Abstract: Method and installation for treating a CO2- and H2O-containing flue gas generated by an industrial process unit before CCUS, whereby the flue gas evacuated from the unit is subjected to cooling to a temperature T2 between 100 and 600° C., whereby the cooled flue gas is pretreated in one or more particle removal and/or gas cleaning and/or drying stages and the temperature of the cooled flue gas is further reduced to a temperature T3<T2, before a first part of pretreated flue gas is subjected to CCUS, a second part of the pretreated flue gas being recycled at temperature T3 as a cooling agent and mixed with the flue gas during the controlled cooling thereof, partially or fully purified CO2 from the CCUS may be recycled at temperature T4<T2 may be recycled as a cooling agent and mixed with the flue gas during the controlled cooling.

Abstract: A fuel cell module according to the present embodiment includes a hydrodesulfurizer, a cell stack, an exhaust gas channel portion, and an air-preheating channel portion. The hydrodesulfurizer is configured to desulfurize fuel gas using a hydrodesulfurization catalyst. A reformer is configured to generate a hydrogen-containing gas. The cell stack is constituted by stacking a plurality of fuel cells and is configured to generate electric power. The exhaust gas channel portion is configured to discharge the hydrogen-containing gas, and discharge exhaust gas that is generated by the combustion of the oxygen-containing gas. The air-preheating channel portion is an air-preheating channel portion that is disposed so as to be adjacent to the exhaust gas channel portion and that is configured to preheat the oxygen-containing gas through heat exchange with the exhaust gas channel portion. The air-preheating channel portion is disposed between the hydrodesulfurizer and the cell stack.

Abstract: A method of fabricating a catalytic reactor assembly having an outer tube and an inner tube is provided. The method may include inserting a catalyst into the outer tube and inserting the inner tube through the catalyst. The method may further include radially expanding the inner tube against the catalyst.

Abstract: A carbon monoxide (CO) Shift reaction apparatus and a CO shift conversion method are capable of increasing the service life of a CO shift catalyst and reducing loss of energy. The CO shift reaction apparatus includes a plurality of CO shift reaction units in which a plurality of CO shift catalysts haying mutually different active-temperature regions are arranged in a gas flow direction.

Abstract: A combustor apparatus is provided, comprising a mixing arrangement for mixing a carbonaceous fuel with enriched oxygen and a working fluid to form a fuel mixture. A combustion chamber is at least partially defined by a porous perimetric transpiration member, at least partially surrounded by a pressure containment member. The combustion chamber has longitudinally spaced apart inlet and outlet portions. The fuel mixture is received by the inlet portion for combustion within the combustion chamber at a combustion temperature to form a combustion product. The combustion chamber further directs the combustion product longitudinally toward the outlet portion.

Abstract: A process for converting carbonaceous materials or light hydrocarbon gases into products comprising predominately C5+ hydrocarbons. The process converts the feedstock into synthesis gas comprising hydrogen and carbon monoxide and then uses the Fischer-Tropsch reaction to produce heavy hydrocarbons. A small excess of hydrogen is produced in the syngas generator or by water gas shift for use in product upgrading and for blending with Fischer-Tropsch tail gas for recycle back to syngas generation. A portion of the Fischer-Tropsch tail gas is used as fuel, thus purging combustible light gases and CO2 from the tail gas. Hydrogen rich purge gas is blended into the remaining tail gas resulting in a recycle stream that is returned to the syngas generator. The tail gas components are therefore efficiently used to produce more products.

Abstract: A system includes a carbon dioxide treatment system that includes a catalyst configured to treat carbon dioxide to produce a treated carbon dioxide. The system also includes a gasifier injector configured to inject the treated carbon dioxide, a fuel, and oxygen into a gasifier. The gasifier injector may be coupled to or located inside the gasifier.

Abstract: A process and system for cooling syngas provides effective syngas cooling and results in reduced levels of fouling in syngas cooling equipment. A process for cooling syngas includes blending syngas with cooled recycled syngas in an amount effective for providing a blended syngas with a temperature at an inlet of a syngas cooler of about 600° F. to about 1400° F. The blended syngas changes direction of flow at least once prior to the inlet of the syngas cooler.

Abstract: A process of drying moisture containing material having a tendency to create dust when dried, said process including the steps of providing said material in a heated chamber having a steam containing atmosphere at a temperature above the dewpoint of the steam, recirculating a hot gas including a portion of the steam through said chamber in order to evaporate moisture from the material to a predetermined level of dryness.

Abstract: A method for producing synthetic gas from biomass by: a) grinding the biomass, feeding the biomass into a pyrolysis furnace while spraying a first superheated water vapor into the pyrolysis furnace, controlling the temperature of the pyrolysis furnace at 500-800° C., contacting the biomass with the first superheated water vapor for a pyrolysis reaction to yield crude synthetic gas and ash including coke; b) cooling the ash, and separating the coke from the ash; c) transporting the crude synthetic gas and the coke into a gasifier, spraying a second superheated water vapor into the gasifier, controlling the gasifier at an operating temperature of 1200-1600° C., contacting the biomass with the second superheated water vapor for a gasification reaction to yield primary synthetic gas; and d) cooling, removing dust, deacidifying, and desiccating the primary synthetic gas to obtain clean synthetic gas.

Abstract: The disclosed embodiments include systems for using an expander. In a first embodiment, a system includes a flow path and a gasification section disposed along the flow path. The gasification section is configured to convert a feedstock into a syngas. The system also includes a scrubber disposed directly downstream of the gasification section and configured to filter the syngas. The system also includes a first expander disposed along the flow path directly downstream from the scrubber and configured to expand the syngas. The syngas comprises an untreated syngas.

Abstract: A gas generator and process for converting a fuel into an oxygen-depleted gas and/or hydrogen-enriched gas. The gas generator is preferably used for generating protection gas or reducing gas for start up, shut down or emergency shut down of a SOFC or SOEC. The process for converting fuel into oxygen-depleted gas and/or a hydrogen-enriched gas includes combusting the fuel in a primary catalytic burner with an oxygen-containing gas to produce a flue gas with oxygen, combusting or partially oxidizing the flue gas comprising oxygen with excess fuel in a secondary catalytic burner to produce a gas with hydrogen and carbon monoxide, and reducing the trace amounts of oxygen from the gas comprising traces of oxygen and obtaining an oxygen-depleted gas, or reducing the carbon monoxide present in the gas by conversion to carbon dioxide or methane to obtain a hydrogen-enriched gas.

Abstract: An energy conversion process that exports by-product CO2 at elevated pressure where a fuel gas feed stream is mixed with a reactant stream and additional CO2 is added to at least part of, the fuel gas feed stream, the reactant stream or both through desorption by contacting with a CO2-rich solvent stream in a first stage contactor to produce a mixed feed gas stream and a CO2-lean solvent stream; passing said mixed feed gas stream to a chemical conversion step, where further CO2 is produced; chilling at least part of the products of said chemical conversion step and thereby produce a CO2-lean gas stream; and passing at least part of said CO2-lean gas stream said to a second stage contactor where further CO2 is removed, by absorption, to produce a product gas stream and a solvent stream rich in CO2 from which said CO2-rich solvent stream is subsequently derived.

Abstract: A gasification-liquefaction disposal method, system and equipment for MSW are disclosed. The method involves the MSW pretreatment of dehydrating and separating, thus reducing water and inorganic substance content of the waste. Then, the MSW is introduced into a plasma gasifier (23) by a carbon dioxide air-sealed feeding device (13) and gasified therein to obtain hydrogen-rich syngas. The hydrogen-rich syngas is then cooled, deacidified, dedusted and separated to obtain carbon dioxide. Then, the hydrogen-rich syngas is catalyzed to produce methanol product in a methanol synthesis reactor (52). The separated carbon dioxide is sent back to a carbonation reaction chamber (2007) of a gasification system to perform carbonation reaction with calcium oxide, thereby releasing heat to provide assistant heat energy for gasification and avoiding greenhouse gas from being discharged into environment.

Abstract: A process for treating offshore natural gas includes processing the natural gas on an off-shore processing facility by, (i) liquefying and fractionating the natural gas to generate a liquefied natural gas stream and a higher hydrocarbon stream, (ii) vaporizing at least a portion of the higher hydrocarbon stream, (iii) passing the vaporized higher hydrocarbon stream and steam over a steam reforming catalyst to generate a reformed gas mixture comprising methane, steam, carbon oxides and hydrogen, (iv) passing the reformed gas mixture over a methanation catalyst to generate a methane rich gas, and (v) combining the methane-rich gas with the natural gas prior to the liquefaction step.

Abstract: The goal of the invention consists in making available a method for supplying fuel to a pressurized gasification system, which ensures, in economically efficient manner, that the emission of pollutants from the coal transfer and the transport is minimized or completely avoided. This is achieved in that a gas that contains at least 10 ppm vol. CO is used for transfer and/or conveying, whereby a gas that contains oxygen is mixed into this gas, and that this gas mixture is heated to a temperature that oxidizes at least 10% of the pollutants contained in the gas.

Abstract: This invention relates to a process for the production of hydrogen from a hydrocarbon feedstock and water vapor comprising: A stage for the production of a synthetic gas in a vapor reforming unit of the hydrocarbon feedstock in the presence of water vapor, with a fuel that provides the heat that is necessary to the reaction, A stage for conversion to vapor of the synthetic gas that is obtained in the preceding stage producing a hydrogen stream that contains methane and carbon dioxide, A stage for recovering carbon dioxide that is present in the stream that is obtained in the stage for conversion to vapor, making it possible to separate the carbon dioxide from the hydrogen stream, A stage for recovery and recycling to the vapor reforming stage of impurities that are present in the hydrogen stream, comprising a decompression phase.

Abstract: A process of catalytic partial oxidation of a hydrocarbon fuel with an oxidant to produce partially-oxidized reaction products including hydrogen, with simultaneous in-situ coke removal. The process involves feeding a hydrocarbon fuel and an oxidant to a reactor in a fuel-rich feed ratio; reacting the fuel and oxidant for a fuel-rich cycle-time so as to produce a partially-oxidized reaction product; varying the fuel feed, or the oxidant feed, or both feeds to produce a fuel-lean feed to the reactor; maintaining the fuel-lean feed for a fuel-lean cycle-time sufficient to reduce coke deposits while maintaining a substantially constant yield of partially-oxidized reaction product; and alternating between the fuel-rich and fuel-lean operating cycles.

Abstract: A system includes a gasification vessel configured to receive a fuel and an oxidizer. The system also includes a gasifier disposed in the gasification vessel. The gasifier is configured to partially oxidize the fuel and the oxidizer to generate a syngas. The system further includes a convective syngas cooler configured to cool the syngas via heat exchange with a coolant. The convective syngas cooler is disposed in an interior of the gasification vessel.

Abstract: A catalyst composition for the oxidation of carbon monoxide and volatile organic compounds and for hydrogenation reactions comprises at least two different high surface area oxide support materials wherein at least one of the high surface area support material supports at least one base metal promoter.

Abstract: The inventive stage system for producing hydrogen consists of at least two upstream/downstream stages, respectively, each of which comprises, optionally, a catalytic reactor (C1 to C5) followed by a separator comprising a space (E1 to E4) for circulation of a gaseous mixture contacting at least one oxygen extracting membrane and a hydrogen collecting space, wherein the reactor (C1) of the upstream stage is connected to a reaction gaseous mixture source, the circulation stage (E1) of the upstream stage separator is connected to the reactor (C2) of the downstream stage and the spaces for extracting/collecting oxygen from two separators are connected to a hydrogen collecting circuit (TC, 8) which is common for two stages.

Abstract: A system and method of capturing carbon dioxide from a flow of raw synthesis gas generated in a gasification system are provided. The carbon capture system includes an acid gas removal subsystem configured to generate a flow of reduced acid gas content syngas, a flow of hydrogen sulfide (H2S) lean gas, and a first flow of H2S-rich gas from a stream of particulate-free raw syngas, an H2S selective membrane separator, said H2S selective membrane separator configured to separate the flow of H2S-lean gas from the AGR into a second flow of H2S-rich gas and a flow of CO2 gas, and a sulfur recovery unit (SRU) coupled in flow communication with said H2S membrane separator downstream of said membrane separator, said SRU configured to generate a flow of elemental sulfur and a flow of tail gas from the first flow of H2S-rich gas and the second flow of H2S-rich gas.

Abstract: An exhaust gas treating system for a gasoline engine, comprising an exhaust gas manifold comprising an annular reforming catalyst mounted within an annular housing and fuel supply means in direct fluid connection with the catalyst, an outlet for reformed fuel products in direct fluid connection with the catalyst, and means to permit a proportion of the engine-out exhaust gases to enter the annular catalyst to mix with fuel from the fuel supply means and to pass through the catalyst, the annular housing being located such that hot engine-out exhaust gases can flow around and through the center of the housing, such that heat is transferred from the exhaust gases to the catalyst within the housing. The reformate may be passed to the inlet side of the engine, to improve overall efficiency of the engine, and/or may be mixed with exhaust gas before catalytic aftertreatment, to improve the control of emissions.

Abstract: In a reforming apparatus, for use in a fuel cell, for reforming a raw fuel into a hydrogen-rich reformed gas, a reformer generates the reformed gas from the raw fuel. A shift reactor reduces carbon monoxide contained in the reformed gas through a shift reaction. A selective oxidation unit reduces the carbon monoxide contained in the reformed gas that has passed through the shift reactor by performing selective oxidation on the carbon monoxide. A reforming reaction tube houses linearly the reformer, the shift reactor and the selective oxidation unit in this order.

Abstract: The present invention relates to a process and a plant for the treatment of the vented gas mixture from a deaerator of a steam production process associated with a hydrocarbon-reforming syngas production process.

Abstract: A diesel engine having an inlet side and an outlet side provided with at least one inlet valve and one outlet valve per cylinder, comprises a reformer catalyst unit comprising a catalyst located downstream of the outlet valve(s) and located such that a proportion of the hot exhaust passes through the catalyst while the remainder of the hot exhaust passes to a turbocharger and/or to exhaust gas aftertreatment, wherein the catalyst unit is provided with diesel fuel supply means, preferably in the form of a diesel fuel injector, such that diesel fuel may be injected to provide heat to the reformer catalyst to raise it to an effective reforming temperature. The output from the reformer unit may be fed to the inlet side of the engine, and/or may be admixed with the remainder of the exhaust gases prior to catalytic aftertreatment. Improvements in emission control are possible.

Abstract: A gasifier 10 includes a first chemical process loop 12 having an exothermic oxidizer reactor 14 and an endothermic reducer reactor 16. CaS is oxidized in air in the oxidizer reactor 14 to form hot CaSO4 which is discharged to the reducer reactor 16. Hot CaSO4 and carbonaceous fuel received in the reducer reactor 16 undergo an endothermic reaction utilizing the heat content of the CaSO4, the carbonaceous fuel stripping the oxygen from the CaSO4 to form CaS and a CO rich syngas. The CaS is discharged to the oxidizer reactor 14 and the syngas is discharged to a second chemical process loop 52. The second chemical process loop 52 has a water-gas shift reactor 54 and a calciner 42. The CO of the syngas reacts with gaseous H2O in the shift reactor 54 to produce H2 and CO2. The CO2 is captured by CaO to form hot CaCO3 in an exothermic reaction.

Abstract: A reactor vessel includes a dipleg connecting a tubular syngas collection chamber and a quench chamber. The collection chamber connects to the dipleg via a slag tap having a frusto-conical part starting from the lower end of the collection chamber and diverging to an opening connected to an interior of the dipleg. The slag tap has a first tubular part connected to the opening of the frusto-conical part and extending in the direction of the dipleg. A second tubular part connects to the frusto-conical part or to the tubular part and extends toward the dipleg. The second tubular part is spaced away from the dipleg to provide an annular space having a discharge conduit. The discharge conduit has a discharge opening located to direct water along the inner wall of the dipleg. At least half of the vertical length of the first tubular part extends below the discharge opening.

Abstract: In a reactor for the gasification of solid and liquid fuels in the entrained flow at temperatures between 1200 and 1900° C. and pressures between ambient pressure and 10 MPa with an oxidizing agent containing free oxygen, the cooling screen is connected in a gas-tight manner to the pressure shell via a bellows compensator to accommodate linear deformation. Continuous sweeping by gas of the annular gap between pressure shell and cooling screen is unnecessary and backflow by producer gas is prevented.

Abstract: In a reactor for gasification of entrained solid and liquid fuels at temperatures between 1,200 and 1,900° C. and at pressures between ambient pressure and 10 MPa using an oxidizing agent containing free oxygen, the cooling screen is connected to the pressure shell in a gastight manner via a sliding seal in order to allow length changes. Continuous gas purging of the annular gap between pressure shell and cooling screen is unnecessary and gasification gas is prevented from flowing behind.

Abstract: A system includes a radiant syngas cooler (RSC). The RSC includes cooling tubing configured to transmit a fluid. The RSC is configured to have a heat transfer area such that the RSC generates a pressure and a temperature of the fluid exiting the RSC to a level allowing for superheating of the fluid to between approximately 750° Fahrenheit and approximately 850° Fahrenheit. Additionally, the heat transfer area is determined based on an amount of heat to be transferred to the fluid as the fluid passes through a heat exchanger in a first path external to the RSC.

Abstract: Reformer and method for producing hydrogen and steam where steam is used for steam-assisted extraction of heavy hydrocarbons. Steam is injected into a hydrocarbon-containing reservoir. Hydrocarbons are extracted from the reservoir along with produced water. Hydrogen is produced in a catalytic steam hydrocarbon reformer. Combustion product gas from the reformer is used to generate wet steam in a once-through steam generator from produced water recycled from the reservoir. The wet steam is used for the steam-assisted extraction of heavy hydrocarbons. The reformer has a heat exchanger section including a first heat exchanger and a second heat exchanger downstream of the first heat exchanger. The second heat exchanger is suitable for processing the produced water by once-through steam generation and is suitable for mechanical cleaning. The reformer also has a first exhaust downstream of the second heat exchanger and a closeable second exhaust downstream of the first heat exchanger.

Abstract: A system for reforming diesel fuel into hydrogen including feeds for water and diesel fuel, a supercritical water (SCW) reactor in fluid communication with the water feed and the diesel fuel, at least one pre-heater in thermal communication with the water feed, the diesel fuel feed that is configured to heat water from the water feed and diesel fuel from the diesel fuel feed to a predetermined temperature equal to or greater than the critical temperature of water before the water and the diesel fuel are mixed, a water-gas shift (WGS) reactor, and a hydrogen capturing system, where the SCW reactor reforms the diesel fuel into a synthesis gas comprising a mixture of hydrogen and carbon monoxide and outputs the synthesis gas, the synthesis gas output by the SCW reactor is fed into the WGS reactor which converts the carbon monoxide into carbon dioxide and hydrogen and outputs an output gas including a higher percentage of hydrogen to carbon monoxide compared to the synthesis gas, and the hydrogen in the output ga

Abstract: A process and device for the material utilization of soot from the waste water of a gasification appliance (heavy oil POX) in which a hydrogen- and carbon monoxide-containing (crude synthesis gas) is generated from relatively high-boiling hydrocarbons by partial oxidation, is disclosed. The soot-loaded waste water from the heavy oil POX is mixed with naphtha and is subsequently introduced into a separator (decanter) from which a substantially soot-free water fraction and a substantially water-free naphtha/soot mixture are taken off separately, where the naphtha/soot mixture is fed as feed to a further gasification appliance (naphtha POX), in which appliance predominantly naphtha is converted into a crude synthesis gas by partial oxidation.

Abstract: The present subject matter is directed to a method for operating a fuel reformer. The method may generally include directing a fluid stream around a reactor assembly of the fuel reformer to cool the reactor assembly, and mixing a heated reformate stream produced by the reactor assembly with the fluid stream to cool the heated reformate stream.

Abstract: An apparatus suitable for generating gaseous hydrocarbon fuel from a carbon based synthesis gas including a reaction chamber having a rotating shaft including a plurality of radial blades mixing and circulating carbon based synthesis gas and particulate catalyst upwardly generating gaseous hydrocarbon fuel, a stripping chamber located above the reaction chamber having a second axial rotating shaft including a plurality of radial blades driving hydrocarbon fuel radially outwardly, a source of hot stripping gas, an annular filter surrounding the stripping chamber and an annular gas collection chamber surrounding the filter. The blades in the stripping chamber are rotated independently at a greater velocity than the blades in the reaction chamber and the reaction is controlled by the temperature of the synthesis gas and the rotational velocity of the mixing blades in the reaction chamber.

Abstract: The invention relates to a method for producing hydrogen and power from a synthesis gas that contains CO, H2 and H2S. The synthesis gas is separated into two partial streams, vapor is added to the first partial stream of synthesis gas, out a CO conversion is carried out at a temperature of 220° C. to 500° C., pure hydrogen is obtained from the converted synthesis gas in a pressure swing absorption device and a residual PSA gas is produced. The second partial stream of synthesis gas is fed to a power-generating gas turbine for combustion, H2S and optionally other sulfur-containing components are removed in one or more separators that are arranged in any position in the process, however, before entry into the gas turbine, the residual PSA gas is mixed with nitrogen, the gas mixture so obtained is compressed and the compressed gas mixture is admixed to the partial stream of synthesis gas that is fed to the power-generating gas turbine.

Abstract: The present subject matter discloses a fluid cooled reformer for gas turbine systems and a method for cooling both a fuel reformer and a heated reformate stream produced by such fuel reformer. The fluid cooled reformer may include a pressure vessel and a reactor assembly disposed within the pressure vessel. The reactor assembly may include a reactor and may be configured to receive and reform an oxygen/fuel mixture to produce a heated reformate stream. Additionally, the fluid cooled reformer may include an inlet configured to direct a fluid stream into the pressure vessel. At least a portion of the fluid stream may be used to cool the reactor assembly. A reformate cooling section may be disposed downstream of the reactor of the reactor assembly and may be configured to cool the heated reformate stream.

Abstract: A quench ring for use with a gasifier system. The quench ring including an annular manifold having a radius, an annular channel coupled in flow communication with said manifold, and at least one inlet coupled in flow communication with said manifold, said at least one inlet having a center line aligned substantially tangentially to said annular manifold.

Abstract: When odorant injection systems are inactive, they may accumulate unwanted vapors in the pump mechanism and associated tubing. In order to restart the odorant injection system, it is best to purge the unwanted vapors from the odorant pumps. The present pump purge system facilitates purging of unwanted vapors from odorant injection systems in an environmentally friendly fashion. The pump purge system purifies these vapors before they are vented to atmosphere. In addition, the pump purge system accumulates liquid odorant which is a byproduct of the purging process and stores it in a tank to reduce the likelihood of improper disposal. As an option, the pump purge system may also include a liquid odorant recapture system. The liquid odorant recapture system uses high pressure gas to return accumulated liquid odorant to the odorant injection system to be reused. This liquid odorant recovery system ensures environmentally responsible behavior.

Abstract: A method of cooling hot fluid flowing through a chamber is provided. The method includes channeling cooling fluid through at least one cooling tube that extends through a passage of the chamber, and circulating the hot fluid flowing within the passage around the at least one cooling tube using at least one fluid diverter.

Abstract: A process for producing a hydrogen-containing product gas with reduced carbon dioxide emissions compared to conventional hydrogen production processes. A hydrocarbon and steam are reformed in a reformer and the resulting reformate stream is shifted in one or more shift reactors. The shifted mixture is scrubbed to remove carbon dioxide to form a carbon dioxide-depleted stream. The carbon dioxide-depleted stream is separated to form a hydrogen-containing product gas and a by-product gas. A portion of the hydrogen containing product gas is used as a fuel in the reformer and a portion of the by-product gas is recycled back into the process. The process may optionally include reforming in a prereformer and/or an oxygen secondary reformer.

Abstract: A process of generating power utilizing a low level heat from a raw syngas produced in a quench gasifier is disclosed. The process includes a first stage that includes: producing raw syngas at the quench gasifier, making 150 psi saturated steam from the produced raw syngas, superheating the saturated steam, and using the superheated saturated steam in a low pressure steam turbine to generate power. The process includes a second stage that includes: providing the raw syngas and a process condensate stream to a thermal fluid vaporizer to vaporize an organic thermal fluid, and using the vaporized organic thermal fluid in an expander turbine to generate power via an organic Rankine cycle.

Abstract: A unified fuel processing reactor for a solid oxide fuel cell can reform hydrocarbon-based fuel into hydrogen-rich gas, remove a sulfur component, and convert non-converted fuel and a low carbon (C2˜C5) hydrocarbon compound into hydrogen and methane in a single reactor. The reactor comprises a primary-reformer which reforms a hydrocarbon-base fuel and generates hydrogen-rich reformed gas, a desulfurizer which removes a sulfur component from the reformed gas, and a post-reformer which selectively decomposes a low carbon (C2˜C5) hydrocarbon in the desulfurized reformed gas into hydrogen and methane. The primary-reformer, desulfurizer and post-reformer are in the unified reactor and isolated, except for a fluid passage, from each other by internal partition walls. The primary-reformer is disposed at a center portion of the reactor. The post-reformer and the desulfurizer are concentrically disposed outside of the primary-reformer.

Abstract: A method of hydrogenation of unsaturated hydrocarbons for syngas production is presented. A hydrogenation feed reactor stream is introduced into a hydrogenation reactor, thereby producing a reformer feed stream. The reformer feed stream is introduced into a reformer, thereby producing a crude syngas stream. The crude syngas stream is introduced into a water gas shift converter, thereby producing a hydrogen-rich stream. The hydrogen-rich stream is separated in a separation means, thereby producing a carbon dioxide-rich stream and a hydrogen product stream. At least a portion of the hydrogen product stream is combined with a refinery fuel gas stream, and a natural gas stream, to form the hydrogenation reactor feed stream.

Abstract: A system and process are disclosed for the controlled combustion of a wide variety of hydrocarbon feedstocks to produce thermal energy, liquid fuels, and other valuable products with little or no emissions. The hydrocarbon feeds, such as coal and biomass, are first gasified and then oxidized in a two-chamber system/process using pure oxygen rather than ambient air. A portion of the intermediate gases generated in the system/process are sent to a Fischer-Tropsch synthesis process for conversion into diesel fuel and other desired liquid hydrocarbons. The remaining intermediate gases are circulated and recycled through each of the gasification/oxidation chambers in order to maximize energy production. The energy produced through the system/process is used to generate steam and produce power through conventional steam turbine technology.

Abstract: A system and process for maximizing the generation of marketable products from a variety of hydrocarbon feedstocks. The hydrocarbon feedstocks are first gasified and then oxidized in a two-chamber system and process using oxygen gas rather than ambient air. Intermediate gases generated in the system and process are recirculated and recycled to the gasification and oxidation chambers in order to maximize both energy generation and the resulting stoichiometric reaction products. The energy produced through the system and process is used to generate steam and produce power through conventional steam turbine technology. In addition to the release of heat energy, the hydrocarbon feedstocks are oxidized to the pure product compounds of water and carbon dioxide. The carbon dioxide is subsequently purified and marketed. The water recovered from the system and process is collected and electrolyzed to generate oxygen and hydrogen gases.

Abstract: A supercritical water reformer (SCWR) and methods for using supercritical water to convert hydrocarbons, particularly hydrocarbon fuels such as diesel fuel or gasoline, into carbonaceous gases and hydrogen. The synthesis gas stream generated by the fuel reforming reaction can then be further refined to increase hydrogen content, and the resultant hydrogen can be utilized to power fuel cells.

Abstract: A gasifier 10 includes a first chemical process loop 12 having an exothermic oxidizer reactor 14 and an endothermic reducer reactor 16. CaS is oxidized in air in the oxidizer reactor 14 to form hot CaSO4 which is discharged to the reducer reactor 16. Hot CaSO4 and carbonaceous fuel received in the reducer reactor 16 undergo an endothermic reaction utilizing the heat content of the CaSO4, the carbonaceous fuel stripping the oxygen from the CaSO4 to form CaS and a CO rich syngas. The CaS is discharged to the oxidizer reactor 14 and the syngas is discharged to a second chemical process loop 52. The second chemical process loop 52 has a water-gas shift reactor 54 and a calciner 42. The CO of the syngas reacts with gaseous H2O in the shift reactor 54 to produce H2 and CO2. The CO2 is captured by CaO to form hot CaCO3 in an exothermic reaction.

Abstract: A method of operating a methanation reactor to reduce carbon monoxide concentration in a reformate stream in a fuel cell reformer. The reactor includes a flowpath with a noble metal catalyst supported by a ceramic support such that the reactor preferentially converts carbon monoxide via methanation over that of carbon dioxide. The reduced level of carbon monoxide present in the reformate stream after passing through the methanation reactor reduces the likelihood of poisoning of the catalyst used on the fuel cell anode.