US20130017460A1 - Sorption enhanced methanation of biomass - Google Patents
Sorption enhanced methanation of biomass Download PDFInfo
- Publication number
- US20130017460A1 US20130017460A1 US13/474,494 US201213474494A US2013017460A1 US 20130017460 A1 US20130017460 A1 US 20130017460A1 US 201213474494 A US201213474494 A US 201213474494A US 2013017460 A1 US2013017460 A1 US 2013017460A1
- Authority
- US
- United States
- Prior art keywords
- hydrogen
- catalyst
- hydroconversion
- methane
- sorbent
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Abandoned
Links
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/047—Pressure swing adsorption
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/22—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
- C10B49/16—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form
- C10B49/20—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form in dispersed form
- C10B49/22—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form in dispersed form according to the "fluidised bed" technique
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
- C10B53/02—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/04—Other carbonising or coking processes; Features of destructive distillation processes in general using charges of special composition
- C10B57/06—Other carbonising or coking processes; Features of destructive distillation processes in general using charges of special composition containing additives
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/463—Gasification of granular or pulverulent flues in suspension in stationary fluidised beds
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/02—Dust removal
- C10K1/026—Dust removal by centrifugal forces
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/32—Purifying combustible gases containing carbon monoxide with selectively adsorptive solids, e.g. active carbon
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
- C10K3/02—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment
- C10K3/04—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment reducing the carbon monoxide content, e.g. water-gas shift [WGS]
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/08—Production of synthetic natural gas
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/102—Removal of contaminants of acid contaminants
- C10L3/104—Carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/24—Hydrocarbons
- B01D2256/245—Methane
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/10—Single element gases other than halogens
- B01D2257/108—Hydrogen
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
- C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/06—Integration with other chemical processes
- C01B2203/062—Hydrocarbon production, e.g. Fischer-Tropsch process
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0916—Biomass
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0966—Hydrogen
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0973—Water
- C10J2300/0976—Water as steam
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0983—Additives
- C10J2300/0996—Calcium-containing inorganic materials, e.g. lime
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
- C10J2300/1656—Conversion of synthesis gas to chemicals
- C10J2300/1662—Conversion of synthesis gas to chemicals to methane (SNG)
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/141—Feedstock
- Y02P20/145—Feedstock the feedstock being materials of biological origin
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Definitions
- the process of the invention applies to hydropyrolysis of carbonaceous feedstocks, and particularly of forestry residues, to generate higher value synthetic fuels, in particular methane and optionally liquid hydrocarbons.
- Thermochemical conversion of biomass such as sawmill wood wastes, forestry residues and agricultural wastes into synthetic fuels is an important emerging avenue for advancement of renewable energy sources to supplement or replace fossils fuels. While air blown gasification is used for generation of lower heating value fuel gas, several variants of oxygen or steam gasification can be used for production of syngas containing minimal nitrogen.
- Syngas is a gas mixture containing mostly hydrogen and carbon monoxide, and is a versatile feedstock for further chemical processing into a wide range of useful fuels and chemical compounds.
- Syngas can be catalytically converted into methane, Fischer-Tropsch liquid fuels, methanol, dimethyl ether, or hydrogen.
- the methanation reaction of syngas to generate methane and byproduct water vapour is typically conducted over nickel catalysts at temperatures in the range of about 300° C. to about 400° C., and preferably at elevated pressure.
- Methane is readily marketed and delivered through existing natural gas distribution infrastructure as substitute natural gas (SNG) for numerous end uses including space heating and electrical power generation. Methane has considerably higher energy density than hydrogen, and can be converted into syngas or hydrogen by catalytic steam reforming. Modern combined cycle power plants are conveniently fueled by natural gas. Methane is also a particularly advantageous fuel for future high temperature fuel cell power plants using highly endothermic internal steam reforming of natural gas to recover high grade heat generated by the fuel cell stack.
- SNG substitute natural gas
- reaction of steam with biomass to generate syngas is highly endothermic, hence conducted with direct or indirect heating by partial oxidation with air or oxygen; and is typically conducted at much higher temperature than the subsequent exothermic methanation reaction.
- the thermal mismatch between gasification and methanation reactions is detrimental to process efficiency.
- Hydrogasification has previously been investigated for gasification of biomass.
- the key reaction is hydrogenation of carbon to form methane, whose exothermicity is a great advantage compared to other gasification approaches.
- the gas composition produced in biomass gasification approaches a complex equilibrium established between CO, CO 2 , H 2 , H 2 O and CH 4 which is a function of temperature, pressure and overall gas composition. Reforming reactions producing syngas increasingly dominate the equilibrium at temperatures above 650° C. at the expense of hydrocarbons, CO 2 and water.
- catalysts such as the use of olivine, dolomite or nickel coated media in fluidized beds, to enhance the rate of syngas formation is well known. These catalysts allow a faster reaction towards syngas equilibrium favoured under the process conditions. Catalysts have also been used in a secondary bed in series with the gasifier for the reduction of tars contained in the syngas or producer gas.
- An oxygen blown entrained flow gasifier may typically operate at about 1300° C. to 1500° C., at which temperatures methane and higher hydrocarbons are all nearly entirely converted to syngas. This has the important advantage of almost completely eliminating tar constituents, but the disadvantage for SNG production that all of the product methane must be generated by the exothermic methanation of syngas at much lower temperature than the gasification temperature.
- Indirect steam gasifiers (such as the US Battelle/FERCO “Silvagas” system, the Austrian fast internally circulating fluidized bed (FICFB) system, and the Dutch ECN “Milena” system) operate at about 850° C. These systems use twin bed configurations, in which fluidized granular heat transfer media is circulated between a gasification zone in which steam reacts with the biomass to produce syngas and char, and an air-blown regeneration zone in which the char is combusted to reheat the media.
- the product syngas contains a significant admixture of methane generated within the gasifier.
- AER adsorption enhanced reforming
- a CO 2 acceptor such as lime or calcined dolomite
- the AER process has been disclosed by Specht et al. (European patent publications EP 1,218,290 B1 and EP 1,637,574 A1).
- the principle of the AER process is to generate hydrogen-rich syngas by shifting the reaction equilibria of the steam reforming and water gas shift reactions by CO 2 removal.
- the AER process has been tested in the FICFB twin bed system, and is being developed for SNG production by using a molten salt methanation reactor to convert the syngas into methane.
- SER sorption enhanced reforming
- AER absorption enhanced reforming
- Methanation as described in this disclosure is hydroconversion of a pyrolysis gas to produce methane, including but not confined to the conversion of syngas to methane.
- Thermodynamic modeling indicates that slightly more than half of the carbon not rejected as char or coke deposits can be converted to methane under conditions of hydrogen self-sufficiency. Approximately 20% of the carbon originally in the biomass will typically be rejected as char or coke to be combusted or gasified in the regeneration reactor. If a supplemental source of hydrogen is available, the conversion of feed carbon to methane can be increased within the scope of the present invention, while even less of the carbon will be removed by carbonation of the sorbent.
- SEM may be advantageously operated at moderately elevated working pressures in a range of just over 1 bara to about 50 bara, or in a preferred range of from about 5 bara to about 30 bara. While SEM can be conducted at atmospheric pressure, the methane concentration will be lower than at higher operating pressures, thus making the gas separation of hydrogen and methane more difficult. Conventional methanation requires much higher working pressures to achieve satisfactory conversion.
- a preferred CO 2 sorbent for SEM is CaO, which can be used in any suitable form, or combinations thereof, such as calcined limestone or dolomite, or CaO on a suitable support such as alumina.
- CaO is readily carbonated at working temperature around 600° C. and moderate pressures from atmospheric upward. Such temperature and pressure conditions have been found to be favourable for the hydrogasification of biomass pyrolysis gas to methane, and for steam reforming of methane to generate hydrogen.
- CO 2 sorbents or “acceptors” will work in the temperature range of from about 500° C. to about 650° C. of interest for SEM. These include calcined dolomite, calcium oxide, calcium hydroxide, lithium zirconate, lithium orthosilicate, and other metal oxides or hydroxides that can react with carbon dioxide to form a carbonate phase.
- CO and CO 2 are extracted from the oxygenated pyrolysis gas by decarbonylation and decarboxylation respectively, in parallel with extraction of H 2 O by hydrodeoxygenation.
- Suitable CO 2 sorbents for the temperature range of from about 300° C. to about 400° include potassium-promoted hydrotalcites, magnesia supported on alumina, or dolomite in combination with alkali (and particularly potassium) promoters.
- the fast pyrolysis step may be performed with externally heated media, e.g. circulating through a pressurized auger reactor, and preferably as hydropyrolysis in a hydrogen atmosphere.
- the heat transfer media may include circulating magnetite pellets, which are readily separable from char according to density and magnetic properties. Some impurities such as alkalis, other metals, sulphur, and chloride will be partially entrained by the char. While very fast pyrolysis will minimize char production, slower pyrolysis may also be considered for coproduction of charcoal or biochar with lower yield of methane and any other desirable hydrocarbon products.
- the catalytic conversion step includes catalytic hydrogasification, such as steam hydrogasification. Hydroconversion, hydrodeoxygenation, and hydrocracking reactions will take place. The net reaction will be exothermic.
- This step may be conducted alternatively in any suitable reactor architecture, such as the following reactor architectures:
- the hydrogasification process requires a source of hydrogen, either externally supplied or internally generated.
- steam addition, plus moisture contained in feed biomass provides sufficient steam for internal, self-sustaining generation of hydrogen required for the hydrogasification reaction to convert biomass feedstock into methane.
- the process may generate excess syngas or hydrogen so that coproduction of methane and hydrogen/syngas may be contemplated. Coproduction of methane and higher hydrocarbon fuel commodities is also attractive.
- the process also may include cleaning steps to remove catalyst poisons (alkalis, other metals, phosphorus, sulfur, chloride, etc.) and tars. Hot or cold clean-up process alternatives are well known.
- Hot clean-up steps include sorbents (e.g. ZnO to remove sulphur), and catalytic tar cracking followed by cool-down in cyclic thermal regenerator loaded with layers of fine filtration metal matrix, porous ceramic, catalyst and adsorbent. Regeneration can be achieved by burning off tar and coke deposits, then air flush to cool the filtration matrix and provide hot air for front end feed dryer.
- sorbents e.g. ZnO to remove sulphur
- catalytic tar cracking followed by cool-down in cyclic thermal regenerator loaded with layers of fine filtration metal matrix, porous ceramic, catalyst and adsorbent. Regeneration can be achieved by burning off tar and coke deposits, then air flush to cool the filtration matrix and provide hot air for front end feed dryer.
- Cold clean-up can be achieved by higher temperature oil quench and wash, followed by lower temperature water quench and wash.
- the process may also include gas separation steps for removing CO 2 , for recovering a hydrogen-enriched recycle stream for the hydrogasification step, and/or for purifying the product methane.
- gas separation alternatives include carbonation of CaO or pressure swing adsorption (PSA) for CO 2 removal, and PSA or polymeric membranes for separation of H 2 from CH 4 .
- One disclosed apparatus includes a hydropyrolysis reactor.
- Alternative embodiments include a single stage reactor, or a two-stage system including a pyrolysis or hydropyrolysis reactor as the first stage, and a methanation or hydroconversion reactor as the second stage.
- the process achieves catalytic steam hydrogasification, with catalytic hydrocracking of tars favoured by relatively high hydrogen partial pressure.
- the process includes sequential steps for (1) the working reaction by hydrogasification or hydroconversion combined with sorbent carbonation, and (2) regeneration of sorbent and catalysts. Combined regeneration of the sorbent (carbon dioxide acceptor) and catalyst is a very attractive operating mode.
- Alternative reactor configurations include fixed beds with granular or monolithic catalyst with directional or rotary valves for cyclic switching of beds between the process steps of working reaction and regeneration, or fluidized beds with circulation to achieve the process steps.
- Twin fluidized beds are a suitable architecture for indirect steam gasifiers, achieving the working reaction in one bed, and regeneration by combustion of char in the other bed.
- An important aspect of the invention is heat management. Combined exothermicity of sorption carbonation and methanation reactions provide abundant heat for preheating feedstock and steam generation, with reduced need for feedstock drying. Heat for sorbent and catalyst regeneration can be generated by combustion of relatively low value fuels, such as byproduct char or raw biomass feedstock.
- Water slurry feed is mechanically attractive, but is incompatible with the normal requirement that the feed biomass be substantially dry.
- the present process is tolerant of relatively wet feed, because of the strong combined exothermicity of the methanation and sorbent carbonation reactions.
- Another novel approach for slurry feed within the present invention is to provide a pusher centrifuge dewatering system within the high pressure containment volume of the plant.
- Catalyst and sorbent regeneration can be achieved in a regeneration reactor zone integrated with the pressurized combustor of gas turbine, or supplied with superheated steam with optional addition of enriched oxygen.
- High methane yield can be achieved in hydrogasification, however in absence of a supplemental source of imported hydrogen up to half of that methane may be consumed downstream to generate recycle hydrogen and CO 2 .
- a preferred operating mode is defined by self-sustaining recycle of H 2 generated within a catalytic stage, with just enough H 2 excess to compensate for incomplete recovery in downstream gas separation of recycle H 2 .
- Methane yield is approximately 50% of carbon after char production, with the remaining carbon being converted to CO 2 .
- Supplemental hydrogen may provided from any combination of (a) an external source of hydrogen-rich gas such as stranded hydrogen offgas from a chlor-alkali or ethylene plant, or (b) oxygen or steam gasification of char, or (c) steam methane reforming of a portion of the methane product.
- the process may be operated with any amount of hydrogen recycle, including the limiting case of zero hydrogen recycle, in which case the methane rich product gas will contain relatively less hydrogen but significantly larger amounts of carbon dioxide and carbon monoxide.
- zero methane is delivered so that maximum hydrogen may be generated; and hydrogen-rich syngas may then be delivered as a desired product.
- Coproduction of methane and hydrogen, or hydrogen-rich syngas is an option within the scope of the invention.
- Separation of hydrogen and methane can be achieved by pressure swing adsorption, membrane permeation, refrigerated hydrate formation or cryogenics. While sorption-enhanced reactors for SMR and/or methanation have integrated bulk CO 2 removal, further purification of product streams will generally be needed to remove slip of CO or CO 2 as required.
- the invention provides a wide spectrum of cogeneration opportunities.
- the process can generate a range of hydrocarbon products (methane, LPG, and liquid hydrocarbons).
- Syngas and hydrogen are generated within the process, either consumed entirely within the hydrocarbon producing hydroconversion processes, or alternatively a portion of syngas or hydrogen may be exported as a useful product at some penalty of reducing the conversion of biomass carbon to hydrocarbons.
- Syngas is an intermediate for synthesis of a wide range of useful fuel and chemical products.
- the hydropyrolysis reaction delivers a product stream of methane plus hydrogen, and minor amounts of CO and CO 2 .
- Syngas may also be generated by oxygen/steam gasification of char.
- the syngas generated by char gasification will typically have a low ratio of H 2 to CO, which can be upgraded by admixture with H 2 generated by the hydropyrolyser.
- a ratio of H 2 :CO ⁇ 2 is desirable for synthesis of methanol, dimethyl ether, or Fischer-Tropsch hydrocarbons.
- Cogeneration opportunities provided by the invention include the production of energy as heat or electricity. Heat recovery within the process can readily generate steam at different temperatures. Product or byproduct fuels can be used to power electrical generators through gas turbines, internal combustion engines or steam turbines. Some of the most attractive future applications of the present invention will be obtained by integration of high temperature fuel cells with the hydrogasfication of biomass.
- biomass hydrogasification may be directly integrated with SOFC power plants having enriched H 2 recycle for the anode of an internal reforming SOFC.
- the present invention develops practicable implementations of that opportunity. Without the relatively low operating pressures enabled by the inventive sorption enhanced methanation process, it would be very difficult to integrate the usually relatively low pressure SOFC system with the relatively high pressure hydrogasification processes.
- a concentrated product stream of CO 2 can be delivered for useful applications including enhanced oil recovery, or for disposal by underground sequestration.
- FIG. 1 is a schematic diagram of one embodiment of an apparatus according to the present invention.
- FIG. 2 shows an embodiment with integration to a gas turbine power plant.
- FIGS. 3 and 4 show an embodiment with a rotary reactor including cyclically switched hydrogasification and regeneration zones.
- FIG. 5 shows a fluidized twin bed embodiment of the invention.
- FIG. 6 shows a two stage double twin bed fluidized embodiment.
- FIG. 7 shows a two stage embodiment, with the first stage a fluidized bed hydropyrolysis reactor and the second stage a methanation or hydroconversion reactor with a cyclic rotary switching mechanism.
- FIG. 8 shows an embodiment for coproduction of methane and liquid hydrocarbons.
- FIG. 9 shows an embodiment with a hydrogasification system coupled to a solid oxide fuel cell (SOFC) for generation of electricity.
- SOFC solid oxide fuel cell
- FIG. 10 is a graph of methane conversion, methane concentration, hydrogen concentration, and the ratio of hydrogen output to hydrogen input from the hydrogasification reactor of the invention, versus the ratio of carbon carbonated on the sorbent to carbon content of the biomass feed to the process.
- FIG. 1 shows a simplified schematic of a system or apparatus 1 according to the invention.
- Apparatus 1 includes a feed preparation section 2 , a feed pressurization section 3 , a hydrogasification reactor 4 , a solids separation section 5 , a regeneration reactor 7 , a heat recovery section 8 , a tar scrubber 9 , and a gas separation section 10 .
- the gas separation section 10 separates hydrogen from methane, and may be based on selective membranes or on pressure swing adsorption (PSA).
- PSA pressure swing adsorption
- Gas separation section 10 delivers a substantially purified methane product stream from conduit 11 , and a hydrogen-enriched recycle stream back to hydrogasification reactor 4 via conduit 12 .
- the gas separation system 10 can be operated so as to minimize hydrogen concentration in the product methane stream, thus preventing most of the hydrogen from exiting apparatus 1 until consumed in hydrogasification to produce the desired methane product.
- a membrane permeation system may be advantageously used as gas separation system 10 for purification of product methane and separation of hydrogen-rich gas for recycle to hydrogasification.
- the polymeric membrane will selectively permeate hydrogen, carbon monoxide, carbon dioxide and water vapour relative to methane.
- three membrane stages may be used in series to progressively concentrate methane with high recovery and purity in the retentate stream.
- the feed gas is introduced to the inlet of the first stage, from which the hydrogen-enriched recycle gas will be delivered as low pressure permeate.
- the permeate of the second stage will be recompressed to join the feed at the inlet of the first stage, while the permeate of the third stage will be recompressed to the inlet of the second stage.
- pressure swing adsorption may be used as gas separation system 10 for purification of product methane and separation of hydrogen-rich gas for recycle to hydrogasification.
- Hydrogasification reactor 4 and regeneration reactor 7 comprise a coupled reactor pair for the working hydrogasification reaction and regeneration steps.
- Each of reactors 4 and 7 comprises at least one bed containing a CO 2 sorbent, and optionally also another solid component having catalytic and favourable heat transfer media characteristics. It is contemplated that the beds will cycle or be switched between the hydrogasification and regeneration reaction zones.
- Pressure and temperature conditions in the hydrogasification reactor 4 will be selected to be favourable for combined methanation and steam reforming reactions such that the process achieves self-sufficiency in producing the amount of hydrogen needed for the methanation reaction, while also favourable for the carbonation reaction binding CO 2 to the sorbent.
- the regeneration reactor 7 will typically be operated at relatively higher temperature in order to release the CO 2 from the sorbent, and may be operated at substantially the same pressure or at lower pressure to facilitate regeneration and reduce air compression requirements for regeneration.
- a preferred CO 2 sorbent is CaO, alternatively provided by calcining of natural limestone or dolomite, or by synthesis to achieve enhanced mesoporosity and stability for extended cycling without rapid deactivation due to sintering and pore blockage.
- CaO a preferred CO 2 sorbent
- composite structures comprising CaO supported on or encapsulated in a mesoporous ceramic (e.g. alumina) may achieve superior durability against deactivation, while also providing a hardened external shell for superior attrition resistance.
- Such mesoporous composite structures may be usefully applied in fixed bed monoliths as well as in granular media for fluidized bed operations.
- the present invention contemplates the use of zirconia and alumina for such mesoporous composites with CaO.
- Ca(OH) 2 may be a useful intermediate between CaO and CaCO 3 . It is known that the sintering longevity problems in cycling between CaO and CaCO 3 may be largely avoided by cycling between oxide, hydroxide and carbonate compounds of the sorbent.
- the regeneration gas for regeneration reactor 7 provides heat for calcining the sorbent, and oxygen and/or steam for decoking the catalyst, while serving as sweep gas to purge CO 2 released in calcining and decoking functions.
- a preheater 15 is provided to preheat air or enriched oxygen provided for oxidation and sweep gas functions, while superheating any steam provided to assist decoking and as sweep gas.
- a feed air compression unit 16 is provided, which would usually be an air compressor. Feed air compression unit 16 may alternatively include a feed air blower, a pressure swing adsorption oxygen enrichment unit, and an oxygen compressor delivering oxygen to preheater 15 . Oxygen enrichment may be desired to reduce air compression loads in higher working pressure embodiments of the process, or to facilitate capture of concentrated CO 2 from the exhaust.
- a heat recovery section 18 is provided to recover heat from the CO 2 and sweep gas discharged to exhaust.
- Heat recovery sections 8 and 18 are here contemplated to be steam generators, providing steam by conduit 19 to hydrogasification reactor 4 and optionally in some embodiments also by conduit 20 to preheater 15 and regeneration reactor 7 .
- Feed preparation section 2 includes steps of sizing and drying as necessary.
- Feed pressurization section 3 includes a lock hopper system or a pressure feeder device to introduce the feed biomass into the pyrolysis and gasification process at a working pressure of preferably about 5 bara to about 50 bara, and more preferably about 10 bara to about 20 bara.
- Solids are removed from the effluent pyrolysis gas exiting hydrogasification reactor 4 by a solids removal section 5 including one or multiple cyclones, and optionally also high temperature filters such as metallic or ceramic candle filters.
- a desulfurization reactor e.g. using zinc oxide for H 2 S removal
- sorbent beds for removal of alkalis or chlorides may be included here for protection of any downstream catalysts.
- FIG. 2 shows a simplified schematic of an alternative apparatus 40 with the regeneration reactor 7 embedded in a gas turbine 41 to enable the efficient use of pressurized air for regeneration.
- Gas turbine 41 includes a compressor 42 coupled to a high temperature expander 43 and a mechanical load 44 which may be an electrical generator.
- the expanded exhaust from expander 43 includes vitiated air and CO 2 released from the sorbent, and is subjected to heat recovery in heat exchanger 47 before generating steam in downstream heat recovery section 18 .
- Heat exchanger 47 provides heat to preheater 15 in this embodiment, and may be directly integrated with preheater 15 in well known recuperator or rotary regenerator embodiments well known in the gas turbine art.
- the hot gas clean-up section 50 will include cyclones, filters (metal fabric, ceramic candles or precoat filters), and chemical sorbents as necessary to capture the alkalis and any other detrimental components. Captured solids and spent sorbents will be released from discharge conduit 51 .
- FIGS. 3 and 4 show an embodiment 60 with rotary fixed bed reactors that will be particularly useful for smaller scale applications of the invention, e.g. for local supply of methane fuel from forestry operations in remote areas.
- Reactors 4 and 7 are combined in a cyclic rotary reactor 61 .
- a plurality of fixed beds 62 are mounted in a rotor 63 rotating about rotary axis 64 between a first rotary valve face 65 and a second rotary valve face 66 .
- First rotary valve face 65 engages sealingly with a first valve stator face 67
- second rotary valve face 66 engages sealingly with a second valve stator face 68 .
- Fluid connection ports 75 , 76 , 77 and 78 are provided in first valve stator face 67
- fluid connection ports 85 , 86 , 87 and 88 are provided in second valve stator face 68 .
- FIG. 4 shows the ports for the first valve stator face, with bracketed reference numerals for the corresponding ports of the second valve stator face.
- the biomass feed is pressurized and decomposed by pyrolysis reactor 70 before admission to port 75 .
- Conduits 12 and 19 respectively provide recycle hydrogen and steam to port 75 .
- Raw product methane gas is delivered from port 85 to heat recovery, clean-up and purifications steps.
- Preheated regeneration air is introduced to port 77 , while the CO 2 containing exhaust is discharged from port 87 to heat recovery.
- Cocurrent regeneration as shown in FIG. 3 may be replaced with countercurrent regeneration by introducing the preheated regeneration air to port 87 , and discharging the exhaust from port 77 .
- Intermediate ports 76 and 78 in the first stator, and intermediate ports 86 and 88 in the second stator, are provided to enable buffer purge steps with steam or other inert gas between the hydrogasification and regenerations steps, so as to avoid hazardous direct contact of undiluted air with high concentration fuel gas.
- the intermediate ports may also be used for pressure equalization steps between the hydrogasification step performed at elevated pressure and the regeneration step performed at lower pressure or substantially atmospheric pressure.
- FIG. 5 shows a circulated fluidized twin bed embodiment 100 of the invention that would be particularly applicable to larger scale installations.
- Fluidized bed loop 101 includes a bubbling bed hydrogasification reactor 4 energized by recycle hydrogen from conduit 12 and steam from conduit 19 , and a circulating fluidized bed regenerator reactor 7 energized by feed air from compressor 42 .
- the fluidized bed solid media includes CaO sorbent, preferably formed in composite mesoporous ceramic pellets.
- the ceramic preferably also impregnated with transition group metal catalysts such as nickel, or noble metal catalysts such as rhodium with ceria
- transition group metal catalysts such as nickel, or noble metal catalysts such as rhodium with ceria
- the granular media may be a mixture of sorbent, catalyst and heat exchange particles.
- the media should have high heat capacity, thermal conductivity and attrition resistance.
- Olivine sand is recognized as having excellent properties as heat transfer media in biomass gasification, including moderate catalytic properties for reforming tar constituents.
- Magnetite may also be useful as heat transfer media, with the potential advantage of downstream magnetic separation between the heat transfer media and char.
- Carbonated sorbent, char and coked catalyst are transferred from hydrogasification reactor 4 to regenerator reactor 7 via siphon 102 .
- Calcined sorbent and regenerated catalyst are transferred back from regenerator reactor 7 to hydrogasification reactor 4 via cyclone 103 and siphon 104 .
- Ash may be released from the bottom of regenerator 7 by a lock hopper or an intermittently operated valve.
- FIG. 6 shows a two stage fluidized bed embodiment 150 , with the first stage 101 using relatively robust but less catalytically active media such as olivine or nickel impregnated olivine or glass-ceramic transition metal (e.g. Ni, Mo, W and combinations thereof) catalysts such as developed by the Gas Technology Institute, and the second stage 201 using more active and more delicate catalysts and lime sorbent for improved conversion of tars and higher yield of methane.
- the first stage 101 is a fluidized bed reactor loop achieving hydropyrolysis and partial conversion to methane and hydrogen, while the second stage 201 performs more complete hydroconversion.
- the solids separation section 5 may here include means to remove catalyst poisons (e.g. sulphur, chlorides, alkalis, etc.).
- Second stage fluidized bed loop 201 includes the second stage hydrogasification reactor 204 , the second stage regeneration reactor 207 . Deactivated catalyst and carbonate sorbent are transferred from hydrogasification reactor 204 to regenerator reactor 207 via siphon 212 . Calcined sorbent and regenerated catalyst are transferred back from regenerator reactor 207 to hydrogasification reactor 204 via siphon 214 .
- catalyst poisons e.g. sulphur, chlorides, alkalis, etc.
- the hot gas effluent from regenerator reactor 207 is delivered through cyclone 213 and hot-gas cleanup section 50 to the inlet of gas turbine expander 43 .
- Fluid control means 215 is provided to control flows of recycle hydrogen from conduit 12 and steam from conduit 19 to energize fluidized beds in first stage reactor 101 and second stage reactor 201 .
- Fluid control means 215 may include control valves, expanders or compressors as needed to control flows and regulate pressures.
- FIG. 7 shows a two stage fluidized bed embodiment 250 , with the first stage 101 a fluidized bed hydropyrolysis reactor as in embodiments 100 or 150 , and the second stage a methanation or hydroconversion reactor 61 with a cyclic rotary switching mechanism for rotary fixed beds 62 as shown in embodiment 60 .
- Beds 62 are switched cyclically between methanation or hydroconversion steps as reactor 254 , and regeneration steps as reactor 257 .
- Hot gas cleanup can be performed in cleanup section 250 with filtered solids and spent sorbents removed by discharge conduit 251 .
- Heat recovery steam generator 258 may be provided to recover heat between first stage hydropyrolysis reactor 4 and second stage methanation or hydroconversion reactor 254 .
- FIG. 8 shows an embodiment 300 for coproduction of methane and liquid hydrocarbons with a three stage reactor system.
- a hydropyrolysis reactor 304 is provided upstream of a hydroconversion reactor 310 for production of liquid hydrocarbons, and itself upstream of a sorption enhanced reactor 314 for production of hydrogen and methane.
- the hydrogen from reactor is delivered to hydropyrolysis reactor 304 .
- Reactor 304 provides rapid heating of the biomass particles to a pyrolysis temperature in the range from about 300° C. to about 500° C., in order to decompose the biomass into pyrolysis gas (including light hydrocarbons, some syngas, and tar vapours) and char.
- pyrolysis gas including light hydrocarbons, some syngas, and tar vapours
- Heating may be achieved by mixing the biomass particles with a granular heat transfer media in a mechanical or fluidized bed contacting system.
- Various mechanisms are well known for fast pyrolysis reactors (e.g. auger reactors and circulating fluidized beds), and may be used in a mechanical contacting system in reactor 304 .
- the granular heat transfer media should have high heat capacity, thermal conductivity and attrition resistance.
- Olivine sand is recognized as having excellent properties as heat transfer media in biomass gasification, including moderate catalytic properties for reforming tar constituents.
- Nickel-impregnated olivine has improved catalytic properties.
- the glass-ceramic catalysts developed by the Gas Technology Institute are believed to be superior for hydropyrolysis applications. Magnetite may also be useful as heat transfer media, with the potential advantage of downstream magnetic separation between the heat transfer media and char.
- the heat exchange media is circulated between reactor 304 and a media heater 315 , with pyrolytic char being discharged from reactor 304 with spent heat exchange media returning to the media heater 315 .
- Combustion of char in media heater 315 may conveniently provide heat required for heating the feed biomass to reaction temperature and for the endothermic pyrolysis and initial gasification reactions.
- Ash is discharged from media heater 315 .
- a portion of the char exiting reactor 304 may be separated from the heat exchange media by char separator 316 as the feedstock for an auxiliary oxygen or steam gasification method to generate syngas. After water gas shift and CO 2 removal from the syngas, supplemental hydrogen may thereby be provided for the subsequent hydrogasification reaction.
- a portion of the char separated by char separator 316 may be diverted to other external uses, including sale of charcoal as a solid fuel, or as a “bio-char” soil amendment for agriculture or forestry uses with an important purpose of carbon sequestration in the soil. Ash may also be a useful byproduct for soil enhancement and recycle of nutrients for overall sustainability of biomass cultivation, harvesting and utilization.
- Solids are removed from the effluent pyrolysis gas exiting pyrolysis reactor 304 by a solids removal section 317 including one or multiple cyclones, and optionally also high temperature filters such as metallic or ceramic candle filters.
- a catalyst poison removal section 318 (including a desulfurization reactor using zinc oxide for H 2 S removal, and optionally including other sorbent beds for removal of chlorides and/or alkalis) may be included here for protection of downstream catalysts.
- the pyrolysis gas is also cooled by a heat recovery steam generator 319 , either upstream or downstream of the catalyst poison removal sorbent beds.
- the cooled pyrolysis gas is introduced to catalytic hydroconversion reactor 310 , together with hydrogen (or hydrogen-rich gas) and optionally also with steam. Hydrogen reactively deoxygenates the pyrolysis gas components to generate a mixture of lighter and heavier hydrocarbons by hydrodeoxygenation and decarboxylation reactions. Hydrogen and steam act to crack larger molecules, and to inhibit coking.
- the reactor effluent is provided to a first separator 321 from which a liquid fraction of heavier hydrocarbons is delivered by conduit 322 as a first liquid hydrocarbon product for further processing and use as desired.
- the overhead fraction from first separator 321 is cooled by heat recovery unit 330 to generate steam or preheat water upstream of second separator 331 in which water is condensed and separated from a liquid fraction of gasoline range hydrocarbons which is delivered as a second liquid hydrocarbon product by conduit 332 for further processing and use as desired.
- the overhead fraction of gases and vapours from second separator 331 contains H 2 , CO, CO 2 , CH 4 and other light hydrocarbons along with some water vapour. This fraction is reheated and admitted to sorption enhanced reactor 314 , optionally together with a portion of the cleaned pyrolysis gas from catalyst poison removal section 318 as controlled by valve 340 in conduit 341 .
- Carbonation of CaO in sorption enhanced reactor 314 removes CO 2 and also CO by water gas shift. Light hydrocarbons are preferentially prereformed so that the product of sorption enhanced reactor 314 will be mostly hydrogen with methane as the main residual carbon-containing compound. After clean-up and cooling of this product gas mixture from reactor 314 , gas separation system 10 separates substantially purified methane into SNG product delivery conduit 11 , and a hydrogen-enriched recycle stream into conduit 12 and back to the hydropyrolysis reactor 304 .
- the gas separation system 10 may be operated to deliver a sufficient amount of hydrogen to the hydropyrolysis reactor and a significant amount of methane, with more methane production feasible if less liquid hydrocarbons are produced.
- approximately half the carbon in the feed biomass may be converted to product hydrocarbons (including heavier liquid hydrocarbons in the first product, gasoline range hydrocarbons in the second product, and product methane as a third product).
- the balance of the carbon is discharged as char or CO 2 . Higher carbon conversion can be achieved with the addition of imported hydrogen.
- the product split between methane and liquid hydrocarbons can be varied operationally by adjusting gas separation unit 10 so that more or less methane is delivered. With lower production of methane, more recycle hydrogen is available to the hydropyrolysis and hydroconversion reactors so that more liquid hydrocarbons are produced.
- the gas separation system 10 is removed so that the entire product effluent of sorption enhanced reactor 314 is delivered to hydropyrolysis reactor 304 , while liquid hydrocarbon delivery of the first and second products is accordingly augmented.
- Reactor 314 is then operating as a sorption enhanced steam reformer, with several advantages including (1) lower temperature operation than a conventional steam reformer, (2) convenient direct use of char combustion for regenerating the sorbent, (3) integrated water gas shift and CO 2 removal, and (4) scavenging of any alkali and chloride impurities in the recycle gas by the lime sorbent.
- Regenerator reactor 7 and sorption enhanced reactor 314 comprise a coupled reactor pair for the working reaction and for regeneration of the sorbent and catalyst.
- a catalyst regeneration reactor 330 is also provided for decoking catalyst from hydroconversion reactor 310 .
- a portion of compressed air from compressor 42 and preheater 15 is provided to pyrolysis media heater 315 for combustion of char to heat the media, with flue gas heat being recovered in steam.
- the remainder of the compressed air from compressor 42 and preheater 15 is provided optionally with steam to regeneration reactors 7 and 330 to burn coke off the catalysts and decarbonate the CaCO 3 formed in sorption enhanced reactor 314 .
- Heat recovery steam generators 8 , 319 and 350 deliver steam to sorption enhanced reactor 314 , or to regeneration reactors 330 and 7 as needed.
- FIG. 9 shows an embodiment 400 , in which a hydrogasification system similar to embodiment 1 is coupled to a solid oxide fuel cell (SOFC) 410 for generation of electricity.
- SOFC solid oxide fuel cell
- the SOFC has a solid oxide electrolyte 412 between a cathode chamber 413 and an anode chamber 414 .
- the cathode chamber has inlet port 415 and outlet port 416
- the anode chamber has inlet port 417 and outlet port 418 .
- the anode chamber includes an internal reforming catalyst (which may be comprised within the anode itself) to convert methane and steam to hydrogen and carbon oxides CO and CO 2 under SOFC operating conditions at elevated temperatures in the range of about 600° C. to about 800° C.
- a portion of the compressed air (or compressed oxygen-enriched air) from air compression unit 16 is heated in thermal recuperator 422 , and fed to cathode inlet port 415 .
- Vitiated cathode gas is discharged from port 416 and exhausted through recuperator 420 which recovers sensible heat from this gas.
- a hot gas clean-up section 430 is provided to remove solid particulate, alkalis and any chloride or sulphur compounds that have not been captured by the sorbent.
- the hot gas clean-up section 430 may include cyclones, filters (metal fabric, ceramic candles or precoat filters), and chemical sorbents as necessary to capture the alkalis and any other detrimental components. Captured solids and spent sorbents will be released from discharge conduit 431 .
- FIG. 10 is a graph of methane conversion, methane concentration, hydrogen concentration, and the ratio of hydrogen output to hydrogen input (H 2out /H 2in ) from the hydrogasification reactor of the invention, versus the ratio of carbon carbonated on the sorbent to carbon content of the biomass feed to the process.
- Disclosed embodiments of the method and system are useful for high efficiency conversion of biomass, including forestry residues (including those generated by logging, thinning, and wildfire prevention fuel load reduction activities) and sawmill waste into SNG, either as a fuel commodity or for high efficiency generation of electrical power.
- Disclosed embodiments provide advantageous integrations with gas turbines and/or solid oxide fuel cells. A portion of the biomass may also be converted into heavier and lighter hydrocarbon liquids.
- Disclosed embodiments of the system may be used at industrial scale limited only by transportation distances for collection of biomass feedstock, or at smaller scale in rural or remote areas for combined generation of heat, high heating value fuel gas and electricity.
- the system may be used for residential heating, methane fuel production and electrical power generation through a solid oxide fuel cell or other energy converter consuming a portion of the product methane.
Abstract
Disclosed embodiments provide a system and method for producing hydrocarbons from biomass. Certain embodiments of the method are particularly useful for producing substitute natural gas from forestry residues. Certain disclosed embodiments of the method convert a biomass feedstock into a product hydrocarbon by hydropyrolysis. Catalytic conversion of the resulting pyrolysis gas to the product hydrocarbon and carbon dioxide occurs in the presence of hydrogen and steam over a CO2 sorbent with simultaneous generation of the required hydrogen by reaction with steam. A gas separator purifies product methane, while forcing recycle of internally generated hydrogen to obtain high conversion of the biomass feedstock to the desired hydrocarbon product. While methane is a preferred hydrocarbon product, liquid hydrocarbon products also can be delivered.
Description
- This is a continuation application under 35 U.S.C. §120 of International Patent Application No. PCT/CA2010/001859, filed Nov. 18, 2010, which claims the benefit of the earlier filing date of U.S. Provisional Application No. 61/262,485, filed Nov. 18, 2009. Each of these prior applications is incorporated herein by reference.
- The process of the invention applies to hydropyrolysis of carbonaceous feedstocks, and particularly of forestry residues, to generate higher value synthetic fuels, in particular methane and optionally liquid hydrocarbons.
- Thermochemical conversion of biomass such as sawmill wood wastes, forestry residues and agricultural wastes into synthetic fuels is an important emerging avenue for advancement of renewable energy sources to supplement or replace fossils fuels. While air blown gasification is used for generation of lower heating value fuel gas, several variants of oxygen or steam gasification can be used for production of syngas containing minimal nitrogen. Syngas is a gas mixture containing mostly hydrogen and carbon monoxide, and is a versatile feedstock for further chemical processing into a wide range of useful fuels and chemical compounds. Syngas can be catalytically converted into methane, Fischer-Tropsch liquid fuels, methanol, dimethyl ether, or hydrogen. The methanation reaction of syngas to generate methane and byproduct water vapour is typically conducted over nickel catalysts at temperatures in the range of about 300° C. to about 400° C., and preferably at elevated pressure.
- Methane is readily marketed and delivered through existing natural gas distribution infrastructure as substitute natural gas (SNG) for numerous end uses including space heating and electrical power generation. Methane has considerably higher energy density than hydrogen, and can be converted into syngas or hydrogen by catalytic steam reforming. Modern combined cycle power plants are conveniently fueled by natural gas. Methane is also a particularly advantageous fuel for future high temperature fuel cell power plants using highly endothermic internal steam reforming of natural gas to recover high grade heat generated by the fuel cell stack.
- The reaction of steam with biomass to generate syngas is highly endothermic, hence conducted with direct or indirect heating by partial oxidation with air or oxygen; and is typically conducted at much higher temperature than the subsequent exothermic methanation reaction. The thermal mismatch between gasification and methanation reactions is detrimental to process efficiency.
- Hydrogasification has previously been investigated for gasification of biomass. The key reaction is hydrogenation of carbon to form methane, whose exothermicity is a great advantage compared to other gasification approaches. As hydrogen is a premium fuel, its consumption in large amounts has presented the appearance of a major economic barrier.
- The endothermic nature of the syngas formation reaction from the reaction of biomass pyrolysis gas and steam requires enthalpy heat to be added (typically by partial combustion with added oxygen). Temperatures well in excess of 650° C. are typically required to reduce tars to reasonable levels.
- The gas composition produced in biomass gasification approaches a complex equilibrium established between CO, CO2, H2, H2O and CH4 which is a function of temperature, pressure and overall gas composition. Reforming reactions producing syngas increasingly dominate the equilibrium at temperatures above 650° C. at the expense of hydrocarbons, CO2 and water.
- The use of catalysts, such as the use of olivine, dolomite or nickel coated media in fluidized beds, to enhance the rate of syngas formation is well known. These catalysts allow a faster reaction towards syngas equilibrium favoured under the process conditions. Catalysts have also been used in a secondary bed in series with the gasifier for the reduction of tars contained in the syngas or producer gas.
- An oxygen blown entrained flow gasifier may typically operate at about 1300° C. to 1500° C., at which temperatures methane and higher hydrocarbons are all nearly entirely converted to syngas. This has the important advantage of almost completely eliminating tar constituents, but the disadvantage for SNG production that all of the product methane must be generated by the exothermic methanation of syngas at much lower temperature than the gasification temperature.
- Indirect steam gasifiers (such as the US Battelle/FERCO “Silvagas” system, the Austrian fast internally circulating fluidized bed (FICFB) system, and the Dutch ECN “Milena” system) operate at about 850° C. These systems use twin bed configurations, in which fluidized granular heat transfer media is circulated between a gasification zone in which steam reacts with the biomass to produce syngas and char, and an air-blown regeneration zone in which the char is combusted to reheat the media. The product syngas contains a significant admixture of methane generated within the gasifier. While downstream processing is required to convert or remove tar constituents, an important advantage for SNG production is that only about 55% to 60% of the final product methane must be generated by methanation of syngas, since a useful fraction of the methane was already produced with the syngas.
- Some recent improvements to the twin bed gasification approach have been based on adsorption enhanced reforming (“AER”) in which a CO2 acceptor such as lime or calcined dolomite is included in the granular media to remove carbon dioxide by carbonation from the gasification zone operating typically at about 600° C., and to release the carbon dioxide by calcining in the regeneration zone operating typically at about 800° C. The AER process has been disclosed by Specht et al. (European patent publications EP 1,218,290 B1 and EP 1,637,574 A1). The principle of the AER process is to generate hydrogen-rich syngas by shifting the reaction equilibria of the steam reforming and water gas shift reactions by CO2 removal. The AER process has been tested in the FICFB twin bed system, and is being developed for SNG production by using a molten salt methanation reactor to convert the syngas into methane.
- Twin bed indirect steam biomass gasifiers, and experimental AER systems derived from twin bed gasifiers, have been operated at atmospheric pressure. Air blown combustion regeneration of pressurized fluidized beds would present challenges. ECN have considered operation of the Milena twin bed gasification system pressurized to about 7 bara.
- There is a need to provide more efficient internally self-sustaining generation of the hydrogen needed for hydrogasification, which otherwise is an extremely attractive approach for conversion of biomass and other carbonaceous feedstocks into methane and other high value synthetic fuels.
- While the “sorption enhanced reforming” (SER) process [known in Europe as “absorption enhanced reforming” or AER] concerns generating hydrogen-rich syngas, which may be converted downstream in a separate methanation reactor into SNG, disclosed embodiments of the present invention concern the new principle of absorption enhanced methanation (“SEM”). Whereas carbon is nearly entirely removed from the feed syngas by carbonation of the sorbent in AER, only about half of the carbon is similarly removed in SEM.
- Methanation as described in this disclosure is hydroconversion of a pyrolysis gas to produce methane, including but not confined to the conversion of syngas to methane.
- It has been found unexpectedly that maintenance of a high hydrogen back-pressure in SEM will inhibit decomposition of methane by steam methane reforming, while carbon oxides are preferentially removed. Because only about half of the carbon contained in the initial syngas is removed by carbonation in SEM, the CO2 sorbent has much lighter duty in SEM as compared with SER.
- Thermodynamic modeling indicates that slightly more than half of the carbon not rejected as char or coke deposits can be converted to methane under conditions of hydrogen self-sufficiency. Approximately 20% of the carbon originally in the biomass will typically be rejected as char or coke to be combusted or gasified in the regeneration reactor. If a supplemental source of hydrogen is available, the conversion of feed carbon to methane can be increased within the scope of the present invention, while even less of the carbon will be removed by carbonation of the sorbent.
- SEM may be advantageously operated at moderately elevated working pressures in a range of just over 1 bara to about 50 bara, or in a preferred range of from about 5 bara to about 30 bara. While SEM can be conducted at atmospheric pressure, the methane concentration will be lower than at higher operating pressures, thus making the gas separation of hydrogen and methane more difficult. Conventional methanation requires much higher working pressures to achieve satisfactory conversion.
- A preferred CO2 sorbent for SEM is CaO, which can be used in any suitable form, or combinations thereof, such as calcined limestone or dolomite, or CaO on a suitable support such as alumina. CaO is readily carbonated at working temperature around 600° C. and moderate pressures from atmospheric upward. Such temperature and pressure conditions have been found to be favourable for the hydrogasification of biomass pyrolysis gas to methane, and for steam reforming of methane to generate hydrogen.
- Various CO2 sorbents or “acceptors” will work in the temperature range of from about 500° C. to about 650° C. of interest for SEM. These include calcined dolomite, calcium oxide, calcium hydroxide, lithium zirconate, lithium orthosilicate, and other metal oxides or hydroxides that can react with carbon dioxide to form a carbonate phase.
- While hydroconversion of biomass pyrolysis gas to methane works favourably at temperatures in the range of from about 500° C. to about 650° C., productive hydroconversion of pyrolysis gas to liquid hydrocarbons requires lower temperatures in the range of from about 300° C. to about 400° C. CO and CO2 are extracted from the oxygenated pyrolysis gas by decarbonylation and decarboxylation respectively, in parallel with extraction of H2O by hydrodeoxygenation. As CO and H2O can be consumed to generate H2 and CO2 by the water gas shift reaction, it may be advantageous to remove CO2 by a carbonation reaction in order to maximize the generation of hydrogen by water gas shift. Suitable CO2 sorbents for the temperature range of from about 300° C. to about 400° include potassium-promoted hydrotalcites, magnesia supported on alumina, or dolomite in combination with alkali (and particularly potassium) promoters.
- Certain disclosed embodiments provide a method for converting a biomass feedstock into a product hydrocarbon comprising:
-
- a. subjecting the feedstock to fast pyrolysis with rapid pyrolytic heating in the substantial absence of oxygen, or hydropyrolysis as fast pyrolysis in the presence of hydrogen, in order to generate fractions of pyrolysis gas and char;
- b. catalytically converting at least a portion of the pyrolysis gas to a product hydrocarbon and carbon dioxide in the presence of hydrogen and steam, while removing carbon dioxide by carbonation of a sorbent;
- c. generating at least a portion of the hydrogen by reaction between steam and a portion of the pyrolysis gas or a product hydrocarbon;
- d. separating hydrogen from the hydrocarbon product, and recycling the hydrogen so as to force the conversion of biomass into the hydrocarbon product; and
- e. regenerating the sorbent by heating through combustion of the char to release the carbon dioxide.
- The fast pyrolysis step may be performed with externally heated media, e.g. circulating through a pressurized auger reactor, and preferably as hydropyrolysis in a hydrogen atmosphere. The heat transfer media may include circulating magnetite pellets, which are readily separable from char according to density and magnetic properties. Some impurities such as alkalis, other metals, sulphur, and chloride will be partially entrained by the char. While very fast pyrolysis will minimize char production, slower pyrolysis may also be considered for coproduction of charcoal or biochar with lower yield of methane and any other desirable hydrocarbon products.
- The catalytic conversion step includes catalytic hydrogasification, such as steam hydrogasification. Hydroconversion, hydrodeoxygenation, and hydrocracking reactions will take place. The net reaction will be exothermic. This step may be conducted alternatively in any suitable reactor architecture, such as the following reactor architectures:
-
- a) bubbling or circulating fluidized bed;
- b) fixed bed with granular packing or monolithic catalyst, and rotary or directional valve logic for cyclically switching beds between reaction and regeneration steps;
- c) moving bed with granular catalyst.
- The hydrogasification process requires a source of hydrogen, either externally supplied or internally generated. According to certain disclosed embodiments of the present invention, steam addition, plus moisture contained in feed biomass, provides sufficient steam for internal, self-sustaining generation of hydrogen required for the hydrogasification reaction to convert biomass feedstock into methane.
- Certain disclosed embodiments of the invention may be realized by any of the following operating modes:
- 1. Self-sustaining recycle of H2 generated within catalytic stage with sufficient H2 excess to overcome incomplete recovery in downstream gas separation of recycle H2. Methane yield is approximately 50% of carbon after char production, balance primarily to CO2 with preferred use of water gas shift reaction to consume most CO.
- 2. Supplemental hydrogen may provided from any combination of (a) an external source of hydrogen rich gas, or (b) oxygen or steam gasification of char offgas, or (c) steam methane reforming of a portion of the methane product.
- 3. The process in preferred embodiments includes methanation, regeneration and reforming steps. Higher temperature, high steam concentration and low hydrogen concentration drive the reforming reaction forward. Lower temperature, low steam concentration and high hydrogen concentration drive the methanation reaction forward. Reforming and methanation may take place in each of the reforming and methanation steps, with the equilibrium balance reflecting not only bed temperature but also the steam/hydrogen ratio over the catalyst. The catalyst beds are cooled by reforming, heated by methanation and strongly heated to the maximum process temperature by regeneration. The reforming step follows the regeneration step to take advantage of sensible heat in the bed, then the methanation step follows after the catalyst bed has been cooled by the reforming step, and then the next regeneration step takes place to finish reheating the bed up to its cyclic maximum temperature. Such embodiments are an inventive extension of the known principle of cyclic reforming in which sensible heat for repeated reforming steps is provided by alternatingly repeated regeneration steps, with certain embodiments of the present inventive process also including methanation steps following reforming steps and preceding regeneration steps.
- With larger steam supply, higher temperature and/or lower operating pressure, the process may generate excess syngas or hydrogen so that coproduction of methane and hydrogen/syngas may be contemplated. Coproduction of methane and higher hydrocarbon fuel commodities is also attractive.
- The process also may include cleaning steps to remove catalyst poisons (alkalis, other metals, phosphorus, sulfur, chloride, etc.) and tars. Hot or cold clean-up process alternatives are well known.
- Hot clean-up steps include sorbents (e.g. ZnO to remove sulphur), and catalytic tar cracking followed by cool-down in cyclic thermal regenerator loaded with layers of fine filtration metal matrix, porous ceramic, catalyst and adsorbent. Regeneration can be achieved by burning off tar and coke deposits, then air flush to cool the filtration matrix and provide hot air for front end feed dryer.
- Cold clean-up can be achieved by higher temperature oil quench and wash, followed by lower temperature water quench and wash.
- The process may also include gas separation steps for removing CO2, for recovering a hydrogen-enriched recycle stream for the hydrogasification step, and/or for purifying the product methane. Preferred gas separation alternatives include carbonation of CaO or pressure swing adsorption (PSA) for CO2 removal, and PSA or polymeric membranes for separation of H2 from CH4.
- One disclosed apparatus includes a hydropyrolysis reactor. Alternative embodiments include a single stage reactor, or a two-stage system including a pyrolysis or hydropyrolysis reactor as the first stage, and a methanation or hydroconversion reactor as the second stage. The process achieves catalytic steam hydrogasification, with catalytic hydrocracking of tars favoured by relatively high hydrogen partial pressure.
- The process includes sequential steps for (1) the working reaction by hydrogasification or hydroconversion combined with sorbent carbonation, and (2) regeneration of sorbent and catalysts. Combined regeneration of the sorbent (carbon dioxide acceptor) and catalyst is a very attractive operating mode.
- Alternative reactor configurations include fixed beds with granular or monolithic catalyst with directional or rotary valves for cyclic switching of beds between the process steps of working reaction and regeneration, or fluidized beds with circulation to achieve the process steps. Twin fluidized beds are a suitable architecture for indirect steam gasifiers, achieving the working reaction in one bed, and regeneration by combustion of char in the other bed.
- An important aspect of the invention is heat management. Combined exothermicity of sorption carbonation and methanation reactions provide abundant heat for preheating feedstock and steam generation, with reduced need for feedstock drying. Heat for sorbent and catalyst regeneration can be generated by combustion of relatively low value fuels, such as byproduct char or raw biomass feedstock.
- Introduction of fibrous biomass with inconsistent properties into pressurized pyrolysis or gasification plants is a difficult challenge. Water slurry feed is mechanically attractive, but is incompatible with the normal requirement that the feed biomass be substantially dry. The present process is tolerant of relatively wet feed, because of the strong combined exothermicity of the methanation and sorbent carbonation reactions. Another novel approach for slurry feed within the present invention is to provide a pusher centrifuge dewatering system within the high pressure containment volume of the plant.
- Catalyst and sorbent regeneration can be achieved in a regeneration reactor zone integrated with the pressurized combustor of gas turbine, or supplied with superheated steam with optional addition of enriched oxygen.
- High methane yield can be achieved in hydrogasification, however in absence of a supplemental source of imported hydrogen up to half of that methane may be consumed downstream to generate recycle hydrogen and CO2. A preferred operating mode is defined by self-sustaining recycle of H2 generated within a catalytic stage, with just enough H2 excess to compensate for incomplete recovery in downstream gas separation of recycle H2. Methane yield is approximately 50% of carbon after char production, with the remaining carbon being converted to CO2.
- Supplemental hydrogen may provided from any combination of (a) an external source of hydrogen-rich gas such as stranded hydrogen offgas from a chlor-alkali or ethylene plant, or (b) oxygen or steam gasification of char, or (c) steam methane reforming of a portion of the methane product. The process may be operated with any amount of hydrogen recycle, including the limiting case of zero hydrogen recycle, in which case the methane rich product gas will contain relatively less hydrogen but significantly larger amounts of carbon dioxide and carbon monoxide. In the opposite limiting case, zero methane is delivered so that maximum hydrogen may be generated; and hydrogen-rich syngas may then be delivered as a desired product. Coproduction of methane and hydrogen, or hydrogen-rich syngas, is an option within the scope of the invention.
- Separation of hydrogen and methane can be achieved by pressure swing adsorption, membrane permeation, refrigerated hydrate formation or cryogenics. While sorption-enhanced reactors for SMR and/or methanation have integrated bulk CO2 removal, further purification of product streams will generally be needed to remove slip of CO or CO2 as required.
- The invention provides a wide spectrum of cogeneration opportunities. The process can generate a range of hydrocarbon products (methane, LPG, and liquid hydrocarbons). Syngas and hydrogen are generated within the process, either consumed entirely within the hydrocarbon producing hydroconversion processes, or alternatively a portion of syngas or hydrogen may be exported as a useful product at some penalty of reducing the conversion of biomass carbon to hydrocarbons. Syngas is an intermediate for synthesis of a wide range of useful fuel and chemical products.
- The hydropyrolysis reaction delivers a product stream of methane plus hydrogen, and minor amounts of CO and CO2. Syngas may also be generated by oxygen/steam gasification of char. The syngas generated by char gasification will typically have a low ratio of H2 to CO, which can be upgraded by admixture with H2 generated by the hydropyrolyser. A ratio of H2:CO˜2 is desirable for synthesis of methanol, dimethyl ether, or Fischer-Tropsch hydrocarbons.
- Other cogeneration opportunities provided by the invention include the production of energy as heat or electricity. Heat recovery within the process can readily generate steam at different temperatures. Product or byproduct fuels can be used to power electrical generators through gas turbines, internal combustion engines or steam turbines. Some of the most attractive future applications of the present invention will be obtained by integration of high temperature fuel cells with the hydrogasfication of biomass.
- As first suggested in copending U.S. patent application Ser. No. 11/869,555, biomass hydrogasification may be directly integrated with SOFC power plants having enriched H2 recycle for the anode of an internal reforming SOFC. The present invention develops practicable implementations of that opportunity. Without the relatively low operating pressures enabled by the inventive sorption enhanced methanation process, it would be very difficult to integrate the usually relatively low pressure SOFC system with the relatively high pressure hydrogasification processes.
- When the oxidant for catalyst and sorbent regeneration by combustion of char and coke is enriched oxygen, a concentrated product stream of CO2 can be delivered for useful applications including enhanced oil recovery, or for disposal by underground sequestration.
- The foregoing and other objects, features, and advantages of the invention will become more apparent from the following detailed description, which proceeds with reference to the accompanying figures.
-
FIG. 1 is a schematic diagram of one embodiment of an apparatus according to the present invention. -
FIG. 2 shows an embodiment with integration to a gas turbine power plant. -
FIGS. 3 and 4 show an embodiment with a rotary reactor including cyclically switched hydrogasification and regeneration zones. -
FIG. 5 shows a fluidized twin bed embodiment of the invention. -
FIG. 6 shows a two stage double twin bed fluidized embodiment. -
FIG. 7 shows a two stage embodiment, with the first stage a fluidized bed hydropyrolysis reactor and the second stage a methanation or hydroconversion reactor with a cyclic rotary switching mechanism. -
FIG. 8 shows an embodiment for coproduction of methane and liquid hydrocarbons. -
FIG. 9 shows an embodiment with a hydrogasification system coupled to a solid oxide fuel cell (SOFC) for generation of electricity. -
FIG. 10 is a graph of methane conversion, methane concentration, hydrogen concentration, and the ratio of hydrogen output to hydrogen input from the hydrogasification reactor of the invention, versus the ratio of carbon carbonated on the sorbent to carbon content of the biomass feed to the process. -
FIG. 1 shows a simplified schematic of a system orapparatus 1 according to the invention.Apparatus 1 includes afeed preparation section 2, afeed pressurization section 3, ahydrogasification reactor 4, asolids separation section 5, aregeneration reactor 7, aheat recovery section 8, atar scrubber 9, and agas separation section 10. Thegas separation section 10 separates hydrogen from methane, and may be based on selective membranes or on pressure swing adsorption (PSA).Gas separation section 10 delivers a substantially purified methane product stream fromconduit 11, and a hydrogen-enriched recycle stream back tohydrogasification reactor 4 viaconduit 12. It is a key feature in some preferred embodiments of the present invention that thegas separation system 10 can be operated so as to minimize hydrogen concentration in the product methane stream, thus preventing most of the hydrogen from exitingapparatus 1 until consumed in hydrogasification to produce the desired methane product. - A membrane permeation system may be advantageously used as
gas separation system 10 for purification of product methane and separation of hydrogen-rich gas for recycle to hydrogasification. The polymeric membrane will selectively permeate hydrogen, carbon monoxide, carbon dioxide and water vapour relative to methane. In order to obtain product methane containing no more than 1% hydrogen, three membrane stages may be used in series to progressively concentrate methane with high recovery and purity in the retentate stream. The feed gas is introduced to the inlet of the first stage, from which the hydrogen-enriched recycle gas will be delivered as low pressure permeate. The permeate of the second stage will be recompressed to join the feed at the inlet of the first stage, while the permeate of the third stage will be recompressed to the inlet of the second stage. - Alternatively, pressure swing adsorption may be used as
gas separation system 10 for purification of product methane and separation of hydrogen-rich gas for recycle to hydrogasification. -
Hydrogasification reactor 4 andregeneration reactor 7 comprise a coupled reactor pair for the working hydrogasification reaction and regeneration steps. Each ofreactors - Pressure and temperature conditions in the
hydrogasification reactor 4 will be selected to be favourable for combined methanation and steam reforming reactions such that the process achieves self-sufficiency in producing the amount of hydrogen needed for the methanation reaction, while also favourable for the carbonation reaction binding CO2 to the sorbent. Theregeneration reactor 7 will typically be operated at relatively higher temperature in order to release the CO2 from the sorbent, and may be operated at substantially the same pressure or at lower pressure to facilitate regeneration and reduce air compression requirements for regeneration. - A preferred CO2 sorbent is CaO, alternatively provided by calcining of natural limestone or dolomite, or by synthesis to achieve enhanced mesoporosity and stability for extended cycling without rapid deactivation due to sintering and pore blockage. It has been found in the art that composite structures comprising CaO supported on or encapsulated in a mesoporous ceramic (e.g. alumina) may achieve superior durability against deactivation, while also providing a hardened external shell for superior attrition resistance. Such mesoporous composite structures may be usefully applied in fixed bed monoliths as well as in granular media for fluidized bed operations. The present invention contemplates the use of zirconia and alumina for such mesoporous composites with CaO.
- At relatively higher pressures around 30 bara and with high steam concentrations during sorbent processing, Ca(OH)2 may be a useful intermediate between CaO and CaCO3. It is known that the sintering longevity problems in cycling between CaO and CaCO3 may be largely avoided by cycling between oxide, hydroxide and carbonate compounds of the sorbent.
- The regeneration gas for
regeneration reactor 7 provides heat for calcining the sorbent, and oxygen and/or steam for decoking the catalyst, while serving as sweep gas to purge CO2 released in calcining and decoking functions. Apreheater 15 is provided to preheat air or enriched oxygen provided for oxidation and sweep gas functions, while superheating any steam provided to assist decoking and as sweep gas. A feedair compression unit 16 is provided, which would usually be an air compressor. Feedair compression unit 16 may alternatively include a feed air blower, a pressure swing adsorption oxygen enrichment unit, and an oxygen compressor delivering oxygen topreheater 15. Oxygen enrichment may be desired to reduce air compression loads in higher working pressure embodiments of the process, or to facilitate capture of concentrated CO2 from the exhaust. Aheat recovery section 18 is provided to recover heat from the CO2 and sweep gas discharged to exhaust. -
Heat recovery sections conduit 19 tohydrogasification reactor 4 and optionally in some embodiments also byconduit 20 topreheater 15 andregeneration reactor 7. -
Feed preparation section 2 includes steps of sizing and drying as necessary.Feed pressurization section 3 includes a lock hopper system or a pressure feeder device to introduce the feed biomass into the pyrolysis and gasification process at a working pressure of preferably about 5 bara to about 50 bara, and more preferably about 10 bara to about 20 bara. - Solids are removed from the effluent pyrolysis gas exiting
hydrogasification reactor 4 by asolids removal section 5 including one or multiple cyclones, and optionally also high temperature filters such as metallic or ceramic candle filters. A desulfurization reactor (e.g. using zinc oxide for H2S removal), or sorbent beds for removal of alkalis or chlorides, may be included here for protection of any downstream catalysts. -
FIG. 2 shows a simplified schematic of analternative apparatus 40 with theregeneration reactor 7 embedded in agas turbine 41 to enable the efficient use of pressurized air for regeneration.Gas turbine 41 includes acompressor 42 coupled to ahigh temperature expander 43 and amechanical load 44 which may be an electrical generator. The expanded exhaust fromexpander 43 includes vitiated air and CO2 released from the sorbent, and is subjected to heat recovery inheat exchanger 47 before generating steam in downstreamheat recovery section 18.Heat exchanger 47 provides heat topreheater 15 in this embodiment, and may be directly integrated withpreheater 15 in well known recuperator or rotary regenerator embodiments well known in the gas turbine art. - In order to protect the turbine blades of
expander 43 from erosion, corrosion or fouling damage, it is necessary to provide a hot gas clean-upsection 50 to remove solid particulate, alkalis and any chloride or sulphur compounds that have not been retained by the sorbent under regeneration conditions. The hot gas clean-upsection 50 will include cyclones, filters (metal fabric, ceramic candles or precoat filters), and chemical sorbents as necessary to capture the alkalis and any other detrimental components. Captured solids and spent sorbents will be released fromdischarge conduit 51. -
FIGS. 3 and 4 show anembodiment 60 with rotary fixed bed reactors that will be particularly useful for smaller scale applications of the invention, e.g. for local supply of methane fuel from forestry operations in remote areas. -
Reactors rotary reactor 61. A plurality of fixedbeds 62 are mounted in arotor 63 rotating aboutrotary axis 64 between a firstrotary valve face 65 and a secondrotary valve face 66. Firstrotary valve face 65 engages sealingly with a firstvalve stator face 67, and secondrotary valve face 66 engages sealingly with a secondvalve stator face 68.Fluid connection ports valve stator face 67, whilefluid connection ports valve stator face 68.FIG. 4 shows the ports for the first valve stator face, with bracketed reference numerals for the corresponding ports of the second valve stator face. - The biomass feed is pressurized and decomposed by
pyrolysis reactor 70 before admission toport 75.Conduits port 75. Raw product methane gas is delivered fromport 85 to heat recovery, clean-up and purifications steps. - Preheated regeneration air is introduced to
port 77, while the CO2 containing exhaust is discharged fromport 87 to heat recovery. Cocurrent regeneration as shown inFIG. 3 may be replaced with countercurrent regeneration by introducing the preheated regeneration air to port 87, and discharging the exhaust fromport 77. -
Intermediate ports intermediate ports -
FIG. 5 shows a circulated fluidizedtwin bed embodiment 100 of the invention that would be particularly applicable to larger scale installations. Fluidizedbed loop 101 includes a bubblingbed hydrogasification reactor 4 energized by recycle hydrogen fromconduit 12 and steam fromconduit 19, and a circulating fluidizedbed regenerator reactor 7 energized by feed air fromcompressor 42. - The fluidized bed solid media includes CaO sorbent, preferably formed in composite mesoporous ceramic pellets. The ceramic (preferably also impregnated with transition group metal catalysts such as nickel, or noble metal catalysts such as rhodium with ceria) may itself have catalytic properties for reforming of pyrolysis gas and tars, and for methanation of syngas.
- The granular media may be a mixture of sorbent, catalyst and heat exchange particles. The media should have high heat capacity, thermal conductivity and attrition resistance. Olivine sand is recognized as having excellent properties as heat transfer media in biomass gasification, including moderate catalytic properties for reforming tar constituents. Magnetite may also be useful as heat transfer media, with the potential advantage of downstream magnetic separation between the heat transfer media and char.
- Carbonated sorbent, char and coked catalyst are transferred from
hydrogasification reactor 4 toregenerator reactor 7 via siphon 102. Calcined sorbent and regenerated catalyst are transferred back fromregenerator reactor 7 tohydrogasification reactor 4 viacyclone 103 and siphon 104. Ash may be released from the bottom ofregenerator 7 by a lock hopper or an intermittently operated valve. -
FIG. 6 shows a two stagefluidized bed embodiment 150, with thefirst stage 101 using relatively robust but less catalytically active media such as olivine or nickel impregnated olivine or glass-ceramic transition metal (e.g. Ni, Mo, W and combinations thereof) catalysts such as developed by the Gas Technology Institute, and thesecond stage 201 using more active and more delicate catalysts and lime sorbent for improved conversion of tars and higher yield of methane. In this embodiment, thefirst stage 101 is a fluidized bed reactor loop achieving hydropyrolysis and partial conversion to methane and hydrogen, while thesecond stage 201 performs more complete hydroconversion. - The
solids separation section 5 may here include means to remove catalyst poisons (e.g. sulphur, chlorides, alkalis, etc.). Second stagefluidized bed loop 201 includes the secondstage hydrogasification reactor 204, the secondstage regeneration reactor 207. Deactivated catalyst and carbonate sorbent are transferred fromhydrogasification reactor 204 toregenerator reactor 207 via siphon 212. Calcined sorbent and regenerated catalyst are transferred back fromregenerator reactor 207 tohydrogasification reactor 204 via siphon 214. - The hot gas effluent from
regenerator reactor 207 is delivered throughcyclone 213 and hot-gas cleanup section 50 to the inlet ofgas turbine expander 43. - Fluid control means 215 is provided to control flows of recycle hydrogen from
conduit 12 and steam fromconduit 19 to energize fluidized beds infirst stage reactor 101 andsecond stage reactor 201. Fluid control means 215 may include control valves, expanders or compressors as needed to control flows and regulate pressures. -
FIG. 7 shows a two stagefluidized bed embodiment 250, with the first stage 101 a fluidized bed hydropyrolysis reactor as inembodiments hydroconversion reactor 61 with a cyclic rotary switching mechanism for rotary fixedbeds 62 as shown inembodiment 60.Beds 62 are switched cyclically between methanation or hydroconversion steps as reactor 254, and regeneration steps asreactor 257. Hot gas cleanup can be performed incleanup section 250 with filtered solids and spent sorbents removed bydischarge conduit 251. Heatrecovery steam generator 258 may be provided to recover heat between firststage hydropyrolysis reactor 4 and second stage methanation or hydroconversion reactor 254. -
FIG. 8 shows an embodiment 300 for coproduction of methane and liquid hydrocarbons with a three stage reactor system. A hydropyrolysis reactor 304 is provided upstream of a hydroconversion reactor 310 for production of liquid hydrocarbons, and itself upstream of a sorption enhanced reactor 314 for production of hydrogen and methane. The hydrogen from reactor is delivered to hydropyrolysis reactor 304. Reactor 304 provides rapid heating of the biomass particles to a pyrolysis temperature in the range from about 300° C. to about 500° C., in order to decompose the biomass into pyrolysis gas (including light hydrocarbons, some syngas, and tar vapours) and char. Heating may be achieved by mixing the biomass particles with a granular heat transfer media in a mechanical or fluidized bed contacting system. Various mechanisms are well known for fast pyrolysis reactors (e.g. auger reactors and circulating fluidized beds), and may be used in a mechanical contacting system in reactor 304. The granular heat transfer media should have high heat capacity, thermal conductivity and attrition resistance. Olivine sand is recognized as having excellent properties as heat transfer media in biomass gasification, including moderate catalytic properties for reforming tar constituents. Nickel-impregnated olivine has improved catalytic properties. The glass-ceramic catalysts developed by the Gas Technology Institute are believed to be superior for hydropyrolysis applications. Magnetite may also be useful as heat transfer media, with the potential advantage of downstream magnetic separation between the heat transfer media and char. - The heat exchange media is circulated between reactor 304 and a media heater 315, with pyrolytic char being discharged from reactor 304 with spent heat exchange media returning to the media heater 315. Combustion of char in media heater 315 may conveniently provide heat required for heating the feed biomass to reaction temperature and for the endothermic pyrolysis and initial gasification reactions. Ash is discharged from media heater 315.
- A portion of the char exiting reactor 304 may be separated from the heat exchange media by char separator 316 as the feedstock for an auxiliary oxygen or steam gasification method to generate syngas. After water gas shift and CO2 removal from the syngas, supplemental hydrogen may thereby be provided for the subsequent hydrogasification reaction. Alternatively a portion of the char separated by char separator 316 may be diverted to other external uses, including sale of charcoal as a solid fuel, or as a “bio-char” soil amendment for agriculture or forestry uses with an important purpose of carbon sequestration in the soil. Ash may also be a useful byproduct for soil enhancement and recycle of nutrients for overall sustainability of biomass cultivation, harvesting and utilization.
- Solids are removed from the effluent pyrolysis gas exiting pyrolysis reactor 304 by a solids removal section 317 including one or multiple cyclones, and optionally also high temperature filters such as metallic or ceramic candle filters. A catalyst poison removal section 318 (including a desulfurization reactor using zinc oxide for H2S removal, and optionally including other sorbent beds for removal of chlorides and/or alkalis) may be included here for protection of downstream catalysts. The pyrolysis gas is also cooled by a heat recovery steam generator 319, either upstream or downstream of the catalyst poison removal sorbent beds.
- The cooled pyrolysis gas is introduced to catalytic hydroconversion reactor 310, together with hydrogen (or hydrogen-rich gas) and optionally also with steam. Hydrogen reactively deoxygenates the pyrolysis gas components to generate a mixture of lighter and heavier hydrocarbons by hydrodeoxygenation and decarboxylation reactions. Hydrogen and steam act to crack larger molecules, and to inhibit coking. The reactor effluent is provided to a first separator 321 from which a liquid fraction of heavier hydrocarbons is delivered by conduit 322 as a first liquid hydrocarbon product for further processing and use as desired.
- The overhead fraction from first separator 321 is cooled by heat recovery unit 330 to generate steam or preheat water upstream of second separator 331 in which water is condensed and separated from a liquid fraction of gasoline range hydrocarbons which is delivered as a second liquid hydrocarbon product by conduit 332 for further processing and use as desired. The overhead fraction of gases and vapours from second separator 331 contains H2, CO, CO2, CH4 and other light hydrocarbons along with some water vapour. This fraction is reheated and admitted to sorption enhanced reactor 314, optionally together with a portion of the cleaned pyrolysis gas from catalyst poison removal section 318 as controlled by valve 340 in conduit 341.
- Carbonation of CaO in sorption enhanced reactor 314 removes CO2 and also CO by water gas shift. Light hydrocarbons are preferentially prereformed so that the product of sorption enhanced reactor 314 will be mostly hydrogen with methane as the main residual carbon-containing compound. After clean-up and cooling of this product gas mixture from reactor 314,
gas separation system 10 separates substantially purified methane into SNGproduct delivery conduit 11, and a hydrogen-enriched recycle stream intoconduit 12 and back to the hydropyrolysis reactor 304. - The
gas separation system 10 may be operated to deliver a sufficient amount of hydrogen to the hydropyrolysis reactor and a significant amount of methane, with more methane production feasible if less liquid hydrocarbons are produced. In the absence of supplemental hydrogen imported to the process, approximately half the carbon in the feed biomass may be converted to product hydrocarbons (including heavier liquid hydrocarbons in the first product, gasoline range hydrocarbons in the second product, and product methane as a third product). The balance of the carbon is discharged as char or CO2. Higher carbon conversion can be achieved with the addition of imported hydrogen. - The product split between methane and liquid hydrocarbons can be varied operationally by adjusting
gas separation unit 10 so that more or less methane is delivered. With lower production of methane, more recycle hydrogen is available to the hydropyrolysis and hydroconversion reactors so that more liquid hydrocarbons are produced. - Production of liquid hydrocarbons can be maximized by turning off the delivery of product methane. In one embodiment of the invention, the
gas separation system 10 is removed so that the entire product effluent of sorption enhanced reactor 314 is delivered to hydropyrolysis reactor 304, while liquid hydrocarbon delivery of the first and second products is accordingly augmented. Reactor 314 is then operating as a sorption enhanced steam reformer, with several advantages including (1) lower temperature operation than a conventional steam reformer, (2) convenient direct use of char combustion for regenerating the sorbent, (3) integrated water gas shift and CO2 removal, and (4) scavenging of any alkali and chloride impurities in the recycle gas by the lime sorbent. -
Regenerator reactor 7 and sorption enhanced reactor 314 comprise a coupled reactor pair for the working reaction and for regeneration of the sorbent and catalyst. A catalyst regeneration reactor 330 is also provided for decoking catalyst from hydroconversion reactor 310. - A portion of compressed air from
compressor 42 andpreheater 15 is provided to pyrolysis media heater 315 for combustion of char to heat the media, with flue gas heat being recovered in steam. The remainder of the compressed air fromcompressor 42 andpreheater 15 is provided optionally with steam toregeneration reactors 7 and 330 to burn coke off the catalysts and decarbonate the CaCO3 formed in sorption enhanced reactor 314. Heatrecovery steam generators 8, 319 and 350 deliver steam to sorption enhanced reactor 314, or toregeneration reactors 330 and 7 as needed. -
FIG. 9 shows anembodiment 400, in which a hydrogasification system similar toembodiment 1 is coupled to a solid oxide fuel cell (SOFC) 410 for generation of electricity. The SOFC has asolid oxide electrolyte 412 between acathode chamber 413 and ananode chamber 414. The cathode chamber hasinlet port 415 andoutlet port 416, and the anode chamber hasinlet port 417 andoutlet port 418. The anode chamber includes an internal reforming catalyst (which may be comprised within the anode itself) to convert methane and steam to hydrogen and carbon oxides CO and CO2 under SOFC operating conditions at elevated temperatures in the range of about 600° C. to about 800° C. - A portion of the compressed air (or compressed oxygen-enriched air) from
air compression unit 16 is heated inthermal recuperator 422, and fed tocathode inlet port 415. Vitiated cathode gas is discharged fromport 416 and exhausted through recuperator 420 which recovers sensible heat from this gas. - A hot gas clean-up
section 430 is provided to remove solid particulate, alkalis and any chloride or sulphur compounds that have not been captured by the sorbent. The hot gas clean-upsection 430 may include cyclones, filters (metal fabric, ceramic candles or precoat filters), and chemical sorbents as necessary to capture the alkalis and any other detrimental components. Captured solids and spent sorbents will be released fromdischarge conduit 431. -
FIG. 10 is a graph of methane conversion, methane concentration, hydrogen concentration, and the ratio of hydrogen output to hydrogen input (H2out/H2in) from the hydrogasification reactor of the invention, versus the ratio of carbon carbonated on the sorbent to carbon content of the biomass feed to the process. - These correlations were derived for the case of an AEM process operating with CaO sorbent at a temperature of 600° C. and a pressure of 10 bara, with 1.0 molecules of hydrogen and 0.6 molecules of water vapour (including initial water content within the biomass) provided per atom of carbon in the original woody biomass feed. Thermodynamic equilibrium was assumed for the water gas shift, steam reforming and methanation reactions, with methane the only hydrocarbon molecule participating in these post-pyrolysis reactions. Char and coke deposition was assumed to consume about 21% of feed biomass carbon.
- Modeling runs were performed for different values of sorption uptake of carbon, shown as fractional carbonation of the original biomass carbon. Maximum fractional carbonation was found to be 0.4491, at which condition the partial pressure of CO2 is at equilibrium with a mixture of CaO and CaCO3. At a fractional carbonation of 0.370, the hydrogen output is equal to the amount of hydrogen input, thus defining an ideal self-sustaining condition without excess hydrogen generated or any external supplemental supply of hydrogen. With allowance for imperfect separation of product methane and recycle hydrogen, the practicable operating condition for self-sustaining hydrogen generation (without supplemental hydrogen supply from any external source) in this example will require fractional carbonation greater than 0.37, and of the order of 0.4.
- The above example shows that high purity methane can be produced by the sorption enhanced methanation method according to the invention, with methane the predominantly surviving carbon compound after nearly complete removal of CO2 and CO. This example contrasts dramatically with the related and well known process of sorption enhanced steam reforming of methane, where methane is nearly completely extinguished along with CO2 and CO in order to achieve hydrogen production with highest possible conversion.
- Disclosed embodiments of the method and system are useful for high efficiency conversion of biomass, including forestry residues (including those generated by logging, thinning, and wildfire prevention fuel load reduction activities) and sawmill waste into SNG, either as a fuel commodity or for high efficiency generation of electrical power. Disclosed embodiments provide advantageous integrations with gas turbines and/or solid oxide fuel cells. A portion of the biomass may also be converted into heavier and lighter hydrocarbon liquids.
- Disclosed embodiments of the system may be used at industrial scale limited only by transportation distances for collection of biomass feedstock, or at smaller scale in rural or remote areas for combined generation of heat, high heating value fuel gas and electricity. At the smallest scale, the system may be used for residential heating, methane fuel production and electrical power generation through a solid oxide fuel cell or other energy converter consuming a portion of the product methane.
- In view of the many possible embodiments to which the principles of the disclosed invention may be applied, it should be recognized that the illustrated embodiments are only preferred examples of the invention and should not be taken as limiting the scope of the invention. Rather, the scope of the invention is defined by the following claims. We therefore claim as our invention all that comes within the scope and spirit of these claims.
Claims (33)
1. A method for converting a biomass feedstock into a product hydrocarbon, comprising:
a. subjecting feedstock to fast pyrolysis or hydropyrolysis to generate fractions of pyrolysis gas and char;
b. converting at least a portion of the pyrolysis gas in a hydroconversion step to a product hydrocarbon and carbon dioxide over a catalyst in the presence of hydrogen and steam, while removing carbon dioxide by carbonation of a sorbent;
c. generating at least a portion of the hydrogen by steam reforming by reaction between steam and a portion of the pyrolysis gas or a product hydrocarbon;
d. separating hydrogen from the hydrocarbon product, and recycling the hydrogen so as to force hydroconversion of biomass into the hydrocarbon product; and
e. regenerating the sorbent in a regeneration step to release the carbon dioxide.
2. The method of claim 1 , in which subjecting the feedstock to fast pyrolysis or hydropyrolysis comprises hydropyrolysis.
3. The method of claim 1 , further comprising regenerating the sorbent by heating through combustion of the char and any coke deposited on the sorbent or catalyst.
4. The method of claim 1 , further comprising regenerating the sorbent by heating with superheated steam.
5. The method of claim 3 , further comprising regenerating or decoking the catalyst in regeneration step (e).
6. The method of claim 4 , further comprising regenerating or decoking the catalyst in regeneration step (e).
7. The method of claim 1 , in which the product hydrocarbon is methane, and where converting at least a portion of the pyrolysis gas includes a methanation step.
8. The method of claim 1 , in which the sorbent comprises CaO.
9. The method of claim 1 , where converting at least a portion of the pyrolysis gas occurs at a temperature in the range of from about 500° C. to about 650° C.
10. The method of claim 1 , where converting at least a portion of the pyrolysis gas occurs at a pressure in the range of from about 1 bara to about 50 bara.
11. The method of claim 1 , where regenerating the sorbent occurs at a temperature in the range of from about 700° C. to about 850° C.
12. The method of claim 1 , where separating hydrogen comprises pressure swing adsorption.
13. The method of claim 1 , where separating hydrogen comprises membrane permeation.
14. The method of claim 1 , further comprising providing the catalyst in any of the following reactor configurations so that the catalyst will cycle between distinct reaction zones for hydroconversion and regeneration steps:
a. moving bed with granular catalyst;
b. fixed bed with granular packing or monolithic catalyst, and rotary or directional valve logic for cyclically switching beds between reaction and regeneration steps;
c. bubbling or circulating fluidized bed.
15. The method of claim 2 , further comprising providing staged reactors for hydropyrolysis and hydroconversion steps.
16. The method of claim 7 , further comprising performing hydropyrolysis and hydroconversion steps in a single bubbling fluidized bed reactor.
17. The method of claim 14 , in which hydroconversion is performed to produce liquid hydrocarbons, and a sorption enhanced reaction step is performed to generate hydrogen required for the hydroconversion step.
18. The method of claim 17 , in which the liquid hydrocarbons are produced as a first product of heavier hydrocarbons and a second product of gasoline range hydrocarbons.
19. The method of claim 17 , in which product methane is also produced in a hydroconversion step with sorption enhanced reaction.
20. The method of claim 1 , further comprising generating electrical power with an internal-reforming solid oxide fuel cell fuelled by methane and hydrogen converted from the biomass feedstock.
21. The method of claim 20 , in which substantially the entire anode exhaust of the solid oxide fuel cell is provided as the source of hydrogen and steam to hydropyrolysis step (a) or hydroconversion step (b).
22. The method of claim 1 , further comprising generating power with a gas turbine to recover heat from regenerating the sorbent.
23. A system for producing hydrocarbons from biomass, the system comprising:
f. fast pyrolysis means operating at a process temperature less than about 650° C. for producing pyrolysis gas and char;
g. catalytic conversion means operating at a process temperature less than about 650° C. for converting the pyrolysis gas to hydrocarbons and hydrogen by hydroconversion over a catalyst and in presence of a CO2 sorbent;
h. gas separation means for purifying a hydrocarbon product and for recycling hydrogen to the catalytic conversion means; and
i. means for regenerating the CO2 sorbent to release the CO2.
24. The system according to claim 23 where the fast pyrolysis means includes a hydrogen sweep gas.
25. The system according to claim 23 in which a portion of the hydrogen is produced in a steam reforming zone.
26. The system according to claim 23 in which hydrocarbons converted over the catalyst are mainly methane, and the catalyst is in a methanation zone.
27. The system according to claim 26 in which a catalyst used in the steam reforming and methanation zones is the same catalyst.
28. The system according to claim 27 in which steam reforming and methanation zones are combined within a hydroconversion reactor.
29. The system according to claim 23 further comprising regeneration means for heating and regenerating the catalyst in a regeneration zone.
30. The system according to claim 29 , further comprising means for cyclically circulating or switching the catalyst between the hydroconversion and regeneration zones.
31. The system according to claim 30 , in which the catalyst is supported in fixed beds with switching valves to establish the hydroconversion and regeneration zones to which each bed is cycled.
32. The system according to claim 31 , in which the fixed beds containing the catalyst are mounted in a rotor with rotary valve ports sealingly engaged with fixed ports to establish the hydroconversion and regeneration zones to which each bed is cycled.
33. The system according to claim 28 wherein substantially all of the hydrogen is produced in the steam reforming zone or hydroconversion reactor.
Priority Applications (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US13/474,494 US20130017460A1 (en) | 2009-11-18 | 2012-05-17 | Sorption enhanced methanation of biomass |
US15/704,918 US10653995B2 (en) | 2009-11-18 | 2017-09-14 | Sorption enhanced methanation of biomass |
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US26248509P | 2009-11-18 | 2009-11-18 | |
PCT/CA2010/001859 WO2011060556A1 (en) | 2009-11-18 | 2010-11-18 | Sorption enhanced methanation of biomass |
US13/474,494 US20130017460A1 (en) | 2009-11-18 | 2012-05-17 | Sorption enhanced methanation of biomass |
Related Parent Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/CA2010/001859 Continuation WO2011060556A1 (en) | 2009-11-18 | 2010-11-18 | Sorption enhanced methanation of biomass |
Related Child Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US15/704,918 Continuation US10653995B2 (en) | 2009-11-18 | 2017-09-14 | Sorption enhanced methanation of biomass |
Publications (1)
Publication Number | Publication Date |
---|---|
US20130017460A1 true US20130017460A1 (en) | 2013-01-17 |
Family
ID=44059167
Family Applications (2)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US13/474,494 Abandoned US20130017460A1 (en) | 2009-11-18 | 2012-05-17 | Sorption enhanced methanation of biomass |
US15/704,918 Active 2031-03-22 US10653995B2 (en) | 2009-11-18 | 2017-09-14 | Sorption enhanced methanation of biomass |
Family Applications After (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US15/704,918 Active 2031-03-22 US10653995B2 (en) | 2009-11-18 | 2017-09-14 | Sorption enhanced methanation of biomass |
Country Status (4)
Country | Link |
---|---|
US (2) | US20130017460A1 (en) |
EP (1) | EP2501788A4 (en) |
CA (1) | CA2781204C (en) |
WO (1) | WO2011060556A1 (en) |
Cited By (15)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2015017875A1 (en) * | 2013-08-05 | 2015-02-12 | Technische Universität Wien | Method and system for storing energy |
US20150240715A1 (en) * | 2013-03-08 | 2015-08-27 | Sulabh K. Dhanuka | Power Generation And Methane Recovery From Methane Hydrates |
CN105174679A (en) * | 2015-10-13 | 2015-12-23 | 中国石油化工股份有限公司 | Method for producing hydrogen by performing catalytic gasification on oil-containing sludge |
WO2016166413A1 (en) * | 2015-04-17 | 2016-10-20 | Valmet Technologies Oy | Catalytic upgrading of pyrolytic vapors |
CN107635913A (en) * | 2015-05-28 | 2018-01-26 | 气体技术学院 | The lower adsorbent powerforming hydrogen manufacturing of air calcining |
US9937484B2 (en) | 2015-01-30 | 2018-04-10 | Battelle Memorial Institute | Reactor, CO2 sorbent system, and process of making H2 with simultaneous CO2 sorption |
US10190066B2 (en) * | 2009-11-18 | 2019-01-29 | G4 Insights Inc. | Method and system for biomass hydrogasification |
US10208948B2 (en) * | 2014-03-28 | 2019-02-19 | Shanghai Boiler Works Co., Ltd. | Solid fuel grade gasification-combustion dual bed poly-generation system and method thereof |
US10283797B2 (en) * | 2013-09-30 | 2019-05-07 | Marek Fulde | Method for storing electric energy by production, storage, and dissociation of methane having closed carbon circuit |
US20190241434A1 (en) * | 2016-07-14 | 2019-08-08 | Zeg Power As | Method and Device for Upgrading of Biogas and Hydrogen Production From Anaerobic Fermentation of Biological Material |
US10570348B2 (en) * | 2017-01-15 | 2020-02-25 | Wormser Energy Solutions, Inc. | All-steam gasification for supercritical CO2 power cycle system |
US10619105B2 (en) | 2014-07-01 | 2020-04-14 | Gas Technology Institute | Hydropyrolysis of biomass-containing feedstocks |
US11142702B2 (en) * | 2017-10-13 | 2021-10-12 | Cortus Ab | Process and apparatus for hydrotreatment of pyrolysis oil |
US11223059B2 (en) | 2016-07-14 | 2022-01-11 | Zeg Power As | Method and power plant comprising a solid oxide fuel cell (SOFC) for production of electrical energy and H2 gas |
EP4230287A1 (en) * | 2022-02-16 | 2023-08-23 | Eidgenössische Materialprüfungs- und Forschungsanstalt | Sorption-enhanced catalytic reactors with thermal moderators |
Families Citing this family (20)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US9657232B2 (en) | 2011-11-14 | 2017-05-23 | Shell Oil Company | Process for producing hydrocarbons |
GB2499404B (en) | 2012-02-14 | 2019-08-14 | Anergy Ltd | Fuel processing using pyrolyser |
CN102829473B (en) | 2012-09-25 | 2016-02-03 | 中国东方电气集团有限公司 | A kind of pyrolysis and combustion double bed solves the system that high sodium coal combustion stains |
CN102829472B (en) * | 2012-09-25 | 2015-09-16 | 中国东方电气集团有限公司 | A kind of method and system of the flyash recirculation preventing boiler from staiing |
CN102829474B (en) | 2012-09-25 | 2016-04-06 | 中国东方电气集团有限公司 | A kind of dual bed systems preventing boiler heating surface from staiing |
CN102937290B (en) * | 2012-11-21 | 2015-08-26 | 中国东方电气集团有限公司 | The double-fluidized-bed system preventing boiler from staiing of a kind of external bed |
CN102944008B (en) * | 2012-11-21 | 2015-10-28 | 中国东方电气集团有限公司 | The system that a kind of double fluidized bed combustion stove prevents boiler heating surface from staiing |
WO2014082038A1 (en) * | 2012-11-26 | 2014-05-30 | Kansas State University Research Foundation | Thermochemical ammonia and hydrocarbons |
WO2014204302A1 (en) | 2013-06-18 | 2014-12-24 | Universiteit Twente | Process for converting a biomass feedstock into at least a liquid hydrocarbon product |
EP3169753B1 (en) | 2014-07-17 | 2020-06-10 | SABIC Global Technologies B.V. | Upgrading hydrogen deficient streams using hydrogen donor streams in a hydropyrolysis process |
WO2016064825A1 (en) * | 2014-10-24 | 2016-04-28 | Research Triangle Institute | Integrated system and method for removing acid gas from a gas stream |
KR101660472B1 (en) * | 2015-05-11 | 2016-09-27 | 고려대학교 산학협력단 | Method of Synthetic Natural Gas Production Using Sorption-enhanced Methanation |
US20180162729A1 (en) * | 2015-05-28 | 2018-06-14 | Gas Technology Institute | Power generation using hydrogen fuel with economical carbon dioxide capture |
WO2020257946A1 (en) * | 2019-06-27 | 2020-12-30 | Hallett Douglas John Frederick | Process for reducing an organic material to produce methane and/or hydrogen |
NO345216B1 (en) * | 2019-08-28 | 2020-11-09 | Zeg Power As | Hydrogen-fuelled gas turbine power system and method for its operation |
GB202001961D0 (en) * | 2020-02-13 | 2020-04-01 | Origen Power Ltd | Grid-energy firming process |
EP3967386A1 (en) * | 2020-09-11 | 2022-03-16 | Nederlandse Organisatie voor toegepast- natuurwetenschappelijk onderzoek TNO | Displacement purge adsorption process for separating co2 from another gas |
CN111921530B (en) * | 2020-09-23 | 2021-10-01 | 广西师范大学 | CaO-multiferroic metal composite catalyst for carbon hydro-gasification and preparation method thereof |
CN112625763B (en) * | 2020-11-30 | 2021-10-01 | 乌海市西部煤化工有限责任公司 | Coke oven gas desulfurization process |
CN113249142A (en) * | 2021-05-21 | 2021-08-13 | 西北大学 | Preparation method of biomass charcoal-metal oxide composite electrode material |
Citations (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2436495A (en) * | 1945-12-26 | 1948-02-24 | Adsorptive Process Company | Process and apparatus for adsorptively and catalytically treating hydrocarbon oil |
US20070000177A1 (en) * | 2005-07-01 | 2007-01-04 | Hippo Edwin J | Mild catalytic steam gasification process |
US20080090113A1 (en) * | 2002-09-27 | 2008-04-17 | Bowie G. Keefer | Enhanced solid oxide fuel cell systems |
US20080145309A1 (en) * | 2006-12-15 | 2008-06-19 | Texaco Inc. | Fluidized Bed System for Single Step Reforming for the Production of Hydrogen |
US20090082604A1 (en) * | 2007-08-27 | 2009-03-26 | Purdue Research Foundation | Novel process for producing liquid hydrocarbon by pyrolysis of biomass in presence of hydrogen from a carbon-free energy source |
US20090165376A1 (en) * | 2007-12-28 | 2009-07-02 | Greatpoint Energy, Inc. | Steam Generating Slurry Gasifier for the Catalytic Gasification of a Carbonaceous Feedstock |
US20090217584A1 (en) * | 2008-02-29 | 2009-09-03 | Greatpoint Energy, Inc. | Steam Generation Processes Utilizing Biomass Feedstocks |
US20100251600A1 (en) * | 2009-04-07 | 2010-10-07 | Gas Technology Institute | Hydropyrolysis of biomass for producing high quality liquid fuels |
US20100256428A1 (en) * | 2009-04-07 | 2010-10-07 | Gas Technology Institute | Hydropyrolysis of biomass for producing high quality liquid fuels |
US20100287836A1 (en) * | 2009-05-13 | 2010-11-18 | Greatpoint Energy, Inc. | Processes for Hydromethanation of a Carbonaceous Feedstock |
Family Cites Families (113)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3070703A (en) | 1960-04-07 | 1962-12-25 | United Aircraft Corp | Solar energy powerplant |
US3336162A (en) | 1963-07-03 | 1967-08-15 | Martin Marietta Corp | Fuel cell and electrical generator system |
US3625664A (en) * | 1967-04-05 | 1971-12-07 | Carlo Padovani | Process for the production of rich fuel to replace natural gas by means of catalytic hydrogasification under pressure of fluid hydrocarbons |
US3847672A (en) | 1971-08-18 | 1974-11-12 | United Aircraft Corp | Fuel cell with gas separator |
US3865924A (en) | 1972-03-03 | 1975-02-11 | Inst Gas Technology | Process for regenerative sorption of CO{HD 2 |
US3748180A (en) | 1972-03-30 | 1973-07-24 | Us Navy | Fuel cell system for underwater vehicle |
US3975913A (en) | 1973-12-20 | 1976-08-24 | Erickson Donald C | Gas generator and enhanced energy conversion systems |
US4135361A (en) | 1976-10-26 | 1979-01-23 | The Charles Stark Draper Laboratory, Inc. | Self-contained heat generating system |
DE3022802C2 (en) | 1980-06-19 | 1982-11-11 | Deutsche Forschungs- Und Versuchsanstalt Fuer Luft- Und Raumfahrt E.V., 5300 Bonn | Device for storing liquid hydrogen |
US4555453A (en) | 1981-10-01 | 1985-11-26 | Electric Power Research, Inc. | Method for forming molten carbonate fuel cell component and structure |
EP0143537B1 (en) | 1983-10-03 | 1990-03-21 | Bowie Gordon Keefer | Method and apparatus for gas separation and synthesis |
US4801308A (en) | 1983-10-03 | 1989-01-31 | Keefer Bowie | Apparatus and process for pressure swing adsorption separation |
US4816121A (en) | 1983-10-03 | 1989-03-28 | Keefer Bowie | Gas phase chemical reactor |
JPS6171561A (en) | 1984-09-14 | 1986-04-12 | Mitsubishi Heavy Ind Ltd | Composite plant of fuel cell |
US4532192A (en) | 1984-11-06 | 1985-07-30 | Energy Research Corporation | Fuel cell system |
JPH06103631B2 (en) | 1986-01-23 | 1994-12-14 | 株式会社日立製作所 | Air supply system device for fuel cell system |
JPS62278770A (en) | 1986-05-27 | 1987-12-03 | Nippon Kokan Kk <Nkk> | Recovering method of co2 and h2 from converter gas |
CA1300885C (en) | 1986-08-26 | 1992-05-19 | Donald S. Scott | Hydrogasification of biomass to produce high yields of methane |
JPS63166702A (en) | 1986-12-26 | 1988-07-09 | Osaka Oxygen Ind Ltd | Concentration of oxygen gas |
US4968329A (en) | 1987-10-26 | 1990-11-06 | Keefer Bowie | Pressure swing adsorption for concentration of a gas component |
US4859545A (en) | 1988-05-05 | 1989-08-22 | International Fuel Cells Corporation | Cathode flow control for fuel cell power plant |
FR2633847B1 (en) | 1988-07-08 | 1991-04-19 | Air Liquide | PROCESS FOR TREATING A GAS MIXTURE BY ADSORPTION |
JPH02117072A (en) | 1988-10-26 | 1990-05-01 | Toyo Eng Corp | Fuel cell power generation system |
JPH02172159A (en) | 1988-12-24 | 1990-07-03 | Ishikawajima Harima Heavy Ind Co Ltd | Molten carbonate fuel cell power generating method and system |
DE3932217A1 (en) | 1989-04-25 | 1990-10-31 | Linde Ag | METHOD FOR OPERATING HIGH-TEMPERATURE FUEL CELLS |
DE3913581A1 (en) | 1989-04-25 | 1990-10-31 | Linde Ag | METHOD FOR OPERATING FUEL CELLS |
JP2926259B2 (en) | 1989-06-09 | 1999-07-28 | 大阪瓦斯株式会社 | Solid electrolyte fuel cell |
CA2016045C (en) | 1990-05-04 | 1994-08-16 | Quest Air Gases Inc. | Gas separation by pressure swing adsorption |
US5096469A (en) | 1990-07-23 | 1992-03-17 | Keefer Bowie | Adsorptive gas separator with inertial energy exchange |
US5082473A (en) | 1990-07-23 | 1992-01-21 | Keefer Bowie | Extraction and concentration of a gas component |
US5366818A (en) | 1991-01-15 | 1994-11-22 | Ballard Power Systems Inc. | Solid polymer fuel cell systems incorporating water removal at the anode |
US5292598A (en) | 1991-12-17 | 1994-03-08 | Stuart Rosner | Method for renewing fuel cells using magnesium anodes |
US5256172A (en) | 1992-04-17 | 1993-10-26 | Keefer Bowie | Thermally coupled pressure swing adsorption |
WO1993025843A1 (en) | 1992-06-08 | 1993-12-23 | Saes Getters S.P.A. | Process for evacuating a thermally insulating jacket, in particular the jacket of a dewar or of another cryogenic device |
WO1994003937A1 (en) | 1992-08-10 | 1994-02-17 | Siemens Aktiengesellschaft | Fuel cell and electrolyte moistening process |
US5504259A (en) | 1992-10-29 | 1996-04-02 | Midwest Research Institute | Process to convert biomass and refuse derived fuel to ethers and/or alcohols |
US5328503A (en) | 1992-11-16 | 1994-07-12 | Air Products And Chemicals, Inc. | Adsorption process with mixed repressurization and purge/equalization |
JPH06208853A (en) | 1993-01-12 | 1994-07-26 | Tokyo Electric Power Co Inc:The | Fuel cell power generating equipment and operating method thereof |
DE4318818C2 (en) | 1993-06-07 | 1995-05-04 | Daimler Benz Ag | Method and device for providing conditioned process air for air-breathing fuel cell systems |
JPH0794200A (en) | 1993-09-28 | 1995-04-07 | Osaka Gas Co Ltd | Reaction air supply unit of fuel cell power generating system |
JPH07279758A (en) | 1994-04-13 | 1995-10-27 | Daikin Ind Ltd | Co-generation device |
WO1995028510A1 (en) | 1994-04-19 | 1995-10-26 | Hydrogen Technology Ltd. | Improvements in electrolysis systems and the availability of over-unity energy |
US5487775A (en) | 1994-05-09 | 1996-01-30 | The Boc Group, Inc. | Continuous pressure difference driven adsorption process |
US5411578A (en) | 1994-05-10 | 1995-05-02 | Air Products And Chemicals, Inc. | Vacuum swing adsorption process with mixed repressurization and provide product depressurization |
US5523176A (en) | 1994-06-17 | 1996-06-04 | Fonda-Bonardi; G. | Apparatus for generating electricity |
JPH0812303A (en) | 1994-07-05 | 1996-01-16 | Ishikawajima Harima Heavy Ind Co Ltd | Plate reformer |
JP3664178B2 (en) | 1994-08-03 | 2005-06-22 | 石川島播磨重工業株式会社 | Multistage fuel cell |
US5982857A (en) | 1994-10-17 | 1999-11-09 | Apropros Technology | Voice recording method and system providing context specific storage and retrieval |
US5900329A (en) | 1994-10-19 | 1999-05-04 | Siemens Aktiengesellschaft | Fuel-cell system and method for operating a fuel-cell system |
US5523326A (en) | 1994-10-28 | 1996-06-04 | Uop | PSA process with reaction for reversible reactions |
US5593640A (en) | 1995-06-07 | 1997-01-14 | Ball Corporation | Portable hydrogen generator |
US6170264B1 (en) | 1997-09-22 | 2001-01-09 | Clean Energy Systems, Inc. | Hydrocarbon combustion power generation system with CO2 sequestration |
US5604047A (en) | 1995-06-23 | 1997-02-18 | Exxon Research And Engineering Company | Carbon monoxide removal method based on adsorption/steam desorption cycle |
US5656064A (en) | 1995-10-04 | 1997-08-12 | Air Products And Chemicals, Inc. | Base treated alumina in pressure swing adsorption |
US6045933A (en) | 1995-10-11 | 2000-04-04 | Honda Giken Kogyo Kabushiki Kaisha | Method of supplying fuel gas to a fuel cell |
JP3554092B2 (en) | 1995-10-11 | 2004-08-11 | 本田技研工業株式会社 | Fuel cell fuel gas supply method |
US5867978A (en) | 1995-12-04 | 1999-02-09 | The Penn State Research Foundation | System for generating hydrogen |
US5711926A (en) | 1996-05-14 | 1998-01-27 | Knaebel; Kent S. | Pressure swing adsorption system for ammonia synthesis |
US5811201A (en) | 1996-08-16 | 1998-09-22 | Southern California Edison Company | Power generation system utilizing turbine and fuel cell |
US5686196A (en) | 1996-10-09 | 1997-11-11 | Westinghouse Electric Corporation | System for operating solid oxide fuel cell generator on diesel fuel |
JP2001507982A (en) | 1996-12-31 | 2001-06-19 | ボーイ ゴードン キーファー | Adsorption by high frequency pressure fluctuation |
DE19701560C2 (en) | 1997-01-17 | 1998-12-24 | Dbb Fuel Cell Engines Gmbh | Fuel cell system |
US6283723B1 (en) | 1997-01-27 | 2001-09-04 | Vairex Corporation | Integrated compressor expander apparatus |
US5832728A (en) | 1997-04-29 | 1998-11-10 | Buck; Erik S. | Process for transmitting and storing energy |
JP4058783B2 (en) | 1997-11-07 | 2008-03-12 | 松下電器産業株式会社 | Fuel cell device |
DE19755116C1 (en) | 1997-12-11 | 1999-03-04 | Dbb Fuel Cell Engines Gmbh | Method of operating a Proton Exchange Membrane fuel cell system |
US6051050A (en) | 1997-12-22 | 2000-04-18 | Questor Industries Inc. | Modular pressure swing adsorption with energy recovery |
JPH11214021A (en) | 1998-01-27 | 1999-08-06 | Ishikawajima Harima Heavy Ind Co Ltd | Solid electrolyte type fuel cell power generating apparatus |
IL138367A0 (en) | 1998-03-12 | 2001-10-31 | Hydrogen Burner Techn Inc | Process gas purification and fuel cell system |
US6206630B1 (en) | 1998-04-24 | 2001-03-27 | Universal Electric Power Corp. | High torque impulse turbine |
JP2000072401A (en) | 1998-08-21 | 2000-03-07 | Japan Steel Works Ltd:The | Sensible heat recovering method of hydrogen absorbing and releasing device and device therefor |
JP3473436B2 (en) | 1998-09-16 | 2003-12-02 | 株式会社豊田自動織機 | Fuel cell device |
NL1010288C2 (en) | 1998-10-12 | 2000-04-13 | Stichting Energie | Method for the conversion of hydrogen into substitute natural gas. |
US6110612A (en) | 1999-04-19 | 2000-08-29 | Plug Power Inc. | Structure for common access and support of fuel cell stacks |
WO2000075559A1 (en) | 1999-06-04 | 2000-12-14 | National University Of Singapore | Method of reversibly storing h2 and h2-storage system based on metal-doped carbon-based materials |
AU5381200A (en) | 1999-06-09 | 2001-01-02 | Questair Technologies, Inc. | Rotary pressure swing adsorption apparatus |
CA2274312A1 (en) | 1999-06-10 | 2000-12-10 | Kevin A. Kaupert | Modular pressure swing adsorption apparatus with clearance-type valve seals |
US6190623B1 (en) | 1999-06-18 | 2001-02-20 | Uop Llc | Apparatus for providing a pure hydrogen stream for use with fuel cells |
US6142758A (en) | 1999-06-28 | 2000-11-07 | Henry Engine Company | Rotary positive displacement engine |
US6231644B1 (en) | 1999-07-23 | 2001-05-15 | The Boc Group, Inc. | Air separation using monolith adsorbent bed |
DE19946381C2 (en) | 1999-09-28 | 2001-09-06 | Zsw | Method and device for producing a low-carbon, hydrogen-rich gas or a conditioned synthesis gas and use thereof |
US6305442B1 (en) | 1999-11-06 | 2001-10-23 | Energy Conversion Devices, Inc. | Hydrogen-based ecosystem |
US6627338B2 (en) | 1999-12-22 | 2003-09-30 | Ballard Power Systems Inc. | Integrated fuel cell and pressure swing adsorption system |
US6293767B1 (en) | 2000-02-28 | 2001-09-25 | Copeland Corporation | Scroll machine with asymmetrical bleed hole |
US7041272B2 (en) | 2000-10-27 | 2006-05-09 | Questair Technologies Inc. | Systems and processes for providing hydrogen to fuel cells |
CA2325072A1 (en) | 2000-10-30 | 2002-04-30 | Questair Technologies Inc. | Gas separation for molten carbonate fuel cell |
US20020142198A1 (en) | 2000-12-08 | 2002-10-03 | Towler Gavin P. | Process for air enrichment in producing hydrogen for use with fuel cells |
US20020112479A1 (en) | 2001-01-09 | 2002-08-22 | Keefer Bowie G. | Power plant with energy recovery from fuel storage |
NL1018159C2 (en) | 2001-05-28 | 2002-12-03 | Gastec Nv | Process for converting hydrocarbonaceous material into a methane-containing gas. |
US6863878B2 (en) | 2001-07-05 | 2005-03-08 | Robert E. Klepper | Method and apparatus for producing synthesis gas from carbonaceous materials |
US7208530B2 (en) | 2002-02-05 | 2007-04-24 | The Regents Of The University Of California | Production of synthetic transportation fuels from carbonaceous material using self-sustained hydro-gasification |
CA2476409A1 (en) | 2002-03-14 | 2003-09-18 | Questair Technologies Inc. | Hydrogen recycle for solid oxide fuel cell |
US20040004031A1 (en) | 2002-06-26 | 2004-01-08 | Boger Thorsten R. | System and process for pyrolysis gasoline hydrotreatment |
US6854273B1 (en) | 2003-10-20 | 2005-02-15 | Delphi Technologies, Inc. | Apparatus and method for steam engine and thermionic emission based power generation system |
US7553568B2 (en) | 2003-11-19 | 2009-06-30 | Bowie Keefer | High efficiency load-following solid oxide fuel cell systems |
DE102004045772A1 (en) | 2004-09-15 | 2006-03-16 | Zentrum für Sonnenenergie- und Wasserstoff-Forschung Baden-Württemberg | Preparation of product gas, useful e.g. as gaseous fuel, comprises low temperature gasification of carbon containing material in presence of absorber materials to give tar poor product gas, and regeneration of absorber material |
US7868214B2 (en) | 2005-05-19 | 2011-01-11 | Uop Llc | Production of olefins from biorenewable feedstocks |
US7754931B2 (en) | 2005-09-26 | 2010-07-13 | Her Majesty The Queen In Right Of Canada As Represented By The Minister Of Natural Resources | Production of high-cetane diesel fuel from low-quality biomass-derived feedstocks |
WO2007041293A2 (en) | 2005-09-29 | 2007-04-12 | Doheny Eye Institute | Microelectrode systems for neuro-stimulation and neuro-sensing and microchip packaging and related methods |
US20090263317A1 (en) | 2005-12-15 | 2009-10-22 | Wei Chen | Method of screening the activity of the smoothened receptor to identify theraputic modulation agents or diagnose disease |
RU2501841C2 (en) | 2006-03-24 | 2013-12-20 | Висконсин Эламнай Рисерч Фаундейшн | Method of producing biofuel, where heat from formation of carbon-carbon bonds is used to carry out biomass gasification reactions |
US20070272538A1 (en) | 2006-05-26 | 2007-11-29 | Satchell Donald P | Flash pyrolosis method for carbonaceous materials |
US8795392B2 (en) | 2006-06-09 | 2014-08-05 | Albemarle Netherlands B.V. | Catalytic hydrodeoxygenation of an oxygenate feedstock |
WO2008033812A2 (en) | 2006-09-11 | 2008-03-20 | Purdue Research Foundation | System and process for producing synthetic liquid hydrocarbon |
CN101541398B (en) * | 2006-09-25 | 2014-01-22 | 俄亥俄州立大学 | High purity hydrogen production and in situ capture of CO<2> and sulfur |
US20100205863A1 (en) | 2007-07-10 | 2010-08-19 | Paul Scherrer Institut | Process to Produce a Methane Rich Gas Mixture From Gasification Derived Sulphur Containing Synthesis Gases |
WO2009124017A2 (en) | 2008-04-01 | 2009-10-08 | Greatpoint Energy, Inc. | Processes for the separation of methane from a gas stream |
US7960598B2 (en) | 2008-12-08 | 2011-06-14 | Chevron U.S.A. Inc. | Selective, integrated processing of bio-derived ester species to yield low molecular weight hydrocarbons and hydrogen for the production of biofuels |
WO2010080733A1 (en) | 2009-01-09 | 2010-07-15 | Cool Planet Biofuels, Llc | System and method for atmospheric carbon sequestration |
WO2010099626A1 (en) | 2009-03-05 | 2010-09-10 | G4 Insights Inc. | Process and system for thermochemical conversion of biomass |
US8915981B2 (en) | 2009-04-07 | 2014-12-23 | Gas Technology Institute | Method for producing methane from biomass |
US8063258B2 (en) | 2009-05-22 | 2011-11-22 | Kior Inc. | Catalytic hydropyrolysis of organophillic biomass |
CA2781195C (en) | 2009-11-18 | 2018-09-18 | G4 Insights Inc. | Method and system for biomass hydrogasification |
-
2010
- 2010-11-18 EP EP10831012.9A patent/EP2501788A4/en not_active Ceased
- 2010-11-18 CA CA2781204A patent/CA2781204C/en active Active
- 2010-11-18 WO PCT/CA2010/001859 patent/WO2011060556A1/en active Application Filing
-
2012
- 2012-05-17 US US13/474,494 patent/US20130017460A1/en not_active Abandoned
-
2017
- 2017-09-14 US US15/704,918 patent/US10653995B2/en active Active
Patent Citations (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2436495A (en) * | 1945-12-26 | 1948-02-24 | Adsorptive Process Company | Process and apparatus for adsorptively and catalytically treating hydrocarbon oil |
US20080090113A1 (en) * | 2002-09-27 | 2008-04-17 | Bowie G. Keefer | Enhanced solid oxide fuel cell systems |
US20070000177A1 (en) * | 2005-07-01 | 2007-01-04 | Hippo Edwin J | Mild catalytic steam gasification process |
US20080145309A1 (en) * | 2006-12-15 | 2008-06-19 | Texaco Inc. | Fluidized Bed System for Single Step Reforming for the Production of Hydrogen |
US20090082604A1 (en) * | 2007-08-27 | 2009-03-26 | Purdue Research Foundation | Novel process for producing liquid hydrocarbon by pyrolysis of biomass in presence of hydrogen from a carbon-free energy source |
US20090165376A1 (en) * | 2007-12-28 | 2009-07-02 | Greatpoint Energy, Inc. | Steam Generating Slurry Gasifier for the Catalytic Gasification of a Carbonaceous Feedstock |
US20090217584A1 (en) * | 2008-02-29 | 2009-09-03 | Greatpoint Energy, Inc. | Steam Generation Processes Utilizing Biomass Feedstocks |
US20100251600A1 (en) * | 2009-04-07 | 2010-10-07 | Gas Technology Institute | Hydropyrolysis of biomass for producing high quality liquid fuels |
US20100256428A1 (en) * | 2009-04-07 | 2010-10-07 | Gas Technology Institute | Hydropyrolysis of biomass for producing high quality liquid fuels |
US20100287836A1 (en) * | 2009-05-13 | 2010-11-18 | Greatpoint Energy, Inc. | Processes for Hydromethanation of a Carbonaceous Feedstock |
Non-Patent Citations (7)
Title |
---|
Bridgwater, Renewable fuels and chemicals by thermal processing of biomass, Chemical Engineering Journal 91 (2003) 87–102; 16 pages total * |
Florin et al. Enhanced hydrogen production from biomass with in situ carbon dioxide capture using calcium oxide sorbents, Chemical Engineering Science 63 (2008) 287-316; 30 pages total. * |
Florin et al., Hydrogen production from biomass coupled with carbon dioxide capture: The implications of thermodynamic equilibrium, International Journal of Hydrogen Energy 32 (2007) 4119 – 4134; 16 pages total. * |
Johnsen et al., Sorption-enhanced steam reforming of methane in a fluidized bed reactor with dolomite asCO2-acceptor, Chemical Engineering Science 61 (2006) 1195 - 1202; 8 pages total. * |
Peacocke et al., Notes on Terminology and Technology in Thermal Conversion, International Biochar Initiative, 2005; 5 pages total * |
Pfeifer et al., Comparison of dual fluidized bed steam gasification of biomass with and without selective transport of CO2 , Chemical Engineering Science 64 (2009) 5073 -5083; 11 pages total. * |
Richard L. Bain, An Introduction to Biomass Thermochemical Conversion, DOE/NASLUGC Biomass and Solar Energy Workshops, August 3-4, 2004, National Renewable Energy Laborator; 77 pages total. * |
Cited By (21)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US10190066B2 (en) * | 2009-11-18 | 2019-01-29 | G4 Insights Inc. | Method and system for biomass hydrogasification |
US20150240715A1 (en) * | 2013-03-08 | 2015-08-27 | Sulabh K. Dhanuka | Power Generation And Methane Recovery From Methane Hydrates |
US9784182B2 (en) * | 2013-03-08 | 2017-10-10 | Exxonmobil Upstream Research Company | Power generation and methane recovery from methane hydrates |
WO2015017875A1 (en) * | 2013-08-05 | 2015-02-12 | Technische Universität Wien | Method and system for storing energy |
US10283797B2 (en) * | 2013-09-30 | 2019-05-07 | Marek Fulde | Method for storing electric energy by production, storage, and dissociation of methane having closed carbon circuit |
US10208948B2 (en) * | 2014-03-28 | 2019-02-19 | Shanghai Boiler Works Co., Ltd. | Solid fuel grade gasification-combustion dual bed poly-generation system and method thereof |
US10619105B2 (en) | 2014-07-01 | 2020-04-14 | Gas Technology Institute | Hydropyrolysis of biomass-containing feedstocks |
US9937484B2 (en) | 2015-01-30 | 2018-04-10 | Battelle Memorial Institute | Reactor, CO2 sorbent system, and process of making H2 with simultaneous CO2 sorption |
WO2016166413A1 (en) * | 2015-04-17 | 2016-10-20 | Valmet Technologies Oy | Catalytic upgrading of pyrolytic vapors |
RU2710020C2 (en) * | 2015-04-17 | 2019-12-24 | Вальмет Текнолоджиз Ой | Catalytic modification of pyrolytic vapour |
US10711198B2 (en) * | 2015-04-17 | 2020-07-14 | Valmet Technologies Oy | Catalytic upgrading of pyrolytic vapors |
CN107635913A (en) * | 2015-05-28 | 2018-01-26 | 气体技术学院 | The lower adsorbent powerforming hydrogen manufacturing of air calcining |
CN105174679A (en) * | 2015-10-13 | 2015-12-23 | 中国石油化工股份有限公司 | Method for producing hydrogen by performing catalytic gasification on oil-containing sludge |
US20190241434A1 (en) * | 2016-07-14 | 2019-08-08 | Zeg Power As | Method and Device for Upgrading of Biogas and Hydrogen Production From Anaerobic Fermentation of Biological Material |
US10927008B2 (en) * | 2016-07-14 | 2021-02-23 | Zeg Power As | Method and device for upgrading of biogas and hydrogen production from anaerobic fermentation of biological material |
US11223059B2 (en) | 2016-07-14 | 2022-01-11 | Zeg Power As | Method and power plant comprising a solid oxide fuel cell (SOFC) for production of electrical energy and H2 gas |
US10570348B2 (en) * | 2017-01-15 | 2020-02-25 | Wormser Energy Solutions, Inc. | All-steam gasification for supercritical CO2 power cycle system |
US11193073B2 (en) * | 2017-01-15 | 2021-12-07 | Wormser Energy Solutions, Inc. | All-steam gasification for supercritical CO2 cycle system |
US11142702B2 (en) * | 2017-10-13 | 2021-10-12 | Cortus Ab | Process and apparatus for hydrotreatment of pyrolysis oil |
EP4230287A1 (en) * | 2022-02-16 | 2023-08-23 | Eidgenössische Materialprüfungs- und Forschungsanstalt | Sorption-enhanced catalytic reactors with thermal moderators |
WO2023156227A1 (en) | 2022-02-16 | 2023-08-24 | Eidgenössische Materialprüfungs- Und Forschungsanstalt | Sorption-enhanced catalytic reactors with thermal moderators |
Also Published As
Publication number | Publication date |
---|---|
EP2501788A4 (en) | 2013-12-04 |
US10653995B2 (en) | 2020-05-19 |
US20180214815A1 (en) | 2018-08-02 |
WO2011060556A1 (en) | 2011-05-26 |
CA2781204C (en) | 2018-05-01 |
CA2781204A1 (en) | 2011-05-26 |
EP2501788A1 (en) | 2012-09-26 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US10653995B2 (en) | Sorption enhanced methanation of biomass | |
US10190066B2 (en) | Method and system for biomass hydrogasification | |
US9174844B2 (en) | Calcium looping process for high purity hydrogen production integrated with capture of carbon dioxide, sulfur and halides | |
KR101275429B1 (en) | Processes for gasification of a carbonaceous feedstock | |
US9371227B2 (en) | Integration of reforming/water splitting and electrochemical systems for power generation with integrated carbon capture | |
US8038746B2 (en) | Reduced-emission gasification and oxidation of hydrocarbon materials for liquid fuel production | |
US8182771B2 (en) | Method and apparatus for substitute natural gas generation | |
RU2670761C9 (en) | Regulation of acid gas in process of liquid fuel production | |
US20100228062A1 (en) | Process and system for thermochemical conversion of biomass | |
WO2010104732A2 (en) | Controlling the synthesis gas composition of a steam methane reformer | |
CA2738270A1 (en) | Production of hydrocarbon liquids | |
EP2195401A2 (en) | Gasification process | |
CN102965131A (en) | Efficient and clean utilization technology for highly volatile young coal | |
CN110951508A (en) | Device and process for preparing methane by coal chemical-looping catalytic gasification based on calcium oxide | |
CN102712469B (en) | Method for operating an IGCC power plant process having integrated CO2 separation | |
WO2020166659A1 (en) | Method for producing biomass gas, method for producing hydrogen, system for producing biomass gas, and system for producing hydrogen | |
Chen et al. | Challenges of hydrogen production from biomass gasification | |
CN115924845A (en) | Circulating IGCC (integrated gasification combined cycle) for completely capturing carbon dioxide and recovering flue gas water and poly-generation method thereof | |
CA2774898A1 (en) | Method for operating a coke oven arrangement |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
AS | Assignment |
Owner name: G4 INSIGHTS INC., CANADA Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:KEEFER, BOWIE G.;BABICKI, MATTHEW L.;SELLARS, BRIAN G.;AND OTHERS;SIGNING DATES FROM 20120612 TO 20120921;REEL/FRAME:030645/0234 |
|
STCB | Information on status: application discontinuation |
Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION |