EP4048651A1 - Dispositif et procédé pour valoriser des gaz de dégagement provenant d'une installation p2x - Google Patents

Dispositif et procédé pour valoriser des gaz de dégagement provenant d'une installation p2x

Info

Publication number
EP4048651A1
EP4048651A1 EP20838920.5A EP20838920A EP4048651A1 EP 4048651 A1 EP4048651 A1 EP 4048651A1 EP 20838920 A EP20838920 A EP 20838920A EP 4048651 A1 EP4048651 A1 EP 4048651A1
Authority
EP
European Patent Office
Prior art keywords
hydrogen
oxy
oxygen
carbon dioxide
power
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.)
Pending
Application number
EP20838920.5A
Other languages
German (de)
English (en)
Inventor
Frank Hannemann
Joachim Lamp
Gerhard Zimmermann
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Siemens Energy Global GmbH and Co KG
Original Assignee
Siemens Energy Global GmbH and Co KG
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
Application filed by Siemens Energy Global GmbH and Co KG filed Critical Siemens Energy Global GmbH and Co KG
Publication of EP4048651A1 publication Critical patent/EP4048651A1/fr
Pending legal-status Critical Current

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    • 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
    • C25B15/081—Supplying products to non-electrochemical reactors that are combined with the electrochemical cell, e.g. Sabatier reactor
    • 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
    • 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
    • C01B3/506—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification at low temperatures
    • 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
    • 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
    • C25B15/00—Operating or servicing cells
    • C25B15/08—Supplying or removing reactants or electrolytes; Regeneration of electrolytes
    • C25B15/083—Separating products
    • 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
    • C25B15/085—Removing impurities
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/44—Details; Accessories
    • F23G5/46—Recuperation of heat
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
    • F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
    • F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
    • F23G7/061—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases with supplementary heating
    • F23G7/063—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases with supplementary heating electric heating
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
    • F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
    • F23G7/061—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases with supplementary heating
    • F23G7/065—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases with supplementary heating using gaseous or liquid fuel
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23N—REGULATING OR CONTROLLING COMBUSTION
    • F23N5/00—Systems for controlling combustion
    • F23N5/003—Systems for controlling combustion using detectors sensitive to combustion gas properties
    • F23N5/006—Systems for controlling combustion using detectors sensitive to combustion gas properties the detector being sensitive to oxygen
    • 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
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/046—Purification by cryogenic separation
    • 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
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/0495—Composition of the impurity the impurity being water
    • 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
    • C01B2203/061—Methanol production
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2204/00—Supplementary heating arrangements
    • F23G2204/20—Supplementary heating arrangements using electric energy
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2206/00—Waste heat recuperation
    • F23G2206/20—Waste heat recuperation using the heat in association with another installation
    • F23G2206/203—Waste heat recuperation using the heat in association with another installation with a power/heat generating installation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2209/00—Specific waste
    • F23G2209/14—Gaseous waste or fumes
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2209/00—Specific waste
    • F23G2209/26—Biowaste
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
    • 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
    • F23L2900/00—Special arrangements for supplying or treating air or oxidant for combustion; Injecting inert gas, water or steam into the combustion chamber
    • F23L2900/07005—Injecting pure oxygen or oxygen enriched air
    • 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
    • F23L2900/00—Special arrangements for supplying or treating air or oxidant for combustion; Injecting inert gas, water or steam into the combustion chamber
    • F23L2900/07006—Control of the oxygen supply
    • 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
    • Y02E20/12—Heat utilisation in combustion or incineration of waste
    • 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
    • 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

Definitions

  • the invention relates to a device and a method for utilizing off-gases that arise in a Power-to-X system.
  • a Power-to-X system is, for example, the production of carbon-based substances such as methanol or hydrocarbons.
  • Power-to-X refers to different ways of using or storing electrical energy, for example from renewable energy (e.g. sun, wind and water power).
  • Part of these technologies are the power-to-liquid / power-to-gas processes, which can be an essential element for decarbonising or defossilising the transport and energy sectors and are also used for energy storage.
  • fossil fuels can in future be partially or completely replaced by electricity-based e-fuels.
  • Such carbon-based e-fuels are produced through the synthesis of hydrogen and carbon dioxide.
  • Hydrogen is produced by electrolysis using renewable electrical energy.
  • the carbon dioxide can come from point sources, or be obtained by separation by means of chemical or physical washes, or from the air by means of adsorption processes.
  • An example of such e-fuels is e-methanol, which can then be used, for example, directly or via admixtures for internal combustion engines.
  • methanol is the starting material for many chemicals and can also be used to produce synthetic gasoline (e-gasoline).
  • the raw material of conventional methanol production processes from fossil raw materials is synthesis gas, a mixture of predominantly hydrogen and carbon monoxide.
  • a Power-to-X system for converting regenerative energy into e-fuel essentially comprises an electrolyser for generating hydrogen H 2 and oxygen O 2 , a system for processing the hydrogen including drying the hydrogen H 2 generated, and a compressor for compression of the hydrogen H 2 , and a chemical reactor for the synthesis of, for example, methanol.
  • the synthesis taking place in tubular reactors cannot be carried out completely in one step. Therefore, the unreacted product stream is returned to the chemical reactor.
  • So-called off-gas flows have to be discharged continuously or discontinuously from the process in order to avoid a concentration of non-condensable gases.
  • Essential components of these off-gas flows are hydrogen H 2 , carbon dioxide CO 2 , carbon monoxide CO, methane CH 4 , methanol CH 3 OH. Further off-gases arise during the preparation of the raw methanol during the distillation to separate water and methanol.
  • the object of the invention is to provide a Power-to-X system by means of which the off-gases can be used economically and an emission of carbon dioxide CO 2 can be avoided.
  • Another object of the invention is to provide a corresponding method for operating such a Power-to-X system for utilizing off-gases.
  • the object of the invention aimed at a device is achieved by a power-to-X system for the use of off gases according to the features of claim 1.
  • This comprises an electrolyzer for generating hydrogen H 2 and oxygen O 2 , one Plant connected to the electrolyser for processing the hydrogen, for separating the remaining oxygen O 2 and water H 2 O from the generated stream of hydrogen H 2 , at least one compressor for compressing the hydrogen H 2 , or the mixture of hydrogen H 2 and carbon dioxide CO 2 , and a chemical reactor for generating a synthesis gas from hydrogen H 2 and feedable carbon dioxide CO 2 .
  • an oxy-fuel combustion system in which non-condensable off-gases from the chemical reactor and oxygen O 2 from the electrolyser can be supplied, and one through the combustion of the off-gases in the oxy-fuel system resulting carbon dioxide CO 2 via a return line into the flow of hydrogen H 2 after which the electrolyser can be returned.
  • the invention is based on the consideration that the off-gases, which inevitably arise during the synthesis in the chemical reactor, are treated thermally in an oxy-fuel incinerator connected downstream of the chemical reactor.
  • the oxy-fuel incinerator is suitable for oxygen-based combustion.
  • the thermal treatment he follows with almost pure oxygen O 2 as the oxidizer.
  • the invention recognizes that the oxygen is inevitably produced in the upstream electrolysis anyway, and otherwise usually cannot be further used economically in any case.
  • This oxygen fraction can contain small traces of hydrogen is not disadvantageous either, since the hydrogen H 2 burns to form pure water.
  • the exhaust gas from the oxygen-based combustion consists almost entirely of water vapor and carbon dioxide CO 2 .
  • the carbon dioxide CO 2 can be extracted in a very pure form and fed back into the production process.
  • the off-gas can advantageously be fed back into the Power-to-X process and does not have to be burned using an air-blown torch.
  • oxygen O 2 from the electrolysis oxygen O 2 from a separate oxygen source can also be used, which means that the device according to the invention can also be integrated into existing systems in which oxygen O 2 occurs as a process gas.
  • climate-damaging CCh emissions can be avoided.
  • the invention can also save energy for an air blower, since no nitrogen N 2 has to be compressed.
  • the Power-to-X system also includes a heat exchanger, through which the heat generated during combustion can be dissipated and can be integrated into other parts of the Power-to-X system.
  • the heat can in particular be integrated into the raw methanol preparation or into the auxiliary steam generation for starting up the chemical reactor.
  • the raw methanol contains water as a reaction product.
  • the methanol / water mixture is separated by distillation.
  • the overall efficiency of the system can be increased by integrating the heat generated in the oxy-fuel combustion system into other parts of the Power-to-X system. This also results in additional opportunities to increase flexibility, since the heat too Can be used to keep components warm in the event of a brief system downtime.
  • the oxy-fuel combustion system can alternatively or additionally be supplied with biomass and / or processed waste for CO 2 -neutral combustion and / or that the oxy-fuel combustion system includes a heating device through which it can be used Electricity from renewable sources can be heated electrically. Other combustible substances can also be burned in the oxy fuel incinerator.
  • the Power-to-X system can also be advantageously integrated into a waste incineration plant, sewage treatment plant or biomass plant or in corresponding processes.
  • off-gas or other residual gases from the Power-to-X system can also be burned.
  • the Power-to-X system preferably comprises a withdrawal flow line through which recirculated synthesis gas from the chemical reactor can be fed to the oxy-fuel combustion system.
  • a withdrawal flow line through which recirculated synthesis gas from the chemical reactor can be fed to the oxy-fuel combustion system.
  • a lambda probe is arranged in the exhaust line of the oxy-fuel combustion system, so that complete combustion of the off and mixed gases to form CO 2 is ensured by measuring and regulating the amount of oxygen O 2 introduced.
  • the oxygen content O 2 in the exhaust gas is measured, and the flow of the oxygen quantity O 2 introduced is then regulated.
  • the regulation avoids in particular a relevant O 2 excess in the exhaust gas, which could lead to problems with regard to the purity of the C0 2 stream generated.
  • the oxygen O 2 remaining in the separated C0 2 stream can be removed by a catalytic reaction with hydrogen H 2 .
  • the compression of the fh / CCd synthesis gas takes place with a piston compressor to operating pressures above 10 bar. Due to the selected operating pressure of the piston compressor, subsequent drying (condensation of H 2 O) and Cd separation (DeOxoDryer) can be carried out cost-effectively. Due to the higher inlet pressure and the proportion of carbon dioxide CO 2 , the compressor can alternatively also be designed as a turbo compressor.
  • the hydrogen flow from the electrolysis contains water vapor and small amounts of oxygen. The oxygen is catalytically reacted with hydrogen to form water, which is then separated off as a whole by condensation.
  • the power-to-X system further comprises a return line for carbon dioxide CO 2 , through which the carbon dioxide CO 2 from the oxy-fuel combustion system can be fed into the line for hydrogen H 2 upstream of the compressor.
  • the return line is connected to the line for hydrogen H 2 between the electrolyzer and the compressor.
  • the Power-to-X system also includes a separation device for impurities, which is connected to the oxy-fuel combustion system, and in which impurities such as sulfur and alkali generated in the oxy-fuel process - and halogen compounds as well as oxygen O 2 are separable.
  • a separation device for impurities which is connected to the oxy-fuel combustion system, and in which impurities such as sulfur and alkali generated in the oxy-fuel process - and halogen compounds as well as oxygen O 2 are separable.
  • the oxygen O 2 can be separated cryogenically.
  • the purified carbon dioxide CO 2 can be fed to the flow of hydrogen H 2 upstream of the compressor via a return line.
  • This severing device is particularly advantageous because the carbon dioxide CO 2 generated in the oxi-fuel process is contaminated with sulfur, alkali and halogen compounds and contains larger amounts of oxygen O 2 , which must be separated off before being mixed with hydrogen H 2.
  • the object of the invention which is directed to a method, is achieved by a method for utilizing off-gases in a power-to-X system according to claim 9.
  • hydrogen H 2 and oxygen O 2 are generated by an electrolyzer, from the hydrogen H 2 remaining water H 2 O and oxygen O 2 are separated in a system for processing the hydrogen, the hydrogen H 2 in at least one compressor to compress the hydrogen H 2 , or the mixture of hydrogen H 2 and carbon dioxide CO 2 , compressed and generated in a chemical reactor alcohols or hydrocarbons.
  • the non-condensable off-gases from the chemical reactor are fed together with oxygen O 2 from the electrolyzer to an oxy-fuel incinerator, and a carbon dioxide CO 2 produced by the combustion of the off-gases is added to the flow of hydrogen H 2 returned to the electrolyser.
  • the oxy fuel combustion system also includes a heat exchanger, through which the heat generated during combustion is dissipated and integrated into other parts of the Power-to-X system.
  • the heat can in particular be transferred to the raw methanol preparation and / or to the auxiliary steam generation for starting the chemical reactor.
  • biomass and / or processed waste is alternatively or additionally used in the oxy-fuel incineration plant for C0 2 -neutral incineration. burned.
  • the oxy-fuel combustion system furthermore comprises a heating device, by means of which it is electrically heated with electricity from renewable sources.
  • off-gas or the residual gases from the Power-to-X system can also be fed to the oxy fuel combustion system.
  • synthesis gas from the chemical reactor is fed to the oxy-fuel incineration plant via an extraction flow line as part of an advantageous further development.
  • the oxygen concentration of the oxy-fuel combustion system is measured by a lambda probe in the exhaust pipe and, by regulating the amount of oxygen O 2 introduced, complete combustion of the mixed gases to form CO 2 is guaranteed.
  • the compressor is a piston compressor which is operated at a pressure of over 10 bar, and the system for processing the hydrogen H 2 is a DeOxoDryer.
  • the carbon dioxide CO 2 from the oxy fuel combustion system is fed through a return line for carbon dioxide CO 2 into the line for hydrogen H 2 upstream of the compressor.
  • the impurities such as sulfur, alkali and halogen compounds and oxygen O 2 generated in the oxy-fuel process are separated in a separation device for impurities, with the oxygen O 2 in particular being separated kyrogenically, and that Purified carbon dioxide CO 2 is fed into the stream of hydrogen H 2 via a return line upstream of the compressor.
  • FIG. 1 shows a power-to-X system according to the prior art.
  • FIG. 2 shows a Power-to-X system according to a first embodiment of the invention.
  • FIG. 3 shows a Power-to-X system according to a further embodiment of the invention.
  • FIG. 1 shows a Power-to-X system 1 according to the prior art. This essentially consists of an electrolyzer 2, a system for processing hydrogen 3, a compressor 4, and a chemical reactor 5 for the synthesis of methanol.
  • the electrolyser 2 is supplied with regenerative electrical energy 18, which comes for example from a wind turbine or photovoltaic system.
  • water 19 is supplied to the electrolyzer 2.
  • Hydrogen fh and oxygen O2 are produced in the electrolyser.
  • the oxygen O2 is released into the atmosphere and the hydrogen H2 is passed into the processing plant 3 for drying.
  • the plant for the preparation of the hydrogen 3 is withdrawn from the hydrogen H2 and discharged.
  • the hydrogen H2 dried in the system 3 is discharged from the system 3 and mixed with carbon dioxide CO2, which is fed to the power-to-X system from the outside.
  • the hydrogen / carbon dioxide CCh mixture is also referred to as synthesis gas 22.
  • the synthesis gas 22 is then fed to the compressor 4, in which it is compressed.
  • the compressed synthesis gas 22 is then passed into the chemical reactor 5, where it is the starting material for the synthesis of methanol.
  • the conversion of synthesis gas 22 to methanol takes place in tubular reactors and is not complete in one step.
  • the chemical reactor 5 after connected is a gas-liquid separation system 20 in which the partially converted product (methanol and water) is withdrawn.
  • the incompletely converted partial stream 21 is returned to the chemical reactor 5 and thus circulated.
  • these off-gases 8 are supplied to a combustion system 23, and with the supply of air 24 ver burns. This creates an exhaust gas 25, which mainly contains Koh lendioxid CO 2 , water H 2 O and nitrogen N2, and is released into the atmosphere.
  • FIG. 2 shows a Power-to-X system according to a first embodiment of the invention.
  • the oxygen O2 generated in the electrolyser 2 is not or not completely released into the atmosphere, but is diverted for use in the further process.
  • another compressor 26 is provided, which is arranged in front of the system for processing the hydrogen 3 what.
  • the central difference to the prior art is an oxy-fuel combustion system 7, which the oxygen O2 from the electrolyzer 2 and the off-gas 8 from the chemical reactor 5 are supplied to.
  • the off-gases 8 are also used thermally, but with almost pure oxygen O2 as the oxidizer, which was taken from the electrolyzer 2 as a by-product.
  • the exhaust gas from oxygen-based combustion consists almost entirely of water vapor and carbon dioxide CO2. By means of a comparatively simple condensation of the water vapor, the carbon dioxide CO2 can be obtained in a very pure form and returned to the production process.
  • the exhaust gas consisting of almost pure carbon dioxide CO2 is returned via a return line 9 to the flow of hydrogen H2 after the electrolyzer 2.
  • a withdrawal flow line 12 is also seen, through which synthesis gas from the chemical reactor 5 of the oxy-fuel combustion system 7 can be supplied.
  • a lambda probe 14 can be arranged in the return line 9 of the oxy-fuel combustion system 7, so that a complete combustion of the off-gases is achieved by measuring and regulating the amount of oxygen O2 introduced to CO2 is guaranteed, but without supplying oxygen in excess.
  • the compressor 4 can be designed as a piston compressor which is designed for operating pressures above 10 bar.
  • the system for processing the hydrogen 3 can be an OxyDryer.
  • Figure 3 shows an alternative embodiment of the invention.
  • the main difference to the embodiment in FIG. 2 is the oxy-fuel combustion system 7, an oxy-fuel boiler to which, alternatively or additionally, biomass and / or processed waste 27 is fed.
  • a heating device can be installed in the oxy-fuel combustion system 7.
  • device 11 are provided, which is electrically heated with electricity from renewable sources.
  • a heat exchanger 10 is provided, which is connected downstream of the oxy fuel combustion system 7. Through the heat exchanger 10, the heat generated during the combustion can be dissipated and can be integrated into other parts of the Power-to-X system 1. The heat can preferably be transferred to the raw methanol processing and / or to the auxiliary steam generation for starting the chemical reactor 5.
  • a return line for carbon dioxide CO215 is connected to the oxy-fuel combustion system 7 in FIG. 3, through which line the carbon dioxide CO2 can be discharged from the oxy-fuel combustion system.
  • a separation device for impurities 16 is connected in the return line 15, which removes impurities generated in the oxy fuel process, such as sulfur, alkali and halogen compounds and larger amounts of oxygen. In particular, the oxygen O2 is separated cryogenically.
  • the stream of largely pure carbon dioxide CO2, which has been purified by the separation device 16, is fed via a return line 17 to the stream of hydrogen H2 upstream of the compressor 4.
  • the invention makes it possible to use the off-gases produced in a Power-to-X system for the process instead of having to release them into the atmosphere. This makes it possible to reduce the C0 2 emissions of the entire system while simultaneously using the carbon dioxide CO2 in the actual process and the oxygen O2 from the electrolyser. Compared to conventional off-gas combustion, this also saves energy for the air blower.

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  • Mechanical Engineering (AREA)
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  • Electrochemistry (AREA)
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Abstract

L'invention concerne une installation P2X (1) destinée à utiliser des gaz de dégagement qui comprend un électrolyseur (2) destiné à produire de l'hydrogène H2 et de l'oxygène O2, une installation raccordée à l'électrolyseur (2) et destinée à préparer l'hydrogène H2 (3), pour séparer l'eau résiduelle H2O et l'oxygène O2 du flux d'hydrogène H2 produit, un compresseur (4) raccordé à l'installation de préparation d'hydrogène H2 (3) qui est destiné à comprimer l'hydrogène H2, et un réacteur (5) chimique raccordé au compresseur (4) et destiné à produire un gaz de synthèse (6) à partir de l'hydrogène H2 et de dioxyde de carbone CO2 pouvant être acheminé. L'invention concerne également une installation de combustion oxygaz (7) jusqu'à laquelle peuvent être acheminés des gaz de dégagement (8) non condensables provenant du réacteur (5) chimique et de l'oxygène O2 provenant de l'électrolyseur (2), et un dioxyde de carbone CO2 formé suite à la combustion des gaz de dégagement (8) dans l'installation de combustion oxygaz (7) peut être renvoyé dans le courant d'hydrogène H2 en aval de l'électrolyseur (2) par l'intermédiaire d'une conduite de retour (9).
EP20838920.5A 2019-12-20 2020-12-15 Dispositif et procédé pour valoriser des gaz de dégagement provenant d'une installation p2x Pending EP4048651A1 (fr)

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DE102019220361 2019-12-20
PCT/EP2020/086200 WO2021122584A1 (fr) 2019-12-20 2020-12-15 Dispositif et procédé pour valoriser des gaz de dégagement provenant d'une installation p2x

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US20230183083A1 (en) * 2021-12-14 2023-06-15 Saudi Arabian Oil Company Ammonia production from carbon- and water-derived hydrogen
JP2024135916A (ja) * 2023-03-23 2024-10-04 東芝エネルギーシステムズ株式会社 二酸化炭素変換装置

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