CN116121786B - Solar-driven solid oxide electrolytic cell distributed poly-generation system and method - Google Patents
Solar-driven solid oxide electrolytic cell distributed poly-generation system and method Download PDFInfo
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- CN116121786B CN116121786B CN202310140186.XA CN202310140186A CN116121786B CN 116121786 B CN116121786 B CN 116121786B CN 202310140186 A CN202310140186 A CN 202310140186A CN 116121786 B CN116121786 B CN 116121786B
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- 239000007787 solid Substances 0.000 title claims abstract description 24
- 238000000034 method Methods 0.000 title claims description 9
- 239000007789 gas Substances 0.000 claims abstract description 124
- 238000005868 electrolysis reaction Methods 0.000 claims abstract description 70
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 56
- 239000001257 hydrogen Substances 0.000 claims abstract description 41
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 41
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 21
- 239000000126 substance Substances 0.000 claims abstract description 12
- 238000006243 chemical reaction Methods 0.000 claims abstract description 11
- 238000002407 reforming Methods 0.000 claims abstract description 10
- 238000005338 heat storage Methods 0.000 claims abstract description 9
- 238000005286 illumination Methods 0.000 claims abstract description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 85
- 150000003839 salts Chemical class 0.000 claims description 54
- 239000000446 fuel Substances 0.000 claims description 51
- 238000004519 manufacturing process Methods 0.000 claims description 17
- 239000003345 natural gas Substances 0.000 claims description 11
- 230000015572 biosynthetic process Effects 0.000 claims description 10
- 238000003786 synthesis reaction Methods 0.000 claims description 10
- 238000010438 heat treatment Methods 0.000 claims description 6
- 150000002431 hydrogen Chemical class 0.000 claims description 4
- 239000000376 reactant Substances 0.000 claims description 3
- 238000001816 cooling Methods 0.000 claims 1
- 230000002194 synthesizing effect Effects 0.000 claims 1
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 15
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
- 238000004146 energy storage Methods 0.000 description 5
- 230000005611 electricity Effects 0.000 description 4
- 239000004215 Carbon black (E152) Substances 0.000 description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 description 3
- 239000000306 component Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 239000003792 electrolyte Substances 0.000 description 3
- 229930195733 hydrocarbon Natural products 0.000 description 3
- 150000002430 hydrocarbons Chemical class 0.000 description 3
- 230000007774 longterm Effects 0.000 description 3
- 239000012528 membrane Substances 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- 239000002253 acid Substances 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 239000008358 core component Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 230000003750 conditioning effect Effects 0.000 description 1
- 230000010485 coping Effects 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 239000008236 heating water Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000006057 reforming reaction Methods 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 238000000629 steam reforming Methods 0.000 description 1
- 238000005979 thermal decomposition reaction Methods 0.000 description 1
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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
- C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
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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
- 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
- C25B1/042—Hydrogen or oxygen by electrolysis of water by electrolysis of steam
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- 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
- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1205—Composition of the feed
- C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
- C01B2203/1235—Hydrocarbons
- C01B2203/1241—Natural gas or methane
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- 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
- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1288—Evaporation of one or more of the different feed components
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- 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
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Abstract
The utility model discloses a solar-driven solid oxide electrolytic cell distributed poly-generation system, which comprises a double-tank heat storage module, a disc CSP high-temperature thermochemical reaction system and an SOEC system; when the illumination is sufficient, the electrolysis mode, namely an SOEC mode, is operated, and the photovoltaic array surplus power drives the electrolysis of the electric pile, and the electrolysis mode comprises two electrolysis modes of steam electrolysis and co-electrolysis which can be switched mutually; the disc CSP high temperature thermochemical reactor uses solar energy to provide heat required for methane external reforming, and converts the solar energy into chemical energy for storage. The disc CSP high-temperature thermochemical reactor is used for solving the problem of high-temperature environment required by external methane reforming, and the high-hydrogen mixed gas and hydrogen are prepared by adopting a co-electrolysis and steam electrolysis mode and stored.
Description
Technical Field
The utility model belongs to the field of energy storage and hydrogen energy, and particularly relates to a solar-driven solid oxide electrolytic cell distributed poly-generation system and method;
background
Energy storage has become a key issue in coping with the increasing deployment of renewable energy sources, especially wind and solar energy, due to the dynamics and intermittence of renewable energy sources and the frequent mismatch of renewable energy supply and demand. There are many energy storage technologies available for short-time power quality regulation and long-time bulk power management. Of these available technologies, only pumped-storage and compressed-air storage have been deployed and operated for large-scale long-term storage, and both technologies are impacted from strict geographic restrictions, very high capital investment, or low round trip efficiency. Therefore, the conversion of renewable electricity to synthetic methane for easy storage/transport by the electricity conversion methane technology (PtM) is considered a promising option for high density, high efficiency, long term energy storage, and multifunctional synthetic methane is also an important energy carrier and commodity, which can be used as clean, renewable transport/home hydrocarbon fuel for low formationCarbon or carbon neutralization makes a significant contribution to society. Accordingly, various PtM systems are currently being intensively studied, developed and exemplified, the core component of which is an electrolytic cell that uses electric power to electrochemically decompose water electricity into H 2 /O 2 And prevents gas remixing by selective membrane/electrolyte. Useful electrolysis techniques include primarily commercial low temperature (40-100 volume) alkaline or acid electrolyte electrolysis of water, and laboratory/exemplary high temperature (650-850 solution) solid oxide vapor electrolysis cells (SOEC). Alkaline cells are generally less efficient and energy density. The core competitiveness of alkaline cells is their high reliability and durability, low cost and long life up to 30 years. The electrolytic cell (PEME) of the acidic proton exchange membrane has high flexibility, quick dynamic response, higher efficiency, compact design and high current density. However, acid cells are more expensive and degrade faster and therefore have a shorter life of about 5 years due to the use of expensive proton exchange membranes and precious materials as catalysts. SOECs with high energy density have much higher electrical efficiency. One unique function of SOEC is to simultaneously convert steam and CO 2 Co-electrolytic decomposition to H 2 And CO, ultimately producing synthesis gas (syngas, H) 2 CO and CO 2 Is a dry mixture of (b) and (c). An important advantage of CO-electrolysis is by conditioning the steam and CO 2 To adjust the syngas composition to synthesize different hydrocarbon fuels. The investment cost of the current national enterprise galvanic pile is higher, but is expected to be greatly reduced along with mass production and technical progress, thereby having higher competitiveness.
Electricity conversion methane technology is considered a promising alternative for providing small or large scale, long term energy storage and opportunities for carbon dioxide utilization. The performance of the core component electrolyzer determines to a large extent the performance of the power conversion to methane system, and high temperature solid oxide electrolysis is attractive due to its inherent high electrical efficiency. More importantly, solid oxide electrolysis uniquely allows for the co-electrolysis of steam and carbon dioxide to produce synthesis gas whose composition can be readily and flexibly adjusted to synthesize different hydrocarbon fuels. For steam electrolysis and combined electrolysis, there is a tradeoff between system efficiency and methane yield: pursuing higher efficiency generally reduces methane production.
The utility model patent CN 208589494U published in 2018, 7 and 9 relates to a solid oxide fuel cell combined system based on solar energy methanol reforming hydrogen production, which comprises a methanol reforming hydrogen production subsystem, a solid oxide fuel cell subsystem and a humid air turbine circulation subsystem. According to the utility model, the methanol is subjected to thermal decomposition through absorbing medium-low temperature solar energy, and is subjected to steam reforming with the gas which is not completely reacted with the anode of the battery, so that the hydrogen yield of 75% is obtained, and the fuel is supplied to a combined system taking the SOFC and the gas turbine as cores. And a wet air turbine circulation system is adopted, so that the power generation efficiency is improved. Although the utility model can change methanol into methane or atomized fuel oil, the utility model is based on the characteristic of high hydrogen production yield of the combined system based on methanol reforming, and the hydrogen production rate after fuel change can not be ensured.
Disclosure of Invention
In order to solve the defects in the prior art, the utility model discloses a solar-driven solid oxide electrolytic cell distributed poly-generation system, which has the following technical scheme:
a solar-driven solid oxide electrolytic cell distributed poly-generation system uses a disc CSP high-temperature thermochemical reactor, uses clean solar energy to externally reform natural gas, converts the solar energy into chemical energy, synthesizes reformed high-temperature synthetic gas in sunshine time, firstly enters a molten salt heat exchanger for heat exchange and stores heat in a hot salt tank, and then enters a gas storage tank for storage. Under the condition of sufficient illumination, two different electrolysis modes are adopted to prepare hydrogen, and in the scheme one (the co-electrolysis mode), the co-electrolysis mode is driven by surplus power of the photovoltaic array to prepare high-hydrogen mixed gas, and the high-hydrogen mixed gas is stored in a gas storage tank. Scheme II (steam electrolysis) uses surplus electric power to drive a steam electrolysis mode to prepare hydrogen and then stores the hydrogen in a gas storage tank. The disc CSP high-temperature thermochemical reactor is used for solving the problem of high-temperature environment required by external methane reforming, and the high-hydrogen mixed gas and hydrogen are prepared by adopting a co-electrolysis and steam electrolysis mode and stored.
The solar-driven solid oxide electrolytic cell distributed poly-generation system comprises a double-tank heat storage module, a disc CSP high-temperature thermochemical reaction system and an SOEC system;
the double-tank heat storage module comprises a cold salt tank, a molten salt heat exchanger, a hot salt tank and a heat exchanger 5 which are dependently connected to form a circulating system;
in the disc CSP high-temperature thermochemical reaction system, a water tank is connected with a water pump, a tail gas heat exchanger and a heat exchanger in series; the disc CSP high-temperature thermochemical reactor is connected with the molten salt heat exchanger and the air storage tank in series;
the method for managing the gas at the fuel side outlet of the electric pile of the system comprises the following steps that the gas at the fuel side outlet of the electric pile firstly heats the synthetic gas through a fuel side heat exchanger, then circulating water separated through a steam-water separator enters a water tank, and the separated gas enters a gas storage tank for storage. The high-temperature gas discharged by the air electrode of the electric pile firstly enters the air side heat exchanger to heat the air after pressure boosting, and then enters the tail gas heat exchanger to heat water from the water tank.
The SOEC system component connection mode is as follows:
when the co-electrolysis mode is adopted, the disc CSP high-temperature thermochemical reactor is connected with the molten salt heat exchanger, the first valve, the fuel side heat exchanger and the galvanic pile in series;
when steam electrolysis is adopted, the steam generator is connected with the second valve, the fuel side heat exchanger and the electric pile in series;
in the two electrolysis modes, the air side connection modes are the same, and the air compressor is connected with the air side heat exchanger, the air side electric heater, the electric pile and the tail gas heat exchanger in series.
The co-production method of the solar-driven solid oxide electrolytic cell distributed poly-production system comprises the following steps:
when the illumination is sufficient, the electrolysis mode, namely an SOEC mode, is operated, and the photovoltaic array surplus power drives the electrolysis of the electric pile, and the electrolysis mode comprises two electrolysis modes of steam electrolysis and co-electrolysis which can be switched mutually; the disc CSP high-temperature thermochemical reactor uses solar energy to provide heat required by external methane reforming, converts the solar energy into chemical energy to be stored, and simultaneously stores the heat for heating water from a water tank;
specifically, the flow of the system components is as follows:
in the co-electrolysis mode: the water in the water tank is heated into steam through the tail gas heat exchanger and the heat exchanger after passing through the water pump, then enters the disc CSP high-temperature thermal chemical reactor to be externally reformed with natural gas to generate high-temperature synthetic gas, the high-temperature synthetic gas enters the molten salt heat exchanger to exchange heat, molten salt in the cold salt tank enters the molten salt heat exchanger to be heated and then enters the hot salt tank to store heat, and a part of cooled synthetic gas enters the gas storage tank to store; at the moment, the first valve is opened, the second valve is closed, and the other part of the synthesis gas sequentially passes through the first valve, the fuel side heat exchanger and the fuel side electric heater to be further heated and then enters a fuel electrode of the electric pile; the air is boosted to an air side heat exchanger through an air compressor to be heated, and then enters a pile air electrode through an air side electric heater; and introducing surplus power of the photovoltaic array into a pile to generate a co-electrolysis reaction, discharging high-hydrogen mixed gas containing unreacted water vapor and hydrogen from a pile reactant electrode, heating the heat-stored synthetic gas through a fuel side heat exchanger, then entering a steam-water separator, enabling separated water to enter a water tank for recycling, and enabling the high-hydrogen mixed gas to enter a gas storage tank for storage. The high-temperature gas discharged by the air electrode of the electric pile firstly enters the air side heat exchanger to heat the air after pressure boosting, and then enters the tail gas heat exchanger to heat water from the water tank.
In the steam electrolysis mode: the water in the water tank is heated into steam through the tail gas heat exchanger and the heat exchanger after passing through the water pump, a part of steam enters the disc CSP high-temperature thermal chemical reactor to be externally reformed with natural gas to generate high-temperature synthetic gas, the high-temperature synthetic gas enters the molten salt heat exchanger to exchange heat, molten salt in the cold salt tank enters the molten salt heat exchanger through the molten salt pump to be heated, then enters the hot salt tank to store heat, and the cooled synthetic gas enters the gas storage tank to store; at the moment, the first valve is closed, the second valve is opened, and the other part of steam is heated up further through the second valve, the fuel side heat exchanger and the fuel side electric heater and then enters the fuel electrode of the electric pile; the air is boosted to an air side heat exchanger through an air compressor to be heated, and then enters a pile air electrode through an air side electric heater; excess electric power of the photovoltaic array is fed into a pile to generate steam electrolysis reaction, the pile fuel electrode discharges water vapor and hydrogen which contain unreacted water vapor and are heated by a fuel side heat exchanger from a second valve, the water vapor enters a steam-water separator, separated water enters a water tank to be recycled, and the separated hydrogen enters a gas storage tank to be stored. The high-temperature gas discharged by the air electrode of the electric pile firstly enters the air side heat exchanger to heat the air after pressure boosting, and then enters the tail gas heat exchanger to heat water from the water tank. The steam generator is used as a means for heating steam when the tail gas heat exchanger and the heat exchanger 5 fail.
The system provided by the utility model has the advantages that the disc CSP high-temperature thermochemical reactor works at the temperature of about 700 ℃, methane and water are subjected to reforming reaction in the reactor, the methane is upgraded, and the solar energy is converted into chemical energy to be stored.
The utility model has the following characteristics and beneficial effects:
(1) External methane reforming is carried out on natural gas or hydrogen-doped natural gas from a natural gas pipeline through a disc CSP high-temperature thermal chemical reactor, solar heat is stored as chemical energy, enough synthetic gas is produced by utilizing the time of day, and reformed synthetic gas is stored in a gas storage tank;
(2) The heat of the high-temperature synthesis gas from the disc CSP high-temperature thermal chemical reactor is stored by using a double-tank molten salt heat storage technology, and the water from the water tank is heated into water vapor together with the tail gas heat exchanger.
(3) Under the condition of sufficient illumination, the co-electrolysis mode or the steam electrolysis mode is used for preparing high-hydrogen mixed gas or hydrogen through the surplus power driving co-electrolysis mode of the photovoltaic array, and meanwhile, the high-hydrogen mixed gas or the hydrogen is stored in the gas storage tank, and the two modes can be switched by using a valve switch to select which mode to use according to the requirement.
Drawings
FIG. 1 is a schematic diagram of the system of the present utility model.
FIG. 2-1 is a schematic diagram of the co-electrolysis mode of the system of the present utility model.
FIG. 2-2 is a schematic diagram of the steam electrolysis mode of the system of the present utility model.
In the figure: 1-dish CSP high temperature thermochemical reactor, 2-water tank, 3-water pump, 4-tail gas heat exchanger, 5-heat exchanger, 6-molten salt heat exchanger, 7-hot salt tank, 8-cold salt tank, 9-gas holder, 10-fuel side heat exchanger, 11-fuel side electric heater, 12-galvanic pile, 13-air compressor, 14-air side heat exchanger, 15-air side electric heater, 16-steam-water separator, 17-photovoltaic array, 18-steam generator, 19-first valve, 20-second valve.
Detailed description of the preferred embodiments
The present utility model provides a co-electrolysis mode and a steam electrolysis mode of a solar-driven solid oxide electrolysis cell distributed polygeneration system, and the description below is made with reference to the accompanying drawings, wherein the described examples are only some examples, but not all examples of the present utility model. All other embodiments, which are suggested to one skilled in the art based on the embodiments of the present utility model without creative efforts, fall within the protection scope of the present utility model.
As shown in fig. 1, a solar-driven solid oxide electrolytic cell distributed poly-generation system comprises a double-tank heat storage module, a disc type CSP (compact strip reactor) thermochemical reaction system and an SOEC (solid oxide electrolyte) system;
the double-tank heat storage module comprises a cold salt tank 8, a molten salt heat exchanger 6, a hot salt tank 7 and a heat exchanger 5 which are dependently connected to form a circulating system;
in the disc CSP high-temperature thermochemical reaction system, a water tank 2 is connected with a water pump 3, a tail gas heat exchanger 4 and a heat exchanger 5 in series; the disc CSP high-temperature thermochemical reactor 1 is connected with the molten salt heat exchanger 6 and the air storage tank 9 in series;
the method for managing the fuel side outlet gas of the system pile comprises the following steps that the fuel side outlet gas of the pile 12 firstly heats the synthetic gas through a fuel side heat exchanger 10, then circulating water separated through a steam-water separator 16 enters a water tank 2, and the separated gas enters a gas storage tank 9 for storage. The high-temperature gas discharged by the air electrode of the electric pile 12 firstly enters the air side heat exchanger 14 to heat the boosted air, and then enters the tail gas heat exchanger 4 to heat the water from the water tank 2.
The SOEC system component connection mode is as follows:
as shown in fig. 2-1, when the co-electrolysis mode is adopted, the disc type CSP high temperature thermochemical reactor 1 is connected in series with the molten salt heat exchanger 6, the first valve 19, the fuel side heat exchanger 10, and the stack 12;
as shown in fig. 2-2, when steam electrolysis is employed, the steam generator 18 is connected in series with the second valve 20, the fuel side heat exchanger 10, the stack 12;
in the two electrolysis modes, the air side connection modes are the same, and the air compressor 13 is connected in series with the air side heat exchanger 14, the air side electric heater 15, the electric pile 12 and the tail gas heat exchanger 4.
As shown in fig. 2-1, in the working flow of the co-electrolysis mode of the solar-driven solid oxide electrolytic cell distributed poly-generation system, water in a water tank 2 is heated into steam through a tail gas heat exchanger 4 and a heat exchanger 5 after passing through a water pump 3 and then enters a disc type CSP high-temperature thermochemical reactor 1, and CH is externally reformed with natural gas at 700 ℃ high temperature 4 +H 2 O→CO 2 +H 2 High temperature synthesis gas (steam, H) 2 、CH 4 、CO 2 CO), the high-temperature synthesis gas enters a molten salt heat exchanger 6 for heat exchange, molten salt in a cold salt tank 8 enters the molten salt heat exchanger 6 for heating and then enters a hot salt tank 7 for heat storage, after being cooled to 200 ℃ and part of the synthesis gas enters a gas storage tank 9 for storage; at this time, the first valve 19 is opened, the second valve 20 is closed, and the other part of the synthesis gas sequentially passes through the first valve 19, the fuel side heat exchanger 10 and the fuel side electric heater 11, and then is heated up further and enters the fuel electrode of the electric pile 12; the air is boosted to an air side heat exchanger 14 through an air compressor 13 to be heated, and then enters an air electrode of the electric pile 12 through an air side electric heater 15; excess electric power of the photovoltaic array 17 is fed into the pile 12 to generate a co-electrolysis reaction, the reactant electrode of the pile 12 discharges high-hydrogen mixed gas containing unreacted water vapor and hydrogen, the high-hydrogen mixed gas is heated by the fuel side heat exchanger 10 to store heat, the synthesis gas enters the steam-water separator 16, the separated water enters the water tank 2 for recycling, and the high-hydrogen mixed gas enters the gas storage tank 9 for storage. The high-temperature gas discharged from the air electrode of the electric pile 12 firstly enters the air side heat exchanger 14 to heat the air after pressure boosting, and the high-temperature tail gas about 300 ℃ after heating enters the tail gas heat exchanger 4 to heat the water from the water tank 2.
As shown in fig. 2-2, in the working flow of the steam electrolysis mode of the solar-driven solid oxide electrolytic cell distributed poly-generation system, water in a water tank 2 is heated into steam through a tail gas heat exchanger (4) and a heat exchanger 5 after passing through a water pump 3, part of the steam enters a disc CSP high-temperature thermochemical reactor 1 to externally reform with natural gas at 700 ℃ to react with CH4+H2OCO2+H2, high-temperature synthetic gas (steam, H2, CH4, CO2 and CO) is generated, the high-temperature synthetic gas enters a molten salt heat exchanger 6 to exchange heat, molten salt in a cold salt tank 8 enters the molten salt heat exchanger 6 to be heated and then enters a hot salt tank 7 to be stored, the heat is cooled to 200, and the left and right synthetic gas enters a gas storage tank 9 to be stored; at this time, the first valve 19 is closed, the second valve 20 is opened, and the other part of steam is heated up further by the second valve 20, the fuel side heat exchanger 10 and the fuel side electric heater 11 and then enters the fuel electrode of the electric pile 12; the air is boosted to an air side heat exchanger 14 through an air compressor 13 to be heated, and then enters an air electrode of the electric pile 12 through an air side electric heater 15; excess electric power of the photovoltaic array 17 is fed into the electric pile 12 to generate steam electrolysis reaction, the electric pile 12 fuel electrode discharge contains unreacted steam and hydrogen, the steam from the second valve 20 is heated by the fuel side heat exchanger 10, then the steam enters the steam-water separator 16, the separated water enters the water tank 2 for recycling, and the separated hydrogen enters the gas storage tank 9 for storage. The high-temperature gas discharged by the air electrode of the electric pile 12 firstly enters the air side heat exchanger 14 to heat the air after pressure boosting, and the high-temperature tail gas with the pressure of about 300 is then enters the tail gas heat exchanger 4 to heat the water from the water tank 2. The steam generator 18 serves as a means for heating the steam in the event of a failure of the off-gas heat exchanger 4 and the heat exchanger 5.
The foregoing has shown and described the basic principles, principal features and advantages of the utility model. It will be understood by those skilled in the art that the present utility model is not limited to the embodiments described above, and that the above embodiments and descriptions are merely illustrative of the principles of the present utility model, and various changes and modifications may be made therein without departing from the spirit and scope of the utility model, which is defined by the appended claims. The scope of the utility model is defined by the appended claims and equivalents thereof.
Claims (3)
1. The co-production method of the solar-driven solid oxide electrolytic cell distributed poly-production system adopts the solar-driven solid oxide electrolytic cell distributed poly-production system, and comprises a double-tank heat storage module, a disc CSP high-temperature thermochemical reaction system and an SOEC system;
the double-tank heat storage module comprises a cold salt tank (8), a molten salt heat exchanger (6), a hot salt tank (7) and a heat exchanger (5) which are dependently connected to form a circulating system;
in the disc CSP high-temperature thermochemical reaction system, a water tank (2) is connected with a water pump (3), a tail gas heat exchanger (4) and a heat exchanger (5) in series; the disc CSP high-temperature thermochemical reactor (1) is connected in series with the molten salt heat exchanger (6) and the air storage tank (9);
the method for managing the fuel side outlet gas of the electric pile (12) of the system comprises the following steps that the fuel side outlet gas of the electric pile (12) firstly heats the synthetic gas through a fuel side heat exchanger (10), then circulating water separated through a steam-water separator (16) enters a water tank (2), and the separated gas enters a gas storage tank (9) for storage; the high-temperature gas discharged by the air electrode of the electric pile (12) firstly enters the air side heat exchanger (14) to heat the air after pressure boosting, and then enters the tail gas heat exchanger (4) to heat water from the water tank (2);
the SOEC system component connection mode is as follows:
when the co-electrolysis mode is adopted, the disc CSP high-temperature thermochemical reactor (1) is connected with the molten salt heat exchanger (6), the first valve (19), the fuel side heat exchanger (10) and the electric pile (12) in series;
when steam electrolysis is adopted, the steam generator (18) is connected with the second valve (20), the fuel side heat exchanger (10) and the electric pile (12) in series;
in the two electrolysis modes, the air side connection modes are the same, and the air compressor (13) is connected in series with the air side heat exchanger (14), the air side electric heater (15), the electric pile (12) and the tail gas heat exchanger (4);
the method is characterized by comprising the following steps: the method comprises the steps of using a disc CSP high-temperature thermochemical reactor, externally reforming natural gas by using clean solar energy, converting the solar energy into chemical energy, synthesizing reformed high-temperature synthetic gas in sunlight time, cooling the synthetic gas in a molten salt heat exchanger, storing heat in a hot salt tank, and storing the cooled synthetic gas in a gas storage tank; under the condition of sufficient illumination, two different electrolysis modes are adopted to prepare hydrogen, the scheme one, the co-electrolysis mode, the high-hydrogen mixed gas is prepared by the excessive electric power driving co-electrolysis mode of the photovoltaic array, and the high-hydrogen mixed gas is stored in a gas storage tank; secondly, steam electrolysis is carried out, and hydrogen is prepared by using an excessive electric power driven steam electrolysis mode and then stored in a gas storage tank; the disc CSP high-temperature thermochemical reactor is used for solving the problem of high-temperature environment required by external methane reforming, and the high-hydrogen mixed gas and hydrogen are prepared by adopting a co-electrolysis and steam electrolysis mode and stored.
2. The co-production method of a solar-driven solid oxide electrolysis cell distributed poly-production system according to claim 1, wherein the co-production method is characterized in that: the system flow of the co-electrolysis mode of the solar-driven solid oxide electrolysis cell distributed poly-generation system is as follows: the water in the water tank (2) is heated into steam through the tail gas heat exchanger (4) and the heat exchanger (5) after passing through the water pump (3), then enters the disc CSP high-temperature thermal chemical reactor (1) to be externally reformed with natural gas to generate high-temperature synthetic gas, the high-temperature synthetic gas enters the molten salt heat exchanger (6) to exchange heat, molten salt in the cold salt tank (8) enters the molten salt heat exchanger (6) to be heated and then enters the hot salt tank (7) to store heat, and a part of cooled synthetic gas enters the gas storage tank (9) to store; at the moment, the first valve (19) is opened, the second valve (20) is closed, and the other part of the synthesis gas sequentially passes through the first valve (19), the fuel side heat exchanger (10) and the fuel side electric heater (11) to be heated up further and then enters a fuel electrode of the electric pile (12); the air is boosted to an air side heat exchanger (14) through an air compressor (13) to be heated, and then enters an air electrode of the electric pile (12) through an air side electric heater (15); excess electric power of the photovoltaic array (17) is fed into the electric pile (12) to generate a co-electrolysis reaction, high-hydrogen mixed gas containing unreacted water vapor and hydrogen is discharged from reactant electrodes of the electric pile (12), heated and stored by the fuel side heat exchanger (10), and then enters the steam-water separator (16), the separated water enters the water tank (2) to be recycled, and the high-hydrogen mixed gas enters the gas storage tank (9) to be stored; the high-temperature gas discharged by the air electrode of the electric pile (12) firstly enters the air side heat exchanger (14) to heat the air after pressure boosting, and then enters the tail gas heat exchanger (4) to heat the water from the water tank (2).
3. The co-production method of a solar-driven solid oxide electrolysis cell distributed poly-production system according to claim 1, wherein the co-production method is characterized in that: the system flow of the steam electrolysis mode of the solar-driven solid oxide electrolysis cell distributed poly-generation system is as follows: the water in the water tank (2) is heated into steam through the tail gas heat exchanger (4) and the heat exchanger (5) after passing through the water pump (3), a part of steam enters the disc CSP high-temperature thermal chemical reactor (1) to be externally reformed with natural gas to generate high-temperature synthetic gas, the high-temperature synthetic gas enters the molten salt heat exchanger (6) to exchange heat, molten salt in the cold salt tank (8) enters the molten salt heat exchanger (6) to be heated and then enters the hot salt tank (7) to store heat, and the cooled synthetic gas enters the gas storage tank (9) to store; at the moment, the first valve (19) is closed, the second valve (20) is opened, and the other part of steam enters the fuel electrode of the electric pile (12) after being further heated by the second valve (20), the fuel side heat exchanger (10) and the fuel side electric heater (11); the air is boosted to an air side heat exchanger (14) through an air compressor (13) to be heated, and then enters an air electrode of the electric pile (12) through an air side electric heater (15); excess electric power of the photovoltaic array (17) is introduced into the electric pile (12) to generate steam electrolysis reaction, unreacted steam and hydrogen contained in fuel electrode discharge of the electric pile (12) are heated by the fuel side heat exchanger (10) and come from the second valve (20), then the steam enters the steam-water separator (16), the separated water enters the water tank (2) to be recycled, and the separated hydrogen enters the gas storage tank (9) to be stored; the high-temperature gas discharged by the air electrode of the electric pile (12) firstly enters the air side heat exchanger (14) to heat the air after pressure boosting, and then enters the tail gas heat exchanger (4) to heat water from the water tank (2); the steam generator (18) is used as a steam heating means when the tail gas heat exchanger (4) and the heat exchanger (5) are in fault.
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