WO2018044720A1 - Système et procédé de production de combustibles renouvelables et de produits chimiques - Google Patents

Système et procédé de production de combustibles renouvelables et de produits chimiques Download PDF

Info

Publication number
WO2018044720A1
WO2018044720A1 PCT/US2017/048637 US2017048637W WO2018044720A1 WO 2018044720 A1 WO2018044720 A1 WO 2018044720A1 US 2017048637 W US2017048637 W US 2017048637W WO 2018044720 A1 WO2018044720 A1 WO 2018044720A1
Authority
WO
WIPO (PCT)
Prior art keywords
electrolyzer
fuel
reactor
membrane
renewable
Prior art date
Application number
PCT/US2017/048637
Other languages
English (en)
Inventor
Richard I. Masel
Original Assignee
Dioxide Materials, Inc.
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Priority claimed from US15/400,775 external-priority patent/US9849450B2/en
Application filed by Dioxide Materials, Inc. filed Critical Dioxide Materials, Inc.
Priority to EP17780538.9A priority Critical patent/EP3504359A1/fr
Priority to JP2019511737A priority patent/JP2020500258A/ja
Priority to KR1020197008480A priority patent/KR20190043156A/ko
Priority to CN201780052076.0A priority patent/CN109642332A/zh
Publication of WO2018044720A1 publication Critical patent/WO2018044720A1/fr

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B1/00—Electrolytic production of inorganic compounds or non-metals
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
    • C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
    • C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
    • C07C29/1516—Multisteps
    • C07C29/1518—Multisteps one step being the formation of initial mixture of carbon oxides and hydrogen for synthesis
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
    • C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
    • C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
    • C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
    • C10G3/42—Catalytic treatment
    • C10G3/44—Catalytic treatment characterised by the catalyst used
    • C10G3/48—Catalytic treatment characterised by the catalyst used further characterised by the catalyst support
    • C10G3/49—Catalytic treatment characterised by the catalyst used further characterised by the catalyst support containing crystalline aluminosilicates, e.g. molecular sieves
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B1/00—Electrolytic production of inorganic compounds or non-metals
    • C25B1/01—Products
    • C25B1/02—Hydrogen or oxygen
    • C25B1/04—Hydrogen or oxygen by electrolysis of water
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B13/00—Diaphragms; Spacing elements
    • C25B13/04—Diaphragms; Spacing elements characterised by the material
    • C25B13/08—Diaphragms; Spacing elements characterised by the material based on organic materials
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B15/00—Operating or servicing cells
    • C25B15/02—Process control or regulation
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B15/00—Operating or servicing cells
    • C25B15/08—Supplying or removing reactants or electrolytes; Regeneration of electrolytes
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
    • C25B9/17—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof
    • C25B9/19—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof with diaphragms
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/02—Gasoline
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/04—Diesel oil
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/08—Jet fuel
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/20—C2-C4 olefins
    • 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
    • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/30—Hydrogen technology
    • Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis
    • 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
    • Y02P20/10—Process efficiency
    • Y02P20/133—Renewable energy sources, e.g. sunlight
    • 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
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
    • 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
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/40—Ethylene production

Definitions

  • the present invention relates to a system that can easily be switched from the production of renewable fuels to the production of renewable chemicals, and that uses a CO2 electrolyzer with a special membrane that enables CO2 electrolysis to be accomplished at temperatures up to 120°C.
  • the process will involve the use of carbon dioxide and water electrolyzers to produce a mixture of carbon monoxide and hydrogen that promotes the production of fuels or that promotes the production of chemicals.
  • the process will then use a series of reactors to produce a desired product.
  • the economics associated with the production of renewable fuel are also favorable.
  • the EISA set up a trading system for Renewable Identification Number (RIN) certificates, where one RIN is awarded for each gallon of "ethanol equivalent" fuel produced. If one produces renewable gasoline, then each gallon of gasoline would be awarded 1.56 RINs. "D3" RINs currently sell for about $2.70/gallon. California has a related low carbon fuel certificate (LCFS), by which the producer is awarded one LCFS certificate for each metric ton (MT) of CO 2 that is converted into fuel. A California LCFS certificate currently sell for $70. Calculations indicate that the sales of certificates from a 150 megawatt (MW) electrolyzer-based renewable gasoline plant would generate over $42,000,000 of revenue ($1.63/gal), thereby lowering the net cost of producing gasoline using the present system.
  • MW megawatt
  • MW metric ton
  • Missing at present is a way to take advantage of the growing market for renewable fuels to also produce renewable chemicals.
  • constructing a large plant that can produce either renewable fuels or renewable chemicals In that way, the plant could serve two markets, so the cost of the plant construction could be divided over the two markets.
  • Such a large-scale plant does not exist today, but if it could be built, it would serve the renewable fuel market and would also lower the cost of the renewable chemicals, to help that market develop.
  • the system comprises:
  • the CO2 electrolyzer comprises an anion- conducting polymeric membrane.
  • the anion conducting membrane comprises a terpolymer of styrene, vinylbenzyl-Rs and vinylbenzyl-Rx, where:
  • Rx is at least one constituent selected from the group
  • the total weight of the vinylbenzyl-Rx groups is greater than 0.3% of the total weight of the membrane.
  • the anion conducting membrane comprises a polymer blend or mixture of a copolymer consisting essentially of styrene and vinylbenzyl-Rs with at least one polymeric constituent selected from the group consisting of:
  • a polymer excluding polystyrene, comprising at least one of a phenylene group and a phenyl group
  • Rs is a preferably positively charged cyclic amine group, and the total weight of the at least one polymeric constituent in the membrane is less than the weight of the copolymer in the membrane.
  • [0013 j Rs is preferably tetra-methyl-imidazolium.
  • the fuel produced by the foregoing system can be synthetic gasoline, diesel, jet fuel and/or avgas.
  • the chemicals produced by the foregoing system are preferably alcohols, olefins, or ethers, most preferably ethylene, propylene, or mixtures thereof.
  • the CO 2 electrolyzer runs at temperatures above 25°C, preferably above 35°C, most preferably above 40°C.
  • a suitable membrane for the CO2 electrolyzer satisfies the following test:
  • a cathode is prepared as follows:
  • Silver ink is made as follows. A mixture of 2 mg carbon black (for example, Vulcan XC 72RXC72, from Fuel Cell Earth), 0.2 ml of a 1% solution of the membrane polymer and 0.5 ml ethanol (SigmaAldrich, USA) is sonicated for 5 minutes. 100 mg of silver nanoparticles (for example, 20-40 nm, 45509, Alfa Aesar, Ward Hill, MA) with 1.5 ml ethanol are added and then sonicated for 5 more minutes.
  • carbon black for example, Vulcan XC 72RXC72, from Fuel Cell Earth
  • 0.2 ml of a 1% solution of the membrane polymer and 0.5 ml ethanol (SigmaAldrich, USA) is sonicated for 5 minutes.
  • 100 mg of silver nanoparticles for example, 20-40 nm, 45509, Alfa Aesar, Ward Hill, MA
  • 1.5 ml ethanol are added and then sonicated for 5 more minutes.
  • the silver ink is then hand-painted onto a gas diffusion layer (for example, Sigracet 35 BC GDL, Ion Power Inc., New Castle, DE) covering an area of 5 cm x 5 cm. It is sintered at 80°C for 15 minutes, followed by 120°C for 15 minutes. It is then soaked in a 1 M KOH bath for 1 hour with the painted side face down.
  • a gas diffusion layer for example, Sigracet 35 BC GDL, Ion Power Inc., New Castle, DE
  • IrO 2 ink is made by mixing 100 mg of IrO 2 (Alfa Aesar) with 1 ml deionized water (18.2 Mohm Millipore), 2 ml isopropanol (3032-16, Macron) and 0.101 ml of 5% Nafion solution (1100EW, DuPont, Wilmington, DE).
  • the IrO 2 ink is then hand-painted onto a 5% wet proofed carbon fiber paper (for example, TGP-H-120 5% Teflon Treated Toray Paper, from Fuel Cell Earth) covering an area of 6 cm x 6 cm. Then, the carbon paper is sintered at 80°C for 30 min.
  • a 5% wet proofed carbon fiber paper for example, TGP-H-120 5% Teflon Treated Toray Paper, from Fuel Cell Earth
  • a 50-300 micrometer thick membrane of a "test" material is made by conventional means such as casting or extrusion.
  • the membrane is sandwiched between a 3x3 cm piece of the anode material and a 2.5x2.5 cm piece of the cathode material with the metal layers on the anode and cathode facing the membrane.
  • the membrane electrode assembly is mounted in Fuel Cell Technologies (Albuquerque, NM) 5 cm 2 fuel cell hardware assembly with serpentine flow fields.
  • CO 2 humidified at 65°C is fed into the cathode at a rate of 20 seem and 10 mM KHCO3 is fed into the anode flow field at a flow rate of 3 ml/min.
  • the cell is heated to 50°C, and a power supply is connected.
  • the cell is maintained at 3 V for 2 hours, then is switched to constant current mode at 200 mA/cm 2 .
  • the cell is maintained in constant current mode for at least 100 hours.
  • the series of reactors preferably includes at least 3 reactors.
  • the series of reactors preferably includes a first reactor that converts the CO and H 2 to methanol, then the methanol is converted dimethyl ether in a second reactor, and the dimethyl ether is converted in a third reactor to a synthetic fuel and/or a chemical.
  • the conversion of dimethyl ether to a synthetic fuel and/or a chemical preferably employs a zeolite catalyst such as ZSM-5 or SAPO-34.
  • the zeolite preferably consists of material with an SiO 2 /Al 2 O 3 weight ratio of 2 to 9, a Bmnauer-Emmett-Teller (BET) surface of 250 to 500 m 2 /g, and an Na content under 200 ppm, such as the catalyst described in U.S. Patent No. 9, 174,204.
  • BET Bmnauer-Emmett-Teller
  • a process for the production of renewable fuel in a CO 2 collection unit for extracting CO 2 from a sustainable source :
  • the fuel produced by the foregoing process can be synthetic gasoline and/or diesel, jet fuel and/or avgas (aviation gasoline).
  • the sustainable source of CO 2 can be atmospheric air or CO 2 output from a fermenter, a municipal waste treatment facility, a wood processing unit, or a landfill.
  • the extracted CO 2 in the foregoing process is preferably substantially pure.
  • the H 2 produced in the foregoing process is also preferably substantially pure. More preferably, both the extracted CO 2 and the H 2 produced in the foregoing process are substantially pure.
  • FIG. 1 is a schematic diagram of the present renewable fuel production system.
  • FIG. 2 is a schematic diagram of the present renewable fuel production system configured to produce mainly gasoline.
  • FIG. 3 is a schematic diagram the present renewable fuel production system configured to produce mainly olefins, preferable propylene.
  • FIG. 4 is a schematic diagram of an alternate design of the present renewable fuel production system in which the system produces both gasoline and olefins.
  • the present production system converts air, water, and renewable electricity into renewable fuel and/or chemicals.
  • the system includes the following subsystems:
  • electrochemical conversion of CO 2 refers to any electrochemical process in which carbon dioxide, carbonate, or bicarbonate is converted into another chemical substance in any step of the process.
  • polymer electrolyte membrane refers to both cation exchange membranes, which generally comprise polymers having multiple covalently attached negatively charged groups, and anion exchange membranes, which generally comprise polymers having multiple covalently attached positively charged groups.
  • Typical cation exchange membranes include proton conducting membranes, such as the per fluoro sulfonic acid polymer available under the trade designation NAFION from E. I. du Pont de Nemours and Company (DuPont) of Wilmington, DE.
  • anion exchange membrane electrolyzer refers to an electrolyzer with an anion-conducting polymer electrolyte membrane separating the anode from the cathode.
  • liquid free cathode refers to an electrolyzer where there are no bulk liquids in direct contact with the cathode during electrolysis. There can be a thin liquid film on or in the cathode, however, and occasional washes or rehydration of the cathode with liquids could occur.
  • radar efficiency refers to the fraction of the electrons applied to the cell that participate in reactions producing carbon- containing products.
  • ME A refers to a membrane electrode assembly
  • GC gas chromatograph
  • imidazolium refers to a positively charged ligand containing an imidazole group. This includes a bare imidazole or a substituted imidazole.
  • Ri- R 5 are each independently selected from hydrogen, halides, linear alkyls, branched alkyls, cyclic alkyls, heteroalkyls, aryls, heteroaryls, alkylaryls, heteroalkylaryls, and polymers thereof, such as the vinyl benzyl copolymers described herein, are specifically included.
  • pyridinium refers to a positively charged ligand containing a pyridine group. This includes a bare pyridine or a
  • R 6 -Rii are each independently selected from hydrogen, halides, linear alkyls, branched alkyls, cyclic alkyls, heteroalkyls, aryls, heteroaryls, alkylaryls, heteroalkylaryls, and polymers thereof, such as the vinyl benzyl copolymers described herein, are specifically included.
  • phosphonium refers to a positively charged ligand containing phosphorous. This includes substituted phosphorous.
  • positively charged cyclic amine refers to a positively charged ligand containing a cyclic amine. This specifically includes imidazoliums, pyridiniums, pyrazoliums, pyrrolidiniums, pyrroliums,
  • PSTMIM Solution refers to a solution prepared as described in Specific Example 3 herein.
  • sustainable source refers to a source of CO 2 other than a CO 2 well or other natural CO2 source. Sustainable sources specifically include CO2 captured from the air, CO2 from a fermenter, CO2 from a municipal waste facility and CO2 from a landfill.
  • FIG. 1 is a schematic flow diagram of the present renewable fuel production system 100.
  • System 100 includes electrolyzers 111 and 112, reactors 102, 103, 104, 105 and 106, separator 107, compressor 108, valves 169, 170, 171, 172, 173, 174, 175, 176, 177, 178 and 179, controller 150, and mix point 133. As further shown in FIG.
  • system 100 also includes a source of renewable CO2 131, a source of water 132, a source of bio-methanol 152, a combined CO and CO2 stream 161 exiting electrolyzer 111 and directed to mix point 133, an H2 stream 162 exiting electrolyzer 112 and directed to mix point 133, an O2 outlet stream 163 exiting electrolyzer 112, and an O2 outlet stream 164 exiting electrolyzer 111.
  • a methanol stream 181 exits reactor 102 and is directed to the inlet stream of reactor 103.
  • a dimethyl ether stream 182 exits reactor 103 and is directed to the inlet stream of reactor 104.
  • a combined gasoline, propylene and tar stream 183 exits reactor 104 and is directed to the inlet stream of reactor 105 and/or to the inlet stream of separator 107.
  • the streams exiting separator 107 include propylene exit stream 135, gasoline exit stream 136, a combined H2, CO and CO2 stream 184 and an H2O stream 185.
  • a renewable energy source 161 powers electrolyzer 111.
  • a renewable energy source 162 powers electrolyzer 112.
  • Electrolyzer 111 converts CO 2 to CO via the reaction CO 2 -» CO + 1 ⁇ 2 O2.
  • a preferred design is set forth in Example 1 of co-owned U.S. Patent No. 9,481,939.
  • Electrolyzer 112 converts H 2 O to H 2 via the reaction H 2 O ⁇ H 2 + 1 ⁇ 2 O 2 .
  • a preferred design is set forth in co-owned U.S. patent application Serial No. 15/406,909.
  • Controller 150 adjusts the ratio of CO, H 2 , CO 2 and H 2 O.
  • Mix point 133 is designed to mix the output streams from the CO 2 and water electrolyzers.
  • Reactor 102 converts mixtures of CO, CO 2 and H 2 to methanol.
  • Reactor 102 preferably contains a Cu/ZnO catalyst such as MK-151 FENCETM from Haldor-Topsoe (Linyi, Denmark).
  • Reactor 103 converts methanol to dimethyl ether.
  • Reactor 103 preferable contains a ⁇ - ⁇ 1 2 ⁇ 3 catalyst such as BASF G-250 catalyst.
  • Reactor 104 converts dimethyl ether to either olefins, such as propylene, or into gasoline.
  • Reactor 104 preferably contains a zeolite catalyst such as ZSM-5 or SAPO-34.
  • the zeolite consists of material with an SiO 2 /Al 2 O 3 weight ratio of 2 to 9, a BET surface of 250 to 500 m 2 /g, and an Na content under 200 ppm, such as the catalyst described in U.S. Patent No. 9,174,204.
  • Reactor 105 hydrogenates durene and other tar molecules.
  • Reactor 105 preferably contains a nickel on alumina catalyst such as Criterion KL6515, or a cobalt molybdate on alumina catalyst, such as Alfa Aesar 45579.
  • Reactor 106 converts the C 5 + molecules (molecules containing 5 or more carbons) back to CO, H 2 and light olefins via reaction with steam.
  • Reactor 106 preferably contains either a ZSM-5 catalyst or a nickel on alumina catalyst.
  • FIG. 2 illustrates operation of renewable fuel production system 100 to produce mainly fuels such as gasoline.
  • valves 173, 174, 175, 176 and 178 are closed, as depicted by the circle-and-backlash symbol (($>) over eacn of those valves, and reactor 106 is shut down or placed into a regeneration cycle.
  • the tar is hydrogenated in reactor 105 before the separation step, and olefins produced are recycled back to reactor 104 to produce more gasoline.
  • FIG. 3 shows how the device will be operated to produce mainly olefins such as propylene.
  • valves 169, 170, 172, 177 and 179 are closed, as depicted by the circle-and-backlash symbol ( ⁇ 5 ) over each of those valves, and reactor 105 is shut down or placed into a regeneration cycle.
  • the controller 201 adjusts the CO, CO 2 to H 2 to promote gasoline production.
  • the tar and gasoline is sent to reactor 106 and the gasoline, tar and other hydrocarbons are cracked to produce light olefins, CO, CO 2 and H 2 .
  • renewable fuel production system and process described herein is carbon negative and provides energy-efficient generation of energy-dense liquid fuels or chemicals from renewable energy, water and air.
  • FIG. 4 shows an alternate system embodiment 200 in which both propylene and gasoline are produced.
  • the design is simplified to omit reactor 106 in system 100 shown in FIG. 1.
  • System 200 includes electrolyzers 211 and 212, reactors 202, 203, 204 and 205, separator 207, compressor 208, controller 250, and mix point 233. As further shown in FIG.
  • system 200 also includes a source of renewable CO 2 231, a source of water 232, a combined CO and CO2 stream 261 exiting electrolyzer 211 and directed to mix point 233, an H 2 stream 262 exiting electrolyzer 212 and directed to mix point 233, an H 2 stream 287 exiting electrolyzer 212 and directed to reactor 205, an O 2 outlet stream 263 exiting electrolyzer 212, and an O 2 outlet stream 264 exiting electrolyzer 211.
  • a methanol stream 281 exits reactor 202 and is directed to the inlet stream of reactor 203.
  • a dimethyl ether stream 282 exits reactor 203 and is directed to the inlet stream of reactor 204.
  • a combined gasoline, propylene and tar stream 283 exits reactor 204 and is directed to the inlet stream of separator 207.
  • the streams exiting separator 207 include propylene exit stream 235, a combined gasoline and tar exit stream 236, a combined H 2 , CO and CO 2 stream 284 and an H 2 O stream 285.
  • a gasoline stream 289 exists reactor 205.
  • a renewable energy source 261 powers electrolyzer 211.
  • a renewable energy source 262 powers electrolyzer 212.
  • Electrolyzer 211 converts CO 2 to CO via the reaction CO 2 -» CO + 1 ⁇ 2 O 2 .
  • a preferred design is set forth in Example 1 of co-owned U.S. Patent No. 9,481,939.
  • Electrolyzer 212 converts H 2 O to H 2 via the reaction H 2 O— » H 2 + 1 ⁇ 2 O 2 .
  • a preferred design is set forth in co-owned U.S. patent application Serial No. 15/406,909.
  • Controller 250 adjusts the ratio of CO, H 2 , CO 2 and H 2 O.
  • Mix point 233 is designed to mix the output streams from the CO 2 and water electrolyzers.
  • Reactor 202 converts mixtures of CO, CO 2 and H 2 to methanol.
  • Reactor 202 preferably contains a Cu/ZnO catalyst such as MK-151 FENCETM from Haldor-Topsoe (Lyngby, Denmark).
  • Reactor 203 converts methanol to dimethyl ether.
  • Reactor 203 preferable contains a ⁇ - ⁇ 1 2 ⁇ 3 catalyst such as BASF G-250 catalyst.
  • Reactor 204 converts dimethyl ether to either olefins, such as propylene, or into gasoline.
  • Reactor 104 preferably contains a zeolite catalyst such as ZSM-5 or SAPO-34. Most preferably, the zeolite consists of material with an SiO 2 /Al 2 O 3 weight ratio of 2 to 9, a BET surface of 250 to 500 m 2 /g, and an Na content under 200 ppm, such as the catalyst described in U.S. Patent No. 9,174,204.
  • Reactor 205 hydrogenates durene and other tar molecules.
  • Reactor 205 preferably contains a nickel on alumina catalyst such as Criterion KL6515, or a cobalt molybdate on alumina catalyst, such as Alfa Aesar 45579.
  • the objective of this example is to demonstrate that a terpolymer of styrene, vinylbenzyl-Rs and vinylbenzyl-Rx, has significant advantages as a membrane for the CO 2 electrolyzer, where
  • Rx is at least one constituent selected from the group consisting of CI, OH and a reaction product between an OH or CI and a species other than a simple amine or a cyclic amine, and
  • the total weight of the vinylbenzyl-Rx groups is greater than 0.3% of the total weight of the membrane.
  • a terpolymer membrane is prepared as described in specific Example 17 in co-owned U.S. patent application Serial No. 15/400,775 as described below.
  • Step 1 Production of PSTMIM solution,
  • Inhibitor-free styrene was prepared by adding a volume V of styrene (Sigma- Aldrich, Saint Louis, MO) and a volume equal to V/4 of 4% aqueous sodium hydroxide into a separatory funnel, followed by agitating the funnel to mix the water and styrene, then decanting the styrene layer. The process was repeated five times until the water layer did not show discernible color change. The procedure was repeated using pure water instead of sodium hydroxide solution until the water layer pH was neutral.
  • Washed styrene was put into a freezer overnight before weighing, to confirm that residual water was mainly in ice form and was then separated from styrene by filtration or decantation.
  • 4- vinylbenzyl chloride (4-VBC) was treated in the same manner as styrene.
  • the membranes were prepared by casting the polymer solutions prepared above directly onto a polyethylene terephthalate (PET) liner.
  • the thickness of the solution on the liner was controlled by a film applicator (MTI Corporation, Richmond, CA) with an adjustable doctor blade.
  • the membranes were then dried in a vacuum oven with temperature increased to 70°C and held for 1 hour. After one more hour in the vacuum oven with temperature slowly decreased, the membrane was taken out of the oven and put into a 1 M KOH solution overnight, during which time the membrane fell from the liner.
  • the KOH solution was changed twice, each with a few hours of immersion, to make sure the membrane chloride ions were substantially completely exchanged, so that the membranes were substantially fully converted into the hydroxide form.
  • a cathode material was prepared as follows. Silver ink was made as follows. A mixture of 2 mg of carbon black (Vulcan XC 72RXC72, Fuel Cell Earth), 0.2 ml of a 1% solution of the membrane polymer and 0.5 ml ethanol (SigmaAldrich, USA) was sonicated for 5 minutes. 100 mg of silver
  • nanoparticles (20-40 nm, 45509, Alfa Aesar, Ward Hill, MA) with 1.5 ml ethanol were added and then sonicated for 5 more minutes.
  • the silver ink was then hand-painted onto a gas diffusion layer (Sigracet 35 BC GDL, Ion Power Inc., New Castle, DE) covering an area of 5 cm x 5 cm. It was sintered at 80°C for 15 min followed by 120°C for 15 min. It was then soaked in a 1 M KOH bath for 1 hour with the painted side face down.
  • An anode material was prepared as follows. IrO 2 ink was made by mixing 100 mg of IrO 2 (Alfa Aesar) with 1 ml deionized water (18.2 Mohm Millipore), 2 ml isopropanol (3032-16, Macron) and 0.101 ml of 5% NAFION solution (1100EW, DuPont, Wilmington, DE). The IrO 2 ink was then hand- painted onto a 5% wet proofed carbon fiber paper (TGP-H-120 5% Teflon Treated Toray Paper, Fuel Cell Earth) covering an area of 6 cm x 6 cm. The ink covered carbon fiber paper was then sintered at 80°C for 30 minutes.
  • IrO 2 ink was made by mixing 100 mg of IrO 2 (Alfa Aesar) with 1 ml deionized water (18.2 Mohm Millipore), 2 ml isopropanol (3032-16, Cell) and 0.101 ml of 5% NAFION
  • the membrane was sandwiched between the a 3x3 cm piece of the anode material and a 2.5x2.5 cm piece of the cathode material with the metal layers on the anode and cathode facing the membrane, and the entire assembly was mounted in a Fuel Cell Technologies 5 cm 2 fuel cell hardware assembly with serpentine flow fields.
  • CO 2 humidified at 25 °C was fed into the cathode flow field at a rate of 20 seem, and 10 mM KHCO3 was fed into the anode flow field at a flow rate of 3 ml/min.
  • the cell was connected to a power supply and the cell was run at a fixed voltage of 3 V for 2 hours, then switched to constant current mode at 200 mA/cm 2 for 250 hours. The cell was stable for 250 hours.
  • the selectivity was over 90%, as shown in FIG. 5 in the '775 application.
  • a second membrane was prepared as above and mounted in a cell as above.
  • CO2 humidified at 65 °C was fed into the cell at a rate of 30 seem, and 10 mM KHCO3 was fed into the anode flow field at a flow rate of 3 ml/min.
  • the cell was heated to 50°C, and the power supply was connected. Again, the cell was maintained at 3 V for 2 hours, and then switched to a constant current mode at 600 mA/cm 2 .
  • the cell was stable for 250 hours at 600 mA/cm 2 with a CO selectivity over 97%.
  • a third membrane was prepared as above and mounted in a cell as above.
  • CO2 humidified at 65 °C was fed into the cell at a rate of 30 seem, and 10 mM KHCO3 was fed into the anode flow field at a flow rate of 3 ml/min.
  • the cell was heated to 50°C, and the power supply was connected. Again, the cell was maintained at 3 V and the current was measured. Subsequently the temperature was raised to 60°C, 70°C, and 80°C for 2 hours each, and the current was measured. Table 1 summarizes these results. Table 1. Cell current density, measured as a function of temperature
  • the objective of this example is to demonstrate that a membrane comprising a polymer blend or mixture of a copolymer consisting essentially of styrene and vinylbenzyl-R s with at least one polymeric constituent selected from the group consisting of:
  • a polymer excluding polystyrene, comprising at least one of a phenylene group and a phenyl group
  • R s is a positively charged cyclic amine group, and wherein the total weight of the at least one polymeric constituent in the membrane is less than the weight of the copolymer in the membrane, as described in co-owned U.S. Patent No. 9,580,824.
  • Step 1 A PSTMIM solution was prepared as described in Specific Example 3.
  • Step 2 The PSTMIM solution was diluted to 20% solids with ethanol.
  • Step 3 A BKY (Geretsried, Germany) Automatic Film Applicator L was used to cast a thin film of the polymer solution onto a polypropylene backing sheet (Home Depot, Atlanta, GA) using a doctor blade. The solution was allowed to dry in ambient environment for 30 minutes to yield an
  • Step 4 a 10 ⁇ thick porous expanded polytetrafluoroethylene (ePTFE) film (Philips Scientific Inc., Rock Hill, SC) was submerged for 30 minutes in a bath of ethanol to activate its surface for better wettability. The porous ePTFE film was then laid carefully taut over the deposited polymer film. The ePTFE film was also stretched in both x and y directions to fully open its pore structure as it was laid over the polymer film.)
  • ePTFE expanded polytetrafluoroethylene
  • Step 5 A 15 ⁇ layer of the PSTMIM polymer solution was deposited on top of the ePTFE. The polymer film was left to settle for 15 minutes in ambient conditions before the whole reinforced membrane was placed in an oven at 65°C for 60 minutes to improve adhesion of the polymer with the ePTFE. After the heating step, the membrane was then separated from the polypropylene backing sheet with the help of a razor blade and tweezers, and then activated in 1 M KOH, as described in Specific Example 3.
  • Numerical value ranges recited herein include all values from the lower value to the upper value in increments of one unit, provided that there is a separation of at least two units between a lower value and a higher value.
  • concentration of a component or value of a process variable such as, for example, size, angle, pressure, time and the like, is, for example, from 1 to 98, specifically from 20 to 80, more specifically from 30 to 70, it is intended that values such as 15 to 85, 22 to 68, 43 to 51, 30 to 32, and the like, are expressly enumerated in this specification.
  • one unit is considered to be 0.0001, 0.001, 0.01 or 0.1 as appropriate.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Electrochemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Automation & Control Theory (AREA)
  • Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
  • Catalysts (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Electrodes For Compound Or Non-Metal Manufacture (AREA)

Abstract

La présente invention concerne un système de production de combustible renouvelable comprenant une unité de capture de dioxyde de carbone pour extraire le dioxyde de carbone de l'air atmosphérique, un électrolyseur de dioxyde de carbone pour convertir le dioxyde de carbone en monoxyde de carbone, un électrolyseur d'eau pour convertir l'eau en hydrogène, un générateur de combustibles de synthèse pour convertir le monoxyde de carbone produit par l'électrolyseur de dioxyde de carbone et l'hydrogène produit par l'électrolyseur d'eau en un combustible. Le carburant produit peut être de l'essence synthétique et/ou du diesel synthétique. Le système est également apte à produire simultanément ou en variante un produit chimique industriel distinct.
PCT/US2017/048637 2016-08-29 2017-08-25 Système et procédé de production de combustibles renouvelables et de produits chimiques WO2018044720A1 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
EP17780538.9A EP3504359A1 (fr) 2016-08-29 2017-08-25 Système et procédé de production de combustibles renouvelables et de produits chimiques
JP2019511737A JP2020500258A (ja) 2016-08-29 2017-08-25 再生可能燃料および化学品を製造するための装置および方法
KR1020197008480A KR20190043156A (ko) 2016-08-29 2017-08-25 재생가능한 연료 및 화학물질의 생산을 위한 시스템 및 방법
CN201780052076.0A CN109642332A (zh) 2016-08-29 2017-08-25 用于生产可再生燃料和化学品的系统和方法

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
US201662380917P 2016-08-29 2016-08-29
US62/380,917 2016-08-29
US15/400,775 2017-01-06
US15/400,775 US9849450B2 (en) 2010-07-04 2017-01-06 Ion-conducting membranes

Publications (1)

Publication Number Publication Date
WO2018044720A1 true WO2018044720A1 (fr) 2018-03-08

Family

ID=60022149

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US2017/048637 WO2018044720A1 (fr) 2016-08-29 2017-08-25 Système et procédé de production de combustibles renouvelables et de produits chimiques

Country Status (5)

Country Link
EP (1) EP3504359A1 (fr)
JP (1) JP2020500258A (fr)
KR (1) KR20190043156A (fr)
CN (1) CN109642332A (fr)
WO (1) WO2018044720A1 (fr)

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2018136798A1 (fr) * 2017-01-20 2018-07-26 Dioxide Materials, Inc. Procédé de fabrication d'une membrane échangeuse d'anions
WO2020002920A1 (fr) * 2018-06-27 2020-01-02 Oxford University Innovation Limited Production d'hydrogène
US10774431B2 (en) 2014-10-21 2020-09-15 Dioxide Materials, Inc. Ion-conducting membranes
EP3722462A1 (fr) * 2019-04-08 2020-10-14 Siemens Aktiengesellschaft Installation et procédé d'accumulation d'énergie électrique
DE102019127037A1 (de) * 2019-10-08 2021-04-08 Forschungszentrum Jülich GmbH Herstellung von Kohlenmonoxid
WO2021089183A1 (fr) * 2019-11-05 2021-05-14 Linde Gmbh Procédé et installation de production de monoéthylène glycol
WO2021220667A1 (fr) * 2020-05-01 2021-11-04 株式会社Ihi Système d'électrolyse et procédé d'électrolyse
CN114307908A (zh) * 2022-01-19 2022-04-12 华中科技大学 二氧化碳多场协同催化加氢合成液体燃料的装置与方法
EP4060090A1 (fr) * 2021-03-18 2022-09-21 Kabushiki Kaisha Toshiba Système de fabrication de composé de carbone et procédé de commande de système de fabrication de composé de carbone
WO2024035474A1 (fr) * 2022-08-12 2024-02-15 Twelve Benefit Corporation Production d'acide acétique

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20230302403A1 (en) * 2020-05-14 2023-09-28 Nitto Denko Corporation Carbon-dioxide capture and treatment system and carbon-dioxide negative emissions plant
CN113174603A (zh) * 2021-04-28 2021-07-27 河钢集团有限公司 用于捕获并电解co2的组合物以及方法
JP2023011306A (ja) * 2021-07-12 2023-01-24 東洋エンジニアリング株式会社 合成燃料の製造方法
JP2023011307A (ja) * 2021-07-12 2023-01-24 東洋エンジニアリング株式会社 合成燃料の製造方法

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20070045125A1 (en) * 2005-08-25 2007-03-01 Hartvigsen Joseph J Electrochemical Cell for Production of Synthesis Gas Using Atmospheric Air and Water
US20080039538A1 (en) * 2006-08-10 2008-02-14 Olah George A Method for producing methanol, dimethyl ether, derived synthetic hydrocarbons and their products from carbon dioxide and water (moisture) of the air as sole source material
US20120116137A1 (en) * 2010-11-09 2012-05-10 Primus Green Energy Inc. Single loop multistage fuel production
US9174204B2 (en) 2010-01-26 2015-11-03 Sud-Chemie Ip Gmbh & Co. Kg Catalyst based on zeolite for producing olefins and for oligomerizing olefins
WO2016039999A1 (fr) * 2014-09-08 2016-03-17 3M Innovative Properties Company Membrane polymère ionique pour un électrolyseur de dioxyde de carbone
WO2016064447A1 (fr) * 2014-10-21 2016-04-28 Dioxide Materials, Inc. Électrolyseur et membranes
US9481939B2 (en) 2010-07-04 2016-11-01 Dioxide Materials, Inc. Electrochemical device for converting carbon dioxide to a reaction product

Family Cites Families (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3894102A (en) * 1973-08-09 1975-07-08 Mobil Oil Corp Conversion of synthesis gas to gasoline
JPS63128097A (ja) * 1986-11-18 1988-05-31 Res Assoc Petroleum Alternat Dev<Rapad> 合成ガスの芳香族炭化水素への転化方法
JP4371601B2 (ja) * 2001-04-11 2009-11-25 株式会社トクヤマ バイポーラ膜
EP2167706B1 (fr) * 2007-07-13 2017-11-15 University of Southern California Electrolyse du dioxyde de carbone dans un milieu aqueux en monoxyde de carbone et hydrogene pour une production de methanol
US20110237830A1 (en) * 2010-03-26 2011-09-29 Dioxide Materials Inc Novel catalyst mixtures
FR2971789B1 (fr) * 2011-02-22 2013-02-22 Areva Methode de production de methanol ou d'hydrocarbures a partir d'une matiere carbonee, avec une etape de reformage dont les conditions de fontionnement sont ajustees selectivement
WO2012137344A1 (fr) * 2011-04-08 2012-10-11 トヨタ自動車株式会社 Dispositif pour générer un gaz mixte
US20130105304A1 (en) * 2012-07-26 2013-05-02 Liquid Light, Inc. System and High Surface Area Electrodes for the Electrochemical Reduction of Carbon Dioxide
KR20150056635A (ko) * 2012-09-19 2015-05-26 리퀴드 라이트 인코포레이티드 할라이드 염을 이용하는 화학물질의 전기화학적 공동-제조
WO2015094687A1 (fr) * 2013-12-20 2015-06-25 Exxonmobil Research And Engineering Company Catalyseur lié pour la conversion sélective d'oxygénats en aromatiques

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20070045125A1 (en) * 2005-08-25 2007-03-01 Hartvigsen Joseph J Electrochemical Cell for Production of Synthesis Gas Using Atmospheric Air and Water
US20080039538A1 (en) * 2006-08-10 2008-02-14 Olah George A Method for producing methanol, dimethyl ether, derived synthetic hydrocarbons and their products from carbon dioxide and water (moisture) of the air as sole source material
US9174204B2 (en) 2010-01-26 2015-11-03 Sud-Chemie Ip Gmbh & Co. Kg Catalyst based on zeolite for producing olefins and for oligomerizing olefins
US9481939B2 (en) 2010-07-04 2016-11-01 Dioxide Materials, Inc. Electrochemical device for converting carbon dioxide to a reaction product
US9580824B2 (en) 2010-07-04 2017-02-28 Dioxide Materials, Inc. Ion-conducting membranes
US20120116137A1 (en) * 2010-11-09 2012-05-10 Primus Green Energy Inc. Single loop multistage fuel production
WO2016039999A1 (fr) * 2014-09-08 2016-03-17 3M Innovative Properties Company Membrane polymère ionique pour un électrolyseur de dioxyde de carbone
WO2016064447A1 (fr) * 2014-10-21 2016-04-28 Dioxide Materials, Inc. Électrolyseur et membranes

Cited By (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10774431B2 (en) 2014-10-21 2020-09-15 Dioxide Materials, Inc. Ion-conducting membranes
WO2018136798A1 (fr) * 2017-01-20 2018-07-26 Dioxide Materials, Inc. Procédé de fabrication d'une membrane échangeuse d'anions
AU2018210399B2 (en) * 2017-01-20 2019-08-29 3M Innovative Properties Company Method of making an anion exchange membrane
WO2020002920A1 (fr) * 2018-06-27 2020-01-02 Oxford University Innovation Limited Production d'hydrogène
US11959181B2 (en) 2018-06-27 2024-04-16 Oxford University Innovation Limited Hydrogen production
EP3722462A1 (fr) * 2019-04-08 2020-10-14 Siemens Aktiengesellschaft Installation et procédé d'accumulation d'énergie électrique
DE102019127037A1 (de) * 2019-10-08 2021-04-08 Forschungszentrum Jülich GmbH Herstellung von Kohlenmonoxid
WO2021089183A1 (fr) * 2019-11-05 2021-05-14 Linde Gmbh Procédé et installation de production de monoéthylène glycol
JPWO2021220667A1 (fr) * 2020-05-01 2021-11-04
AU2021261991B2 (en) * 2020-05-01 2023-12-07 Ihi Corporation Electrolysis system and electrolysis method
WO2021220667A1 (fr) * 2020-05-01 2021-11-04 株式会社Ihi Système d'électrolyse et procédé d'électrolyse
JP7501616B2 (ja) 2020-05-01 2024-06-18 株式会社Ihi 電解システム及び電解方法
EP4060090A1 (fr) * 2021-03-18 2022-09-21 Kabushiki Kaisha Toshiba Système de fabrication de composé de carbone et procédé de commande de système de fabrication de composé de carbone
US11701631B2 (en) 2021-03-18 2023-07-18 Kabushiki Kaisha Toshiba Carbon compound manufacturing system and method of controlling carbon compound manufacturing system
CN114307908A (zh) * 2022-01-19 2022-04-12 华中科技大学 二氧化碳多场协同催化加氢合成液体燃料的装置与方法
CN114307908B (zh) * 2022-01-19 2023-03-28 华中科技大学 一种二氧化碳催化加氢合成c8+航空燃油的方法
WO2024035474A1 (fr) * 2022-08-12 2024-02-15 Twelve Benefit Corporation Production d'acide acétique
US11939284B2 (en) 2022-08-12 2024-03-26 Twelve Benefit Corporation Acetic acid production

Also Published As

Publication number Publication date
JP2020500258A (ja) 2020-01-09
KR20190043156A (ko) 2019-04-25
EP3504359A1 (fr) 2019-07-03
CN109642332A (zh) 2019-04-16

Similar Documents

Publication Publication Date Title
US10280378B2 (en) System and process for the production of renewable fuels and chemicals
WO2018044720A1 (fr) Système et procédé de production de combustibles renouvelables et de produits chimiques
Ogungbemi et al. Fuel cell membranes–Pros and cons
Lees et al. Gas diffusion electrodes and membranes for CO2 reduction electrolysers
Ma et al. An overview of flow cell architecture design and optimization for electrochemical CO 2 reduction
Merino‐Garcia et al. Productivity and selectivity of gas‐phase CO2 electroreduction to methane at copper nanoparticle‐based electrodes
Chen et al. High-performance bipolar membrane development for improved water dissociation
Varcoe et al. Anion-exchange membranes in electrochemical energy systems
Albert et al. Radiation-grafted polymer electrolyte membranes for water electrolysis cells: evaluation of key membrane properties
EP3453065A1 (fr) Réacteur à architecture avancée pour la réaction électrochimique du co2, du co et d&#39;autres composés chimiques
JP7475072B2 (ja) 水素の製造のための装置
US20200063273A1 (en) System And Process For The Production Of Renewable Fuels And Chemicals
Cermenek et al. Alkaline direct ethanol fuel cell
AU2018369463A1 (en) Ethylene-selective electrode with a mixed valence Cu4O3 catalyst
Im et al. Research and development trend of electrolyte membrane applicable to water electrolysis system
CN114481158A (zh) 一种高温碱性电解水制氢系统及其方法
CN114622234A (zh) 一种柔性气体扩散电极结构及其在二氧化碳电化学还原中的应用
Qiu et al. Recent developments in ion conductive membranes for CO2 electrochemical reduction
Xu et al. Review on electrochemical carbon dioxide capture and transformation with bipolar membranes
Yu et al. Preparation and research progress of anion exchange membranes
AU2013217231B2 (en) Method and apparatus for producing gas
Al-Dhubhani et al. Combined Electrospinning–Electrospraying for High-Performance Bipolar Membranes with Incorporated MCM-41 as Water Dissociation Catalysts
Saada et al. Is Direct Seawater Splitting Realistic with Conventional Electrolyzer Technologies?
Kulkarni et al. ACS Spotlight: Bipolar Membranes for Electrochemical Energy Conversion, Chemical Manufacturing, and Separations
Wang et al. Applications of Anion Exchange Membranes Excluding Fuel Cells

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 17780538

Country of ref document: EP

Kind code of ref document: A1

ENP Entry into the national phase

Ref document number: 2019511737

Country of ref document: JP

Kind code of ref document: A

NENP Non-entry into the national phase

Ref country code: DE

ENP Entry into the national phase

Ref document number: 20197008480

Country of ref document: KR

Kind code of ref document: A

ENP Entry into the national phase

Ref document number: 2017780538

Country of ref document: EP

Effective date: 20190329