second synthesis gas mixture; (d) passing the second synthesis gas mixture to a second quench zone; (e) introducing into the second quench zone a cooling gas for admixture with the second synthesis gas mixture, thus cooling the second synthesis gas mixture, where the molten flyash is solidified, and thus for

Abstract: A partial oxidation process for the production of a stream of cooled and cleaned synthesis gas, reducing gas, or fuel gas substantially free from entrained particulate matter and slag. The hot raw gas stream from the partial oxidation gas generator is quench cooled with deaerated grey water in a quench tank to produce black quench water or cooled in a radiant and/or convection cooler. The cooled gas is scrubbed with deaerated grey water in a scrubbing zone to remove all of the entrained particulate matter and to produce black scrubbing waters. The black water is resolved in a flashing zone and reused by flashing it in two or three flash stages connected in series and separating the overhead flash vapors comprising vaporized grey water and sour gas from the bottoms comprising concentrated black water. The flash vapors from the first flash stage are used to heat a stream of deaerated grey water being recycled to the quench tank and gas scrubbing zone or to the gas scrubbing zone.

Abstract: A process for the partial oxidation of a sulfur- and silicate-containing carbonaceous fuel to produce a synthesis gas with reduced sulfur content which comprises partially oxidizing said fuel at a temperature in the range of 1900.degree.-2600.degree. F. in the presence of a temperature moderator, an oxygen-containing gas and a sulfur capture additive which comprises a calcium-containing compound portion, a sodium-containing compound portion, and a fluoride-containing compound portion to produce a synthesis gas comprising H.sub.2 and CO with a reduced sulfur content and a molten slag which comprises (1) a sulfur-containing sodium-calcium-fluoride silicate phase; and (2) a sodium-calcium sulfide phase.

Abstract: A hydrocarbon reforming apparatus having a furnace casing, a combustion gas passage formed in the furnace casing, a cylindrical reactor which is made up of multi-layered passages arranged concentrically around the combustion gas passage, with the multilayered passages being filled with catalysts, a combustion gas discharge passage communicating with the combustion gas passage, and a feedstock gas intake passage communicating with any one of the multilayered passages, characterized in that the combustion gas discharge passage is arranged on the inside of either of the outer passage of the multilayered passages or the feedstock gas intake passage, so that the combustion gas discharge passage is separated from the furnace casing.

Abstract: An endothermic reaction apparatus for converting a raw gas, or a feed gas, into a reaction gas or a produced gas, under the influence of an endothermic reaction catalyst includes a reaction tube having a pair of inner and outer vertical tubular spaces which are separated by a vertical partition wall and communicate with each other at their lower ends. The endothermic reaction catalyst is disposed in the inner and outer tubular spaces to form a continuous catalyst structure. The catalyst structure has an inlet portion for introducing the raw gas into the catalyst structure and an outlet portion for discharging the reaction gas from the catalyst structure. The inlet and outlet portions of the catalyst structure are disposed generally at the same level. A burner is disposed inwardly of the inner tubular space for heating the catalyst structure.

Abstract: This process pertains to a achieving high on-stream time and maintaining the temperature and composition of the raw effluent gas stream from a partial oxidation gas generator being fed simultaneously with a stream of gaseous fuel and separate stream of liquid hydrocarbonaceous fuel. Two parallel oxygen streams equipped with flow transmitters and control valves are used to supply the oxygen associated with two separate and different fuel streams. Each stream of oxygen is controlled by an O.sub.2 /fuel ratio control so that if the flow rate of either stream of fuel or its related oxygen stream changes, the oxygen/carbon atomic ratio of the remaining O.sub.2 and fuel stream in the gasifier is maintained at a desired value. Further, if either fuel flow is stopped, its associated O.sub.2 flow will stop, but the remaining fuel stream and its associated O.sub.2 stream will continue to flow at the same rate with no change in the oxygen/fuel weight ratio. Complete shut down of the unit is thereby avoided.

Abstract: A process starting from a hydrocarbon feedstock, and aiming to produce a synthesis gas suitable either for methanol synthesis or for other applications requiring a low H.sub.2 /CO ratio.In this process, the feedstock, supposed to be desulfurized, is divided into two fractions; a first fraction undergoes a primary steam reforming at high pressure and moderate temperature; the gas effluent from said primary steam reforming, as well as the second fraction of the feedstock, are combined and subsequently undergo a secondary reforming by reaction with a free-oxygen rich gas in a reactor operating under essentially adiabatic conditions.The synthesis gas, obtained as effluent from said secondary reforming, has a composition adjustable at will in a wide range, and therefore can be made as close as necessary to the stoichiometric composition required for methanol synthesis, or it can be made with a low H.sub.2 /CO ratio for other applications.

Abstract: Synthesis gases are prepared by partial autothermal oxidation of liquid fuels and/or solid fuels in the presence of oxygen or oxygen-containing gases with the addition of a temperature moderator, such as steam and/or CO.sub.2, in an empty reactor space without baffles, at from 1000.degree. to 1500.degree. C. under from 1 to 100 bar, the reactants fuel and oxygen-containing gas being fed separately to the reactor, by a process in which the steam or CO.sub.2 is fed in simultaneously with the feed of the fuel, and the steam is let down through one or more nozzles into the fuel steam directly before the orifice for the fuel, let-down being effected at from 30 to 250%, preferably from 80 to 140%, of the critical pressure ratio. An apparatus for carrying out the process is also described.

Abstract: A process for the production of a fuel gas which includes the steps of:hydrogentation of a liquid hydrocarbon or solid carbonaceous material in the presence of air and optionally steam to produce a raw fuel gas stream comprising methane and unreacted hydrogen,gasification of a liquid hydrocarbon or solid carbonaceous material in the presence of air and optionally steam to produce a second gas stream comprising hydrogen, nitrogen and carbon oxides,removing solids therefrom from the gas streams, mixing the fuel gas stream with the second gas stream and with steam and subjecting the resulting stream to carbon monoxide shift to convert at least a portion of the carbon monoxide present to carbon dioxide with generation of hydrogen,removing at least a portion of the carbon dioxide and other acid gas from the shifted gas stream; andreacting the hydrogen in the gas stream with carbon oxides present in the gas stream to generate methane and subjecting the methanated gas stream to cryogenic separation to yield at least

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

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

Abstract: Process for the partial oxidation of a liquid or solid and/or a gaseous fuel using a multi-orifice burner comprising a central channel and four concentric channels encircling the central channel. Liquid or solid fuel is supplied through the second concentric channel and the oxidizer is supplied through the first concentric channel and the third concentric channel. Hydrocarbon gas and/or moderator is supplied through the central channel and the fourth concentric channel. The mass ratio of liquid or solid fuel to hydrocarbon gas ranges from 0 to 1.

Abstract: A process starting from a hydrocarbon feedstock, and aiming to produce a synthesis gas suitable either for methanol synthesis or for other applications requiring a low H.sub.2 /CO ratio.In this process, the feedstock, supposed to be desulfurized, is divided into two fractions; a first fraction undergoes a primary steam reforming at high pressure and moderate temperature; the gas effluent from said primary steam reforming, as well as the second fraction of the feedstock, are combined and subsequently undergo a secondary reforming by reaction with an oxygen-containing gas in a reactor operating under essentially adiabatic conditions.The synthesis gas, obtained as effluent from said secondary reforming, has a composition adjustable at will in a wide range, and therefore can be made as close as necessary to the stoichiometric composition required for methanol synthesis, or it can be made with a low H.sub.2 /CO ratio for other applications.

Abstract: The hot process gas stream from the partial oxidation of sulfur-containing heavy liquid hydrocarbonaceous fuel and/or sulfur-containing solid carbonaceous fuel comprising gaseous mixtures of H.sub.2 +CO, sulfur-containing gases, entrained particulate carbon, and molten slag is passed through the unobstructed central passage of a radiant cooler where the temperature is reduced to a temperature in the range of about 1800.degree. F. to 1200.degree. F. From about 0 to 95 wt. % of the molten slag and/or entrained material may be removed from the hot process gas stream prior to the radiant cooler with substantially no reduction in temperature of the process gas stream. In the radiant cooler, after substantially all of the molten slag has solidified, the sulfur-containing gases are contacted with a calcium-containing material to produce calcium sulfide.

Abstract: Gases which are rich in carbon monoxide are producted by a catalytic cracking of gaseous or vaporized hydrocarbons. A part of the hydrocarbons is combusted with an oxygen-containing gas which is added at a rate that is twice to ten times the stoichiometric oxygen demand. The combustion temperature are between 800.degree. and 1500.degree. C. The oxygen-containing combustion gas is admixed to the preheated remainder of the hydrocarbon and a mixture is producted which is at a temperature between about 700.degree. and about 1300.degree. C. That mixture is passed through a fixed bed consisting of a granular cracking catalyst. A high-CO product gas at a temperature between about 800.degree. and about 1150.degree. C. is withdrawn from the fixed bed.

Abstract: In a partial oxidation process, the gaseous effluent from the generator is contacted with water to cool the synthesis gas and remove the solid particulates of ash and soot. The water from this operation is then mixed with an organic extractant and feed into a decanter to form aqueous and organic phases. The aqueous phase from the decanter is feed to a water flash separator to remove dissolved gases. The solids are removed from the water flash separator in an aqueous stream which is processed for removal of undesirable sulfides, cyanides, metals and particulate matter and steam stripped for removal of undesirable gases while retaining quantitites of ammonia therein. The overhead, an ammonia containing aqueous stream, is recycled for the control of pH in the quench scrubber vessel and the attendant equipment utilized to process the aqueous phase from the decanter.

Abstract: Asbestos-containing hazardous waste materials are known causes of cancer and other serious diseases. By the subject process, asbestos-containing wastes are rendered harmless by altering the physical form of the fibers, by (i) melting the asbestos, and by (ii) incorporating the molten asbestos into the slag phase produced by the partial oxidation of ash-containing liquid hydrocarbonaceous fuel and/or solid carbonaceous fuel. Further, gaseous mixtures comprising H.sub.2 +CO e.g. synthesis gas, reducing gas, or fuel gas, are simultaneously produced.

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 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 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 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: Process for the production of synthesis gas and higher hydrocarbons in which a saturated hydrocarbon and an oxygen containing gas having a ratio of hydrocarbon to oxygen of greater than the stoichiometric ratio for complete combustion are introduced into a bed of an inert particulate material. The upward flow rate of the hydrocarbon/oxygen containing gas stream is sufficient to fluidize or to produce a spouting action of the bed material, whereby the particulate material is thrown up above the bed surface and subsequently falls back into the bed. The hydrocarbon and oxygen containing gas are ignited reacted together, and the products of the reaction withdrawn.

Abstract: Process for the production of gaseous mixtures comprising H.sub.2 +CO e.g. synthesis gas, reducing gas, or fuel gas by the partial oxidation of a vanadium-containing liquid hydrocarbonaceous fuel, solid carbonaceous fuel, or mixtures thereof in a free-flow vertical refractory lined gas generator. The feed mixture to the gas generator comprises (i) a vanadium-containing fuel; (ii) supplemental iron-containing ash fusion temperature reducing agent; and (iii) at least a portion of the remainder of the iron-containing slag after separation of an enriched vanadium-containing coarse slag fraction. The coarse slag fraction has a decreased Fe/V weight ratio and is formed by depositing a portion of the slag entrained in the hot raw effluent gas stream from the partial oxidation reaction zone on the walls of a slag separation chamber located between the bottom discharge outlet in the reaction zone and the effluent gas quench tank located at the bottom of the gas generator.

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: 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: The temperature of a burner in the reaction zone of a partial oxidation gas generator is controlled so that there is substantially no condensation of H.sub.2 O from the hot raw product gas on the surface of the burner. Burner corrosion is thereby reduced. In the method, burner coolant is introduced into the burner at a pressure greater than that in the reaction zone and at a temperature in the range of about 5.degree. to 50.degree. F. higher than the dew point of the raw product gas contacting the burner in the reaction zone. The heated water coolant leaving the burner flows to a pressurized receiving vessel and its temperature is reduced by expansion into a feed vessel. Saturated steam is produced from a portion of the flashed water and is separated in the feed vessel for use as a heat source. Steam condensate is thereby produced and recycled to the feed vessel as make-up. The cooled liquid water coolant is then pumped into the inlet to the burner at a higher pressure than that in the feed vessel.

Abstract: An ash fusion temperature reducing agent comprising a mixture of about 70-97 wt. % of an iron compound and the remainder comprising a silicon compound is mixed with an ash-containing fuel comprising liquid hydrocarbonaceous material and/or petroleum coke. The comminuted mixture is reacted in a free-flow partial oxidation reaction zone with a free-oxygen containing gas in the presence of a temperature moderator to produce a hot raw effluent gas stream comprising H.sub.2 +CO along with molten ash having a reduced initial deformation temperature. The weight ratio of ash fusion temperature reducing agent to ash in said ash-containing fuel is in the range of about 0.5 to 10, and the weight ratio of iron oxide to SiO.sub.2 in said molten ash is about 1.5, or more. The molten ash is then separated from the hot raw effluent gas stream.

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.