WO2015015433A1 - Procede de conversion thermochimique d'une charge carbonee en gaz de synthese contenant majoritairement h2 et co - Google Patents
Procede de conversion thermochimique d'une charge carbonee en gaz de synthese contenant majoritairement h2 et co Download PDFInfo
- Publication number
- WO2015015433A1 WO2015015433A1 PCT/IB2014/063543 IB2014063543W WO2015015433A1 WO 2015015433 A1 WO2015015433 A1 WO 2015015433A1 IB 2014063543 W IB2014063543 W IB 2014063543W WO 2015015433 A1 WO2015015433 A1 WO 2015015433A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- electrolysis
- carbonaceous feedstock
- synthesis gas
- synthesis
- thermochemical conversion
- Prior art date
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
- C25B15/00—Operating or servicing cells
- C25B15/08—Supplying or removing reactants or electrolytes; Regeneration of electrolytes
-
- 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
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
-
- 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
- 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
- C25B3/00—Electrolytic production of organic compounds
- C25B3/20—Processes
- C25B3/25—Reduction
-
- 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
- C25B9/70—Assemblies comprising two or more cells
- C25B9/73—Assemblies comprising two or more cells of the filter-press type
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
- F23L7/00—Supplying non-combustible liquids or gases, other than air, to the fire, e.g. oxygen, steam
- F23L7/007—Supplying oxygen or oxygen-enriched air
-
- 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
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
-
- 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
- Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery
-
- 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
- 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
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or 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
- 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
- Y02P20/141—Feedstock
- Y02P20/145—Feedstock the feedstock being materials of biological origin
Definitions
- the present invention relates to a novel process for the thermochemical conversion of a carbonaceous feedstock to synthesis gas containing predominantly hydrogen (H 2 ) and carbon monoxide (CO), in order to produce liquid fuels (Fischer-Trop Diesel).
- the main application of the invention is that for which the carbonaceous feedstock is biomass.
- carbonaceous filler refers to any combustible material made of carbon-containing compounds.
- biomass ie any inhomogeneous material of vegetable origin containing carbon, such as lignocellulosic biomass, forest or agricultural residues (straw), which can be almost dry or soaked with water as household waste.
- thermochemically converting biomass into liquid fuel by chemical synthesis necessarily include a step gasification of biomass with water vapor to obtain a synthesis gas containing mainly carbon monoxide (CO) and hydrogen (H 2 ).
- the actual gasification stage is carried out continuously from biomass of different types and sizes, usually stored at atmospheric pressure, in a chemical reactor (gasification reactor), either of fluidized bed type or of a flow-driven type. operating under pressure.
- a chemical reactor gasification reactor
- Fluidized bed type reactors are of lesser efficiency because of the reaction temperature generally between 800.deg.C and 1000.deg.C, which leads to a lower conversion of biomass to CO synthesis gas and H 2 with the generation, among others, of methane (CH4) and tars. On the other hand, they have the advantage of only requiring drying and grinding of the average particle size of the biomass without any other specific preparation. Drying and grinding only result in a small loss of efficiency of the overall process. Fluidized bed reactors can be adapted to produce synthetic natural gas ("SNG").
- SNG synthetic natural gas
- BtL Biomass to Liquid
- the heat input of the currently known processes is generally done by the combustion of a part of the biomass itself (raw biomass, gas, solid residues, tars, etc.). These processes are called “autothermic”. In autothermal processes, part of the carbon from the biomass is not converted into liquid fuel.
- the heat input of the process can be done by an external thermal source, preferably of nuclear electrical origin without emission of CO 2 .
- These processes are said to be “allothermic” with the advantage that the mass yield is higher than that of autothermal processes.
- WO 2013/064552 a new process for converting a carbonaceous feedstock into synthesis gas mainly containing hydrogen (H 2 ) and carbon monoxide (CO), the technical and economic evaluations of which have shown the interest with in particular a better energetic and / or mass efficiency than those of the currently known processes and in particular those evaluated economically in the publication [2].
- the method according to this patent application WO 2013/064552 has already considerably improved the energy efficiency of the conversion process compared with known thermochemical conversion processes which implement a gasification of the carbonaceous feedstock.
- the object of the invention is to propose a new process for the thermochemical conversion of a carbonaceous feedstock into synthesis gas mainly containing hydrogen (H 2 ) and carbon monoxide (CO), in order to produce liquid fuels. or other synthetic chemicals, which further improves the best energy efficiency and / or mass compared to the method according to the patent application WO 2013/064552.
- a particular aim is to propose a new process for the thermochemical conversion of a carbonaceous feedstock into synthesis gas which makes it possible to reduce the investment cost compared with the process according to the patent application WO 2013/064552.
- the subject of the invention is a process for converting a carbonaceous feedstock into a synthesis gas mainly containing hydrogen (H 2 ) and carbon monoxide (CO), comprising the following steps: a / oxycombustion of the carbonaceous charge to make a cogeneration of electricity and heat;
- the method further comprises a step c / cleaning and separation of gases, for extracting the hydrogen (H2) and carbon monoxide (CO) produced according to step b /, or if appropriate hydrogen (H2) and carbon monoxide (CO) produced separately according to step b /, so as to extract only CO and H 2 products.
- a step c / cleaning and separation of gases for extracting the hydrogen (H2) and carbon monoxide (CO) produced according to step b /, or if appropriate hydrogen (H2) and carbon monoxide (CO) produced separately according to step b /, so as to extract only CO and H 2 products.
- the carbon dioxide (C0 2 ) separated according to step c / is injected as an input product to the co-electrolysis according to step b1.
- the water (H 2 O) separated from the gas according to step c1 is recycled and injected as an input product of the co-electrolysis according to step b1.
- the carbon monoxide (CO) and the hydrogen (H 2 ) separated according to step c1 are injected as input products of a step d1 according to which a Fischer- Tropsch (FT) to obtain a liquid fuel.
- FT Fischer- Tropsch
- the water (H 2 O) resulting from the Fischer Tropsch FT synthesis according to step d1 is recycled and injected as an input product for the co-electrolysis according to step b1.
- the overhead gas of the synthesis FT according to step d1 is injected as input product of the oxycombustion according to step a1 and / or of the co-electrolysis according to step bl in addition to water and C0 2 .
- the overhead gas of the FT synthesis consists mainly of CH4 methane.
- the heat generated by the FT synthesis according to step d1 may be used preferably for the production of water vapor at the input of the co-electrolysis according to step b1.
- the overhead gas can be used independently, for example injected into a gas turbine or a gas turbine. motor for generating electricity and heat, this electricity and heat being advantageously used in the co-electrolysis step b /.
- the co-electrolysis according to step b / is implemented in accordance with the patent application filed in France on December 17, 2012 under No. 12 62174 in the name of the Applicant.
- step b / is implemented in an electrolysis reactor comprising a stack of elementary electrolysis cells SOEC type each formed of a cathode, an anode and an electrolyte interposed between the cathode and the anode, and a plurality of electrical and fluidic interconnectors each arranged between two adjacent elementary cells with one of its faces in electrical contact with the anode of one of the two elementary cells and the other of its electrically contacting faces with the cathode of the other of the two elementary cells, step b / of co-electrolysis according to which the steam and, if applicable, the overhead gas of the FT synthesis are fed and distributed to the cathode of one of the two adjacent elementary cells and is fed and distributed carbon dioxide or nitrogen dioxide to the cathode of the other of the two elementary cells.
- the co-electrolysis according to step b / is advantageously a co-electrolysis of CO 2 and H 2 O but which is separated in the electrolysis reactor.
- the gases CO and H 2, which are separated, are thus obtained at the outlet of the reactor, thus avoiding the reactions in the gas phase between the CO and the H 2 at the outlet of the electrolyser, the recovery of the oxygen produced being able for its part to be common.
- the composition of the gases leaving the electrolysis reactor can theoretically be 12.66 moles of H 2 and 6 moles of CO, for example for 1 mole of biomass composition ⁇ 6 ⁇ 8; 6 ⁇ 3 , 65, which would make it possible to obtain even better efficiency in synthesis gas and therefore in biofuel.
- the co-electrolysis of step b / is also carried out from the electricity produced according to step a /.
- the efficiency of the process is further increased because there is less electricity external to the process to be supplied.
- the invention as defined makes it possible to retain the advantages of the process according to the patent application WO 2013/064552 while improving its energy efficiency which can be defined as the ratio between the energy content of the product. obtained at the output of the process by the energy introduced into the process (energy contained in the carbonaceous charge, such as biomass + external electrical energy injected).
- the conversion process according to the invention makes it possible to eliminate the reverse water gas reaction (RWGS) step and take advantage of the flexibility of a high-temperature reactor for co-electrolysis to optimize the heat and power flows produced.
- RWGS reverse water gas reaction
- step b1 all the oxygen produced by the co-electrolysis according to step b1 is used as the oxidant of step a / oxycombustion.
- step b1 only a part of the oxygen produced by the co-electrolysis according to step b1 is used as the oxidant of step a / oxycombustion, the other part being recovered.
- the method advantageously applies to a carbonaceous feedstock which is biomass, preferably lignocellulosic biomass with preferably a biomass moisture content of less than 50%.
- Oxycombustion of biomass produces water and C0 2 , this water can be recycled in the process according to the invention and is sufficient in quantity for it.
- the biomass must therefore be sufficiently dry because the water contained in the biomass will be heated unnecessarily and thus reduce the yield of the process. Also, a moisture content of less than 50% is advantageous.
- Figure 1 is a diagram of the principle of an embodiment of the method according to the invention.
- Figure 2 partially replicates the diagram of Figure 1 by incorporating material balances, that is to say the species produced or consumed at each stage of the process;
- FIG. 3 is a diagrammatic sectional view of an electrolysis reactor implementing the simultaneous high temperature co-electrolysis method of water vapor H 2 O and carbon dioxide oxide C0 2, with both separate streams in the process according to the invention
- thermochemical conversion process of the C6H904 lignocellulosic biomass as input consists in carrying out the following steps in combination:
- a / oxycombustion of the biomass preferably at temperatures of the order of 1273 K for heat cogeneration at high temperatures of the order of 1100 K and electricity.
- this step a / oxyfuel combustion is carried out in a fluidized bed type cogeneration reactor.
- co-electrolysis EHT bl co-electrolysis of water and carbon dioxide at high temperatures (EHT), preferably at temperatures close to 1100 K
- co-electrolysis EHT being carried out by providing all the heat and all the electricity produced by the cogeneration according to step a / and all the carbon dioxide (C0 2 ) produced according to step a /.
- the water produced according to the oxy-combustion can be recycled and injected as an input product for the electrolysis according to step b1.
- the product gas is cleaned to essentially recover the CO and ⁇ 2 necessary for Fischer-Tropsch FT synthesis with a separation of the water produced and possibly of C0 2 .
- the produced water may optionally be reinjected into the reactor using the high temperature co-electrolysis step EHT.
- the cleaned CO + H 2 synthesis gas serves as a basic reaction intermediate for the production of synthesis products (liquid fuels (FT diesel, "DME", methanol) or gaseous fuels (“SNG”) , or synthetic chemicals such as methanol for example).
- synthesis products liquid fuels (FT diesel, "DME", methanol) or gaseous fuels (“SNG”)
- SNG gaseous fuels
- synthetic chemicals such as methanol for example
- the produced overhead gas can be recycled and injected as input to the oxy-combustion according to step a / and / or co-electrolysis according to step b /.
- the water produced during the FT synthesis can be recycled and injected at the beginning of the co-electrolysis and the heat released by the synthesis, even at lower temperatures (BT), typically between 200 and 300 ° C. can be used for co-electrolysis according to step b /.
- BT lower temperatures
- the hydrocarbon chains of average formula -CH 2 - produced serve as a liquid fuel which can be usually referred to as a biofuel.
- the inventors have made calculations on the thermochemical conversion process of the biomass according to the invention which has just been described. Specifically, first material balance and energy calculations were made to evaluate the performance of the process.
- FIG. 2 An example of a balance of the species consumed or produced is shown in a block diagram in Figure 2, based on one mole of C6H biomass 8; 603.65 injected at the input of the process.
- step b / the hydrogen H 2 and carbon monoxide CO are produced simultaneously in the co-electrolysis reactor and that they react together to give a corresponding gas mixture. at thermodynamic equilibrium at the temperature of the electrolyser.
- FIG. 2 gives the gas compositions at the outlet of the reactor implementing this simultaneous co-electrolysis with CO 2 and H 2 0 mixed within the reactor.
- thermodynamic equilibrium calculation at 1100K show that with 6 moles of CO 2 (produced from the oxy-fuel combustion of one mole of biomass according to step a /), and of 12, 66 moles of H 2 0 in entry of the co-electrolysis at high temperatures, obtained by the co-electrolysis reaction at the outlet of 11.8 moles of H2 and 5.4 moles of CO, with a molar ratio H 2 / CO close to 2 necessary for the synthesis FT.
- the amounts of H2 and CO obtained with the co-electrolysis according to step b / of the invention are greater than those obtained according to the conversion method comprising a step RWGS as described in the patent application WO 2013/064552.
- the electrical energy to be supplied to the co-electrolysis reactor according to the invention is greater.
- FIG. 3 schematically shows a high-temperature solid-oxide electrolyser (SOEC) which in turn allows co-electrolysis according to step b /, that is to say simultaneous electrolysis of the steam. water and carbon dioxide, each electrolysis taking place simultaneously but separately in one of the elementary electrolysis cells.
- SOEC solid-oxide electrolyser
- the step of high-temperature co-electrolysis of water vapor H 2 O and carbon dioxide C0 2 is carried out by a reactor b / comprising a stack of elementary electrolysis cells of SOEC type. , C1, C2, C3 each formed of a cathode 2.1, 2.2, 2.3, an anode 4.1, 4.2, 4.3 and an electrolyte 3.1, 3.2, 3.3, interposed between the cathode and the anode, and a plurality electrical and fluidic interconnectors 5 each arranged between two adjacent elementary cells with one of its faces in electrical contact with the anode of one of the two elementary cells and the other of its faces in electrical contact with the cathode of the other of the two elementary cells.
- the water vapor at the cathode 2.1, 2.3 of a Cl or C3 of the two cells C1, C2 is fed and distributed; C2, C3 adjacent elementary and is supplied and distributed carbon dioxide to the cathode 2.2 of the other C2 of the two elementary cells C1, C2; C2, C3.
- the hydrogen-producing water vapor is supplied and distributed in cathode compartments separate from those in which carbon dioxide C0 2 is supplied. producing carbon monoxide and recovering all the oxygen produced by the two electrolysis reactions in anode compartments.
- the invention can be used for the conversion of other charges of carbonaceous material (coal, petcoke, etc.).
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Electrochemistry (AREA)
- Materials Engineering (AREA)
- Metallurgy (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Combustion & Propulsion (AREA)
- General Chemical & Material Sciences (AREA)
- Inorganic Chemistry (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
- Hydrogen, Water And Hydrids (AREA)
Abstract
Description
Claims
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP14767132.5A EP3027715B1 (fr) | 2013-08-01 | 2014-07-30 | Procede de conversion thermochimique d'une charge carbonee en gaz de synthese contenant majoritairement h2 et co |
ES14767132.5T ES2648258T3 (es) | 2013-08-01 | 2014-07-30 | Procedimiento de conversión termoquímica de una carga carbonada en gas de síntesis que contiene principalmente H2 y CO |
DK14767132.5T DK3027715T3 (en) | 2013-08-01 | 2014-07-30 | PROCEDURE FOR THERMOCHEMICAL CONVERSION FOR SYNTHESE GAS OF A CARBON-CONTAINED RAW MATERIAL CONTAINING MAINLY H2 AND CO |
BR112016002207A BR112016002207A2 (pt) | 2013-08-01 | 2014-07-30 | método de conversão termoquímica de uma carga carbônica em gás de síntese contendo principalmente hidrogênio (h2) e monóxido de carbono (co) |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR1357631A FR3009308B1 (fr) | 2013-08-01 | 2013-08-01 | Procede de conversion thermochimique d'une charge carbonee en gaz de synthese contenant majoritairement h2 et co. |
FR1357631 | 2013-08-01 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2015015433A1 true WO2015015433A1 (fr) | 2015-02-05 |
Family
ID=49378491
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/IB2014/063543 WO2015015433A1 (fr) | 2013-08-01 | 2014-07-30 | Procede de conversion thermochimique d'une charge carbonee en gaz de synthese contenant majoritairement h2 et co |
Country Status (6)
Country | Link |
---|---|
EP (1) | EP3027715B1 (fr) |
BR (1) | BR112016002207A2 (fr) |
DK (1) | DK3027715T3 (fr) |
ES (1) | ES2648258T3 (fr) |
FR (1) | FR3009308B1 (fr) |
WO (1) | WO2015015433A1 (fr) |
Cited By (9)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2017077090A1 (fr) * | 2015-11-05 | 2017-05-11 | Commissariat A L'energie Atomique Et Aux Energies Alternatives | Procédé et installation pour la conversion chimique d'une matière carbonée avec trempe au gaz de tête |
CN107922863A (zh) * | 2015-07-16 | 2018-04-17 | 前苏伊士环能集团 | 生成合成气的设备和方法 |
WO2019067349A1 (fr) * | 2017-09-29 | 2019-04-04 | Research Triangle Institute | Procédés et appareil pour la production d'hydrogène |
EP3670705A1 (fr) * | 2018-12-21 | 2020-06-24 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Procédé de conversion de dioxyde de carbone |
US11401165B2 (en) | 2016-02-26 | 2022-08-02 | Haldor Topsøe A/S | Carbon monoxide production process optimized by SOEC |
WO2022161823A1 (fr) * | 2021-01-27 | 2022-08-04 | Topsoe A/S | Production de gaz de synthèse à partir de co2 et de vapeur pour la synthèse de combustibles |
FR3126992A1 (fr) * | 2021-09-10 | 2023-03-17 | IFP Energies Nouvelles | Production d'éthanol par oxycombustion, conversion de gaz à l'eau inversée, et fermentation. |
WO2023180856A3 (fr) * | 2022-03-22 | 2024-03-14 | Dioxycle | Renforcement de processus d'évolution de gaz de synthèse à l'aide d'une électrolyse |
US11965260B2 (en) | 2022-03-22 | 2024-04-23 | Dioxycle | Augmenting syngas evolution processes using electrolysis |
Families Citing this family (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FI20185852A1 (fi) * | 2018-10-12 | 2020-04-13 | Ari Piispanen | Menetelmä ja laitteisto hapen talteenottamiseksi ja käyttämiseksi hapen avulla tapahtuvassa poltossa ja menetelmän käyttö |
Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR1262174A (fr) | 1960-06-30 | 1961-05-26 | Silika & Schamotte Fabriken Ma | Plafond suspendu, en particulier voûte pour fours industriels, à blocs maintenus par des fils à ligatures |
US20090235587A1 (en) | 2008-03-24 | 2009-09-24 | Battelle Energy Alliance, Llc | Methods and systems for producing syngas |
US20110041740A1 (en) * | 2009-08-20 | 2011-02-24 | Reilly Timothy J | Recuperative combustion system |
WO2012003849A1 (fr) * | 2010-07-09 | 2012-01-12 | Haldor Topsøe A/S | Procédé de conversion de biogaz en un gaz riche en méthane |
WO2013064552A1 (fr) | 2011-11-04 | 2013-05-10 | Commissariat A L'energie Atomique Et Aux Energies Alternatives | Procede de conversion thermochimique d'une charge carbonee en gaz de synthese contenant majoritairement h2 et co |
-
2013
- 2013-08-01 FR FR1357631A patent/FR3009308B1/fr active Active
-
2014
- 2014-07-30 WO PCT/IB2014/063543 patent/WO2015015433A1/fr active Application Filing
- 2014-07-30 EP EP14767132.5A patent/EP3027715B1/fr active Active
- 2014-07-30 ES ES14767132.5T patent/ES2648258T3/es active Active
- 2014-07-30 BR BR112016002207A patent/BR112016002207A2/pt not_active Application Discontinuation
- 2014-07-30 DK DK14767132.5T patent/DK3027715T3/en active
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR1262174A (fr) | 1960-06-30 | 1961-05-26 | Silika & Schamotte Fabriken Ma | Plafond suspendu, en particulier voûte pour fours industriels, à blocs maintenus par des fils à ligatures |
US20090235587A1 (en) | 2008-03-24 | 2009-09-24 | Battelle Energy Alliance, Llc | Methods and systems for producing syngas |
US20110041740A1 (en) * | 2009-08-20 | 2011-02-24 | Reilly Timothy J | Recuperative combustion system |
WO2012003849A1 (fr) * | 2010-07-09 | 2012-01-12 | Haldor Topsøe A/S | Procédé de conversion de biogaz en un gaz riche en méthane |
WO2013064552A1 (fr) | 2011-11-04 | 2013-05-10 | Commissariat A L'energie Atomique Et Aux Energies Alternatives | Procede de conversion thermochimique d'une charge carbonee en gaz de synthese contenant majoritairement h2 et co |
Non-Patent Citations (4)
Title |
---|
CARL M STOOTS: "High-Temperature Co- Electrolysis of H 2 O and CO 2 for Syngas Production 2006 Fuel Cell Seminar", 1 November 2006 (2006-11-01), XP055096660, Retrieved from the Internet <URL:http://www.inl.gov/technicalpublications/Documents/3562841.pdf> [retrieved on 20140115] * |
GÉRARD ANTONINI: "Technique de l'ingénieur Manuel G2051", article "Traitements thermiques des déchets" |
JEAN-MARIE SEILER; CAROLE HOHWILLER; JULIETTE IMBACH; JEAN-FRANÇOIS LUCIANI: "Technical and economical évaluation of enhanced biomass to liquid fuel processes", ENERGY, vol. 35, 2010, pages 3587 - 3592 |
QINGXI FU ET AL: "Syngas production via high-temperature steam/CO2 co-electrolysis: an economic assessment", ENERGY & ENVIRONMENTAL SCIENCE, vol. 3, no. 10, 1 January 2010 (2010-01-01), pages 1382, XP055028296, ISSN: 1754-5692, DOI: 10.1039/c0ee00092b * |
Cited By (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN107922863A (zh) * | 2015-07-16 | 2018-04-17 | 前苏伊士环能集团 | 生成合成气的设备和方法 |
WO2017077090A1 (fr) * | 2015-11-05 | 2017-05-11 | Commissariat A L'energie Atomique Et Aux Energies Alternatives | Procédé et installation pour la conversion chimique d'une matière carbonée avec trempe au gaz de tête |
FR3043340A1 (fr) * | 2015-11-05 | 2017-05-12 | Commissariat Energie Atomique | Procede et installation pour la conversion chimique d'une matiere carbonee avec trempe au gaz de tete |
US11401165B2 (en) | 2016-02-26 | 2022-08-02 | Haldor Topsøe A/S | Carbon monoxide production process optimized by SOEC |
WO2019067349A1 (fr) * | 2017-09-29 | 2019-04-04 | Research Triangle Institute | Procédés et appareil pour la production d'hydrogène |
US11724938B2 (en) | 2017-09-29 | 2023-08-15 | Research Triangle Institute | Methods for production of hydrogen |
EP3670705A1 (fr) * | 2018-12-21 | 2020-06-24 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Procédé de conversion de dioxyde de carbone |
WO2022161823A1 (fr) * | 2021-01-27 | 2022-08-04 | Topsoe A/S | Production de gaz de synthèse à partir de co2 et de vapeur pour la synthèse de combustibles |
FR3126992A1 (fr) * | 2021-09-10 | 2023-03-17 | IFP Energies Nouvelles | Production d'éthanol par oxycombustion, conversion de gaz à l'eau inversée, et fermentation. |
WO2023180856A3 (fr) * | 2022-03-22 | 2024-03-14 | Dioxycle | Renforcement de processus d'évolution de gaz de synthèse à l'aide d'une électrolyse |
US11965260B2 (en) | 2022-03-22 | 2024-04-23 | Dioxycle | Augmenting syngas evolution processes using electrolysis |
Also Published As
Publication number | Publication date |
---|---|
ES2648258T3 (es) | 2017-12-29 |
FR3009308B1 (fr) | 2015-09-11 |
EP3027715B1 (fr) | 2017-09-06 |
BR112016002207A2 (pt) | 2017-08-01 |
EP3027715A1 (fr) | 2016-06-08 |
FR3009308A1 (fr) | 2015-02-06 |
DK3027715T3 (en) | 2017-12-04 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
EP3027715B1 (fr) | Procede de conversion thermochimique d'une charge carbonee en gaz de synthese contenant majoritairement h2 et co | |
EP2788453B1 (fr) | Procede de conversion thermochimique d'une charge carbonee en gaz de synthese contenant majoritairement h2 et co | |
EP1854761B1 (fr) | Procédé de production d'électricité et d'un gaz riche en hydrogène par vaporéformage d'une coupe hydrocarbure avec apport de calories par combustion à l'hydrogène in situ | |
EP2142622B1 (fr) | Procede de production d'un gaz de synthese purifie a partir de biomasse incluant une etape de purification en amont de l'oxydation partielle | |
EP2166064A1 (fr) | Système pour fournir un produit chimique et procédé pour fournir un produit chimique | |
CA2565936A1 (fr) | Procede de production de gaz de synthese a partir de matiere carbonee et d'energie electrique | |
EP2706103B1 (fr) | Procédé de gazéification de charge de matière carbonée à rendement amélioré | |
FR2989366A1 (fr) | Production de dihydrogene par une transformation de gaz de tete issus d'une synthese | |
EP3060673B1 (fr) | Procede de production d'un produit organique a partir d'une charge de matiere carbonee mettant en oeuvre une gazeification suivie d'une fermentation du gaz de synthese | |
EP2282369B1 (fr) | Dispositif de production d'électricité et de chaleur, incluant une pile à combustible admettant au moins du méthane comme combustible | |
FR2955865A1 (fr) | Procede de recyclage du dioxyde de carbone (co2) | |
EP1474500A1 (fr) | Gazeification de dechets par plasma | |
FR2969998A1 (fr) | Procede de synthese d'hydrocarbones avec rejets de co2 minimum | |
CN111902362A (zh) | 由可再生木质纤维素生物质原料生产纯的且高度浓缩的二氧化碳的方法 | |
EP3031884B1 (fr) | Procédé de gazéification de charge de matière carbonée à rendement matière et coût de production optimisés | |
EP2622086A2 (fr) | Procédé de production de composé oxygéné | |
WO2022013239A1 (fr) | Dispositif et procédé de production hybride de dihydrogène de synthèse et/ou de méthane de synthèse | |
FR2956398A1 (fr) | Procede et dispositif de deshydrogenation catalytique d'hydrocarbures satures en hydrocarbures insatures. |
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: 14767132 Country of ref document: EP Kind code of ref document: A1 |
|
DPE1 | Request for preliminary examination filed after expiration of 19th month from priority date (pct application filed from 20040101) | ||
REEP | Request for entry into the european phase |
Ref document number: 2014767132 Country of ref document: EP |
|
WWE | Wipo information: entry into national phase |
Ref document number: 2014767132 Country of ref document: EP |
|
NENP | Non-entry into the national phase |
Ref country code: DE |
|
REG | Reference to national code |
Ref country code: BR Ref legal event code: B01A Ref document number: 112016002207 Country of ref document: BR |
|
ENP | Entry into the national phase |
Ref document number: 112016002207 Country of ref document: BR Kind code of ref document: A2 Effective date: 20160201 |