WO2022193349A1 - 一种基于可再生能源电解水和碳捕技术的联合制氢系统 - Google Patents

一种基于可再生能源电解水和碳捕技术的联合制氢系统 Download PDF

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WO2022193349A1
WO2022193349A1 PCT/CN2021/082892 CN2021082892W WO2022193349A1 WO 2022193349 A1 WO2022193349 A1 WO 2022193349A1 CN 2021082892 W CN2021082892 W CN 2021082892W WO 2022193349 A1 WO2022193349 A1 WO 2022193349A1
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hydrogen production
production system
hydrogen
oxygen
water electrolysis
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PCT/CN2021/082892
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English (en)
French (fr)
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廖勇
刘清友
王国荣
吴秋伟
刘武
董立臣
丁涛
李俊荣
胡强
李汶颖
张琳东
王均
陈石义
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成都精智艺科技有限责任公司
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Publication of WO2022193349A1 publication Critical patent/WO2022193349A1/zh

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    • H—ELECTRICITY
    • H02—GENERATION; CONVERSION OR DISTRIBUTION OF ELECTRIC POWER
    • H02J—CIRCUIT ARRANGEMENTS OR SYSTEMS FOR SUPPLYING OR DISTRIBUTING ELECTRIC POWER; SYSTEMS FOR STORING ELECTRIC ENERGY
    • H02J15/00—Systems for storing electric energy
    • H02J15/008—Systems for storing electric energy using hydrogen as energy vector
    • 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
    • H—ELECTRICITY
    • H02—GENERATION; CONVERSION OR DISTRIBUTION OF ELECTRIC POWER
    • H02J—CIRCUIT ARRANGEMENTS OR SYSTEMS FOR SUPPLYING OR DISTRIBUTING ELECTRIC POWER; SYSTEMS FOR STORING ELECTRIC ENERGY
    • H02J3/00—Circuit arrangements for ac mains or ac distribution networks
    • H02J3/28—Arrangements for balancing of the load in a network by storage of energy
    • H—ELECTRICITY
    • H02—GENERATION; CONVERSION OR DISTRIBUTION OF ELECTRIC POWER
    • H02J—CIRCUIT ARRANGEMENTS OR SYSTEMS FOR SUPPLYING OR DISTRIBUTING ELECTRIC POWER; SYSTEMS FOR STORING ELECTRIC ENERGY
    • H02J3/00—Circuit arrangements for ac mains or ac distribution networks
    • H02J3/28—Arrangements for balancing of the load in a network by storage of energy
    • H02J3/32—Arrangements for balancing of the load in a network by storage of energy using batteries with converting means
    • H—ELECTRICITY
    • H02—GENERATION; CONVERSION OR DISTRIBUTION OF ELECTRIC POWER
    • H02J—CIRCUIT ARRANGEMENTS OR SYSTEMS FOR SUPPLYING OR DISTRIBUTING ELECTRIC POWER; SYSTEMS FOR STORING ELECTRIC ENERGY
    • H02J3/00—Circuit arrangements for ac mains or ac distribution networks
    • H02J3/38—Arrangements for parallely feeding a single network by two or more generators, converters or transformers
    • H02J3/381—Dispersed generators
    • H—ELECTRICITY
    • H02—GENERATION; CONVERSION OR DISTRIBUTION OF ELECTRIC POWER
    • H02J—CIRCUIT ARRANGEMENTS OR SYSTEMS FOR SUPPLYING OR DISTRIBUTING ELECTRIC POWER; SYSTEMS FOR STORING ELECTRIC ENERGY
    • H02J7/00—Circuit arrangements for charging or depolarising batteries or for supplying loads from batteries
    • H02J7/34—Parallel operation in networks using both storage and other dc sources, e.g. providing buffering
    • H02J7/345—Parallel operation in networks using both storage and other dc sources, e.g. providing buffering using capacitors as storage or buffering devices
    • H—ELECTRICITY
    • H02—GENERATION; CONVERSION OR DISTRIBUTION OF ELECTRIC POWER
    • H02J—CIRCUIT ARRANGEMENTS OR SYSTEMS FOR SUPPLYING OR DISTRIBUTING ELECTRIC POWER; SYSTEMS FOR STORING ELECTRIC ENERGY
    • H02J2207/00—Indexing scheme relating to details of circuit arrangements for charging or depolarising batteries or for supplying loads from batteries
    • H02J2207/50—Charging of capacitors, supercapacitors, ultra-capacitors or double layer capacitors
    • H—ELECTRICITY
    • H02—GENERATION; CONVERSION OR DISTRIBUTION OF ELECTRIC POWER
    • H02J—CIRCUIT ARRANGEMENTS OR SYSTEMS FOR SUPPLYING OR DISTRIBUTING ELECTRIC POWER; SYSTEMS FOR STORING ELECTRIC ENERGY
    • H02J2300/00—Systems for supplying or distributing electric power characterised by decentralized, dispersed, or local generation
    • H02J2300/20—The dispersed energy generation being of renewable origin
    • H02J2300/22—The renewable source being solar energy
    • H02J2300/24—The renewable source being solar energy of photovoltaic origin
    • H—ELECTRICITY
    • H02—GENERATION; CONVERSION OR DISTRIBUTION OF ELECTRIC POWER
    • H02J—CIRCUIT ARRANGEMENTS OR SYSTEMS FOR SUPPLYING OR DISTRIBUTING ELECTRIC POWER; SYSTEMS FOR STORING ELECTRIC ENERGY
    • H02J2300/00—Systems for supplying or distributing electric power characterised by decentralized, dispersed, or local generation
    • H02J2300/20—The dispersed energy generation being of renewable origin
    • H02J2300/28—The renewable source being wind energy
    • H—ELECTRICITY
    • H02—GENERATION; CONVERSION OR DISTRIBUTION OF ELECTRIC POWER
    • H02J—CIRCUIT ARRANGEMENTS OR SYSTEMS FOR SUPPLYING OR DISTRIBUTING ELECTRIC POWER; SYSTEMS FOR STORING ELECTRIC ENERGY
    • H02J2300/00—Systems for supplying or distributing electric power characterised by decentralized, dispersed, or local generation
    • H02J2300/40—Systems for supplying or distributing electric power characterised by decentralized, dispersed, or local generation wherein a plurality of decentralised, dispersed or local energy generation technologies are operated simultaneously
    • 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
    • Y02P80/00—Climate change mitigation technologies for sector-wide applications
    • Y02P80/20—Climate change mitigation technologies for sector-wide applications using renewable energy
    • 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
    • Y02P90/00—Enabling technologies with a potential contribution to greenhouse gas [GHG] emissions mitigation
    • Y02P90/50—Energy storage in industry with an added climate change mitigation effect

Definitions

  • the invention relates to the technical field of new energy, in particular to a technology that integrates photovoltaics, wind power, hydrogen energy, oxygen-enriched combustion, carbon capture and other new energy technologies, and finally realizes multi-energy complementation, supply coupling, and renewable energy for green production.
  • An energy system for supplying clean hydrogen under the capture and recovery of hydrogen and carbon dioxide proposes an implementable technical solution for a high-efficiency green hydrogen production plant to achieve carbon neutrality goals.
  • Photovoltaic power generation is a technology that directly converts light energy into electrical energy by utilizing the photovoltaic effect of the semiconductor interface. It is mainly composed of solar panels (components), controllers and inverters, and the main components are composed of electronic components. After the solar cells are connected in series, they can be packaged and protected to form a large-area solar cell module, and then combined with power controllers and other components to form a photovoltaic power generation device.
  • Wind power generation converts the kinetic energy of the wind into mechanical kinetic energy, and then converts the mechanical energy into electrical kinetic energy.
  • the principle of wind power generation is to use the wind to drive the blades of the windmill to rotate, and then increase the speed of rotation through the speed increaser to promote the generator to generate electricity. According to current windmill technology, it is about three meters per second (the degree of breeze) to start generating electricity.
  • the process of hydrogen production by electrolysis of water is actually an energy conversion process, that is, the process of converting primary energy into energy carrier hydrogen energy.
  • two types of water electrolysis hydrogen production technologies can be practically applied under low temperature conditions, namely alkaline liquid water electrolysis and solid polymer (PEM) water electrolysis.
  • Alkaline liquid water electrolysis technology uses KOH and NaOH aqueous solution as electrolyte, such as using asbestos cloth as diaphragm, under the action of direct current, the water is electrolyzed to generate hydrogen and oxygen.
  • the produced gas needs to be treated with a dealkalizing mist.
  • PEM water electrolysis technology The main components of a typical PEM water electrolysis technology include cathode and anode gas diffusion layers, cathode and anode catalytic layers, and proton exchange membranes.
  • PEM technology hydrogen ions in water pass through the proton exchange membrane and combine with electrons to form hydrogen atoms, which combine with each other to form hydrogen molecules.
  • PEM proton exchange membrane generally uses perfluorosulfonic acid membrane, which can isolate the gas generated by the cathode and anode, prevent the transfer of electrons, and transfer protons at the same time.
  • the proton exchange membrane replaces the asbestos membrane to isolate the gas on both sides of the electrode, and avoids the shortcomings caused by the use of strong alkaline liquid electrolytes in alkaline liquid electrolyte electrolyzers.
  • the PEM water electrolysis cell adopts a zero-gap structure, and the volume of the electrolytic cell is more compact and streamlined, which reduces the ohmic resistance of the electrolytic cell and greatly improves the overall performance of the electrolytic cell.
  • Hydrocarbon steam reforming hydrogen production process is a chemical process that has been widely used in my country.
  • raw materials suitable for the conversion of hydrocarbons to hydrogen including natural gas, liquefied petroleum gas, various refinery gases, synthesis gas, straight-run naphtha, raffinate oil, topping oil and secondary processing oil.
  • hydrogen production from natural gas with the lightest molecular weight and the smallest carbon-hydrogen ratio is the best.
  • the patent description mainly takes natural gas as an example: the production of hydrogen from natural gas consists of two parts: natural gas steam reforming to transform gas and pressure swing adsorption (PSA) purification of hydrogen (H 2 ).
  • PSA pressure swing adsorption
  • the natural gas is converted into hydrogen (H 2 ), carbon monoxide ( CO ) and carbon dioxide (CO 2 ). It becomes a shift gas, and then the shift gas or shift gas is passed through a pressure swing adsorption (PSA) process to obtain high-purity hydrogen (H 2 ).
  • PSA pressure swing adsorption
  • CCUS technology is a key solution for reducing emissions in the energy industry and plays an important role in advancing the low-carbon transition of the energy system and achieving global climate goals.
  • carbon capture methods are mainly divided into three major researches: post-combustion capture, pre-combustion capture and oxy-combustion carbon capture systems. direction.
  • Oxygen-enriched combustion capture technology is an in-combustion capture technology. Different from the traditional combustion technology that directly uses air to support combustion, oxygen-enriched combustion uses very high-purity oxygen to support combustion, and CO2 generated by combustion is used to replace N2 in the air for repeated use. O 2 /CO 2 ratio to suit different combustion requirements.
  • Oxygen-enriched combustion exhaust gas is rich in high-concentration CO 2 , which facilitates subsequent implementation of low-cost carbon dioxide capture.
  • Microgrid is a concept relative to the traditional large power grid. It refers to a network composed of multiple distributed power sources and their related loads according to a certain topology structure, and is related to the conventional power grid through static switches.
  • the development and extension of microgrid can fully promote the large-scale access of distributed power and renewable energy, and achieve highly reliable supply of various energy forms to loads. Smart grid transition.
  • DC microgrid and AC microgrid are typical microgrid modes, and the main difference between the two is whether direct current or alternating current is used as the energy transmission carrier.
  • the threshold for low-carbon hydrogen is 14.51kgCO2e/kgH2
  • the threshold for clean hydrogen and renewable hydrogen is 14.51kgCO2e/kgH2.
  • the threshold is 4.9kgCO2e/kgH2
  • the renewable hydrogen also requires the hydrogen production energy to be renewable energy.
  • the present invention proposes a combined hydrogen production system based on renewable energy water electrolysis and carbon capture technology, aiming to realize renewable energy
  • the production of clean hydrogen and renewable energy hydrogen in combination with CCUS technology meets the social needs of carbon neutrality in the future and has broad application prospects.
  • the technical scheme adopted by the present invention to solve the technical problem is: a combined hydrogen production system based on renewable energy electrolysis of water and carbon capture technology, including a photovoltaic power generation system, a wind power generation system, an external power grid access system, and hydrogen production by electrolysis of water.
  • System oxygen-enriched combustion hydrogen production system, carbon dioxide capture and liquefaction system, energy storage system, wherein: the photovoltaic power generation system, wind power generation system, external power grid access system, energy storage system through the power bus and the electrolysis water hydrogen production system connection; the electrolysis water hydrogen production system is connected with the oxygen-enriched combustion hydrogen production system, and the oxygen-enriched combustion hydrogen production system is connected with the carbon dioxide capture and liquefaction system.
  • the present invention provides a solution for supplying clean hydrogen and renewable energy hydrogen using renewable energy + carbon dioxide capture technology, and proposes for the first time a new method integrating photovoltaic, wind power, hydrogen energy, oxygen-enriched combustion, carbon capture, etc. Energy technology, and finally realize multi-energy complementation, supply coupling, renewable energy production of green hydrogen and carbon dioxide capture and recovery to supply clean hydrogen energy system, and put forward an implementable green hydrogen production plant technology to achieve carbon neutrality goals Program.
  • Figure 1 is a schematic diagram of a combined hydrogen production system based on renewable energy water electrolysis and carbon capture technology
  • FIG 2 is a schematic diagram of a combined hydrogen production system based on renewable energy water electrolysis and carbon capture technology (DC microgrid system);
  • FIG 3 is a schematic diagram of a combined hydrogen production system based on renewable energy water electrolysis and carbon capture technology (AC microgrid system);
  • Reference numerals in the figure include: grid power access device 1, first AC/DC converter 2, solar cell array 3, combiner box 4, first DC/DC converter 5, wind turbine 6, second AC /DC converter 7, second DC/DC converter 8, battery pack 9, super capacitor pack 10, DC microgrid bus 11, third DC/DC converter 12, water electrolysis device 13, hydrogen purification device 14, hydrogen gas Storage device 15, oxygen storage device 16, liquid hydrocarbon storage tank 17, BOG compressor 18, liquid hydrocarbon booster gasifier 19, liquid hydrocarbon booster pump 20, liquid hydrocarbon main gasifier 21, oxygen-enriched combustion hydrogen conversion Furnace 22, steam generator 23, shift reactor 24, steam preheater 25, cooling separator 26, PSA separation unit 27, tail gas heat exchanger 28, primary compressor 29, CO dehydration unit 30, condensate water pump 31 , secondary compressor 32 , CO 2 liquefaction cold box 33 , refrigeration device 34 , liquid CO 2 storage tank 35 , CO 2 buffer storage tank 36 , and smart energy management system 37 .
  • a combined hydrogen production system based on renewable energy water electrolysis and carbon capture technology includes: photovoltaic power generation system, wind power generation system, external power grid access system, water electrolysis hydrogen production system, oxygen-enriched combustion system. Hydrogen systems, liquid hydrocarbon storage and supply systems, carbon dioxide capture and liquefaction systems, energy storage systems, etc., among which:
  • Photovoltaic power generation system, wind power generation system, external power grid access system, and energy storage system supply power to the electrolysis water hydrogen production system through the power bus, and the surplus power is supplied to the energy storage system through the power bus for storage;
  • Gas and fuel gas are supplied to the oxygen-enriched combustion hydrogen production system, and the oxygen-enriched combustion hydrogen production system supplies the generated hydrogen to the water electrolysis hydrogen production system;
  • the water electrolysis hydrogen production system supplies the generated hydrogen to the rich Oxygen combustion hydrogen production system;
  • the tail gas generated by the oxygen-enriched combustion hydrogen production system enters the carbon dioxide capture and liquefaction system for carbon capture, the liquid CO2 produced by the carbon dioxide capture and liquefaction system is transported out, and the condensed water produced is used for production Steam reuse.
  • Example 1 Supplying clean hydrogen by means of DC microgrid multi-energy complementary green hydrogen production and oxy-fuel combustion CO 2 capture technology, as shown in Figure 2:
  • An external power grid access system is composed of a grid power access device 1 and a first AC/DC converter 2 .
  • the grid power access device 1 is connected to the first AC/DC converter 2 through a cable and finally connected to the DC microgrid bus 11 .
  • a photovoltaic power generation system is composed of a square array of solar cells 3 , a combiner box 4 and a first DC/DC converter 5 .
  • the solar cell array 3 is connected to the combiner box 4 through a cable to collect the power produced by the solar cell group, and the collected power of the combiner box 4 is adjusted to the reference voltage through the cable and the first DC/DC converter 5 and finally connected to the DC microcomputer.
  • Grid bus 11
  • the wind power generation system is composed of the wind power generator 6 and the second AC/DC converter 7 .
  • Said wind turbine 6 produces electricity and is regulated to a reference voltage via a cable and a second AC/DC converter 7 and finally connected to a DC microgrid bus 11 .
  • the energy storage system is composed of the second DC/DC converter 8 , the battery pack 9 , the super capacitor pack 10 , and the DC microgrid bus 11 .
  • Photovoltaic power generation system, wind power generation system, and external grid access system are adjusted to the reference voltage through various converters and finally connected to the DC microgrid bus 11.
  • the DC microgrid bus 11 is the meeting point of the joint production system.
  • the DC mode is aggregated to the DC microgrid bus 11, and then distributed.
  • the DC microgrid bus 11 is connected to the second DC/DC converter 8 through cables, and the second DC/DC converters 8 are respectively connected to storage devices of electrical energy such as the battery pack 9 and the super capacitor pack 10 through cables.
  • the electrolysis water hydrogen production system is composed of the third DC/DC converter 12, the water electrolysis device 13, the hydrogen purification device 14, the hydrogen storage device 15, and the oxygen storage device 16.
  • the third DC/DC converter 12, the water electrolysis device 13, the hydrogen purification device 14, and the hydrogen storage device 15 are connected in sequence, and the crude hydrogen generated by the water electrolysis device 13 passes through the hydrogen purification device 14 to become a high-purity product hydrogen, which enters the After the hydrogen storage device 15, it is supplied as product hydrogen.
  • the water electrolysis device 13 is connected to the oxygen storage device 16 , and the hydrogen produced by the water electrolysis device 13 enters the oxygen storage device 16 .
  • the water electrolysis device 13 can be an alkaline liquid water electrolysis cell, a solid polymer (PEM) water electrolysis cell or a solid oxide (SOEC) electrolysis cell, and different electrolysis water processes can be determined according to different construction scales and project construction conditions. .
  • PEM solid polymer
  • SOEC solid oxide
  • the composition of the hydrogen purification device 14 includes a gas-liquid analyzer, a demineralized water scrubber, a cooler, a steam-water separator, a deoxygenation tower, a TSV drying tower and a series of hydrogen drying and deoxidizing equipment. And following the production of hydrogen utilization objects and the production of hydrogen impurities, different requirements will increase or decrease equipment and a reasonable process.
  • a liquid hydrocarbon storage and supply system is composed of a liquid hydrocarbon storage tank 17, a BOG compressor 18, a liquid hydrocarbon booster gasifier 19, a liquid hydrocarbon booster pump 20, and a liquid hydrocarbon main gasifier 21.
  • the LNG fuel is stored in the liquid hydrocarbon storage tank 17 .
  • the liquid phase outlet of the liquid hydrocarbon storage tank 17 is connected to the inlet of the liquid hydrocarbon booster pump 20 by a pipeline, and the outlet of the liquid hydrocarbon booster pump 20 is connected to the inlet of the liquid hydrocarbon booster gasifier 19 through a pipeline, and the liquid hydrocarbon is boosted and gasified.
  • the outlet of the device 19 is returned to the liquid hydrocarbon storage tank 17 to realize self-pressurization.
  • the LNG fuel reaching 0.3-0.4MPa is connected to the inlet of the main liquid hydrocarbon gasifier 21 from another liquid phase outlet of the liquid hydrocarbon storage tank 17 by a pipeline, and gasified to normal temperature; the gas phase outlet of the liquid hydrocarbon storage tank 17 is connected by a pipeline
  • the BOG Boil Off Gas flash gas, the static evaporation of liquid hydrocarbons produced during static storage
  • the pipelines and fuel pipelines are sent to the oxy-combustion hydrogen-producing converter 22 of the oxy-combustion hydrogen-producing system to participate in the reaction.
  • the liquid hydrocarbon storage tank 17 can be a vacuum powder insulation tank or a high vacuum Dewar when storing low-temperature materials such as LNG and ethane, and can be a carbon steel horizontal tank when storing LPG and other normal temperature materials;
  • the BOG compressor 18 can be a screw Compressor, labyrinth compressor, and balanced reciprocating compressor;
  • the liquid hydrocarbon booster pump 20 can be a barrel bag submersible pump, an external centrifugal pump;
  • the liquid hydrocarbon main vaporizer 21 can be an air temperature vaporizer, a water bath Type gasifier, steam heat exchange gasifier.
  • the oxygen-enriched combustion hydrogen production system is composed of an oxygen-enriched combustion hydrogen production converter 22, a steam generator 23, a shift reactor 24, a steam preheater 25, a cooling separator 26, a PSA separator 27, and a tail gas heat exchanger 28. .
  • the oxygen-enriched combustion hydrogen conversion furnace 22, the steam generator 23, the shift reactor 24, the steam preheater 25, the cooling separator 26, and the PSA separation device 27 are connected in sequence, and the high-purity produced after separation by the PSA separation device 27
  • the product hydrogen enters the hydrogen storage device 15 .
  • the oxygen from the oxygen storage device 16 enters the oxygen-enriched combustion hydrogen-producing converter 22, the oxygen-enriched combustion hydrogen-producing converter 22 is connected to the tail gas heat exchanger 28, and the exhaust gas generated by the oxygen-enriching combustion hydrogen-producing converter 22 passes through the exhaust heat exchanger 28 Then it enters the first stage compressor 29 of the carbon dioxide capture and liquefaction system.
  • the oxygen-enriched combustion hydrogen-producing reformer 22 uses hydrocarbons as raw materials and adopts steam reforming and gas-making process equipment.
  • the raw materials suitable for hydrocarbon conversion to hydrogen production include natural gas, liquefied petroleum gas, various refinery gases, synthesis gas, straight-run naphtha, raffinate oil, topping oil and secondary processing oil. Among them, hydrogen production from natural gas with the lightest molecular weight and the smallest carbon-hydrogen ratio is the best.
  • This patent mainly uses LNG as an example.
  • the basic principle is that steam is used as the oxidant, and the natural gas is converted under the action of nickel catalyst to obtain the raw material gas for hydrogen production.
  • This process is an endothermic process, so external heat is required, and the heat required for the conversion is provided by the fuel gas or the desorption gas after the oxygen-enriched combustion chemical reaction.
  • the natural gas as the raw material first enters the tail gas convection section of the oxygen-enriched combustion hydrogen production converter, and is preheated to 500-520 °C, and then sent to the top of the radiant section of the hydrogen production converter, distributed into each reaction tube, and flows through the catalyst layer from top to bottom.
  • the reforming reaction conditions are that the temperature is maintained at 750-920°C.
  • the gas undergoes a steam reforming reaction in the reforming tube, and the reformed gas from each reforming tube is collected from the bottom to the gas collecting tube.
  • the reformed gas produced by the oxygen-enriched combustion hydrogen conversion furnace 22 enters the shift reactor 24 after the steam generator 23 exchanges heat to produce steam.
  • carbon monoxide and water vapor react as follows:
  • the CO shift reaction is an exothermic reaction, and the temperature around 300 °C is beneficial to the shift balance, which can obtain a higher CO shift rate, which in turn can increase the hydrogen production per unit of raw material.
  • the two-stage heat exchange conversion technology can be used to increase the yield of product hydrogen.
  • the primary compressor 29, the CO 2 dehydration device 30, the secondary compressor 32, the CO 2 liquefied cold box 33, and the liquid CO 2 storage tank 35 are connected in sequence; the primary compressor 29 is connected to the CO 2 buffer storage tank 36 connected, the CO 2 evaporation gas in the liquid CO 2 storage tank 35 enters the CO 2 buffer storage tank 36 from the gas phase; the CO 2 dehydration device 30 is connected to the condensate water pump 31, and the effluent of the condensed water pump 31 is recovered as condensed water; the The liquid CO 2 from the liquid-phase outlet of the liquid CO 2 storage tank 35 is loaded into the vehicle for export; the CO 2 liquefied cold box 33 is connected to the refrigeration device 34 .
  • the primary compressor 29 and the secondary compressor 32 may be reciprocating compressors, screw compressors, or the like.
  • the CO 2 dehydration device 30 is a method of removing carbon dioxide from carbon dioxide by adsorbing water molecules in the gas to the inner pores of the desiccant by utilizing the adsorption tension of the desiccant.
  • the commonly used desiccants are silica gel, molecular sieve, etc., the technology is mature and reliable, the water content of dry gas after dehydration can be as low as 1 ⁇ 10 -6 , and the dew point of dry natural gas after dehydration with molecular sieve can be as low as -100 °C, which can meet the subsequent carbon dioxide liquefaction. the dew point requirements to avoid freezing blockage of the cold box flow path.
  • the CO 2 liquefaction cold box 33 does not require high cooling temperature, so an aluminum multi-flow cold box or an evaporative heat exchanger can be used.
  • the refrigeration device can be a R134a refrigeration cycle system, a R410a refrigeration cycle system, a R290 (propane) refrigeration cycle system, and a R600a refrigeration cycle system. Choose one of the refrigeration cycles.
  • the liquid CO 2 storage tank 35 is a metal storage tank with a cold-insulating function, and can be vacuum powder insulation, perlite accumulation insulation, polyurethane-coated insulation, etc. to achieve cold insulation and insulation.
  • the smart energy management system 37 is the nerve center and energy management center of the system. It collects, manages and coordinates and controls the equipment in the area, which is the guarantee for the safe, stable and efficient operation of the system.
  • the management system will comprehensively perceive the operation, environmental status and personnel management of various equipment (photovoltaics, converters, switches, electrolysis equipment, hydrogen storage/oxygen equipment, hydrocarbon conversion hydrogen production equipment, carbon capture equipment, etc.) Real-time monitoring, coordinated control, peak shaving and valley filling, economic operation management, and support for load tracking, photovoltaic power generation forecast, demand side management, energy sales and other functions.
  • the solar cell array 3 of the photovoltaic power generation system is connected to the combiner box 4 through the cable, and the combiner box 4 is connected to the first DC/DC converter 5 through the cable and finally connected to the DC microgrid bus 11.
  • the system can generate electricity by using a square array of solar cells to achieve an effective power generation time of about 1500-2000 hours per year, and supply it to the microgrid.
  • the wind generator 6 of the wind power generation system is connected to the second AC/DC converter 7 and finally to the DC microgrid bus 11 by means of cables.
  • This system relies on wind turbines to generate electricity in areas with wind resources, and can achieve an annual effective power generation time of about 2000-3500 hours, which can be supplied to the microgrid.
  • the second DC/DC converter 8 is connected to the DC microgrid bus 11 through cables, and the second DC/DC converter 8 is connected to the battery pack 9 and the supercapacitor pack 10 by cables respectively; the photovoltaic power generation and wind power generation of this system can be In a short period of time (according to the actual demand, it can be stored with the energy storage scale of the system for 24 hours) by the battery pack and super capacitor for storage and release to ensure the power supply of the microgrid.
  • Hydrogen production system by electrolysis of water The rich of photovoltaic and wind power can produce hydrogen into hydrogen storage device 15 through the hydrogen production system of electrolysis water.
  • Example 2 Supplying clean hydrogen by means of AC microgrid multi-energy complementary green hydrogen production and oxy-fuel combustion CO 2 capture technology, as shown in Figure 3:
  • the equipment in the DC micro-grid system of the present invention is slightly changed, it can be turned into an AC micro-grid system for electrolyzing water to produce hydrogen.
  • the first AC/DC converter 2 is adjusted to the first transformer 102; the first DC/DC converter 5 is adjusted to the DC/AC inverter 105; the second AC/DC converter 7 is adjusted to the second transformer 107; The DC/DC converter 8 is adjusted to an AC/DC bidirectional converter 108 ; the third DC/DC converter 12 is adjusted to an AC/DC converter 112 .
  • the solar cell array 103 of the photovoltaic power generation unit is connected to the combiner box 104 through the cable, and the combiner box 104 is connected to the DC/AC inverter 105 through the cable and finally connected to the AC microgrid bus 111.
  • This system can achieve effective power generation time of about 1,500 hours per year by relying on solar cell arrays in areas with sunshine resources, and supply the micro grid.
  • the wind generators of the wind power units are connected to the second transformer 107 and finally to the AC microgrid busbars through cables.
  • the system can generate about 2,500 hours of effective power generation per year by relying on wind turbines to supply the microgrid.
  • the AC/DC bidirectional converter 108 is connected to the AC microgrid bus 111 through a cable, and the AC/DC bidirectional converter 108 is connected to the battery pack 109 and the supercapacitor pack 110 with cables respectively; the photovoltaic power generation and wind power generation of this system can be generated in a short time. (According to the actual demand, it can be matched with the energy storage scale of 1 to 12 hours) The storage and release are carried out by the battery pack and the super capacitor to ensure the power supply of the micro grid.
  • the wealth of photovoltaic and wind power generation can be converted into direct current through the AC/DC converter, and then the hydrogen can be produced into the hydrogen storage device 115 through the water electrolysis hydrogen production system.
  • the oxygen-enriched combustion hydrogen production system and the carbon dioxide capture and liquefaction system are completely the same as those in the first embodiment.
  • the working principle of the present invention is:
  • the present invention produces hydrogen and oxygen through photovoltaics, wind power, and grid valley electricity: the electricity produced by the solar cell array and the wind turbine can be made into hydrogen and oxygen through the electrolysis water hydrogen production system and stored in the storage device; it can also be stored at night without sunlight. Through the grid access device, the cheap valley electricity is taken from the grid through the water electrolysis system to produce hydrogen and oxygen into the storage device for storage.
  • the hydrogen and oxygen produced by the hydrogen production of the water electrolysis system are stored in the corresponding storage devices respectively, in which the hydrogen can be pressurized or liquefied and then sent to the consumer terminal; the oxygen is mainly sent to the oxygen-enriched combustion hydrogen conversion furnace 22 for oxygen-enriched combustion , to provide heat for steam reforming hydrogen production, and the produced hydrogen will be sent to the hydrogen storage tank after being purified to the product requirements, and finally sent to the consumer terminal after being pressurized or liquefied.
  • the oxygen-enriched combustion hydrogen conversion furnace 22 is based on steam reforming of hydrocarbon steam reforming, which is a mature technology in the direction of hydrogen production from fossil energy, which includes endothermic reaction and exothermic reaction.
  • the raw materials suitable for the conversion of hydrocarbons to hydrogen include natural gas, liquefied petroleum gas, various refinery gases, and synthesis gas. Among them, hydrogen production from natural gas with the lightest molecular weight and the smallest carbon-hydrogen ratio is the best.
  • This patent mainly uses LNG as an example.
  • the basic principle is that steam is used as the oxidant, and the natural gas is converted under the action of nickel catalyst to obtain the raw material gas for hydrogen production. Its main reaction under the action of nickel catalyst is as follows:
  • the process of methane reforming in steam reforming is an endothermic process.
  • the temperature of the reaction is as high as 750-920 °C.
  • the heat required for the conversion is provided by the fuel gas after the oxygen-enriched combustion chemical reaction.
  • the reformed gas produced by the oxygen-enriched combustion hydrogen conversion furnace 22 is subjected to heat exchange by the steam generator 23 to produce steam, and then enters the conversion reactor 24 at a controlled temperature of about 300°C. Under the action of the medium conversion catalyst, carbon monoxide and water vapor The following reaction occurs:
  • the CO shift reaction is an exothermic reaction, and the reaction temperature of 300°C is favorable for the shift balance, and a higher CO shift rate can be obtained, thereby increasing the hydrogen production per unit of raw material.
  • the two-stage heat exchange conversion technology can be used to increase the yield of product hydrogen.
  • the hydrogen produced from natural gas will be purified by pressure swing adsorption hydrogen.
  • the realization of the PSA purification process is due to the two properties of the adsorbent in this physical adsorption: one is that the adsorption capacity of different components is different, and the other is the adsorption capacity of the adsorbate on the adsorbent.
  • the partial pressure of the adsorbate increases and decreases with the increase of the adsorption temperature.
  • the preferential adsorption of impurity components in the hydrogen-containing source can be achieved to achieve the purpose of hydrogen purification; using the second property of the adsorbent, the adsorbent can be adsorbed at low temperature and high pressure.
  • Desorption and regeneration at high temperature and low pressure constitute the adsorption and regeneration cycle of the adsorbent to achieve the purpose of continuous hydrogen extraction.
  • the degassed gas from the PSA separation unit is stabilized and sent to the reformer as fuel.
  • the CO 2 dehydration device we use is a method that uses the adsorption tension of the desiccant to make the water molecules of the gas adsorbed by the inner pores of the desiccant and removed from the carbon dioxide.
  • the commonly used desiccants are silica gel, molecular sieve, etc., the technology is mature and reliable, the water content of dry gas after dehydration can be as low as 1 ⁇ 10 -6 , and the dew point of dry natural gas after dehydration with molecular sieve can be as low as -100 °C, which can meet the subsequent carbon dioxide liquefaction. the dew point requirements to avoid freezing blockage of the cold box flow path.
  • the cooling temperature requirement is not high, so a multi-flow cold box or an evaporative heat exchanger can be used.
  • the refrigeration device can be used in various refrigeration cycles such as R134a refrigeration cycle system, R410a refrigeration cycle system, R290 (propane) refrigeration cycle system, and R600a refrigeration cycle system. Choose the most suitable process according to the site conditions.
  • the liquid CO 2 storage tank it belongs to is a metal storage tank with cold insulation function.
  • the device can also be used as a power grid peak-shaving energy storage facility. Reduce the power of electrolyzed water to output electricity during the peak electricity consumption during the day, and increase the power of electrolyzed water to absorb valley electricity when electricity consumption is low at night. The fluctuation of hydrogen production from water ensures the smooth operation of downstream hydrogen terminals.

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Abstract

一种基于可再生能源电解水和碳捕技术的联合制氢系统，包括光伏发电系统、风力发电系统、外部电网接入系统、电解水制氢系统、富氧燃烧制氢系统、二氧化碳捕集与液化系统和储能系统。通过整合光伏、风电、氢能、富氧燃烧、碳捕集等多种技术，实现多能互补、供应耦合，是一种可再生能源制绿氢与二氧化碳捕集回收的供应清洁氢的能源系统。

Description

一种基于可再生能源电解水和碳捕技术的联合制氢系统 技术领域
本发明涉及新能源技术领域，尤其是涉及一种整合光伏、风电、氢能、富氧燃烧、碳捕集等多种新能源技术，最终实现进行多能互补、供应耦合，可再生能源制绿氢与二氧化碳捕集回收下供应清洁氢的能源系统，为实现碳中和目标提出了一种可实施的高效绿色制氢工厂技术方案。
背景技术
2015年12月联合国巴黎气候变化大会通过了《巴黎协定》要求，根据协定各国以“自主贡献”的方式参与全球应对气候变化行动，发达国家继续带头减缓碳排放，并对发展中国家减缓碳排放和适应气候变化提供资金、技术和能力建设的支持。根据协定要求，2019年12月欧盟明确提出了2050年实现碳中和。因此研发出具有可操作性、可实施性和经济性的近零碳排放能源供应系统成为世界各国的达到碳中和目标的重要手段之一。
根据欧盟委员会发布的《欧洲氢能战略》，提出到2030年，欧盟的绿氢年产能将超过1000万吨，绿氢制备总功率达到40GW。可以预见未来可再生能源电解水制氢的项目将是支撑零碳经济的核心基础设施。因此我们判断大量的绿氢电解项目伴生氧气利用将是未来降低碳捕集能耗的关键点，据此我们开发了一种基于可再生能源电解水和碳捕技术的联合制氢系统及方法，以建设低能耗的氢气工厂为未来社会提供清洁的能源。
光伏发电是利用半导体界面的光生伏特效应而将光能直接转变为电能的一种技术。主要由太阳能电池板(组件)、控制器和逆变器三大部分组成，主要部件由电子元器件构成。太阳能电池经过串联后进行封装保护可形成大面积 的太阳能电池组件，再配合上功率控制器等部件就形成了光伏发电装置。
风力发电是把风的动能转变成机械动能，再把机械能转化为电力动能。风力发电的原理，是利用风力带动风车叶片旋转，再透过增速机将旋转的速度提升，来促使发电机发电。依据目前的风车技术，大约是每秒三米的风速(微风的程度)，便可以开始发电。
全球风能、水能、太阳能等清洁能源资源非常丰富，理论年可开采量相当于全球化石能源剩余探明可采储量的38倍。但他们致命缺点是不能长期稳定的提供能源输出，需要依靠现有能源系统补能调峰或单独配置储能调峰系统。
电解水制氢过程实际上是一种能量转换过程，即将一次能源转换为能源载体氢能的过程。目前两大类水电解制氢技术可以在低温条件下进行实际应用，分别是碱性液体水电解与固体聚合物(PEM)水电解两类。碱性液体水电解技术是以KOH、NaOH水溶液为电解质，如采用石棉布等作为隔膜，在直流电的作用下，将水电解，生成氢气和氧气。产出的气体需要进行脱碱雾处理。典型的PEM水电解技术主要部件包括阴阳极气体扩散层、阴阳极催化层和质子交换膜等。在PEM技术中，水中的氢离子穿过质子交换膜与电子结合成为氢原子，氢原子相互结合形成氢分子。PEM质子交换膜作为固体电解质，一般使用全氟磺酸膜，起到隔绝阴阳极生成气，阻止电子的传递，同时传递质子的作用。质子交换膜替代了石棉膜隔绝电极两侧的气体，避免了碱性液体电解质电解槽使用强碱性液体电解质所带来的缺点。此外，PEM水电解池采用零间隙结构，电解池体积更为紧凑精简降低了电解池的欧姆电阻，大幅提高了电解池的整体性能。
烃类蒸汽转化制氢工艺是一种在我国大量成熟应用的化工工艺过程。适用于烃类转化制氢的原料种类很多，包括天然气、液化石油气、各种炼厂气、合 成气、直馏石脑油、抽余油、拔头油及二次加工油等。其中以分子量最轻、碳氢比最小的天然气制氢为最佳。专利描述主要以天然气为示例：天然气制氢由天然气蒸汽转化制转化气和变压吸附(PSA)提纯氢气(H 2)两部分组成，压缩并脱硫后天然气与水蒸汽混合后，在镍催化剂的作用下于750～850℃将天然气物质转化为氢气(H 2)、一氧化碳(CO)和二氧化碳(CO 2)的转化气，转化气可以通过变换将一氧化碳(CO)变换为氢气(H 2)，成为变换气，然后，转化气或者变换气通过变压吸附(PSA)过程，得到高纯度的氢气(H 2)。相关反应属于吸热反应，需要燃烧燃料进行热量补充。
CCUS技术是能源行业降低排放的关键解决方案，在推进能源系统低碳转型、实现全球气候目标方面发挥重要作用。根据国际能源署(IEA)的《CCUS在低碳发电系统中的作用》报告中分类，碳捕集方式主要分为燃烧后捕集、燃烧前捕集和富氧燃烧碳捕集系统三大研究方向。富氧燃烧捕集技术是一种燃烧中捕集技术。与传统直接用空气助燃的燃烧技术不同，富氧燃烧是用纯度非常高的氧气助燃，用燃烧生成的CO 2代替空气中的N 2反复循环使用，通过调整助燃空气与循环烟气的比例控制O 2/CO 2配比以适应不同的燃烧要求。富氧燃烧排烟中富含高浓度CO 2，便于后续实施低成本的二氧化碳捕集。
微电网是相对传统大电网的一个概念，是指多个分布式电源及其相关负载按照一定的拓扑结构组成的网络，并通过静态开关关联至常规电网。开发和延伸微电网能够充分促进分布式电源与可再生能源的大规模接入，实现对负荷多种能源形式的高可靠供给，是实现主动式配电网的一种有效方式，使传统电网向智能电网过渡。直流微电网和交流微电网是典型的微电网模式，两者之间主要区别在于采用的是直流电还是交流电作为能量传输载体。
根据中国氢能联盟提出的《低碳氢、清洁氢与可再生能源氢的标准与评价》在单位氢气碳排放量方面，低碳氢的阈值为14.51kgCO2e/kgH2，清洁氢和可 再生氢的阈值为4.9kgCO2e/kgH2，可再生氢同时要求制氢能源为可再生能源。
发明内容
为了开发有效利用于含碳燃料的提高燃烧效率和降低石化燃料脱碳成本的技术，本发明提出了一种基于可再生能源电解水和碳捕技术的联合制氢系统，旨在实现可再生能源与CCUS技术结合下生产清洁氢与可再生能源氢，符合未来碳中和的社会需求，应用前景广阔。
本发明解决其技术问题所采用的技术方案是：一种基于可再生能源电解水和碳捕技术的联合制氢系统，包括光伏发电系统、风力发电系统、外部电网接入系统、电解水制氢系统、富氧燃烧制氢系统、二氧化碳捕集与液化系统、储能系统，其中：所述光伏发电系统、风力发电系统、外部电网接入系统、储能系统通过电力母线与电解水制氢系统连接；所述电解水制氢系统与富氧燃烧制氢系统连接，所述富氧燃烧制氢系统与二氧化碳捕集与液化系统连接。
与现有技术相比，本发明的积极效果是：
本发明提供了一套采用可再生能源+二氧化碳捕集技术供给清洁氢与可再生能源氢的方案，首次提出了一种整合光伏、风电、氢能、富氧燃烧、碳捕集等多种新能源技术，最终实现进行多能互补、供应耦合，可再生能源制绿氢与二氧化碳捕集回收下供应清洁氢的能源系统，为实现碳中和目标提出了一种可实施的绿色制氢工厂技术方案。
附图说明
本发明将通过例子并参照附图的方式说明，其中：
图1是一种基于可再生能源电解水和碳捕技术的联合制氢系统框架示意图；
图2是一种基于可再生能源电解水和碳捕技术的联合制氢系统的示意图 (直流微电网系统)；
图3是一种基于可再生能源电解水和碳捕技术的联合制氢系统的示意图(交流微电网系统)；
图中附图标记包括：网电接入装置1、第一AC/DC转换器2、太阳能电池方阵3、汇流箱4、第一DC/DC转换器5、风力发电机6、第二AC/DC转换器7、第二DC/DC转换器8、蓄电池组9、超级电容组10、直流微电网母线11、第三DC/DC转换器12、电解水装置13、氢气提纯装置14、氢气储存装置15、氧气储存装置16、液烃储罐17、BOG压缩机18、液烃增压气化器19、液烃增压泵20、液烃主气化器21、富氧燃烧制氢转换炉22、蒸汽发生器23、变换反应器24、蒸汽预热器25、冷却分离器26、PSA分离装置27、尾气换热器28、一级压缩机29、CO 2脱水装置30、冷凝水泵31、二级压缩机32、CO 2液化冷箱33、制冷装置34、液态CO 2储罐35、CO 2缓冲储罐36、智慧能量管理系统37。
具体实施方式
一种基于可再生能源电解水和碳捕技术的联合制氢系统，如图1所示，包括：光伏发电系统、风力发电系统、外部电网接入系统、电解水制氢系统、富氧燃烧制氢系统、液烃储存与供应系统、二氧化碳捕集与液化系统、储能系统等，其中：
光伏发电系统、风力发电系统、外部电网接入系统、储能系统将电力通过电力母线供给电解水制氢系统，富余的电力通过电力母线供给储能系统进行储存；液烃储存与供应系统将原料气和燃料气供给富氧燃烧制氢系统，富氧燃烧制氢系统将产生的氢气供给电解水制氢系统；所述电解水制氢系统将产生的氢气外供，将产生的氧气提供给富氧燃烧制氢系统；所述富氧燃烧制氢系统产生的尾气进入二氧化碳捕集与液化系统进行碳捕集，二氧化碳捕集与液化系统产 生的液态CO 2外运、产生的凝结水用于制蒸汽回用。
实施例一、依托直流微电网多能互补制绿氢与富氧燃烧CO 2捕集技术下供应清洁氢，如图2所示：
1)由网电接入装置1、第一AC/DC转换器2组成外部电网接入系统。
所述网电接入装置1通过电缆与第一AC/DC转换器2连接并最终连接至直流微电网母线11。
2)由太阳能电池方阵3、汇流箱4、第一DC/DC转换器5组成光伏发电系统。
所述太阳能电池方阵3通过电缆与汇流箱4连接汇集太阳能电池组生产的电力，汇流箱4汇集后的电力通过电缆与第一DC/DC转换器5调节到基准电压并最终连接至直流微电网母线11。
3)由风力发电机6、第二AC/DC转换器7组成风力发电系统。
所述风力发电机6生产电力并通过电缆与第二AC/DC转换器7调节到基准电压并最终连接至直流微电网母线11。
4)由第二DC/DC转换器8、蓄电池组9、超级电容组10、直流微电网母线11组成储能系统。
光伏发电系统、风力发电系统、外部电网接入系统通过各类转换器调节到基准电压并最终连接至直流微电网母线11，直流微电网母线11是联合生产系统的汇合点，所有的能源都以直流的方式汇总到直流微电网母线11上，再进行分配。
直流微电网母线11通过电缆连接第二DC/DC转换器8，第二DC/DC转换器8分别通过电缆连接蓄电池组9和超级电容组10等电能的储存装置。
5)由第三DC/DC转换器12、电解水装置13、氢气提纯装置14、氢气储 存装置15、氧气储存装置16组成电解水制氢系统。
所述第三DC/DC转换器12、电解水装置13、氢气提纯装置14、氢气储存装置15依次连接，通过电解水装置13产生的粗氢气经过氢气提纯装置14后成为高纯产品氢气，进入氢气储存装置15后，作为产品氢气外供。所述电解水装置13与氧气储存装置16连接，电解水装置13产生的氢气进入氧气储存装置16。
所述电解水装置13可以是碱性液体水电解槽、固体聚合物(PEM)水电解槽或固体氧化物(SOEC)电解槽，可以根据不同建设规模与项目建设条件情况确定不同的电解水工艺。
所述氢气提纯装置14的组成包括气液分析器、除盐水洗涤器、冷却器、汽水分离器、脱氧塔、TSV干燥塔等一系列的氢气干燥、除氧设备组成。并跟随制得氢气利用对象而产生氢杂质要求不同会增减设备搭配合理的流程。
6)由液烃储罐17、BOG压缩机18、液烃增压气化器19、液烃增压泵20、液烃主气化器21组成液烃储存与供应系统。
LNG燃料储存于液烃储罐17。液烃储罐17的液相出口由管道连接至液烃增压泵20的入口，液烃增压泵20的出口通过管道与液烃增压气化器19入口相连，液烃增压气化器19出口返回至液烃储罐17实现自增压。达到0.3～0.4MPa的LNG燃料从液烃储罐17的另一个液相出口由管道连接至液烃主气化器21的入口，气化为常温；液烃储罐17的气相出口通过管道连接到BOG压缩机18，经过BOG压缩机18增压的BOG(Boil Off Gas闪蒸气，液烃在静态储存时产生的静态蒸发)和液烃主气化器21出口的气态烃连通混合后通过原料管道和燃料管道被送至富氧燃烧制氢系统的富氧燃烧制氢转换炉22参与反应。其中：
所述液烃储罐17在储存LNG、乙烷等低温物料时可以是真空粉末绝热罐、高真空杜瓦，在储存LPG等常温物料时可以是碳钢卧罐；BOG压缩机18可以是螺杆压缩机、迷宫压缩机、平衡式往复式压缩机；液烃增压泵20可以是筒袋潜液泵、外置离心泵；液烃主气化器21可以是空温式气化器、水浴式气化器、蒸汽换热气化器。
7)由富氧燃烧制氢转换炉22、蒸汽发生器23、变换反应器24、蒸汽预热器25、冷却分离器26、PSA分离器27、尾气换热器28组成富氧燃烧制氢系统。
所述富氧燃烧制氢转换炉22、蒸汽发生器23、变换反应器24、蒸汽预热器25、冷却分离器26、PSA分离装置27依次连接，经过PSA分离装置27分离后产生的高纯产品氢气进入氢气储存装置15。来自氧气储存装置16的氧气进入富氧燃烧制氢转换炉22，富氧燃烧制氢转换炉22与尾气换热器28连接，富氧燃烧制氢转换炉22产生的尾气经过尾气换热器28后进入二氧化碳捕集与液化系统的一级压缩机29。
所述富氧燃烧制氢转换炉22是以烃类为原料，采用蒸汽转化造气工艺的设备。适用于烃类转化制氢的原料包括天然气、液化石油气、各种炼厂气、合成气、直馏石脑油、抽余油、拔头油及二次加工油等。其中以分子量最轻、碳氢比最小的天然气制氢为最佳。本专利主要以液化天然气为示例。
其基本原理是以水蒸汽为氧化剂，在镍催化剂的作用下将天然气物质转化，得到制取氢气的原料气。这一过程为吸热过程，故需外供热量，转化所需的热量由燃料气或解吸气进行富氧燃烧化学反应后提供。天然气为原料首先进入富氧燃烧制氢转换炉的尾气对流段预热到500～520℃，然后送到制氢转换炉的辐射段顶部，分配进入各反应管，从上而下流经催化剂层。重整反应条件为 温度维持在750～920℃。气体在转化管内进行蒸汽转化反应，从各转化管出来的转化气由底部汇整到集气管。
在镍催化剂作用下其主要反应如下：
CH 4+H 2O----CO+3H 2–Q
CO+H 2O----CO 2+H 2+Q
在普通空气助燃的情况下占比4/5的氮气并没有参与燃烧反应，在燃烧过程中带走大量热量，并且生成氮氧化物。本发明提出二氧化碳+纯氧替代空气助燃，可增加燃烧效率，并且最终产物只有二氧化碳与水，将极大利于降低后续碳捕集的成本。
所述富氧燃烧制氢转换炉22生产的转化气经蒸汽发生器23换热生产蒸汽后进入变换反应器24，在中变催化剂的作用下，一氧化碳与水蒸气发生如下反应：
CO+H 2O----CO 2+H 2+Q
CO变换反应为放热反应，300℃左右温度对变换平衡有利，可得到较高的CO变换率，进而可提高单位原料的产氢量。为简化工艺流程，节省投资，在小规模的天然气转化制氢只采用一段变换。而在较大规模式则可以采用两段换热式转化技术，增加产品氢的收率。
8)由一级压缩机29、CO 2脱水装置30、冷凝水泵31、二级压缩机32、CO 2液化冷箱33、制冷装置34、液态CO 2储罐35、CO 2缓冲储罐36组成二氧化碳捕集与液化系统。
所述一级压缩机29、CO 2脱水装置30、二级压缩机32、CO 2液化冷箱33、液态CO 2储罐35依次连接；所述一级压缩机29与CO 2缓冲储罐36连接，所述液态CO 2储罐35中的CO 2蒸发气从气相进入CO 2缓冲储罐36；所述CO 2脱水装置30与冷凝水泵31连接，冷凝水泵31出水作为冷凝水回收；所述液 态CO 2储罐35液相出口的液态CO 2装车外输；所述CO 2液化冷箱33与制冷装置34连接。
所述一级压缩机29和二级压缩机32可以是往复式压缩机、螺杆压缩机等。
所述CO 2脱水装置30是利用干燥剂吸附张力使气体的水分子被干燥剂内孔吸附而从二氧化碳中除去的方法。常用的干燥剂有硅胶、分子筛等，技术成熟可靠，脱水后干气含水量可低至1×10 -6，采用分子筛脱水后的干天然气水露点可低至-100℃，可以满足后续二氧化碳液化的露点要求，避免结冰堵塞冷箱流道。
所述CO 2液化冷箱33由于CO 2的最佳液化点在-30℃左右，对冷却的温度要求并不高，因此可以采用铝制多股流冷箱、或者蒸发式换热器等。
所述制冷装置34由于CO 2的最佳液化点在-30℃左右，因此本制冷装置可以是R134a制冷循环系统、R410a制冷循环系统、R290(丙烷)制冷循环系统、R600a制冷循环系统等多种制冷循环中选择一种。
所述液态CO 2储罐35是具备保冷功能的金属储罐，可以是真空粉末绝热、珍珠岩堆积绝热、聚氨酯包覆绝热等方案来实现保冷绝热。
智慧能量管理系统37是本系统的神经中枢和能量管理中心，对区域内设备进行采集管理和协调控制，是系统安全、稳定、高效运行的保障。管理系统将对各类设备(光伏、转换器、开关、电解设备、储氢/氧设备、烃类转化制氢设备、碳捕集设备等)运行、环境状态及人员管理进行综合的信息感知，实现实时监控、协调控制、削峰填谷、经济运行管理，并可支持负荷跟踪、光伏发电预测、需求侧管理、售能等功能。
本实施例采用多能互补的直流微电网制氢：
光伏发电系统的太阳能电池方阵3通过电缆与汇流箱4连接，汇流箱4通 过电缆与第一DC/DC转换器5连接并最终连接至直流微电网母线11。本系统在具备阳光资源地区依托太阳能电池方阵发电每年可实现有效发电时间1500-2000小时左右，供给微电网。
风力发电系统的风力发电机6通过电缆与第二AC/DC转换器7连接并最终连接至直流微电网母线11。本系统在具备风力资源地区依托风力发电机发电可实现每年有效发电时间2000-3500小时左右，供给微电网。
第二DC/DC转换器8通过电缆与直流微电网母线11相连接，同时第二DC/DC转换器8分别与蓄电池组9和超级电容组10电缆连接；本系统的光伏发电和风力发电可以短时间(根据实际需求可存储配合系统自用电24小时的储能规模)由蓄电池组和超级电容进行储存和释放，保障微电网的供电。
电解水制氢系统：光伏和风力发电的富裕可以通过电解水制氢系统制成氢气进入氢气储存装置15。
实施例二、依托交流微电网多能互补制绿氢与富氧燃烧CO 2捕集技术下供应清洁氢，如图3所示：
只要本发明的直流微电网系统中的设备进行少许改变就能变成交流微电网系统进行电解水制氢。
第一AC/DC转换器2调整成第一变压器102；第一DC/DC转换器5调整成DC/AC逆变器105；第二AC/DC转换器7调整成第二变压器107；第二DC/DC转换器8调整成AC/DC双向转换器108；第三DC/DC转换器12调整成AC/DC转换器112。
最终变换后如图3一种基于可再生能源电解水和碳捕技术的联合制氢系统的示意图(交流微电网系统)所示。
光伏发电单元的太阳能电池方阵103通过电缆与汇流箱104连接，汇流箱 104通过电缆与DC/AC逆变器105连接并最终连接至交流微电网母线111。本系统在具备阳光资源地区依托太阳能电池方阵发电每年可实现有效发电时间1500小时左右，供给微电网。
风力发电单元的风力发电机通过电缆与第二变压器107并最终连接至交流微电网母线。本系统在具备风力资源地区依托风力发电机发电可实现每年有效发电时间2500小时左右，供给微电网。
AC/DC双向转换器108通过电缆与交流微电网母线111相连接，同时AC/DC双向转换器108分别与蓄电池组109和超级电容组110电缆连接；本系统的光伏发电和风力发电可以短时间(根据实际需求可配合1～12小时的储能规模)由蓄电池组和超级电容进行储存和释放，保障微电网的供电。
电解水制氢系统，光伏和风力发电的富裕可以通过AC/DC转换器转换成直流电后再通过电解水制氢系统制成氢气进入氢气储存装置115。
富氧燃烧制氢系统和二氧化碳捕集与液化系统则与实施例一完全一致。
本发明的工作原理是：
本发明通过光电、风电、电网谷电制氢气、氧气：太阳能电池方阵和风力发电机生产的电力可以通过电解水制氢系统制成氢气和氧气进入储存装置内储存；没有阳光的夜晚也可以通过网电接入装置从电网取便宜的谷电通过电解水系统制成氢气和氧气进入储存装置内储存。
电解水系统制氢产生的氢和氧气分别存储在对应的储存装置中，其中氢可以经增压或液化后送至消费终端；氧气则主要送于富氧燃烧制氢转换炉22进行富氧燃烧，为蒸汽转化制氢提供热量，制得的氢气将在提纯到产品要求后送至氢气储存储罐，最终经增压或液化后送至消费终端。
所述富氧燃烧制氢转换炉22是基于烃类蒸汽转化水蒸气重整，是化石能源制氢方向中一项成熟技术，其中包含了吸热反应和放热反应。适用于烃类转化制氢的原料包括天然气、液化石油气、各种炼厂气、合成气等。其中以分子量最轻、碳氢比最小的天然气制氢为最佳。本专利主要以液化天然气为示例。
其基本原理是以水蒸汽为氧化剂，在镍催化剂的作用下将天然气物质转化，得到制取氢气的原料气。在镍催化剂作用下其主要反应如下：
CH 4+H 2O----CO+3H 2–Q
CO+H 2O----CO 2+H 2+Q
甲烷在水蒸气重整转化反应的过程为吸热过程，反应的温度高达750～920℃，转化所需的热量由燃料气进行富氧燃烧化学反应后提供。
所述富氧燃烧制氢转换炉22生产的转化气经蒸汽发生器23换热生产蒸汽后，控制温度大约在300℃左右进入变换反应器24，在中变催化剂的作用下，一氧化碳与水蒸气发生如下反应：
CO+H 2O----CO 2+H 2+Q
CO变换反应为放热反应，反应温度在300℃对变换平衡有利，可得到较高的CO变换率，进而可提高单位原料的产氢量。为简化工艺流程，节省投资，在小规模的天然气转化制氢只采用一段变换。而在较大规模式则可以采用两段换热式转化技术，增加产品氢的收率。
而对天然气制得的氢气将采用变压吸附氢提纯工艺。变压吸附提纯工艺过程之所以得以实现是由于吸附剂在这种物理吸附中所具有的两个性质：一是对不同组分的吸附能力不同，二是吸附质在吸附剂上的吸附容量随吸附质的分压上升而增加，随吸附温度的上升而下降。利用吸附剂的第一个性质，可实现对含氢气源中杂质组分的优先吸附而实现氢提纯的目的；利用吸附剂的第二个性 质，可实现吸附剂在低温、高压下吸附而在高温、低压下解吸再生，从而构成吸附剂的吸附与再生循环，达到连续提氢的目的。所述PSA分离装置的解吸气经稳压后将送至转化炉作为燃料。
在普通空气助燃的情况下占比4/5的氮气并没有参与燃烧反应，在燃烧过程中带走大量热量，并且生成氮氧化物。本发明提出二氧化碳+纯氧替代空气助燃，可增加燃烧效率，并且最终产物只有二氧化碳与水将极大利于降低后续碳捕集的成本。
在CO 2浓度一定的情况下，降低液化温度和提高液化压力均有利于CO 2液化，在本发明的实施例中选择-30℃和3MPa更利于尾气组分的捕集。
我们采用的CO 2脱水装置是利用干燥剂吸附张力使气体的水分子被干燥剂内孔吸附而从二氧化碳中除去的方法。常用的干燥剂有硅胶、分子筛等，技术成熟可靠，脱水后干气含水量可低至1×10 -6，采用分子筛脱水后的干天然气水露点可低至-100℃，可以满足后续二氧化碳液化的露点要求，避免结冰堵塞冷箱流道。
CO 2液化冷箱由于CO 2的最佳液化点在-30℃左右，对冷却的温度要求并不高，因此可以采用多股流冷箱、或者蒸发式换热器等。
制冷装置由于CO 2的最佳液化点在-30℃左右，因此本制冷装置可以是R134a制冷循环系统、R410a制冷循环系统、R290(丙烷)制冷循环系统、R600a制冷循环系统等多种制冷循环中根据现场情况选择一种最为合适的工艺。
所属液态CO 2储罐是具备保冷功能的金属储罐，可以是真空粉末绝热、珍珠岩堆积绝、聚氨酯包覆绝热等方案来实现保冷绝热。
本装置除了可以用作清洁氢和可再生能源氢的联合生产系统外，也可以作为电网调峰储能设施。在白天的用电高峰时减小电解水功率对外输出电力，在 夜晚等用电低谷时可以增大电解水功率吸纳谷电，同时利用调节制氢氧气的供应可以调节烃类制氢规模对冲电解水制氢的波动，保障下游用氢气终端的平稳运行。

Claims (10)

  1. 一种基于可再生能源电解水和碳捕技术的联合制氢系统，其特征在于：包括光伏发电系统、风力发电系统、外部电网接入系统、电解水制氢系统、富氧燃烧制氢系统、二氧化碳捕集与液化系统、储能系统，其中：所述光伏发电系统、风力发电系统、外部电网接入系统、储能系统通过电力母线与电解水制氢系统连接；所述电解水制氢系统与富氧燃烧制氢系统连接，所述富氧燃烧制氢系统与二氧化碳捕集与液化系统连接。
  2. 根据权利要求1所述的一种基于可再生能源电解水和碳捕技术的联合制氢系统，其特征在于：所述电解水制氢系统包括依次连接的电解水装置、氢气提纯装置和氢气储存装置，所述电解水装置与氧气储存装置连接。
  3. 根据权利要求1所述的一种基于可再生能源电解水和碳捕技术的联合制氢系统，其特征在于：所述富氧燃烧制氢系统包括依次连接的富氧燃烧制氢转换炉、蒸汽发生器、变换反应器、蒸汽预热器、冷却分离器和PSA分离装置，所述富氧燃烧制氢转换炉与尾气换热器连接。
  4. 根据权利要求1所述的一种基于可再生能源电解水和碳捕技术的联合制氢系统，其特征在于：所述二氧化碳捕集与液化系统包括依次连接的一级压缩机、CO 2脱水装置、二级压缩机、CO 2液化冷箱、液态CO 2储罐，所述一级压缩机与CO 2缓冲储罐连接，所述液态CO 2储罐的气相与CO 2缓冲储罐连接。
  5. 根据权利要求4所述的一种基于可再生能源电解水和碳捕技术的联合制氢系统，其特征在于：所述CO 2脱水装置与冷凝水泵连接。
  6. 根据权利要求4所述的一种基于可再生能源电解水和碳捕技术的联合制氢系统，其特征在于：所述CO 2液化冷箱与制冷装置连接。
  7. 根据权利要求1所述的一种基于可再生能源电解水和碳捕技术的联合制氢系统，其特征在于：所述富氧燃烧制氢系统与液烃储存与供应系统连接。
  8. 根据权利要求7所述的一种基于可再生能源电解水和碳捕技术的联合制氢系统，其特征在于：所述液烃储存与供应系统包括液烃储罐和分别与液烃储罐连接的BOG压缩机、液烃增压泵和液烃主气化器，所述液烃增压泵的出口通过管道与液烃增压气化器入口相连，液烃增压气化器出口返回至液烃储罐。
  9. 根据权利要求1所述的一种基于可再生能源电解水和碳捕技术的联合制氢系统，其特征在于：所述电力母线为直流微电网母线，所述外部电网接入系统、风力发电系统分别通过第一AC/DC转换器、第二AC/DC转换器与直流微电网母线连接，所述光伏发电系统、储能系统、电解水制氢系统分别通过第一DC/DC转换器、第二DC/DC转换器、第三DC/DC转换器与直流微电网母线连接。
  10. 根据权利要求1所述的一种基于可再生能源电解水和碳捕技术的联合制氢系统，其特征在于：所述电力母线为交流微电网母线，所述外部电网接入系统、风力发电系统分别通过第一变压器、第二变压器与交流微电网母线连接，所述光伏发电系统、储能系统、电解水制氢系统分别通过DC/AC逆变器、AC/DC双向转换器、AC/DC转换器与交流微电网母线连接。
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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP7439368B2 (ja) 2023-04-11 2024-02-28 喜次 吉川 グリーンエネルギー輸送システム及びエネルギー輸送方法
GR20220100863A (el) * 2022-10-20 2024-05-16 Αλεξανδρος Χρηστου Παπαδοπουλος Παραγωγη υπερ-πρασινου υδρογονου και υπερ-πρασινων πτητικων βιομαζας για μειξη με φυσικο αεριο και ορυκτα καυσιμα για υπερ-πρασινη ηλεκτρικη ενεργεια, υπερ- πρασινα καυσιμα μεσων μεταφορας, δωρεαν αφαλατωση νερου και απανθρακοποιηση της βιομηχανιας

Families Citing this family (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113327180B (zh) * 2021-07-05 2023-09-29 华北电力大学 一种考虑氢能应用的电力系统低碳经济调度方法及系统
CN113824153A (zh) * 2021-10-29 2021-12-21 西安交通大学 一种地下空间支撑下的电力能源系统
CN114024326B (zh) * 2021-11-08 2024-01-23 西安热工研究院有限公司 一种可用于调峰的风光制氢耦合发电和储能系统及方法
CN114320490A (zh) * 2021-11-18 2022-04-12 中国大唐集团新能源科学技术研究院有限公司 一种基于可再生能源制氢的绿色能源化工系统
CN114123521A (zh) * 2021-11-22 2022-03-01 清华大学无锡应用技术研究院 一种针对可再生能源的电解氢与压缩二氧化碳联合储能系统
CN114247270A (zh) * 2021-12-14 2022-03-29 西安热工研究院有限公司 一种二氧化碳循环电吸附捕集及封存系统
CN115173444A (zh) * 2022-08-11 2022-10-11 内蒙古工业大学 一种风光可再生能源耦合氢储综合能源系统

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN207166137U (zh) * 2017-04-11 2018-03-30 赫普热力发展有限公司 一种应用清洁能源发电电解制氢注入燃气管网的系统
CN109687002A (zh) * 2018-11-13 2019-04-26 中广核研究院有限公司 一种分布式冷热电联供系统
CN110649650A (zh) * 2019-09-06 2020-01-03 华电电力科学研究院有限公司 一种可再生能源制氢与生物质气化耦合的发电系统及工作方法
CN111146803A (zh) * 2019-12-31 2020-05-12 国电龙源电力技术工程有限责任公司 一种弃风电解水制氢耦合燃煤发电系统
KR20200127384A (ko) * 2019-05-02 2020-11-11 울산대학교 산학협력단 수소생산 기능을 가지는 하이브리드 발전 시스템
CN112448413A (zh) * 2020-11-16 2021-03-05 成都精智艺科技有限责任公司 一种近零碳排放的分布式能源供给系统及方法

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP5280348B2 (ja) * 2009-12-25 2013-09-04 東京瓦斯株式会社 ハイブリッド水素製造システム
US20130133337A1 (en) * 2011-11-30 2013-05-30 General Electric Company Hydrogen assisted oxy-fuel combustion
CN110543157A (zh) * 2019-09-11 2019-12-06 中国石油工程建设有限公司 一种多能互补智慧供应热电氢的系统及方法

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN207166137U (zh) * 2017-04-11 2018-03-30 赫普热力发展有限公司 一种应用清洁能源发电电解制氢注入燃气管网的系统
CN109687002A (zh) * 2018-11-13 2019-04-26 中广核研究院有限公司 一种分布式冷热电联供系统
KR20200127384A (ko) * 2019-05-02 2020-11-11 울산대학교 산학협력단 수소생산 기능을 가지는 하이브리드 발전 시스템
CN110649650A (zh) * 2019-09-06 2020-01-03 华电电力科学研究院有限公司 一种可再生能源制氢与生物质气化耦合的发电系统及工作方法
CN111146803A (zh) * 2019-12-31 2020-05-12 国电龙源电力技术工程有限责任公司 一种弃风电解水制氢耦合燃煤发电系统
CN112448413A (zh) * 2020-11-16 2021-03-05 成都精智艺科技有限责任公司 一种近零碳排放的分布式能源供给系统及方法

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GR20220100863A (el) * 2022-10-20 2024-05-16 Αλεξανδρος Χρηστου Παπαδοπουλος Παραγωγη υπερ-πρασινου υδρογονου και υπερ-πρασινων πτητικων βιομαζας για μειξη με φυσικο αεριο και ορυκτα καυσιμα για υπερ-πρασινη ηλεκτρικη ενεργεια, υπερ- πρασινα καυσιμα μεσων μεταφορας, δωρεαν αφαλατωση νερου και απανθρακοποιηση της βιομηχανιας
JP7439368B2 (ja) 2023-04-11 2024-02-28 喜次 吉川 グリーンエネルギー輸送システム及びエネルギー輸送方法

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