CN114149043A - Method and device for preparing ammonium bicarbonate by solar beam splitting thermoelectric conversion - Google Patents
Method and device for preparing ammonium bicarbonate by solar beam splitting thermoelectric conversion Download PDFInfo
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- CN114149043A CN114149043A CN202111285859.8A CN202111285859A CN114149043A CN 114149043 A CN114149043 A CN 114149043A CN 202111285859 A CN202111285859 A CN 202111285859A CN 114149043 A CN114149043 A CN 114149043A
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- 238000006243 chemical reaction Methods 0.000 title claims abstract description 106
- ATRRKUHOCOJYRX-UHFFFAOYSA-N Ammonium bicarbonate Chemical compound [NH4+].OC([O-])=O ATRRKUHOCOJYRX-UHFFFAOYSA-N 0.000 title claims abstract description 66
- 229910000013 Ammonium bicarbonate Inorganic materials 0.000 title claims abstract description 66
- 235000012538 ammonium bicarbonate Nutrition 0.000 title claims abstract description 66
- 239000001099 ammonium carbonate Substances 0.000 title claims abstract description 66
- 238000000034 method Methods 0.000 title claims abstract description 20
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 95
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 61
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 60
- 239000001301 oxygen Substances 0.000 claims abstract description 60
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 60
- 239000003546 flue gas Substances 0.000 claims abstract description 52
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 50
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 39
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 39
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 37
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 30
- 150000003839 salts Chemical class 0.000 claims abstract description 28
- 238000002485 combustion reaction Methods 0.000 claims abstract description 26
- 239000013535 sea water Substances 0.000 claims abstract description 25
- 238000001228 spectrum Methods 0.000 claims abstract description 18
- 238000005516 engineering process Methods 0.000 claims abstract description 10
- 238000005868 electrolysis reaction Methods 0.000 claims abstract description 9
- 238000004519 manufacturing process Methods 0.000 claims abstract description 8
- 238000003860 storage Methods 0.000 claims description 73
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 52
- 238000000926 separation method Methods 0.000 claims description 39
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 31
- 239000001257 hydrogen Substances 0.000 claims description 31
- 229910052739 hydrogen Inorganic materials 0.000 claims description 31
- 238000011033 desalting Methods 0.000 claims description 26
- 238000004146 energy storage Methods 0.000 claims description 26
- 229910052757 nitrogen Inorganic materials 0.000 claims description 23
- 238000000746 purification Methods 0.000 claims description 18
- 239000000243 solution Substances 0.000 claims description 16
- 238000001704 evaporation Methods 0.000 claims description 15
- 239000007789 gas Substances 0.000 claims description 15
- 239000003245 coal Substances 0.000 claims description 12
- 230000003595 spectral effect Effects 0.000 claims description 12
- 239000012267 brine Substances 0.000 claims description 10
- 230000008020 evaporation Effects 0.000 claims description 10
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims description 10
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 8
- 239000013505 freshwater Substances 0.000 claims description 8
- 229910001873 dinitrogen Inorganic materials 0.000 claims description 6
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 4
- 239000003054 catalyst Substances 0.000 claims description 4
- 230000005611 electricity Effects 0.000 claims description 4
- 229910052742 iron Inorganic materials 0.000 claims description 4
- 238000005057 refrigeration Methods 0.000 claims description 4
- 239000000203 mixture Substances 0.000 claims description 2
- 238000010612 desalination reaction Methods 0.000 abstract description 23
- 238000005265 energy consumption Methods 0.000 abstract description 6
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 15
- 239000000376 reactant Substances 0.000 description 7
- 238000010248 power generation Methods 0.000 description 6
- 229910052799 carbon Inorganic materials 0.000 description 5
- 230000008569 process Effects 0.000 description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- 238000005286 illumination Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 238000002360 preparation method Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 239000004065 semiconductor Substances 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 239000002803 fossil fuel Substances 0.000 description 2
- 239000005431 greenhouse gas Substances 0.000 description 2
- 125000001967 indiganyl group Chemical group [H][In]([H])[*] 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 230000005855 radiation Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- 230000009471 action Effects 0.000 description 1
- 238000012271 agricultural production Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000003792 electrolyte Substances 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 239000008236 heating water Substances 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000000618 nitrogen fertilizer Substances 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- 239000012782 phase change material Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Images
Classifications
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/06—Flash evaporation
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/02—Preparation, purification or separation of ammonia
- C01C1/04—Preparation of ammonia by synthesis in the gas phase
- C01C1/0405—Preparation of ammonia by synthesis in the gas phase from N2 and H2 in presence of a catalyst
- C01C1/0488—Processes integrated with preparations of other compounds, e.g. methanol, urea or with processes for power generation
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/26—Carbonates or bicarbonates of ammonium
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D3/00—Halides of sodium, potassium or alkali metals in general
- C01D3/04—Chlorides
- C01D3/06—Preparation by working up brines; seawater or spent lyes
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B1/00—Electrolytic production of inorganic compounds or non-metals
- C25B1/01—Products
- C25B1/02—Hydrogen or oxygen
- C25B1/04—Hydrogen or oxygen by electrolysis of water
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- 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
-
- H—ELECTRICITY
- H02—GENERATION; CONVERSION OR DISTRIBUTION OF ELECTRIC POWER
- H02J—CIRCUIT ARRANGEMENTS OR SYSTEMS FOR SUPPLYING OR DISTRIBUTING ELECTRIC POWER; SYSTEMS FOR STORING ELECTRIC ENERGY
- H02J7/00—Circuit arrangements for charging or depolarising batteries or for supplying loads from batteries
- H02J7/34—Parallel operation in networks using both storage and other dc sources, e.g. providing buffering
- H02J7/35—Parallel operation in networks using both storage and other dc sources, e.g. providing buffering with light sensitive cells
-
- 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
- H02S40/30—Electrical components
- H02S40/32—Electrical components comprising DC/AC inverter means associated with the PV module itself, e.g. AC modules
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/08—Seawater, e.g. for desalination
-
- 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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
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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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
- Y02A20/138—Water desalination using renewable energy
- Y02A20/142—Solar thermal; Photovoltaics
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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
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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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 relates to a device for preparing ammonium bicarbonate by solar beam splitting thermoelectric conversion, which realizes full-spectrum solar energy utilization by a solar beam splitting technology, provides electric energy for an electrolytic cell, provides heat for a thermal desalination and ammonia reaction device, and produces ammonium bicarbonate by carbon dioxide in flue gas of a coal-fired power plant, produced ammonia and water produced by a flue gas compressor; the method for preparing the ammonium bicarbonate through the solar beam splitting thermoelectric conversion improves the utilization rate of the system to solar energy, realizes the capture of carbon dioxide, produces the ammonium bicarbonate, not only improves the overall efficiency of the solar energy utilization system, but also promotes the production of salt and ammonium bicarbonate added value products, reduces the energy consumption of the oxygen-enriched combustion and saves energy through the steps of solar beam splitting, seawater desalination, water electrolysis, oxygen-enriched combustion, ammonium bicarbonate production and the like.
Description
Technical Field
The invention relates to a solar beam splitting technology, in particular to a method and a device for preparing ammonium bicarbonate by solar beam splitting thermoelectric conversion.
Background
Solar energy is considered to be one of the most promising energy sources due to its non-pollution and abundant reserves, and is considered to be an ideal alternative energy source for fossil energy. Solar photovoltaic power generation and solar thermal power generation are two main methods for utilizing solar energy, wherein the main principle of the solar photovoltaic power generation is as follows: photovoltaic semiconductor materials convert the radiant energy in solar illumination into corresponding electrical energy by the photovoltaic effect, which conversion requires the provision of the basic device, i.e. a solar cell. When sunlight irradiates on the photovoltaic semiconductor material, the semiconductor material can convert the sunlight into electric energy, and further corresponding current is formed. The disadvantages are large floor space, low conversion efficiency, large influence of climate environment and no storage function. The main principle of solar thermal power generation is as follows: the solar heat collection field is characterized in that heat generated by solar illumination radiation is used for generating power, a built-in solar heat collector absorbs radiation energy in the solar illumination, the heat is used for heating water and converting the water into working medium steam, and finally the steam pushes a steam turbine to operate and generate the power.
In order to deal with the emission of a large amount of global greenhouse gases and realize the carbon peak-reaching goal early, the nation will increase the strength to control the emission of greenhouse gases such as carbon dioxide, wherein the carbon dioxide content emitted by a power plant accounts for a larger proportion of the whole industrial production. At present, a carbon capture mode of a power plant is capture before combustion, and the main principle is to separate carbon-containing components in fossil fuel before combustion, namely, the carbon-containing components are reacted with the fossil fuel in a gasification furnace through oxygen, water vapor to generate synthesis gas mainly comprising hydrogen and carbon monoxide, the synthesis gas is converted into carbon dioxide through a water gas shift process, and then the carbon dioxide is separated and captured. The disadvantages are high investment cost and power generation cost; the principle of post-combustion capture refers to a process of capturing carbon dioxide from flue gas after combustion of fossil energy. The defects are that the concentration of carbon dioxide in the flue gas generated by combustion is low because the air supporting combustion contains a large amount of nitrogen, so that the trapping process is complex and the cost is high.
Disclosure of Invention
The invention relates to a method for preparing ammonium bicarbonate by solar energy beam splitting thermoelectric conversion, which solves the problems existing in the prior art, improves the utilization rate of a system on solar energy, realizes the capture of carbon dioxide and produces ammonium bicarbonate by the steps of solar energy beam splitting, seawater desalination, water electrolysis, oxygen-enriched combustion, ammonium bicarbonate production and the like, has high safety, and simultaneously designs a device for preparing ammonium bicarbonate by solar energy beam splitting thermoelectric conversion.
One of the technical schemes for realizing the invention is as follows: a solar energy beam splitting thermoelectric conversion prepares ammonium bicarbonate device, characterized by, it includes: the device comprises a thermal desalination device 1, a heat exchanger 2, an electrolytic cell 3, a hydrogen storage tank 4, an oxygen storage tank 5, an ammonia reaction device 6, an ammonium bicarbonate reaction device 7, a nitrogen storage tank 8, a pump 9, an air compressor 10, an air separation device 11, a coal-fired power plant 12, a flue gas compressor 13, a compressor 14, a purification device 15, an ammonium bicarbonate storage device 16, a thermal energy storage 17, a photovoltaic inverter 18, a solar cell panel 19, a spectrum beam splitter 20, a condenser 21 and a salt storage tank 22, wherein solar rays are uniformly irradiated onto the spectrum beam splitter 20 through the condenser 21, the spectrum beam splitter 20 guides sunlight onto the solar cell panel 19, the solar cell panel 19 is connected with the photovoltaic inverter 18, the photovoltaic inverter 18 is connected with an electrode of the electrolytic cell 3, the spectrum beam splitter 20 is connected with the thermal energy storage 17, the thermal energy storage 17 is connected with the heat exchanger 2, the first heat outlet of the heat exchanger 2 is connected with the heat desalting device 1, a seawater inlet is arranged on the heat desalting device 1, a salt outlet of the heat desalting device 1 is connected with a salt storage tank 22, a solution outlet of the heat desalting device 1 is connected with an electrolytic tank 3, an oxygen outlet of the electrolytic tank 3 is connected with an oxygen storage tank 5, a hydrogen outlet of the electrolytic tank 3 is connected with a hydrogen storage tank 4, the hydrogen storage tank 4 is connected with an ammonia reaction device 6, a second heat outlet of the heat exchanger 2 is connected with the ammonia reaction device 6, the air compressor 10 is connected with the air separation device 11, a nitrogen outlet of the air separation device 11 is connected with a nitrogen storage tank 8, the nitrogen storage tank 8 is connected with the ammonia reaction device 6, an oxygen outlet of the air separation device 11 is connected with a coal-fired power plant 12, oxygen holding vessel 5 and coal fired power plant 12 be connected, coal fired power plant 12's electric energy export output electric energy, coal fired power plant 12's exhanst gas outlet be connected with gas compressor 13 the carbon dioxide export of gas compressor 13 and purification device 15 between set up compressor 14 purification device 15 and ammonium bicarbonate reaction unit 7 between set up pump 9, gas compressor 13's solution outlet be connected with ammonium bicarbonate reaction unit 7, ammonia reaction unit 6 be connected with ammonium bicarbonate reaction unit 7, ammonium bicarbonate reaction unit 7 be connected with ammonium bicarbonate storage device 16.
Further, an iron catalyst is arranged in the ammonia reaction device 6.
Further, the condenser 21 is a flat fresnel type condenser.
The second technical scheme for realizing the invention is as follows: a method for preparing ammonium bicarbonate by solar beam splitting thermoelectric conversion is characterized by comprising the following steps:
1) solar energy beam splitting:
the sunlight is uniformly irradiated onto the spectrum beam splitter 20 through the condenser 21, the sunlight with the wavelength of 0.3 mu m < lambda <1.2 mu m is guided to the solar cell panel 19 for power generation, and the electric energy is obtained through the photovoltaic inverter 18; converting photons of wave bands with the wavelength range of 0.3 mu m < lambda <1.2 mu m into heat and storing the heat in a heat energy storage 17;
2) electrical utilization of spectral beam splitter:
connecting a photovoltaic inverter 18 with the electrolytic cell 3 to supply power to the electrodes of the electrolytic cell 3;
3) thermal utilization of spectral beam splitter:
the heat energy in the heat energy storage 17 is transmitted to the thermal desalination device 1 through the heat exchanger 2 to provide heat for evaporating seawater, and the heat energy W in the heat energy storage 172Conveying the mixture to an ammonia reaction device 6 through a heat exchanger 2 to ensure that the temperature in the ammonia reaction device 6 reaches 500 ℃ and the pressure reaches 20-50 MPa;
4) thermal desalting:
inputting seawater into a thermal desalination device 1, wherein the thermal desalination device 1 adopts a multistage flash evaporation technology, after the seawater is heated to 90-100 ℃, hot brine is formed, the hot brine sequentially flows through flash evaporation chambers with gradually reduced pressure, the hot brine becomes superheated water after entering the flash evaporation chambers, the temperature of the hot brine is reduced after the water is rapidly gasified, the generated steam is condensed into fresh water, the fresh water flows into an electrolytic tank 3 from the thermal desalination device 1, and the generated salt enters a salt storage tank 22;
5) water electrolysis:
the electrolytic cell 3 adopts a PEM water electrolysis technology, the internal temperature is lower than 80 ℃, oxygen ionized in the electrolytic cell 3 is input into an oxygen storage tank 5 and is conveyed to a coal-fired power plant 12 through the oxygen storage tank 5, and hydrogen ionized in the electrolytic cell 3 is input into a hydrogen storage tank 4;
6) oxygen-enriched combustion:
the external air is conveyed to an air separation device 11 through an air compressor 10, nitrogen separated by the air separation device 11 is stored in a nitrogen storage tank 8, and the air separation device 11 separates oxygen by utilizing a low-temperature refrigeration principle and conveys the oxygen to a coal-fired power plant 12 for oxygen-enriched combustion;
7) preparing ammonium bicarbonate:
will in hydrogen among the hydrogen holding vessel 4 lets in ammonia reaction unit 6, nitrogen among the nitrogen holding vessel 8 lets in ammonia reaction unit 6, after the reaction generates the ammonia, carry the ammonia to ammonium bicarbonate reaction unit 7 in, after 12 oxygen boosting combustion of coal fired power plant, the flue gas of production separates through flue gas compressor 13, separates out the separation of water among the flue gas, water carry to ammonium bicarbonate reaction unit 7 in, ammonia and water take place to react and generate the aqueous ammonia, the flue gas of separating through flue gas compressor 13 is carried to purification device 15 by compressor 14 in, the pure carbon dioxide who produces through purification device 15 sends into ammonium bicarbonate reaction unit 7 through pump 9 in, the aqueous ammonia reacts with excessive carbon dioxide and generates ammonium bicarbonate.
Further, in the step 3), the heat energy W in the heat energy storage 17 is stored240% of the total amount of the water is transferred to the thermal desalination device 1 through the heat exchanger 2 to provide heat for evaporating the seawater, and the heat energy W in the heat energy storage 17 is transferred to the thermal desalination device260 percent of the total ammonia gas is conveyed into an ammonia gas reaction device 6 through a heat exchanger 2, so that the temperature in the ammonia gas reaction device 6 reaches 500 ℃ and the pressure reaches 40 MPa.
The invention relates to a method for preparing ammonium bicarbonate by solar beam splitting thermoelectric conversion and a device thereof, and has the beneficial effects that:
1. in the method for preparing ammonium bicarbonate by solar beam splitting thermoelectric conversion, full-spectrum solar energy is used for cogeneration by a solar beam splitting technology, and the method is combined with thermal desalination, water electrolysis, oxygen-enriched combustion and ammonium bicarbonate preparation, so that the overall efficiency of a solar energy utilization system is improved, and the generation of chemical value-added products such as salt and ammonium bicarbonate can be promoted;
2. a solar energy beam splitting thermoelectric conversion prepares ammonium bicarbonate device, after generating electricity through the solar energy of the spectral beam splitter, provide the electric energy for the electrolytic cell, electrolyze fresh water in the electrolytic cell, thus obtain hydrogen and oxygen that oxygen boosting burning needs that ammonia production needs, save a large amount of electric energy for the air separation plant, meanwhile, provide sufficient heat for the ammonia production plant, carbon dioxide and ammonia produced in the flue gas of the coal fired power plant and water produced by the flue gas compressor produce ammonium bicarbonate, has realized the capture of carbon dioxide, ammonium bicarbonate is more favorable to storing at normal temperature, relatively more stable, the security is higher, in agricultural production, ammonium bicarbonate is nitrogen fertilizer, change waste into wealth;
3. a method for preparing ammonium bicarbonate by solar energy beam splitting thermoelectric conversion is characterized in that seawater is desalted by a thermal desalting device to produce chemical value-added salt, sufficient raw material water is provided for an electrolytic cell, and hydrogen and oxygen are obtained by separation.
Drawings
FIG. 1 is a schematic diagram of a device for preparing ammonium bicarbonate by solar energy beam-splitting thermoelectric conversion;
in the figure: 1. a thermal desalination device, 1-1, a desalination heat inlet, 1-2, a seawater inlet, 1-3, a solution outlet, 1-4, a salt outlet, 2, a heat exchanger, 2-1, a heat inlet, 2-2, a first heat outlet, 2-3, a second heat outlet, 3, an electrolytic cell, 3-1, an electric energy inlet, 3-2, a solution inlet, 3-3, an oxygen outlet, 3-4, a hydrogen outlet, 4, a hydrogen storage tank, 4-1, a hydrogen inlet, 4-2, a hydrogen outlet, 5, an oxygen storage tank, 5-1, an oxygen inlet, 5-2, an oxygen outlet, 6, an ammonia reaction device, 6-1, a reaction device heat inlet, 6-2, a nitrogen inlet, 6-3, a hydrogen inlet, 6-4, an ammonia outlet, 7. an ammonium bicarbonate reaction device, 7-1 ammonia gas inlet, 7-2 solution inlet, 7-3 carbon dioxide inlet, 7-4 reactant outlet, 8 nitrogen gas storage tank, 8-1 nitrogen gas inlet, 8-2 nitrogen gas outlet, 9 pump, 9-1 carbon dioxide inlet, 9-2 carbon dioxide outlet, 10 air compressor, 10-1 air inlet, 10-2 air outlet, 11 air separation device, 11-1 air inlet, 11-2 oxygen outlet, 11-3 nitrogen gas outlet, 12 coal-fired power plant, 12-1 oxygen inlet, 12-2 electric energy outlet, 12-3 flue gas outlet, 13 flue gas compressor, 13-1 flue gas inlet, 13-2 solution outlet, 13-3 carbon dioxide outlet, 14 compressor, 14-1 carbon dioxide inlet, 14-2 carbon dioxide outlet, 15 purifying device, 15-1 carbon dioxide inlet, 15-2 exhaust outlet, 15-3 carbon dioxide outlet, 16 ammonium bicarbonate storing device, 16-1 reactant inlet, 17 heat energy storage, 17-1 heat outlet, 17-2 heat inlet, 18 photovoltaic inverter, 18-1 electric energy inlet, 18-2 electric energy outlet, 19 solar cell panel, 19-1 light inlet, 19-2 electric energy outlet, 20 spectrum beam splitter, 20-1 light inlet, 20-2 first outlet, 20-3 second outlet, 21 condenser, 21-1 light inlet, 21-2, a light outlet, 22, a salt storage tank and 22-1, a salt inlet.
Detailed Description
The present invention will be described in further detail with reference to the accompanying fig. 1 and the embodiments, which are described herein for the purpose of illustration only and are not intended to be limiting.
As shown in fig. 1, a device for preparing ammonium bicarbonate by solar energy beam splitting thermoelectric conversion comprises: the system comprises a thermal desalting device 1, a heat exchanger 2, an electrolytic bath 3, a hydrogen storage tank 4, an oxygen storage tank 5, an ammonia reaction device 6, an ammonium bicarbonate reaction device 7, a nitrogen storage tank 8, a pump 9, an air compressor 10, an air separation device 11, a coal-fired power plant 12, a flue gas compressor 13, a compressor 14, a purification device 15, an ammonium bicarbonate storage device 16, a thermal energy storage 17, a photovoltaic inverter 18, a solar cell panel 19, a spectrum beam splitter 20, a condenser 21 and a salt storage tank 22, wherein a light ray inlet 21-1 of the condenser 21 is connected with the outside; a light inlet 20-1 of the spectral beam splitter 20 is connected with a light outlet 21-2 of the condenser 21, a first outlet 20-2 of the spectral beam splitter 20 is connected with a heat inlet 17-1 of the heat energy storage 17, and a second outlet 20-3 of the spectral beam splitter 20 is connected with a light inlet 19-1 of the solar panel 19; the heat outlet 17-2 of the thermal energy storage 17 is connected to the heat inlet 2-1 of the heat exchanger 2; the electric energy outlet 19-2 of the solar panel 19 is connected with the electric energy inlet 18-1 of the photovoltaic inverter 18; the electric energy outlet 18-2 of the photovoltaic inverter 18 is connected with the electric energy inlet 3-1 of the electrolytic bath 3; a desalting hot inlet 1-1 of the thermal desalting device 1 is connected with a first heat outlet 2-2 of the heat exchanger 2, a seawater inlet 1-2 of the thermal desalting device 1 is connected with external seawater, a solution outlet 1-3 of the thermal desalting device 1 is connected with a solution inlet 3-2 of the electrolytic cell 3, and a salt outlet 1-4 of the thermal desalting device 1 is connected with a salt inlet 22-1 of a salt storage device 22; a second heat outlet 2-3 of the heat exchanger 2 is connected with a heat inlet 6-1 of the ammonia reaction device 6; an oxygen outlet 3-3 of the electrolytic cell 3 is connected with an oxygen inlet 5-1 of an oxygen storage tank 5, and a hydrogen outlet 3-4 of the electrolytic cell 3 is connected with a hydrogen inlet 4-1 of the hydrogen storage tank 5; an oxygen outlet 5-2 of the oxygen storage tank 5 is connected with an oxygen inlet 12-1 of the coal-fired power plant 12; a hydrogen inlet 6-3 of the ammonia reaction device 6 is connected with a hydrogen outlet 4-2 of the hydrogen storage tank 4, a nitrogen inlet 6-2 of the ammonia reaction device 6 is connected with a nitrogen outlet 8-2 of the nitrogen storage tank 8, and an ammonia outlet 6-4 of the ammonia reaction device 6 is connected with an ammonia inlet 7-1 of the ammonium bicarbonate reaction device 7; a solution inlet 7-2 of the ammonium bicarbonate reaction device 7 is connected with a solution outlet 13-2 of a flue gas compressor 13, a reactant outlet 7-4 of the ammonium bicarbonate reaction device 7 is connected with a reactant inlet 16-1 of an ammonium bicarbonate storage device 16, and a carbon dioxide inlet 7-3 of the ammonium bicarbonate reaction device 7 is connected with a carbon dioxide outlet 15-3 of a purification device 15 through a pump 9; an air inlet 10-1 of the air compressor 10 is connected with the outside, and an air outlet 10-2 of the air compressor 10 is connected with an air inlet 11-1 of the air separation device 11; a nitrogen outlet 11-3 of the air separation device 11 is connected with a nitrogen inlet 8-1 of the nitrogen storage tank 8, and an oxygen outlet 11-2 of the air separation device 11 is connected with an oxygen inlet 12-1 of the coal-fired power plant 12; a flue gas outlet 12-2 of the coal-fired power plant 12 is connected with a flue gas inlet 13-1 of a flue gas compressor; a carbon dioxide outlet 13-3 of the flue gas compressor 13 is connected with a flue gas inlet 14-1 of the compressor 14; the carbon dioxide outlet 14-2 of the compressor 14 is connected to the carbon dioxide inlet 15-1 of the purification device 15.
A working process of a device for preparing ammonium bicarbonate by solar beam splitting thermoelectric conversion comprises the following steps:
the light inlet 21-1 of the condenser 21 absorbs the external sunlight and flows into the spectrum beam splitter 20 through the light outlet 21-2 of the condenser 21, and the spectrum beam splitter 20 divides the incident light into 0.3 μm<λ<Photons of 1.2 μm flow into the solar panel 19 from the second outlet 20-3 of the spectral beam splitter 20 through the light inlet of the solar panel 19, the generated direct current flows into the photovoltaic inverter 18 from the power outlet 19-2 of the solar panel 19 through the power inlet of the photovoltaic inverter 18, and finally, alternating current power W is generated1Light ofSpectral beam splitter 20 will be 0.3 μm<λ<Conversion of photons of wavelengths other than 1.2 μm into heat W2From the first outlet 20-2 of the spectral beam splitter 20, it flows into the thermal energy reservoir 17 via the thermal energy inlet 17-1 of the thermal energy reservoir 17.
Electric energy W generated by photovoltaic inverter 181The electric energy flows into the electrolytic cell 3 from the electric energy outlet 18-2 of the photovoltaic inverter 18 through the electric energy inlet 3-1 of the electrolytic cell 3 to produce H for the electrolytic cell 32And O2Providing stable electric energy.
Thermal energy W in the thermal energy storage 172From the heat outlet 17-2 of the thermal energy storage 17, through the heat inlet of the heat exchanger 2 into the heat exchanger 2, 40% of the thermal energy W in the heat exchanger 22Flows into the thermal desalination device 1 from a first heat outlet 2-2 of the heat exchanger 2 through a desalination heat inlet 1-1 of the thermal desalination device 1, and 60 percent of heat energy W in the heat exchanger 22From a second outlet 2-3 of the heat exchanger 2, through NH3NH flows into the first inlet 6-1 of the reaction device 63In the reaction apparatus 6.
The seawater inlet 1-2 of the thermal desalting device 1 is connected with the outside seawater, the seawater passes through a flash evaporation chamber in the thermal desalting device, and the gas is cooled and condensed into H2O, flows into the electrolytic bath 3 from a solution outlet 1-3 of the thermal desalination device 1 through a solution inlet 3-2 of the electrolytic bath 3 to produce H for the electrolytic bath2And O2Sufficient raw material H is provided2O, and the obtained salt flows from the salt outlet 1-4 of the thermal desalination device 1 through the salt inlet 22-1 of the salt storage tank 22 into the salt storage tank 22.
The electrolytic cell 3 consumes electric energy W1Ionized H2H from the electrolytic cell 32Outlet 3-3, through H2H of storage tank 42Inlet 4-1 flows into H2In storage tank 4, for next step NH3Preparing; ionized O2O from the electrolytic cell 32An outlet 3-4 through O2O of storage tank 52Inlet 5-1 flows into O2In the storage tank 5, prepared for oxyfuel combustion, this portion O2The energy consumption of the whole oxygen-enriched combustion system can be reduced.
Air inlet 10-1 of air compressor 10 and the outsideAir is connected, when the air is heated to 40 ℃ by the air compressor 10, the air flows into the air separation device 11 from an air outlet 10-2 of the air compressor 10 through an air inlet 11-1 of the air separation device 11, and the air is separated into O in the air separation device 11 by utilizing the low-temperature refrigeration principle of the air2O from air separation unit 112An outlet 11-2 for flowing into the coal-fired power plant 12 through an inlet 12-1 of the coal-fired power plant 12, and O2O in the storage tank 52From O2O of storage tank 52An outlet 5-2 flows into the coal-fired power plant 12 through an inlet 12-1 of the coal-fired power plant 12, and participates in oxygen-enriched combustion together, the generated electric energy is connected to the grid from an electric energy outlet 12-2 of the coal-fired power plant 12, and the oxygen-enriched combustion enables CO in the flue gas flowing out of a flue gas outlet 12-32The concentration is higher, and the next step of separation of H in the flue gas is convenient2O and CO2And N is separated out2From N of the air separation unit 112The outlet 11-3 passes through N2N of storage tank 82Inlet 8-1 flows into N2In storage tank 8, for next step NH3Ready for preparation.
NH3The first inlet 6-1 of the reaction device 6 is connected with the second outlet 2-3 of the heat exchanger 2; second inlet 6-2 and N2N of storage tank2The outlet 8-2 is connected; third inlet 6-3 and H2H of storage tank2And the outlet 4-2 is connected. N is a radical of2And H2When the iron contacts the coal catalyst, the temperature is about 500 ℃, and the pressure in the ammonia reaction device 6 is maintained at 20-50MPa, the reaction is carried out to generate NH3，NH3From NH rapidly3NH of reaction unit 63At the outlet 6-4, passing through NH4HCO3NH of reaction unit 73The inlet 7-1 flows into NH4HCO3In the reaction device 7, the flue gas flows from the flue gas outlet 12-3 of the coal-fired power plant 12 to the flue gas inlet 13-1 of the flue gas compressor 13, and the main component of the flue gas is H due to the oxygen-enriched combustion in the coal-fired power plant 122O and CO2Under the action of the flue gas compressor 13, H2O flows from the solution outlet 13-2 of the flue gas compressor 13 into NH4HCO3Solution inlet 7-2 of reaction device 7, and residual flue gas from CO of flue gas compressor2CO flowing from outlet 13-3 to compressor 142CO at inlet 14-1 and then through compressor 142CO flowing from outlet 14-2 to purification unit 152An inlet 15-1 for introducing the exhaust gas from the exhaust gas outlet 15-2 of the purification apparatus 15 into the outside, and high purity CO2CO from the purification unit 152The outlet flow is sent to NH by a pump 94HCO3At gas inlet 7-3 in NH4HCO3NH in the reaction unit 73And H2O reacts first to form NH3·H2O，NH3·H2O and CO2Reaction to form (NH)4)2CO3With CO2The concentration is continuously increased to finally generate NH4HCO3。NH4HCO3From NH4HCO3A reactant outlet 7-4 of the reaction device 7 is connected with NH4HCO3The reactant inlet of the storage tank 16 is fed with NH4HCO3In the storage tank 16.
A method for preparing ammonium bicarbonate by solar beam splitting thermoelectric conversion comprises the following steps:
1) solar energy beam splitting:
the solar ray enters through the ray inlet 21-1 of the condenser 21, the condenser 21 is a flat Fresnel type condenser which can highly uniformly reflect the solar ray from the ray outlet 21-2 to the ray inlet 20-1 of the spectrum beam splitter 20, and the spectrum beam splitter 20 reflects the solar ray with a thickness of 0.3 μm<λ<The sunlight with the diameter of 1.2 mu m is guided to the solar panel 19 through the second outlet 20-2 to generate electricity, so that the temperature of the solar panel 19 can be effectively prevented from being too high, the conversion rate of the solar panel is improved, the direct current generated by the solar panel 19 enters the electric energy inlet 18-1 of the photovoltaic inverter 18, and finally, the alternating current electric energy W is obtained through the photovoltaic inverter 181And 0.3 μm<λ<Conversion of photons of wavelengths other than 1.2 μm into heat W2And the heat energy storage 17 is connected with a heat inlet 17-1 of the heat energy storage 17, the heat energy storage 17 adopts a phase change material, the assumed energy efficiency is 99%, the phase change temperature is 368K, and the latent heat capacity is 205 kJ/kg.
2) Electrical utilization of spectral beam splitter:
obtaining electrical energy W from the photovoltaic inverter 181Flows into a power supply inlet 3-1 of the electrolytic bath 3 to supply power to the electrodes of the electrolytic bath 3.
3) Thermal utilization of spectral beam splitter:
40% heat energy W of the thermal energy storage 172Is delivered to the thermal desalination device 1 through a first outlet 2-2 of the heat exchanger 2 to provide sufficient heat for evaporating seawater; the remaining 60% of the heat energy W2Through a second outlet 2-3 of the heat exchanger 2 to the sealed NH3In reaction apparatus 6, N2And H2The reaction can be fully carried out when the temperature of the iron catalyst is about 500 ℃, and NH is generated3The pressure in the reaction apparatus 6 needs to be maintained at 20 to 50 MPa.
4) Thermal desalting:
seawater enters the thermal desalination device 1 from the outside, the thermal desalination device 1 adopts a multi-stage flash evaporation technology, the temperature of the seawater when the seawater enters is between 15 and 30 ℃, the seawater flows through a plurality of flash evaporation chambers with gradually reduced pressure after being heated to 90 to 100 ℃, the hot brine immediately becomes superheated water after entering the flash evaporation chambers, so that part of the water is quickly gasified, the temperature of the hot brine is reduced, the generated steam is fresh water after being condensed, the temperature of the fresh water is between 20 and 35 ℃, the fresh water flows into the electrolytic tank 3 from the thermal desalination device 1, and the obtained salt flows into the salt storage tank 22. The seawater desalination not only provides enough raw material water for the electrolytic bath 2, but also can produce salt.
5) Water electrolysis:
the electrolytic cell 3 uses PEM water electrolysis technology, PEM is taken as electrolyte, pure water is taken as reactant, and H of PEM is added2Lower permeability, production of H2And O2High purity, only need to remove H2O; the electrolytic tank adopts a zero-spacing structure, the ohmic resistance is lower, the overall efficiency of the electrolytic process is obviously improved, and the volume is more compact; large pressure regulation range, H2The output pressure can reach several megapascals, the solar energy is suitable for the rapidly changing renewable energy power, and the electrolytic cell 3 consumes the electric energy W1At an internal temperature of 80 ℃ or lower and ionized O2Introduction of O2In the storage tank 5, finally O2From O2An outlet 5-2 of the storage tank 5O to coal fired power plant 122The inlet 12-1 participates in the subsequent oxygen-enriched combustion; h ionized by the electrolytic bath 32Introduction of H2In the storage tank 4, finally from H2An outlet 4-2 of the storage tank 4 is connected with NH3The third inlet of the reaction device 6 participates in the subsequent NH4HCO3And (4) preparation. 6) Oxygen-enriched combustion:
the outside air is sent into the air separation device 11 when the temperature of the outside air is raised to 400 ℃ by the air compressor 10, and the air separation device 11 utilizes the low-temperature refrigeration principle to carry out O separation2Separated from the electric energy W1Ionized portion O2Warp of O2The storage tank 5 is jointly sent to a coal-fired power plant for oxygen-enriched combustion, and the electric energy consumed by the air separation device 11 is W3In the absence of O2The electrical energy consumed by the air separation unit 11 with the aid of oxygen supplied from the storage tank 5 is W4Electric energy W1Ionized portion O2The huge energy consumption of the oxygen-enriched combustion air separation device 11 can be avoided to be W5And W is5＝W4-W3While also avoiding the air compressor 10 from separating relative to this portion O2Large energy consumption W of air6Since the power consumption in the air separation unit 11 includes the sum of the power consumption of the refrigerator, the power consumption of the electric heater, and other power consumption, O is separated from the air separation unit 112The power consumption is 5-6 kW.h.N-1m-3And the energy consumption of the air separation system increases along with the increase of the oxygen supply concentration, and the power consumption of the general large air compressor 10 for introducing air from the outside is about 3-4 kW.h.N-1m-3And the power consumption of the electrolytic cell 3 adopting the PEM technology is 4-5 kW.h.N-1m-3Thus W5+W6>W1And the overall energy consumption of the oxygen-enriched combustion system is reduced. Oxygen-enriched combustion for CO in flue gas2Higher concentration and convenient separation of H in flue gas2O and CO2。
7)NH4HCO3Preparing:
H2the storage tank 4 is filled with H2Introduction of NH3N separated by the air separator 11 in the reactor 62Warp of N2Storage tank 8Is a reaction of N2To NH3In the reaction apparatus 6, NH formed by the reaction3Into NH4In the HCO reaction device 7, flue gas flows out from a flue gas outlet 12-3 of a coal-fired power plant 12, the temperature of the flue gas is 110-120 ℃, the pressure is about 0.01MPa, the flue gas flows into a flue gas inlet 13-1 of a flue gas compressor 13, and the flue gas compressor 13 is used for compressing H in the flue gas2O is separated off and fed to NH4In the HCO reaction apparatus 7, NH3And H2O reacts first to form NH3·H2O, and the separated flue gas flows into a flue gas inlet 15-1 of a purification device 15 through a compressor 14, and pure CO generated in the purification device 152Is fed into NH by a pump 94HCO3In the reaction apparatus 7, NH3·H2O and excess CO2Reaction to form NH4HCO3。
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and improvements can be made without departing from the principle of the present invention, and these modifications and improvements should also be considered as the protection scope of the present invention.
Claims (5)
1. A solar energy beam splitting thermoelectric conversion prepares ammonium bicarbonate device, characterized by, it includes: the device comprises a thermal desalting device (1), a heat exchanger (2), an electrolytic bath (3), a hydrogen storage tank (4), an oxygen storage tank (5), an ammonia reaction device (6), an ammonium bicarbonate reaction device (7), a nitrogen storage tank (8), a pump (9), an air compressor (10), an air separation device (11), a coal-fired power plant (12), a flue gas compressor (13), a compressor (14), a purification device (15), an ammonium bicarbonate storage device (16), a heat energy storage device (17), a photovoltaic inverter (18), a solar cell panel (19), a spectrum beam splitter (20), a condenser (21) and a salt storage tank (22), wherein sunlight uniformly irradiates the spectrum beam splitter (20) through the condenser (21), the spectrum beam splitter (20) guides the sunlight to the solar cell panel (19), and the solar cell panel (19) is connected with the photovoltaic inverter (18), the photovoltaic inverter (18) is connected with an electrode of an electrolytic cell (3), the spectrum beam splitter (20) is connected with a heat energy storage (17), the heat energy storage (17) is connected with a heat exchanger (2), a first heat outlet of the heat exchanger (2) is connected with a heat desalting device (1), a seawater inlet is arranged on the heat desalting device (1), a salt outlet of the heat desalting device (1) is connected with a salt storage tank (22), a solution outlet of the heat desalting device (1) is connected with the electrolytic cell (3), an oxygen outlet of the electrolytic cell (3) is connected with an oxygen storage tank (5), a hydrogen outlet of the electrolytic cell (3) is connected with a hydrogen storage tank (4), the hydrogen storage tank (4) is connected with an ammonia reaction device (6), a second heat outlet of the heat exchanger (2) is connected with the reaction device (6), air compressor (10) be connected with air separation device (11), the nitrogen outlet and nitrogen gas holding vessel (8) of air separation device (11) be connected, nitrogen gas holding vessel (8) be connected with ammonia reaction unit (6), the oxygen outlet and coal fired power plant (12) of air separation device (11) be connected, oxygen holding vessel (5) be connected with coal fired power plant (12), the electric energy export output electric energy of coal fired power plant (12), the exhanst gas outlet and the gas compressor (13) of coal fired power plant (12) be connected the carbon dioxide export and the purification device (15) of gas compressor (13) between set up compressor (14) purification device (15) and ammonium bicarbonate reaction unit (7) between set up pump (9), the solution outlet and ammonium bicarbonate reaction unit (7) of gas compressor (13) be connected, the ammonia reaction device (6) is connected with the ammonium bicarbonate reaction device (7), and the ammonium bicarbonate reaction device (7) is connected with the ammonium bicarbonate storage device (16).
2. The device for preparing ammonium bicarbonate by the solar energy beam splitting thermoelectric conversion according to claim 1, which is characterized in that an iron catalyst is arranged in the ammonia gas reaction device (6).
3. The device for preparing ammonium bicarbonate by thermoelectric conversion of solar energy beam splitting according to claim 1, characterized in that the condenser (21) is a flat fresnel type condenser.
4. A method for preparing ammonium bicarbonate by solar beam splitting thermoelectric conversion is characterized by comprising the following steps:
1) solar energy beam splitting:
the sunlight is uniformly irradiated onto the spectrum beam splitter (20) through the condenser (21), the sunlight with the thickness of 0.3 mu m and the thickness of lambda being less than 1.2 mu m is guided to the solar cell panel (19) to generate electricity, and the electricity is obtained through the photovoltaic inverter (18); converting photons of wave bands with the wavelength range of 0.3 mu m < lambda <1.2 mu m into heat and storing the heat in a heat energy storage (17);
2) electrical utilization of spectral beam splitter:
connecting a photovoltaic inverter (18) with the electrolytic cell (3) to supply power to the electrodes of the electrolytic cell (3);
3) thermal utilization of spectral beam splitter:
the heat energy in the heat energy storage (17) is transferred into the heat desalting device (1) through the heat exchanger (2) to provide heat for evaporating seawater, and the heat energy W in the heat energy storage (17)2Conveying the mixture into an ammonia reaction device (6) through a heat exchanger (2) to ensure that the temperature in the ammonia reaction device (6) reaches 500 ℃ and the pressure reaches 20-50 MPa;
4) thermal desalting:
inputting seawater into a thermal desalting device (1), wherein the thermal desalting device (1) adopts a multi-stage flash evaporation technology, the seawater is heated to 90-100 ℃ to form hot brine, the hot brine sequentially flows through flash evaporation chambers with gradually reduced pressure, the hot brine becomes superheated water after entering the flash evaporation chambers, the temperature of the hot brine is reduced after the water is rapidly gasified, the generated steam is condensed to form fresh water, the fresh water flows into an electrolytic tank (3) from the thermal desalting device (1), and the generated salt enters a salt storage tank (22);
5) water electrolysis:
the electrolytic cell (3) adopts a PEM water electrolysis technology, the internal temperature is lower than 80 ℃, oxygen ionized in the electrolytic cell (3) is input into an oxygen storage tank (5) and is conveyed to a coal-fired power plant (12) through the oxygen storage tank (5), and hydrogen ionized in the electrolytic cell (3) is input into a hydrogen storage tank (4);
6) oxygen-enriched combustion:
the method comprises the following steps that outside air is conveyed into an air separation device (11) through an air compressor (10), nitrogen separated by the air separation device (11) is stored in a nitrogen storage tank (8), and oxygen is separated by the air separation device (11) through a low-temperature refrigeration principle and conveyed to a coal-fired power plant (12) for oxygen-enriched combustion;
7) preparing ammonium bicarbonate:
will in hydrogen among the hydrogen holding vessel (4) lets in ammonia reaction unit (6), in nitrogen among the nitrogen holding vessel (8) lets in ammonia reaction unit (6), after the reaction generates the ammonia, carry the ammonia to ammonium bicarbonate reaction unit (7), after coal fired power plant (12) oxygen boosting burning, the flue gas of production separates through flue gas compressor (13), separates out the separation of water among the flue gas, water carry to ammonium bicarbonate reaction unit (7) in, ammonia and water take place to react and generate the aqueous ammonia, the flue gas of separating through flue gas compressor (13) is carried to purification device (15) by compressor (14), the pure carbon dioxide who produces through purification device (15) sends into ammonium bicarbonate reaction unit 7 through pump (9), the aqueous ammonia reacts with excessive carbon dioxide and generates ammonium bicarbonate.
5. The method for preparing ammonium bicarbonate by the solar energy beam splitting thermoelectric conversion according to claim 2, wherein in the step 3), the heat energy W in the heat energy storage (17) is stored240% of the heat energy W is transmitted to a thermal desalting device (1) through a heat exchanger (2) to provide heat for evaporating seawater, and the heat energy W in a heat energy storage (17)260 percent of the total ammonia gas is conveyed into an ammonia gas reaction device (6) through a heat exchanger (2), so that the temperature in the ammonia gas reaction device (6) reaches 5000 ℃, and the pressure reaches 40 MPa.
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