CN113463113A - Photovoltaic and chemical heat pump coupled solar high-temperature water electrolysis hydrogen production system and process - Google Patents
Photovoltaic and chemical heat pump coupled solar high-temperature water electrolysis hydrogen production system and process Download PDFInfo
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 111
- 239000001257 hydrogen Substances 0.000 title claims abstract description 64
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 64
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 63
- 239000000126 substance Substances 0.000 title claims abstract description 45
- 238000005868 electrolysis reaction Methods 0.000 title claims abstract description 31
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 29
- 238000000034 method Methods 0.000 title abstract description 8
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 25
- 239000001301 oxygen Substances 0.000 claims abstract description 25
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 25
- 125000002924 primary amino group Chemical group [H]N([H])* 0.000 claims abstract description 18
- 238000010248 power generation Methods 0.000 claims abstract description 16
- 230000008878 coupling Effects 0.000 claims abstract description 4
- 238000010168 coupling process Methods 0.000 claims abstract description 4
- 238000005859 coupling reaction Methods 0.000 claims abstract description 4
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 62
- 239000007789 gas Substances 0.000 claims description 38
- 229910021529 ammonia Inorganic materials 0.000 claims description 23
- 238000006243 chemical reaction Methods 0.000 claims description 22
- 239000003990 capacitor Substances 0.000 claims description 21
- 238000000354 decomposition reaction Methods 0.000 claims description 15
- 238000005286 illumination Methods 0.000 claims description 12
- 230000002457 bidirectional effect Effects 0.000 claims description 9
- 239000003792 electrolyte Substances 0.000 claims description 4
- 238000003786 synthesis reaction Methods 0.000 claims description 4
- 229910001233 yttria-stabilized zirconia Inorganic materials 0.000 claims description 4
- 238000000926 separation method Methods 0.000 claims description 3
- MCMNRKCIXSYSNV-UHFFFAOYSA-N ZrO2 Inorganic materials O=[Zr]=O MCMNRKCIXSYSNV-UHFFFAOYSA-N 0.000 claims description 2
- HBAGRTDVSXKKDO-UHFFFAOYSA-N dioxido(dioxo)manganese lanthanum(3+) Chemical compound [La+3].[La+3].[O-][Mn]([O-])(=O)=O.[O-][Mn]([O-])(=O)=O.[O-][Mn]([O-])(=O)=O HBAGRTDVSXKKDO-UHFFFAOYSA-N 0.000 claims description 2
- 229910002119 nickel–yttria stabilized zirconia Inorganic materials 0.000 claims description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 abstract 2
- 229910002092 carbon dioxide Inorganic materials 0.000 abstract 1
- 239000001569 carbon dioxide Substances 0.000 abstract 1
- 238000012544 monitoring process Methods 0.000 description 6
- 230000005855 radiation Effects 0.000 description 5
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- 238000006460 hydrolysis reaction Methods 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 3
- 230000003287 optical effect Effects 0.000 description 3
- 230000002441 reversible effect Effects 0.000 description 3
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 2
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 2
- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical compound CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 description 2
- BAVYZALUXZFZLV-UHFFFAOYSA-N Methylamine Chemical compound NC BAVYZALUXZFZLV-UHFFFAOYSA-N 0.000 description 2
- 239000001110 calcium chloride Substances 0.000 description 2
- 229910001628 calcium chloride Inorganic materials 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 239000007772 electrode material Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000002808 molecular sieve Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 239000000376 reactant Substances 0.000 description 2
- 238000007086 side reaction Methods 0.000 description 2
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 2
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000004146 energy storage Methods 0.000 description 1
- 239000008236 heating water Substances 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000035939 shock Effects 0.000 description 1
- 239000007787 solid Substances 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
- 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
-
- 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
- C25B11/00—Electrodes; Manufacture thereof not otherwise provided for
- C25B11/04—Electrodes; Manufacture thereof not otherwise provided for characterised by the material
- C25B11/042—Electrodes formed of a single material
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B15/00—Operating or servicing cells
- C25B15/02—Process control or regulation
- C25B15/021—Process control or regulation of heating or cooling
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
- C25B9/60—Constructional parts of cells
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
- C25B9/60—Constructional parts of cells
- C25B9/65—Means for supplying current; Electrode connections; Electric inter-cell connections
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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
- C25B9/60—Constructional parts of cells
- C25B9/67—Heating or cooling means
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- H—ELECTRICITY
- H02—GENERATION; CONVERSION OR DISTRIBUTION OF ELECTRIC POWER
- H02S—GENERATION OF ELECTRIC POWER BY CONVERSION OF INFRARED RADIATION, VISIBLE LIGHT OR ULTRAVIOLET LIGHT, e.g. USING PHOTOVOLTAIC [PV] MODULES
- H02S40/00—Components or accessories in combination with PV modules, not provided for in groups H02S10/00 - H02S30/00
- H02S40/40—Thermal components
- H02S40/44—Means to utilise heat energy, e.g. hybrid systems producing warm water and electricity at the same time
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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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E10/00—Energy generation through renewable energy sources
- Y02E10/50—Photovoltaic [PV] energy
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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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E10/00—Energy generation through renewable energy sources
- Y02E10/60—Thermal-PV hybrids
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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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis
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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
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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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
Abstract
The invention discloses a photovoltaic and chemical heat pump coupled solar high-temperature water electrolysis hydrogen production system and a process thereof, wherein the system comprises a photovoltaic power generation system, an amino chemical heat pump system and a high-temperature oxide electrolytic cell electrolytic water system, the photovoltaic power generation system is connected with the high-temperature oxide electrolytic cell electrolytic water system, the high-temperature oxide electrolytic cell electrolytic water system is coupled with the amino chemical heat pump system through a third heat exchanger, the photovoltaic power generation system converts solar energy into electric energy to provide electric energy for the high-temperature oxide electrolytic cell electrolytic water system, the amino chemical heat pump system converts the solar energy into chemical energy and heat energy in sequence to provide heat energy for the high-temperature oxide electrolytic cell electrolytic water system, and water electrolysis is performed to generate oxygen and hydrogen. The invention realizes zero carbon dioxide emission by coupling the photovoltaic power generation system, the amino chemical heat pump system and the high-temperature oxide electrolytic cell electrolytic water system.
Description
Technical Field
The invention belongs to the technical field of hydrogen production by water electrolysis, and particularly relates to a photovoltaic and chemical heat pump coupled solar high-temperature water electrolysis hydrogen production system and process.
Background
Compared with renewable energy sources such as wind energy, geothermal energy, biological energy and the like, the solar energy has the unique advantages of rich sources, wide application and the like: annual earth surface reception of 3.9 x 1024Total of 18.92 multiplied by 10 of MJ solar energy converted into standard coal7Billion tons, only 1% of which are needed to meet the energy needs of all mankind. However, solar energy utilization is limited by time and space: the solar radiation energy varies with day, night, season, latitude and altitude. The solar hydrogen production process converts and stores solar energy in the chemical energy of hydrogen, and can overcome the intermittency and the regionality of solar energy utilization. On the other hand, solar energy is the only input energy, H2O is the only raw material gas to realize zero CO2Preparing discharged green hydrogen.
Most of the traditional photovoltaic water electrolysis hydrogen production systems are low-temperature water electrolysis systems (LTE) coupled with the photovoltaic systems, and compared with LTE, in recent years with the development of Solid Oxide Electrolytic Cells (SOEC), the high-temperature water electrolysis (HTE) technology becomes a hydrogen production technology with great potential by virtue of the advantages of higher efficiency, better reaction kinetics, lower electric energy requirement and the like. At present, solar high-temperature electrolytic water canThe solar photovoltaic solar thermal power generation system is realized by combining photo-thermal and photovoltaic photo-thermal modes. Since photovoltaic power generation efficiency is generally higher than photo-thermal, photovoltaic photo-thermal bonding has more potential: the photovoltaic system provides electric energy, the photothermal system provides heat energy (high-temperature steam), and complementation of the electric energy and the heat energy in the solar hydrogen production process is realized. The SOEC operation temperature is 700-. Meanwhile, since the direct solar radiation intensity changes with time during a day, heating water vapor directly by the light condensing device causes fluctuation of the temperature of high-temperature water vapor, thereby generating thermal shock on the SOEC electrode material to influence the service life of the SOEC electrode material. Relatively simple and extensive utilization of high-grade photo-thermal to directly heat water, NH3/N2/H2The system chemical heat pump has the advantages of improving the quality and the efficiency of relatively low-grade photo-thermal and providing stable high-temperature water vapor for the SOEC.
The chemical heat pump is a device for realizing energy transfer by means of reversible reaction, and can convert low-grade heat energy into high-grade heat energy by utilizing the difference of endothermic and exothermic reaction temperatures. By utilizing the time difference of the positive and negative processes, the chemical heat pump system also has the function of stable energy storage at normal temperature. The chemical heat pump can be divided into complex reaction systems such as calcium chloride/methanol, calcium chloride/methylamine and the like according to different chemical reactions; chemisorption systems such as molecular sieve/water, molecular sieve/ammonia, and the like; catalytic reaction systems such as cyclohexane/benzene, acetone/isopropanol, and the like. By NH3Compared with other systems, the chemical heat pump system based on the reversible reaction has the advantages of simple reaction, no side reaction, sufficient reactants and the like.
Disclosure of Invention
In order to solve the problems, the invention aims to provide a photovoltaic and chemical heat pump coupled solar high-temperature water electrolysis hydrogen production system and process.
In order to achieve the purpose, the following technical scheme is provided:
the photovoltaic and chemical heat pump coupled solar high-temperature water electrolysis hydrogen production system comprises a photovoltaic power generation system, an amino chemical heat pump system and a high-temperature oxide electrolytic cell electrolytic water system, wherein the photovoltaic power generation system is connected with the high-temperature oxide electrolytic cell electrolytic water system, and the high-temperature oxide electrolytic cell electrolytic water system is coupled with the amino chemical heat pump system through a third heat exchanger.
Furthermore, the photovoltaic power generation system comprises a photovoltaic panel array, a one-way controller, a two-way controller, a super capacitor and a controller, wherein the output end of the photovoltaic panel array is connected with the input end of the one-way controller, the output end of the one-way controller is connected with the controller through a first lead, the super capacitor is connected with the two-way controller in two ways, the two-way controller is connected with the first lead through a two-way lead, and the controller is connected with the high-temperature oxide electrolytic cell water electrolysis system.
Further, the high-temperature oxide electrolytic cell water electrolysis system comprises a high-temperature oxide electrolytic cell, a fourth heat exchanger, a first separator, a second separator, a water tank, a third delivery pump, an oxygen collecting tank and a hydrogen collecting tank, wherein a controller is connected with the high-temperature oxide electrolytic cell, the water tank is connected with a cold end inlet of the fourth heat exchanger through the third delivery pump, a cold end outlet of the fourth heat exchanger is connected with a cold end inlet of the third heat exchanger, a cold end outlet of the third heat exchanger is connected with the high-temperature oxide electrolytic cell through a second pipeline, a negative electrode of the high-temperature oxide electrolytic cell is connected with the first separator through the fourth heat exchanger, an upper outlet of the first separator is connected with the oxygen collecting tank, an anode of the high-temperature oxide electrolytic cell is connected with the second separator through the fourth heat exchanger, and an upper outlet of the second separator is connected with the hydrogen collecting tank.
Furthermore, the lower outlet of the second separator is connected with the water tank through a first pipeline, and the lower outlet pipeline of the first separator and the first pipeline are converged into a pipeline and then connected with the water tank.
Furthermore, the upper outlet of the second separator is divided into two pipelines, one pipeline is connected with the hydrogen collecting tank, and the other pipeline is connected with the second pipeline between the third heat exchanger and the high-temperature oxide electrolytic cell.
Furthermore, a third heat exchanger is coupled with an amino chemical heat pump system, the amino chemical heat pump system comprises a heliostat field, an endothermic reactor, a first heat exchanger, a first delivery pump, a storage tank, a second delivery pump, a second heat exchanger and an exothermic reactor, the endothermic reactor, the first heat exchanger and the storage tank are sequentially connected to form a circulation loop, the first delivery pump is arranged on an output pipeline of the storage tank connected with the first heat exchanger, the second delivery pump, the second heat exchanger, the exothermic reactor and a hot end inlet of the third heat exchanger are sequentially connected with another output pipeline of the storage tank, a hot end outlet of the third heat exchanger is connected with a hot end inlet of the second heat exchanger, and a hot end outlet of the second heat exchanger is connected with the storage tank.
A solar high-temperature water electrolysis hydrogen production process with coupling of photovoltaic and chemical heat pump comprises the following steps:
1) sunlight is reflected to the endothermic reactor from the heliostat field, liquid ammonia in the storage tank is conveyed to the first heat exchanger by the first conveying pump, enters the endothermic reactor through the first heat exchanger to absorb the solar energy gathered from the heliostat field, and simultaneously carries out ammonia decomposition endothermic reaction, and N generated by the reaction2And H2Flows back to the storage tank through the first heat exchanger, N2And H2The ammonia is conveyed to a second heat exchanger by a second conveying pump and enters an exothermic reactor through the second heat exchanger to carry out synthetic ammonia reaction; the ammonia generated by the reaction flows out of the exothermic reactor to exchange heat with the third heat exchanger to provide heat energy for the exothermic reactor, then enters the storage tank after exchanging heat with the second heat exchanger, and the steps are repeated in such a way to continuously provide heat energy for the high-temperature oxide electrolytic cell water electrolysis system;
2) the photovoltaic panel array absorbs solar energy and converts the solar energy into electric energy which is transmitted to the one-way controller, when the illumination is sufficient, the one-way controller transmits the electric energy to the two-way controller and the controller respectively, the two-way controller transmits the electric energy to the super capacitor for storage, and the controller transmits the electric energy to the high-temperature oxide electrolytic cell to provide the electric energy; when the illumination is insufficient, the electric energy stored in the super capacitor is transmitted to the controller through the bidirectional controller, and the controller transmits the electric energy to the high-temperature oxide electrolytic cell;
3) the water in the water tank is conveyed to a fourth heat exchanger through a third conveying pump for heat exchange to reach a critical state, the water is subjected to heat exchange through the third heat exchanger to reach an overheated state, high-temperature water vapor in the overheated state is conveyed to a high-temperature oxide electrolytic cell for electrolysis, a mixed gas of hydrogen and water vapor generated by a negative electrode enters the fourth heat exchanger for heat exchange and cooling, the mixed gas enters a second separator for separation after heat exchange, the separated condensed water enters the water tank along a first pipeline to participate in circulation, the hydrogen is discharged from an upper gas outlet of the second separator and is divided into two pipelines, one pipeline is introduced into a hydrogen collecting tank for storage, and the other pipeline is introduced into the high-temperature oxide electrolytic cell to keep the reduction state of the negative electrode; oxygen and a small amount of water vapor generated by the anode of the high-temperature oxide electrolytic cell enter a fourth heat exchanger for heat exchange and cooling, the oxygen and the water vapor are introduced into a first separator after heat exchange, the separated condensed water is introduced into a first pipeline to participate in circulation, and the separated oxygen is introduced into an oxygen collecting tank for storage.
Further, the high temperature oxide electrolytic cell includes a cathode, an anode, and an electrolyte supported by the two electrodes. The materials of the cathode, anode and electrolyte are strontium-doped lanthanum manganate (LSM), nickel-zirconia (Ni-YSZ) and yttria-stabilized zirconia (YSZ), respectively.
Furthermore, the one-way controller is an MPPT solar controller, the power generation voltage of the photovoltaic panel can be detected in real time, the maximum voltage and current value can be tracked, the system supplies power to the high-temperature oxide electrolytic cell through maximum power output, the MPPT tracking efficiency is 99%, the power generation efficiency of the whole system is 97%, the controller can monitor the stability of the high-temperature oxide electrolytic cell, and when insufficient power supply is caused by insufficient illumination, the two-way controller can be adjusted to supply electric energy to the electrolytic cell.
Further, the temperature of an ammonia decomposition reaction inlet in the endothermic reactor ranges from 300 ℃ to 380 ℃, and the mass flow of ammonia gas in the ammonia decomposition reaction ranges from 1.8g/s to 2.6 g/s.
The invention has the beneficial effects that:
1) the photovoltaic and chemical heat pump coupled solar high-temperature water electrolysis hydrogen production system integrates a photovoltaic system, an amino chemical heat pump system and an SOEC system, the system utilizes the photovoltaic system to generate electric energy, the amino chemical heat pump system converts low-grade solar energy into high-grade heat energy and uses the high-grade heat energy to heat water, the electric energy and high-temperature steam are respectively provided for the SOEC electrolysis process, the complementation of the heat energy and the electric energy is realized, and the clean, efficient and stable solar hydrogen production process is completed.
2) The storage tank of the system can store heat energy, and the super capacitor can store electric energy, so that the intermittence and the regionality of solar energy utilization can be overcome.
3) The invention uses NH3Compared with other systems, the chemical heat pump system based on the reversible reaction has the advantages of simple reaction, no side reaction, sufficient reactants and the like, solar energy is the only input energy, and H2O is the only raw material gas to realize zero CO2Preparing discharged green hydrogen.
4) The stronger the function of the amino chemical heat pump is, the lower the temperature of the energy absorption end is, and the higher the temperature of the energy release side is, so that the demand on light-gathering and heat-collecting equipment and the occupation ratio of electric energy in the water electrolysis process of the SOEC are reduced, the capital cost of the system is greatly reduced, and the solar hydrogen production efficiency is improved.
Drawings
FIG. 1 is a schematic flow chart of the present invention.
In the figure: 1. a heliostat field; 2. an endothermic reactor; 3. a first heat exchanger; 4. a first delivery pump; 5. a storage tank; 6. a second delivery pump; 7. a second heat exchanger; 8. an exothermic reactor; 9. a third heat exchanger; 10. a high temperature oxide electrolytic cell; 11. a fourth heat exchanger; 12. a first separator; 13. a second separator; 14. a water tank; 15. a third delivery pump; 16. an array of photovoltaic panels; 17. a one-way controller; 18. a bi-directional controller; 19. a super capacitor; 20. a controller; 21. a first pipeline; 22. a second pipeline; 23. a first conductive line; 24. an oxygen collection tank; 25. a hydrogen collection tank; 26. a bidirectional conductive line.
Detailed Description
The invention will be further described with reference to the drawings and examples in the following description, but the scope of the invention is not limited thereto.
As shown in figure 1, the photovoltaic and chemical heat pump coupled solar high-temperature water electrolysis hydrogen production system comprises a photovoltaic power generation system, an amino chemical heat pump and a high-temperature oxide electrolytic cell electrolytic water system, wherein the photovoltaic power generation system comprises a photovoltaic panel array 16, a one-way controller 17, a two-way controller 18, a super capacitor 19 and a controller 20, the output end of the photovoltaic panel array 16 is connected with the input end of the one-way controller 17, the output end of the one-way controller 17 is connected with the controller 20 through a first lead 23, the super capacitor 19 is connected with the two-way controller 18 in a two-way mode, the two-way controller 18 is connected with the first lead 23 through a two-way lead 26, the controller 20 is connected with a high-temperature oxide electrolytic cell 10 in the high-temperature oxide electrolytic cell electrolytic water system, and the high-temperature oxide electrolytic cell electrolytic water system comprises the high-temperature oxide electrolytic cell 10, a fourth heat exchanger 11, a heat exchanger, A first separator 12, a second separator 13, a water tank 14, a third transfer pump 15, an oxygen collection tank 24 and a hydrogen collection tank 25, wherein the water tank 14 is connected with a cold inlet of a fourth heat exchanger 11 through the third transfer pump 15, a cold outlet of the fourth heat exchanger 11 is connected with a cold inlet of a third heat exchanger 9, a cold outlet of the third heat exchanger 9 is connected with a high-temperature oxide electrolytic cell 10 through a second pipeline 22, a cathode of the high-temperature oxide electrolytic cell 10 is connected with the first separator 12 through the fourth heat exchanger 11, an upper outlet of the first separator 12 is connected with the oxygen collection tank 24, an anode of the high-temperature oxide electrolytic cell 10 is connected with the first separator 12 through the fourth heat exchanger 11, an upper outlet of the second separator 13 is divided into two pipelines, one pipeline is connected with the hydrogen collection tank 25, the other pipeline is connected with the second pipeline 22 in a converging manner, a lower outlet of the second separator 13 is connected with the water tank 14 through the first pipeline 21 to realize circulation loop connection, the lower outlet line of the first separator 12 is joined to the first line 21; the third heat exchanger 9 is coupled with an amino chemical heat pump system, the amino chemical heat pump system comprises a heliostat field 1, an endothermic reactor 2, a first heat exchanger 3, a first delivery pump 4, a storage tank 5, a second delivery pump 6, a second heat exchanger 7 and an exothermic reactor 8, the endothermic reactor 2, the first heat exchanger 3 and the storage tank 5 are sequentially connected to form a circulation loop, the first delivery pump 4 is arranged on an output pipeline of the storage tank 5 connected with the first heat exchanger 3, the other output pipeline of the storage tank 5 is sequentially connected with the second delivery pump 6, the second heat exchanger 7, the exothermic reactor 8 and a hot end inlet of the third heat exchanger 9, a hot end outlet of the third heat exchanger 9 is connected with a hot end inlet of the second heat exchanger 7, and a hot end outlet of the second heat exchanger 7 is connected with the storage tank 5.
Example 1
The direct solar radiation intensity is 1000W/m2The solar light generates electric energy on the photovoltaic panel array 16, the electric energy is adjusted through the one-way controller 17 to enable the system to output with the maximum power, the monitoring controller 20 provides required electric power for the high-temperature oxide electrolytic cell 10, and the total area of the required photovoltaic panel is 20m2The working temperature of the photovoltaic panel is 25 ℃, the size (H/W/D) of a single photovoltaic panel is 2279 multiplied by 1134 multiplied by 35mm, the weight is 29kg, the number of batteries is 144, the maximum output power is 550W, and the efficiency is 21.2%; when the illumination is sufficient, the redundant electric energy generated by the photovoltaic panel array 16 is stored in the super capacitor 19 through the bidirectional controller 18; when the illumination is insufficient, the monitoring controller 20 will adjust the size of the switch of the bidirectional controller 18 to release the electric energy stored in the super capacitor 19 to supply the insufficient electric energy to the high-temperature oxide electrolytic cell 10; at night, the photovoltaic panel array 16 is not operated, the one-way controller 17 is turned off, and the two-way controller 18 is turned on to allow the super capacitor 19 to supply the required power to the high temperature oxide electrolytic cell 10.
Sunlight is reflected to the endothermic reactor 2 through the heliostat field 1 with the condensation ratio of 200 to provide reaction conditions for ammonia decomposition reaction, and the area of the heliostat field 1 is 10m2The optical efficiency of the heliostat is 75 percent, the receiver efficiency is 87.5 percent, the normal-temperature liquid ammonia stored at the bottom of the storage tank 5 flows out of a liquid outlet at the bottom, enters the first heat exchanger 3 through the first conveying pump 4 to absorb heat and raise the temperature, the ammonia gas with the temperature of 350 ℃ and the mass flow of 2.6g/s enters the endothermic reactor 2 to carry out ammonia decomposition reaction (2 NH)3⇔ N2+3H2) The mixed gas (N2 + H2) generated by ammonia decomposition is discharged from the outlet of the endothermic reactor 2, the temperature of the mixed gas is 504 ℃, and the mixed gas is stored in a storage tank 5 after heat exchange by a first heat exchanger 3; the mixed gas stored at the top of the storage tank 5 is discharged from a gas outlet at the top, enters a second heat exchanger 7 through a second delivery pump 6 to absorb heat and raise the temperature, and then enters an exothermic reactor 8 to participate in ammonia synthesis reaction (N)2+3H2⇔ 2NH3) The mass flow of the mixed gas is 7.6359g/s, the inlet temperature of the exothermic reactor 8 is 610 ℃, the temperature of the ammonia gas generated by the reaction is 703 DEG CAnd the generated gas is stored in the storage tank 5 after heat exchange through the third heat exchanger 9 and the second heat exchanger 7.
Normal temperature water flowing out of a water outlet of a water tank 14 enters a fourth heat exchanger 11 to absorb heat and raise the temperature after passing through a third delivery pump 15, reaches a critical state after heat exchange, then enters a third heat exchanger 9 to exchange heat and reach an overheat state, and high temperature steam with the temperature of 700 ℃ and the mass flow of 0.5821g/s enters a high temperature oxide electrolytic cell 10 to carry out hydrolysis reaction; the mixed gas of hydrogen and water vapor (the volume ratio is 9: 1) generated by the negative electrode enters a fourth heat exchanger 11 for heat exchange, the mixed gas enters a second separator 13 after heat exchange, the separated condensed water enters a water tank 14 along a first pipeline 21 to participate in circulation, the hydrogen is discharged from the gas outlet of the second separator 13 and is introduced into a hydrogen collecting tank 25 for storage, 10% of the generated hydrogen in volume is introduced into the negative electrode of the high-temperature oxide electrolytic cell 10, and the reduction state of the negative electrode is kept; oxygen and a small amount of water vapor generated by the anode of the high-temperature oxide electrolytic cell 10 enter a fourth heat exchanger 11 for heat exchange, the heat exchanged water is introduced into a first separator 12, the separated condensed water is introduced into a first pipeline 21 for circulation, and the separated oxygen is introduced into an oxygen collecting tank 24 for storage; the current density of SOEC is 3741A/m2The solar hydrogen production efficiency is 20.16 percent, and the hydrogen yield is 37.8Nm3/d。
Example 2
The direct solar radiation intensity is 1000W/m2The solar light generates electric energy on the photovoltaic panel array 16, the electric energy is adjusted through the one-way controller 17 to enable the system to output with the maximum power, the monitoring controller 20 provides required electric power for the high-temperature oxide electrolytic cell 10, and the total area of the required photovoltaic panel is 20m2The working temperature of the photovoltaic panel is 25 ℃, the size (H/W/D) of a single photovoltaic panel is 2279 multiplied by 1134 multiplied by 35mm, the weight is 29kg, the number of batteries is 144, the maximum output power is 550W, and the efficiency is 21.2%; when the illumination is sufficient, the redundant electric energy generated by the photovoltaic panel array 16 is stored in the super capacitor 19 through the bidirectional controller 18; when the illumination is insufficient or cloudy, the monitoring controller 20 will adjust the size of the switch of the bidirectional controller 18 to release the electric energy stored in the super capacitor 19 to supply insufficient electric energy to the high-temperature oxide electrolytic cell 10; when night, the photovoltaic panel array 16 does not work, the one-way controller 17 is closed, and two-way control is carried outThe controller 18 is turned on to allow the super capacitor 19 to provide the required electrical energy to the high temperature oxide electrolyzer 10.
Sunlight is reflected to the endothermic reactor 2 through the heliostat field 1 with the condensation ratio of 200 to provide reaction conditions for ammonia decomposition reaction, and the area of the heliostat field 1 is 10m2The optical efficiency of the heliostat is 75 percent, the receiver efficiency is 87.5 percent, the normal-temperature liquid ammonia stored at the bottom of the storage tank 5 flows out of a liquid outlet at the bottom, enters the first heat exchanger 3 through the first conveying pump 4 to absorb heat and raise the temperature, the ammonia gas with the temperature of 300 ℃ and the mass flow of 1.8g/s enters the endothermic reactor 2 to carry out ammonia decomposition reaction (2 NH)3⇔ N2+3H2) Mixed gas (N) produced by decomposition of ammonia2+H2) The mixed gas is discharged from an outlet of the endothermic reactor 2, the temperature of the mixed gas is 553 ℃, and the mixed gas is stored in a storage tank 5 after heat exchange by a first heat exchanger 3; the mixed gas stored at the top of the storage tank 5 is discharged from a gas outlet at the top, enters a second heat exchanger 7 through a second delivery pump 6 to absorb heat and raise the temperature, and then enters an exothermic reactor 8 to participate in ammonia synthesis reaction (N)2+3H2⇔ 2NH3) The mass flow of the mixed gas is 7.6359g/s, the inlet temperature of the exothermic reactor 8 is 610 ℃, the temperature of the ammonia gas generated by the reaction is 703 ℃, and the generated gas is stored in the storage tank 5 after heat exchange through the third heat exchanger 9 and the second heat exchanger 7.
Normal temperature water flowing out of a water outlet of a water tank 14 enters a fourth heat exchanger 11 to absorb heat and raise the temperature after passing through a third delivery pump 15, reaches a critical state after heat exchange, then enters a third heat exchanger 9 to exchange heat and reach an overheat state, and high temperature steam with the temperature of 700 ℃ and the mass flow of 0.5821g/s enters a high temperature oxide electrolytic cell 10 to carry out hydrolysis reaction; the mixed gas of hydrogen and water vapor (the volume ratio is 9: 1) generated by the negative electrode enters a fourth heat exchanger 11 for heat exchange, the mixed gas enters a second separator 13 after the heat exchange, the separated condensed water enters a water tank 14 along a first pipeline 21 to participate in circulation, the hydrogen is discharged from an air outlet of the second separator I13 and is introduced into a hydrogen collecting tank 25 for storage, 10% of the generated hydrogen in volume is introduced into the negative electrode of the high-temperature oxide electrolytic cell 10, and the reduction state of the negative electrode is kept; oxygen and a small amount of water vapor generated by the anode of the high-temperature oxide electrolytic cell 10 enter a fourth heat exchanger 11 for heat exchange, and are introduced into a first separator after heat exchange12, introducing the separated condensed water into a first pipeline 21 to participate in circulation, and introducing the separated oxygen into an oxygen collecting tank 24 for storage; the current density of SOEC is 3741A/m2The solar hydrogen production efficiency is 20.04%, and the hydrogen yield is 33.5Nm3/d。
Example 3
The direct solar radiation intensity is 1000W/m2The solar light generates electric energy on the photovoltaic panel array 16, the electric energy is adjusted through the one-way controller 17 to enable the system to output with the maximum power, the monitoring controller 20 provides required electric power for the high-temperature oxide electrolytic cell 10, and the total area of the required photovoltaic panel is 20m2The working temperature of the photovoltaic panel is 25 ℃, the size (H/W/D) of a single photovoltaic panel is 2279 multiplied by 1134 multiplied by 35mm, the weight is 29kg, the number of batteries is 144, the maximum output power is 550W, and the efficiency is 21.2%; when the illumination is sufficient, the redundant electric energy generated by the photovoltaic panel array 16 is stored in the super capacitor 19 through the bidirectional controller 18; when the illumination is insufficient or cloudy, the monitoring controller 20 will adjust the size of the switch of the bidirectional controller 18 to release the electric energy stored in the super capacitor 19 to supply insufficient electric energy to the high-temperature oxide electrolytic cell 10; at night, the photovoltaic panel array 16 is not operated, the one-way controller 17 is turned off, and the two-way controller 18 is turned on to allow the super capacitor 19 to supply the required power to the high temperature oxide electrolytic cell 10.
Sunlight is reflected to the endothermic reactor 2 through the heliostat field 1 with the condensation ratio of 200 to provide reaction conditions for ammonia decomposition reaction, and the area of the heliostat field 1 is 10m2The optical efficiency of the heliostat is 75 percent, the receiver efficiency is 87.5 percent, the normal-temperature liquid ammonia stored at the bottom of the storage tank 5 flows out of a liquid outlet at the bottom, enters the first heat exchanger 3 through the first delivery pump 4 to absorb heat and raise the temperature, the ammonia gas with the temperature of 380 ℃ and the mass flow of 2.2g/s enters the endothermic reactor 2 to carry out ammonia decomposition reaction (2 NH)3⇔ N2+3H2) Mixed gas (N) produced by decomposition of ammonia2+H2) The mixed gas is discharged from an outlet of the endothermic reactor 2, the temperature of the mixed gas is 523 ℃, and the mixed gas is stored in a storage tank 5 after heat exchange by a first heat exchanger 3; the mixed gas stored at the top of the storage tank 5 is discharged from a gas outlet at the top, enters a second heat exchanger 7 through a second delivery pump 6 to absorb heat and raise temperature, and then enters a heat release reactionReactor 8 participates in the ammonia synthesis reaction (N)2+3H2⇔ 2NH3) The mass flow of the mixed gas is 7.6359g/s, the inlet temperature of the exothermic reactor 8 is 610 ℃, the temperature of the ammonia gas generated by the reaction is 703 ℃, and the generated gas is stored in the storage tank 5 after heat exchange through the third heat exchanger 9 and the second heat exchanger 7.
Normal temperature water flowing out of a water outlet of a water tank 14 enters a fourth heat exchanger 11 to absorb heat and raise the temperature after passing through a third delivery pump 15, reaches a critical state after heat exchange, then enters a third heat exchanger 9 to exchange heat and reach an overheat state, and high temperature steam with the temperature of 700 ℃ and the mass flow of 0.5821g/s enters a high temperature oxide electrolytic cell 10 to carry out hydrolysis reaction; the mixed gas of hydrogen and water vapor (the volume ratio is 9: 1) generated by the negative electrode enters a fourth heat exchanger 11 for heat exchange, the mixed gas enters a second separator 13 after the heat exchange, the separated condensed water enters a water tank 14 along a first pipeline 21 to participate in circulation, the hydrogen is discharged from the air outlet of the second separator 13 and is introduced into a hydrogen collecting tank 25 for storage, 10% of the generated hydrogen in volume is introduced into the negative electrode of the high-temperature oxide electrolytic cell 10, and the reducing state of the negative electrode is kept; oxygen and a small amount of water vapor generated by the anode of the high-temperature oxide electrolytic cell 10 enter a fourth heat exchanger 11 for heat exchange, the heat exchanged water is introduced into a first separator 12, the separated condensed water is introduced into a first pipeline 21 for circulation, and the separated oxygen is introduced into an oxygen collecting tank 24 for storage; the current density of SOEC is 3741A/m2The solar hydrogen production efficiency is 20.1 percent, and the hydrogen yield is 35.9Nm3/d。
Claims (10)
1. The photovoltaic and chemical heat pump coupled solar high-temperature water electrolysis hydrogen production system is characterized by comprising a photovoltaic power generation system, an amino chemical heat pump system and a high-temperature oxide electrolytic cell electrolytic water system, wherein the photovoltaic power generation system is connected with the high-temperature oxide electrolytic cell electrolytic water system, and the high-temperature oxide electrolytic cell electrolytic water system is connected with the amino chemical heat pump system in a coupling mode through a third heat exchanger (9).
2. The photovoltaic and chemical heat pump coupled solar high-temperature water electrolysis hydrogen production system according to claim 1, wherein the photovoltaic power generation system comprises a photovoltaic panel array (16), a one-way controller (17), a two-way controller (18), a super capacitor (19) and a controller (20), an output end of the photovoltaic panel array (16) is connected with an input end of the one-way controller (17), an output end of the one-way controller (17) is connected with the controller (20) through a first lead (23), the super capacitor (19) is connected with the two-way controller (18) in a two-way manner, the two-way controller (18) is connected with the first lead (23) through a two-way lead (26), and the controller (20) is connected with the high-temperature oxide electrolytic cell electrolytic water system.
3. The photovoltaic and chemical heat pump coupled solar high-temperature water electrolysis hydrogen production system according to claim 2, wherein the high-temperature oxide electrolytic cell water electrolysis system comprises a high-temperature oxide electrolytic cell (10), a fourth heat exchanger (11), a first separator (12), a second separator (13), a water tank (14), a third transfer pump (15), an oxygen collection tank (24) and a hydrogen collection tank (25), the controller (20) is connected with the high-temperature oxide electrolytic cell (10), the water tank (14) is connected with a cold-end inlet of the fourth heat exchanger (11) through the third transfer pump (15), a cold-end outlet of the fourth heat exchanger (11) is connected with a cold-end inlet of the third heat exchanger (9), a cold-end outlet of the third heat exchanger (9) is connected with the high-temperature oxide electrolytic cell (10) through a second pipeline (22), a negative electrode of the high-temperature oxide electrolytic cell (10) is connected with the first separator (12) through the fourth heat exchanger (11), the upper outlet of the first separator (12) is connected with an oxygen collecting tank (24), the anode of the high-temperature oxide electrolytic cell (10) is connected with the second separator (13) through a fourth heat exchanger (11), and the upper outlet of the second separator (13) is connected with a hydrogen collecting tank (25).
4. The photovoltaic and chemical heat pump coupled solar high-temperature water electrolysis hydrogen production system according to claim 3, wherein the lower outlet of the second separator (13) is connected with the water tank (14) through a first pipeline (21), and the lower outlet pipeline of the first separator (12) is connected with the water tank (14) after being merged into a pipeline with the first pipeline (21).
5. The photovoltaic and chemical heat pump coupled solar high-temperature water electrolysis hydrogen production system according to claim 4, characterized in that the upper outlet of the second separator (13) is divided into two pipelines, one pipeline is connected with the hydrogen collecting tank (25), and the other pipeline is connected with the second pipeline (22) between the third heat exchanger (9) and the high-temperature oxide electrolytic cell (10).
6. The photovoltaic and chemical heat pump coupled solar high-temperature water electrolysis hydrogen production system according to claim 5, wherein the third heat exchanger (9) is coupled with an amino-based chemical heat pump system, the amino-based chemical heat pump system comprises a heliostat field (1), an endothermic reactor (2), a first heat exchanger (3), a first delivery pump (4), a storage tank (5), a second delivery pump (6), a second heat exchanger (7) and an exothermic reactor (8), the endothermic reactor (2), the first heat exchanger (3) and the storage tank (5) are sequentially connected to form a circulation loop, the first delivery pump (4) is arranged on an output pipeline of the storage tank (5) connected with the first heat exchanger (3), another output pipeline of the storage tank (5) is sequentially connected with hot end inlets of the second delivery pump (6), the second heat exchanger (7), the exothermic reactor (8) and the third heat exchanger (9), the hot end outlet of the third heat exchanger (9) is connected with the hot end inlet of the second heat exchanger (7), and the hot end outlet of the second heat exchanger (7) is connected with the storage tank (5).
7. A photovoltaic and chemical heat pump coupled solar high temperature water electrolysis hydrogen production process according to claim 6, characterized by comprising the steps of:
1) sunlight is reflected to the endothermic reactor (2) from the heliostat field (1), liquid ammonia in the storage tank (5) is conveyed to the first heat exchanger (3) by the first conveying pump (4), enters the endothermic reactor (2) through the first heat exchanger (3) to absorb solar energy gathered by the heliostat field (1), and simultaneously, ammonia decomposition endothermic reaction is carried out, and N generated by the reaction2And H2Flows back to the storage tank (5) through the first heat exchanger (3), and N2And H2The ammonia is conveyed to a second heat exchanger (7) by a second conveying pump (6) and enters an exothermic reactor (8) through the second heat exchanger (7) to carry out ammonia synthesis reaction; the ammonia generated by the reaction flows out of the exothermic reactor (8) to exchange heat with the third heat exchanger (9) to provide heat energy for the exothermic reactor, then enters the storage tank (5) after exchanging heat through the second heat exchanger (7), and the steps are repeated in such a way to continuously provide heat energy for the electrolytic water system of the high-temperature oxide electrolytic cell;
2) the photovoltaic panel array (16) absorbs solar energy and converts the solar energy into electric energy which is transmitted to the one-way controller (17), when the illumination is sufficient, the one-way controller (17) transmits the electric energy to the two-way controller (18) and the controller (20) respectively, the two-way controller (18) transmits the electric energy to the super capacitor (19) for storage, and the controller (20) transmits the electric energy to the high-temperature oxide electrolytic cell (10) to provide the electric energy; when the illumination is insufficient, the electric energy stored in the super capacitor (19) is transmitted to the controller (20) through the bidirectional controller (18), and the controller (20) transmits the electric energy to the high-temperature oxide electrolytic cell (10);
3) water in a water tank (14) is conveyed to a fourth heat exchanger (11) through a third conveying pump (15) for heat exchange to reach a critical state, the water is subjected to heat exchange through a third heat exchanger (9) and then reaches an overheated state, high-temperature steam in the overheated state is conveyed to a high-temperature oxide electrolytic cell (10) for electrolysis, a mixed gas of hydrogen and steam generated by a negative electrode enters the fourth heat exchanger (11) for heat exchange and temperature reduction, the mixed gas enters a second separator (13) for separation after heat exchange, condensed water obtained by separation enters the water tank (14) along a first pipeline (21) to participate in circulation, hydrogen is discharged from an upper gas outlet of the second separator (13) and is divided into two pipelines, one pipeline is introduced into a hydrogen collecting tank (25) for storage, and hydrogen in the other pipeline is introduced into the high-temperature oxide electrolytic cell (10) to keep the reduction state of the negative electrode; oxygen and a small amount of water vapor generated by the anode of the high-temperature oxide electrolytic cell (10) enter a fourth heat exchanger (11) for heat exchange and temperature reduction, the oxygen and the water vapor are introduced into a first separator (12) after heat exchange, the separated condensed water is introduced into a first pipeline (21) to participate in circulation, and the separated oxygen is introduced into an oxygen collecting tank (24) for storage.
8. The photovoltaic and chemical heat pump coupled solar high-temperature electrolytic water hydrogen production process according to claim 7, wherein the high-temperature oxide electrolytic cell (10) comprises a cathode, an anode and an electrolyte supported by the two electrodes, and the cathode, the anode and the electrolyte are made of strontium-doped lanthanum manganate (LSM), nickel-zirconia (Ni-YSZ) and yttria-stabilized zirconia (YSZ), respectively.
9. The process for preparing hydrogen by solar high-temperature water electrolysis with coupling of photovoltaic and chemical heat pump according to claim 7, characterized in that the one-way controller (17) is an MPPT solar controller, which can detect the generated voltage of the photovoltaic panel in real time and track the highest voltage and current value, so that the system supplies power to the high-temperature oxide electrolytic cell (10) with the maximum power output, the MPPT tracking efficiency is 99%, the generating efficiency of the whole system is 97%, the controller (20) can monitor the stability of the high-temperature oxide electrolytic cell (10), and when the power supply is insufficient due to insufficient illumination, the two-way controller (18) can be adjusted to supply power to the electrolytic cell.
10. The photovoltaic and chemical heat pump coupled solar high-temperature water electrolysis hydrogen production process according to claim 7, characterized in that the temperature of the ammonia decomposition reaction inlet in the endothermic reactor (2) is in the range of 300 ℃ to 380 ℃, and the mass flow rate of ammonia gas in the ammonia decomposition reaction is in the range of 1.8g/s to 2.6 g/s.
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Application publication date: 20211001 |