CN117105242A - Floating wind power platform off-grid system for preparing green ammonia and preparation process thereof - Google Patents
Floating wind power platform off-grid system for preparing green ammonia and preparation process thereof Download PDFInfo
- Publication number
- CN117105242A CN117105242A CN202311066190.2A CN202311066190A CN117105242A CN 117105242 A CN117105242 A CN 117105242A CN 202311066190 A CN202311066190 A CN 202311066190A CN 117105242 A CN117105242 A CN 117105242A
- Authority
- CN
- China
- Prior art keywords
- module
- ammonia
- hydrogen
- unit
- electrolytic tank
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 340
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 146
- 238000007667 floating Methods 0.000 title claims abstract description 64
- 238000002360 preparation method Methods 0.000 title claims abstract description 16
- 239000007789 gas Substances 0.000 claims abstract description 75
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 74
- 239000013535 sea water Substances 0.000 claims abstract description 58
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 50
- 239000001257 hydrogen Substances 0.000 claims abstract description 47
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 47
- 238000000926 separation method Methods 0.000 claims abstract description 40
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 39
- 239000012528 membrane Substances 0.000 claims abstract description 35
- 239000007787 solid Substances 0.000 claims abstract description 33
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 28
- 238000004519 manufacturing process Methods 0.000 claims abstract description 26
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 23
- 239000002994 raw material Substances 0.000 claims abstract description 12
- 238000006243 chemical reaction Methods 0.000 claims description 37
- 238000010612 desalination reaction Methods 0.000 claims description 33
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 25
- 238000003860 storage Methods 0.000 claims description 21
- 238000001704 evaporation Methods 0.000 claims description 18
- 230000008020 evaporation Effects 0.000 claims description 17
- 238000009833 condensation Methods 0.000 claims description 15
- 230000005494 condensation Effects 0.000 claims description 15
- 238000002242 deionisation method Methods 0.000 claims description 12
- 238000005868 electrolysis reaction Methods 0.000 claims description 12
- 238000001223 reverse osmosis Methods 0.000 claims description 12
- 239000008367 deionised water Substances 0.000 claims description 10
- 229910021641 deionized water Inorganic materials 0.000 claims description 10
- 239000000446 fuel Substances 0.000 claims description 8
- 230000002194 synthesizing effect Effects 0.000 claims description 8
- 230000005611 electricity Effects 0.000 claims description 7
- 238000001179 sorption measurement Methods 0.000 claims description 6
- 239000007788 liquid Substances 0.000 claims description 5
- 238000000034 method Methods 0.000 description 12
- 238000012423 maintenance Methods 0.000 description 8
- 238000010438 heat treatment Methods 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 238000013461 design Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 238000004873 anchoring Methods 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 238000010248 power generation Methods 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 238000002407 reforming Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000003463 adsorbent Substances 0.000 description 1
- 229910052786 argon Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000003032 molecular docking Methods 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 230000002265 prevention Effects 0.000 description 1
- 239000008400 supply water Substances 0.000 description 1
- 238000013022 venting Methods 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C13/00—Details of vessels or of the filling or discharging of vessels
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
- B63B—SHIPS OR OTHER WATERBORNE VESSELS; EQUIPMENT FOR SHIPPING
- B63B35/00—Vessels or similar floating structures specially adapted for specific purposes and not otherwise provided for
- B63B35/44—Floating buildings, stores, drilling platforms, or workshops, e.g. carrying water-oil separating devices
-
- 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
- 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
- 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
- C25B15/00—Operating or servicing cells
- C25B15/08—Supplying or removing reactants or electrolytes; Regeneration of electrolytes
- C25B15/081—Supplying products to non-electrochemical reactors that are combined with the electrochemical cell, e.g. Sabatier reactor
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B15/00—Operating or servicing cells
- C25B15/08—Supplying or removing reactants or electrolytes; Regeneration of electrolytes
- C25B15/085—Removing impurities
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
- C25B9/60—Constructional parts of cells
- C25B9/65—Means for supplying current; Electrode connections; Electric inter-cell connections
-
- 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
- C25B9/70—Assemblies comprising two or more cells
-
- H—ELECTRICITY
- H02—GENERATION; CONVERSION OR DISTRIBUTION OF ELECTRIC POWER
- H02J—CIRCUIT ARRANGEMENTS OR SYSTEMS FOR SUPPLYING OR DISTRIBUTING ELECTRIC POWER; SYSTEMS FOR STORING ELECTRIC ENERGY
- H02J3/00—Circuit arrangements for ac mains or ac distribution networks
- H02J3/38—Arrangements for parallely feeding a single network by two or more generators, converters or transformers
- H02J3/388—Islanding, i.e. disconnection of local power supply from the network
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
- B63B—SHIPS OR OTHER WATERBORNE VESSELS; EQUIPMENT FOR SHIPPING
- B63B35/00—Vessels or similar floating structures specially adapted for specific purposes and not otherwise provided for
- B63B35/44—Floating buildings, stores, drilling platforms, or workshops, e.g. carrying water-oil separating devices
- B63B2035/4433—Floating structures carrying electric power plants
- B63B2035/446—Floating structures carrying electric power plants for converting wind energy into electric energy
-
- H—ELECTRICITY
- H02—GENERATION; CONVERSION OR DISTRIBUTION OF ELECTRIC POWER
- H02J—CIRCUIT ARRANGEMENTS OR SYSTEMS FOR SUPPLYING OR DISTRIBUTING ELECTRIC POWER; SYSTEMS FOR STORING ELECTRIC ENERGY
- H02J2300/00—Systems for supplying or distributing electric power characterised by decentralized, dispersed, or local generation
- H02J2300/20—The dispersed energy generation being of renewable origin
- H02J2300/28—The renewable source being wind energy
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Metallurgy (AREA)
- Materials Engineering (AREA)
- Electrochemistry (AREA)
- Inorganic Chemistry (AREA)
- Mechanical Engineering (AREA)
- Architecture (AREA)
- Ocean & Marine Engineering (AREA)
- Analytical Chemistry (AREA)
- Combustion & Propulsion (AREA)
- Structural Engineering (AREA)
- Civil Engineering (AREA)
- Power Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The application discloses an off-grid green ammonia production system of a floating wind power platform and a preparation process thereof, which are arranged on a floating platform body and comprise an off-grid power supply unit, an electrolytic tank unit, a seawater treatment unit, a raw material supply unit, an air separation unit, a synthesis ammonia unit and a solid oxide electrolytic tank module, wherein the off-grid power supply unit is used for supplying electric energy to the green ammonia production system, the electrolytic tank unit is used for obtaining hydrogen required for preparing green ammonia, the seawater treatment unit is used for supplying raw materials to an electrolytic tank module, the air separation unit is used for separating nitrogen required for preparing green ammonia from air, the synthesis ammonia unit is used for reacting hydrogen and nitrogen mixed gas to synthesize ammonia, and the electrolytic tank unit comprises a proton exchange membrane electrolytic tank module and a solid oxide electrolytic tank module.
Description
Technical Field
The application belongs to the technical field of offshore green ammonia preparation, and particularly relates to an off-grid green ammonia preparation system of a floating wind power platform and a preparation process thereof.
Background
Environmental protection and increasing energy demands have driven the development and utilization of renewable energy sources. The potential of 80% of the global offshore wind energy resources is reserved in the sea area with the water depth exceeding 60m, the quality of the wind resources is high, and the annual utilization rate can reach more than 45%. Conventionally, wind energy is converted into electric energy by a fan, boosted and transmitted to the shore for grid connection. The manufacturing cost of the submarine cable is high due to the fact that the far-sea wind power is far away from the coastline; meanwhile, due to the fact that the wind power utilization time and the wind power utilization intermittence are not matched with each other, the phenomenon of wind power abandoning and electricity abandoning is generated, and the wind power utilization rate is further reduced.
For this purpose, people openThe wind power is converted into hydrogen by utilizing an electrolysis water technology and then is conveyed to the shore to solve the problems. The process does not discharge CO 2 And is therefore considered a direction of future offshore wind power utilization. However, the volume energy density of the hydrogen is low, the transportation cost is high, and the development of wind power hydrogen production is restricted to a certain extent. In order to solve the problem, people transport the hydrogen and nitrogen in the air to synthesize ammonia, so that the problem of high hydrogen transportation cost is solved, and ammonia is also the most widely used chemical raw material and emerging fuel.
The traditional ammonia synthesis technology and the water electrolysis hydrogen production and intermittent wind power have the matching problem, and the Chinese patent with the application number of CN202110729287.1 is found through search, so that the renewable energy source ammonia synthesis system for combined cooling, heating and power is disclosed, and in the raw gas purification section, pressure swing adsorption is adopted, and a hydrogen catalytic oxidation catalyst and a water adsorbent are filled in an adsorption column at the same time, so that the raw gas purification process is simplified; in the ammonia separation section, temperature swing adsorption is combined with two times of cooling, so that the power consumption of the ammonia separation process is greatly reduced, the system saves energy, but the system still uses a power grid as production energy, does not meet the condition of offshore green ammonia production, and the byproduct energy is not fully utilized, so that a large amount of resources are wasted.
Disclosure of Invention
In order to solve the problems, the application provides the off-grid green ammonia production system of the floating wind power platform and the preparation process thereof, and the two water electrolysis hydrogen production modes and the air separation device are utilized to optimize the process flow, solve the problem of intermittent utilization of wind power, stop wind and electricity abandon and improve the utilization rate of wind power.
The technical scheme provided by the application is as follows:
the first part, a floating wind ionization net system for producing green ammonia, is arranged on the floating platform body, comprises an off-net power supply unit and is used for providing electric energy for the system for producing green ammonia;
an electrolyzer unit for obtaining hydrogen required for the preparation of green ammonia;
a seawater treatment unit for providing raw materials for the electrolytic tank module;
an air separation unit for separating nitrogen required for preparing green ammonia from air;
the ammonia synthesis unit is used for synthesizing ammonia gas by reacting the hydrogen-nitrogen mixed gas;
the electrolytic tank unit comprises a proton exchange membrane electrolytic tank module and a solid oxide electrolytic tank module, the seawater treatment unit comprises a seawater reverse osmosis desalination deionization module and a seawater evaporation type desalination module, the seawater reverse osmosis desalination deionization module provides deionized water for the proton exchange membrane electrolytic tank module, and the seawater evaporation type desalination module provides water vapor for the solid oxide electrolytic tank module.
In the above system, preferably, the proton exchange membrane electrolyzer module and the solid oxide electrolyzer module are each provided in plural.
In the above system, preferably, the air separation unit includes an air separation nitrogen making module that separates nitrogen in air as one of raw materials for synthesizing ammonia by using a pressure swing adsorption principle.
In the above system, preferably, the ammonia synthesis unit includes an ammonia synthesis reaction module, and a mixed gas pressurizing module is disposed at the front end of the ammonia synthesis reaction module, and is used for pressurizing the hydrogen-nitrogen mixed gas, and the circulating gas formed after the reaction of the ammonia synthesis reaction module passes through a seawater evaporation type desalination module to provide heat energy for the circulating gas.
In the above system, preferably, a circulating gas condensation separation module is disposed at the rear end of the synthesis ammonia reaction module, and is used for liquefying and separating ammonia gas, and the remaining circulating gas returns to the synthesis ammonia reaction module again through a circulating gas pressurization module.
In the above system, preferably, the cycle gas condensation separation module is provided with a vent device.
The second part, a preparation flow of green ammonia by a floating wind ionization net, is suitable for the system of green ammonia by the floating wind ionization net, and comprises the following steps:
s1: part of seawater enters a seawater reverse osmosis desalination and deionization module to form deionized water, and then enters a proton exchange membrane electrolysis tank module to prepare hydrogen;
s2: the other part of seawater enters a seawater evaporation type desalination module, and steam is formed by heat energy generated by the synthetic ammonia reaction module and enters a solid oxide electrolysis tank module to prepare hydrogen;
s3: the air enters an air separation nitrogen preparation module to separate out nitrogen, then is mixed with the hydrogen prepared in the S, S step, pressurized by a mixed gas pressurizing module, and then enters a synthetic ammonia reaction module to prepare ammonia;
s4: the high Wen Anqi prepared by the synthetic ammonia reaction module and the hydrogen and nitrogen which are not fully reacted enter a circulating gas condensation separation module to liquefy and separate ammonia after the temperature of the heated seawater is reduced, and the rest circulating gas returns to the synthetic ammonia reaction module again through a circulating gas pressurizing module to continuously synthesize ammonia;
s5: when the power supplied by the off-grid power supply unit is insufficient, the synthetic ammonia reaction module needs to perform load reduction operation, at the moment, part of the proton exchange membrane electrolyzer modules are closed first, and when the load is smaller and smaller until all the proton exchange membrane electrolyzer modules are closed, the load of the solid oxide electrolyzer modules starts to be reduced.
In the above preparation scheme, it is preferable that the mass ratio of the hydrogen gas provided in the proton exchange membrane electrolyzer module to the hydrogen gas provided in the solid oxide electrolyzer module is 9:1.
The third part, a floating wind power platform for bear the above-mentioned floating wind ionization net system green ammonia, including floating platform body, be equipped with centralized control room, quick-witted pump cabin, torch arm and liquid ammonia storage cabin on the floating platform body, the torch arm sets up at floating platform body bow, and liquid ammonia storage cabin connects the liquid outlet of circulating gas condensation separation module, is used for storing finished product liquid ammonia.
Preferably, the floating platform body is further provided with an ammonia output module, the ammonia output module is connected with the liquid ammonia storage cabin and used for the connection of liquid ammonia, the floating platform body is further provided with a standby power supply and a debugging power supply, and the standby power supply and the debugging power supply utilize ammonia in the liquid ammonia storage cabin as fuel to generate electricity.
In summary, the beneficial effects of the application are as follows:
(1) The application optimizes the technological process by utilizing two modes of water electrolysis hydrogen production and an air separation device, solves the problem of wind power intermittent utilization by the elastic operation of the proton exchange membrane electrolytic tank and the solid oxide electrolytic tank, eliminates wind abandon and electricity abandon, improves the wind power utilization rate, simultaneously the solid oxide electrolytic tank can utilize the heat of circulating gas to supply water vapor, forms thermal circulation, reduces energy consumption, and improves the commercialization degree of the deep-open sea wind field, the proton exchange membrane electrolytic tank and the solid oxide electrolytic tank.
(2) The application is provided with a standby power supply and a power supply for debugging, and utilizes the product ammonia as fuel to generate power, so that the problems of standby power supply and project initial debugging are solved, and meanwhile, the whole ammonia synthesis process is maintained in a hot standby state when the wind farm cannot output power, and the continuity of the subsequent process is ensured.
(3) The raw materials of the application are water and air, the electric power energy source is wind power generation, the air discharge amount is less than that of the traditional natural gas reforming synthetic ammonia, and the whole device production process does not discharge CO 2 Meets the requirement of green ammonia production.
Drawings
FIG. 1 is a flow chart of the process of synthesizing ammonia according to the present application;
FIG. 2 is a schematic top view of a floating wind platform according to the present application;
FIG. 3 is a schematic side view of a floating wind power platform of the present application.
The reference numerals are as follows:
1. a floating platform body; 2. a centralized control room; 3. a pump cabin; 4. a flare boom; 5. a liquid ammonia storage tank; 6. an air separation nitrogen making module; 7. a seawater reverse osmosis desalination deionization module; 8. an ammonia output module; 9. a proton exchange membrane electrolyzer module; 10. a solid oxide electrolyser module; 11. a circulating gas condensation separation module; 12. a recycle gas pressurizing module; 13. a seawater evaporation type desalination module; 14. a synthetic ammonia reaction module; 15. and the mixed gas pressurizing module.
Detailed Description
The present application will be further described in detail with reference to the following examples, which are only for the purpose of illustrating the application and are not to be construed as limiting the scope of the application.
As shown in fig. 1 and fig. 2, the floating wind ionization net green ammonia production system is arranged on a floating platform body 1 and comprises an off-net power supply unit, an electrolytic tank unit, a seawater treatment unit, an air separation unit and a synthetic ammonia unit, wherein the off-net power supply unit is used for providing electric energy for the green ammonia production system, the electrolytic tank unit is used for obtaining hydrogen required for preparing green ammonia, the seawater treatment unit is used for providing raw materials for an electrolytic tank module, the air separation unit is used for separating nitrogen and synthetic ammonia required for preparing green ammonia from air, and the nitrogen and synthetic ammonia unit is used for reacting hydrogen and nitrogen mixture to synthesize ammonia;
in order to solve the problem of intermittent utilization of wind power, two hydrogen preparation methods are configured, wherein an electrolytic tank unit comprises a proton exchange membrane electrolytic tank module 9 and a solid oxide electrolytic tank module 10, a seawater treatment unit comprises a seawater reverse osmosis desalination and deionization module 7 and a seawater evaporation type desalination module 13, the seawater reverse osmosis desalination and deionization module 7 provides deionized water for the proton exchange membrane electrolytic tank module 9, and the seawater evaporation type desalination module 13 provides water vapor for the solid oxide electrolytic tank module 10.
The annual production of synthetic ammonia is obtained based on factors such as annual energy production of a wind farm, annual average utilization coefficient and the like, and one or more systems for producing green ammonia by using the floating wind ionization net can be configured to operate according to the size of the wind farm, and the specific configuration mode is common knowledge of a person skilled in the art and is not repeated in the application.
Specifically, in this embodiment, the off-grid power supply unit is wind power, and electricity generated by the wind farm is used as a main energy source for driving the platform to work, so that CO is not discharged during the process of preparing the green ammonia 2 Therefore, the prepared product ammonia is green, and further, the off-grid power supply unit can be connected with a standby power supply and a debugging power supply, the standby power supply and the debugging power supply generate power by taking ammonia in the liquid ammonia storage cabin as fuel, and the standby power supply and the debugging power supply are in a redundant design and adopt an N+1 mode.
After seawater from the ocean is lifted onto a floating body, a part of the seawater enters a seawater reverse osmosis desalination and deionization module 7 for treatment, and the prepared deionized water at least needs to meet GB/T37562-2019 (corresponding to ISO 3696GRADE 2 or ASTM D1193-92 TYPE II), namely the conductivity is not more than 1 mu s/cm, and the deionized water meeting the requirements enters a proton exchange membrane electrolytic tank module 9 for hydrogen production operation; the other part of seawater enters a seawater evaporation type desalination module 13, and the steam obtained by heating enters a solid oxide electrolysis tank module 10 to carry out hydrogen production operation, and hydrogen produced by the proton exchange membrane electrolysis tank module 9 and the solid oxide electrolysis tank module 10 jointly provides hydrogen raw materials for synthesizing ammonia.
In a preferred embodiment, the proton exchange membrane electrolyzer module 9 and the solid oxide electrolyzer module 10 are each provided in several numbers.
In particular, the proton exchange membrane electrolyzer module 9 and the solid oxide electrolyzer module 10 are both configured with multiple electrolyzers in parallel, which can adapt the system to the instability of renewable energy sources and increase the flexibility of variable working conditions.
Each proton exchange membrane electrolyzer module 9 and solid oxide electrolyzer module 10 can be designed by adopting a container, so that the system can be conveniently lifted away after being disassembled and replaced immediately, and the running reliability of the system is improved.
As a further optimized embodiment, the air separation unit is an air separation nitrogen making module 6, the air separation nitrogen making module 6 adopts a PSA air separation device, nitrogen in air is separated by using a pressure swing adsorption principle, the air separation module technology is one of raw materials for synthesizing ammonia, the air separation module technology is the prior art, and is used for separating components of the air by using a low-temperature freezing principle, and the application is not repeated, and is applied to the green ammonia making system of the application, the separated effective components are nitrogen, and the other components can be recycled.
The synthesis ammonia unit comprises a synthesis ammonia reaction module 14, a mixed gas pressurizing module 15 is arranged at the front end of the synthesis ammonia reaction module 14 and is used for pressurizing the hydrogen-nitrogen mixed gas, and circulating gas formed after the reaction of the synthesis ammonia reaction module 14 passes through a seawater evaporation type desalination module 13 and provides heat energy for the circulating gas.
Specifically, the hydrogen and the nitrogen are mixed according to a certain proportion and then enter a mixed gas pressurizing module 15, the pressurized mixture enters a synthetic ammonia reaction module 14, the hydrogen and the nitrogen are synthesized to generate ammonia gas under a certain pressure and temperature, the high-temperature ammonia gas and the unreacted hydrogen and nitrogen are called circulating gas, the circulating gas enters a seawater evaporation type desalination module 13 to heat seawater, and the synthetic ammonia unit is further provided with a safety fire protection system and an anti-pollution system. The safety fire protection system meets the requirements of SOLAS and the pollution prevention system meets the requirements of MAPROL.
The rear end of the synthesis ammonia reaction module 14 is provided with a circulating gas condensation separation module 11 for liquefying and separating ammonia gas, and the rest circulating gas returns to the synthesis ammonia reaction module 14 again through a circulating gas pressurizing module 12.
Further, the recycle gas condensation separation module 11 is provided with a venting device, compared with the natural gas reforming process, the recycle gas is cleaner, and impurities such as argon, water vapor and the like are fewer, so that the discharge amount is very small, and the influence on the environment is small.
The system can also produce pure oxygen and other substances as by-products, and the application can provide corresponding equipment for collecting the pure oxygen and other substances.
The preparation process of the green ammonia by the floating wind ionization net is suitable for the system for preparing the green ammonia by the floating wind ionization net, uses sea water and air as preparation raw materials, uses wind power generation as main power supply, realizes green ammonia preparation and comprises the following steps:
s1: part of seawater enters a seawater reverse osmosis desalination and deionization module 7 to form deionized water, and then enters a proton exchange membrane electrolytic cell module 9 to prepare hydrogen;
seawater from the sea enters a seawater reverse osmosis desalination and deionization module 7 for seawater desalination, deionized water is further deionized after desalination, and deionized water enters a proton exchange membrane electrolytic cell module 9 for hydrogen production.
S2: the other part of seawater enters a seawater evaporation type desalination module 13, and the heat energy generated by a synthetic ammonia reaction module 14 forms vapor to enter a solid oxide electrolysis tank module 10 for preparing hydrogen;
the solid oxide electrolyzer module 10 requires water vapor for hydrogen production, which is provided by the seawater evaporative desalination module 13, and the heat required by the seawater evaporative desalination module 13 is derived from the synthesis ammonia recycle gas.
S3: the air enters an air separation nitrogen making module 6 to separate out nitrogen, is mixed with the hydrogen prepared in the steps S1 and S2, is pressurized by a mixed gas pressurizing module 15, and then enters a synthetic ammonia reaction module 14 to prepare ammonia;
specifically, the mixing ratio of nitrogen to hydrogen is 1:3, and then the mixture enters the mixed gas pressurizing module 15, and the pressurizing pressure is more than 200bar.
The mixed gas is heated to high temperature in the synthesis ammonia reaction module 14, the synthesis tower in the synthesis ammonia reaction module 14 adopts an iron-based catalyst, the heating temperature is 380-500 ℃, and a heat source for heating is provided by wind power and is connected with a standby power supply.
The mixed gas (1:3 molar ratio of nitrogen to hydrogen) is synthesized as ammonia in the synthesis column in the ammonia synthesis reaction module 14, and only about 20% of hydrogen is often synthesized as ammonia according to production experience.
The high temperature ammonia gas produced by the reaction and the hydrogen gas and nitrogen gas which are not completely reacted are referred to as recycle gas.
S4: the high Wen Anqi prepared by the synthetic ammonia reaction module 14 and the hydrogen and nitrogen which are not fully reacted enter the circulating gas condensation separation module 11 to liquefy and separate the ammonia after the temperature of the heated seawater is reduced, and the rest circulating gas returns to the synthetic ammonia reaction module 14 again through the circulating gas pressurizing module 12 to continuously synthesize the ammonia;
the circulating gas enters the seawater evaporation type desalination module 13, the temperature of the circulating gas is reduced to the point that the circulating gas cannot be evaporated and then leaves the seawater evaporation type desalination module 13, the circulating gas enters the circulating gas condensation separation module 11, ammonia in the circulating gas is condensed into a liquid state, the ammonia is further separated, the residual hydrogen and nitrogen mixed circulating gas enters the circulating gas pressurizing module 12, and the pressurized circulating gas enters the synthetic ammonia reaction module 14 again and enters the synthetic ammonia flow path again.
Specifically, the high temperature of the circulating gas is utilized, the principle of depressurization and heating is adopted, the seawater is distilled to obtain water vapor, and the water vapor is used as the raw material gas of the solid oxide electrolytic cell module 10 at the temperature of 120-150 ℃.
The circulating gas with reduced temperature enters the circulating gas condensation separation module 11, the temperature of the circulating gas is reduced to-20-20 ℃ (according to the pressure during ammonia liquefaction), and ammonia is liquefied, so that the ammonia is separated.
The rest circulating gas enters the circulating gas pressurizing module 12, is pressurized to more than 200bar, and then enters the synthetic ammonia reacting module 14 to continuously circulate synthetic ammonia.
S5: when the off-grid power supply unit is not enough in power supply, the ammonia synthesis reaction module 14 needs to perform load reduction operation, at this time, part of the proton exchange membrane electrolyzer modules 9 are turned off first, and when the load is smaller and smaller until all the proton exchange membrane electrolyzer modules 9 are turned off, the load of the solid oxide electrolyzer module 10 starts to be reduced.
Specifically, because the hydrogen production temperature of the proton exchange membrane electrolyzer module 9 is low, generally 60-100 ℃, and the maintenance is relatively simple, a part of the proton exchange membrane electrolyzer module 9 is first selected to be closed, and the proton exchange membrane electrolyzer module 9 and the solid oxide electrolyzer module 10 which are in line are closed or reduced to be in a hot standby state all the time.
When the output power of the wind farm is small to a certain proportion, the proton exchange membrane electrolytic cell 9 is closed to produce hydrogen, and the solid oxide electrolytic cell 10 and the synthetic ammonia reaction module 14 are in a hot standby state.
When the wind farm cannot output power, a standby power supply is needed to provide power to maintain the whole ammonia synthesis process in a hot standby state. The power required at this time is about 8-10% of the energy consumption of the maximum operation condition of the whole system, when the wind speed of the external wind field reaches 3-4M/S of the cutting-in speed of the fan, the wind power field can output power, and at this time, the synthetic ammonia in the hot standby state can be started rapidly.
Further, the mass ratio of hydrogen gas provided in the proton exchange membrane electrolyzer module 9 to hydrogen gas provided in the solid oxide electrolyzer module 10 was 9:1.
Specifically, most of the time, the steam provided after evaporating the seawater can make the ratio of the amount of hydrogen generated by the solid oxide electrolytic cell module 10 to the amount of hydrogen required for synthesizing ammonia about 10% according to the heat carried by the recycle gas after the reaction of the synthetic ammonia, and the remaining 90% needs to be provided by the proton exchange membrane electrolytic cell module 9.
A floating wind power platform is used for bearing the system for preparing green ammonia by a floating wind ionization net and comprises a floating platform body 1, wherein a centralized control chamber 2, a pump cabin 3, a flare boom 4 and a liquid ammonia storage cabin 5 are arranged on the floating platform body 1, the flare boom 4 is arranged at the bow part of the floating platform body 1, and the liquid ammonia storage cabin 5 is connected with a liquid outlet of a circulating gas condensation separation module 11 and is used for storing finished liquid ammonia.
Specifically, the floating platform body 1 adopts a barge-type floating body structure, the ship-type bow and stern adopt streamline design, and the specific placement layout is designed according to the condition of wind, wave and sea conditions of the installation area, which is common knowledge of the person skilled in the art.
The floating platform body 1 can be fixed by adopting a distributed anchoring system or a single-point anchoring system, and a ballast system is further arranged on the floating platform body 1 and used for adjusting the floating state of the floating platform.
The centralized control room 2 is arranged at the tail part of the floating platform body 1 and is used for centralized measurement, monitoring, alarming and control of the whole device, and the centralized control room 2 is also provided with a living area and a maintenance area which are used for guaranteeing daily maintenance and repair of the whole very ammonia process. The maintenance comprises at least one spare part crane, one spare part lifting platform and one maintenance room, the spare part is lifted from the outside of the floating platform body 1 to the main deck, the general maintenance can be performed in the maintenance room of the floating body maintenance area as much as possible, if special personnel and tools are needed, the crane is used for lifting to the transport means, and the specified place is maintained.
The pump cabin 3 is provided with a generator set, a nitrogen generating device, a compressed air and instrument gas generating device and the like, and is also provided with pumps and related systems necessary for ballast, fire protection, bilge and the like, wherein the generator set is a standby power supply and a debugging power supply, and adopts a redundant design and adopts ammonia as fuel.
The flare boom 4 is arranged at the bow part of the floating platform body 1, and is provided with a pilot burner for burning off the discharged in the process.
Further, the floating platform body 1 is further provided with an ammonia output module 8, the ammonia output module 8 is connected with the liquid ammonia storage cabin 5 and used for the connection of liquid ammonia to be connected with the liquid ammonia storage cabin 5, the floating platform body 1 is further provided with a standby power supply and a power supply for debugging, and the standby power supply and the power supply for debugging utilize ammonia in the liquid ammonia storage cabin 5 as fuel to generate electricity.
The generated product ammonia is in a liquid state and is stored in the liquid ammonia storage cabin 5 of the floating platform body 1, the liquid ammonia storage cabin 5 can be provided with a plurality of liquid ammonia lighters such as 5a,5b,5c and 5d in fig. 3, the liquid ammonia is lightered by a pump arranged in the liquid ammonia storage cabin 5, the liquid ammonia lighters an ammonia external conveying module 8, the ammonia external conveying module 8 has a metering function, and the external conveying liquid ammonia is lightered to a liquid ammonia conveying ship which is stopped beside the floating platform body 1 after being metered and is carried away.
In other embodiments, the floating platform body 1 may also act as a fueling station for a commercial vessel that uses ammonia as fuel.
In particular, the ammonia delivery module 8 is mainly used for delivering the liquid ammonia storage tank 5 outwards, but has the function of simultaneously docking ammonia into the liquid ammonia storage tank 5 from the outside, so that it can be ensured that in the phase of debugging and wind farm no power delivery, if the amount of liquid ammonia stored in the liquid ammonia storage tank 5 is insufficient, enough ammonia is available from the outside to maintain the hot standby of the whole ammonia synthesis system.
It should be noted that, in the drawings or the description, the implementation manner not shown or described is a manner known to those of ordinary skill in the art, and is not described in detail, and the above definitions of the elements and the methods are not limited to the specific structures, shapes or manners mentioned in the embodiments.
It should be noted that, in the embodiments, directional terms such as "upper", "lower", "front", "rear", "left", "right", "inner", "outer", etc. refer to the directions of the drawings only, and are not intended to limit the scope of the present application.
While the foregoing description illustrates and describes the preferred embodiments of the present application, as noted above, it is to be understood that the application is not limited to the forms disclosed herein but is not to be construed as excluding other embodiments, and that various other combinations, modifications and environments are possible and may be made within the scope of the inventive concepts described herein, either by way of the foregoing teachings or by those of skill or knowledge of the relevant art. And that modifications and variations which do not depart from the spirit and scope of the application are intended to be within the scope of the appended claims.
Claims (10)
1. The floating wind ionization net green ammonia production system is arranged on a floating platform body (1) and is characterized by comprising an off-net power supply unit for providing electric energy for the green ammonia production system;
an electrolyzer unit for obtaining hydrogen required for the preparation of green ammonia;
a seawater treatment unit for providing raw materials for the electrolytic tank module;
an air separation unit for separating nitrogen required for preparing green ammonia from air;
the ammonia synthesis unit is used for synthesizing ammonia gas by reacting the hydrogen-nitrogen mixed gas;
the electrolytic tank unit comprises a proton exchange membrane electrolytic tank module (9) and a solid oxide electrolytic tank module (10), the sea water treatment unit comprises a sea water reverse osmosis desalination deionization module (7) and a sea water evaporation type desalination module (13), the sea water reverse osmosis desalination deionization module (7) provides deionized water for the proton exchange membrane electrolytic tank module (9), and the sea water evaporation type desalination module (13) provides water vapor for the solid oxide electrolytic tank module (10).
2. The floating wind ionization net system for producing green ammonia according to claim 1, wherein the proton exchange membrane electrolyzer module (9) and the solid oxide electrolyzer module (10) are both provided with a plurality of.
3. The floating wind ionization net system for producing green ammonia according to claim 1, wherein the air separation unit comprises an air separation nitrogen producing module (6), and the air separation nitrogen producing module (6) adopts a pressure swing adsorption principle to separate nitrogen in the air as one of raw materials for synthesizing ammonia.
4. The floating wind ionization net system for producing green ammonia according to claim 1, wherein the synthetic ammonia unit comprises a synthetic ammonia reaction module (14), and a mixed gas pressurizing module (15) is arranged at the front end of the synthetic ammonia reaction module (14) and is used for pressurizing the hydrogen-nitrogen mixed gas, and the circulating gas formed after the reaction of the synthetic ammonia reaction module (14) passes through a seawater evaporation type desalination module (13) to provide heat energy for the circulating gas.
5. The floating wind ionization net system for producing green ammonia according to claim 4, wherein the rear end of the synthetic ammonia reaction module (14) is provided with a circulating gas condensation separation module (11) for liquefying and separating ammonia gas, and the rest circulating gas returns to the synthetic ammonia reaction module (14) again through a circulating gas pressurizing module (12).
6. The system for producing green ammonia by using the floating wind ionization network according to claim 5, wherein the circulating gas condensation separation module (11) is provided with an emptying device.
7. A process for preparing green ammonia by a floating wind ionization net, which is applicable to the system for preparing green ammonia by the floating wind ionization net as claimed in claims 1-6, and is characterized by comprising the following steps:
s1: part of seawater enters a seawater reverse osmosis desalination deionization module (7) to form deionized water, and then enters a proton exchange membrane electrolysis tank module (9) to prepare hydrogen;
s2: the other part of seawater enters a seawater evaporation type desalination module (13), and the heat energy generated by a synthetic ammonia reaction module (14) forms vapor to enter a solid oxide electrolysis tank module (10) for preparing hydrogen;
s3: air enters an air separation nitrogen making module (6) to separate nitrogen, is mixed with hydrogen prepared in the steps S1 and S2, is pressurized by a mixed gas pressurizing module (15), and then enters a synthetic ammonia reaction module (14) to prepare ammonia;
s4: the high Wen Anqi prepared by the synthetic ammonia reaction module (14) and hydrogen and nitrogen which are not fully reacted enter a circulating gas condensation separation module (11) to liquefy and separate ammonia after the temperature of the heated seawater is reduced, and the rest circulating gas returns to the synthetic ammonia reaction module (14) again through a circulating gas pressurizing module (12) to continuously synthesize ammonia;
s5: when the power supplied by the off-grid power supply unit is insufficient, the synthetic ammonia reaction module (14) needs to perform load reduction operation, at the moment, part of the proton exchange membrane electrolyzer modules (9) are closed first, and when the load is smaller and smaller until all the proton exchange membrane electrolyzer modules (9) are closed, the load of the solid oxide electrolyzer modules (10) starts to be reduced.
8. The process for preparing green ammonia by using the floating wind ionization network according to claim 7, wherein the mass ratio of the hydrogen provided in the proton exchange membrane electrolyzer module (9) to the hydrogen provided in the solid oxide electrolyzer module (10) is 9:1.
9. a floating wind power platform for carrying the system for preparing green ammonia by a floating wind ionization network according to claims 1-6, which is characterized by comprising a floating platform body (1), wherein a centralized control chamber (2), a pump cabin (3), a flare boom (4) and a liquid ammonia storage cabin (5) are arranged on the floating platform body (1), the flare boom (4) is arranged at the bow of the floating platform body (1), and the liquid ammonia storage cabin (5) is connected with a liquid outlet of a circulating gas condensation separation module (11) and is used for storing finished liquid ammonia.
10. The floating wind power platform according to claim 9, wherein the floating platform body (1) is further provided with an ammonia output module (8), the ammonia output module (8) is connected with the liquid ammonia storage cabin (5) for the liquid ammonia to be connected in and out, the floating platform body (1) is further provided with a standby power supply and a power supply for debugging, and the standby power supply and the power supply for debugging utilize ammonia in the liquid ammonia storage cabin (5) as fuel to generate electricity.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202311066190.2A CN117105242A (en) | 2023-08-23 | 2023-08-23 | Floating wind power platform off-grid system for preparing green ammonia and preparation process thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202311066190.2A CN117105242A (en) | 2023-08-23 | 2023-08-23 | Floating wind power platform off-grid system for preparing green ammonia and preparation process thereof |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN117105242A true CN117105242A (en) | 2023-11-24 |
Family
ID=88806987
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202311066190.2A Pending CN117105242A (en) | 2023-08-23 | 2023-08-23 | Floating wind power platform off-grid system for preparing green ammonia and preparation process thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN117105242A (en) |
-
2023
- 2023-08-23 CN CN202311066190.2A patent/CN117105242A/en active Pending
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN107893237B (en) | Hydrogenation stations based on high-temperature electrolysis vapor hydrogen producing technology | |
| US8715581B2 (en) | Modular power plant unconnected to the grid | |
| CN110904464A (en) | Seawater electrolysis hydrogen production system based on offshore wind power | |
| US20130039833A1 (en) | Systems and methods for producing ammonia fertilizer | |
| CN211848150U (en) | Seawater electrolysis hydrogen production system based on offshore wind power | |
| WO2019204857A1 (en) | Offshore energy generation system | |
| JP2005145218A (en) | Hydrogen manufacturing facility and hydrogen manufacturing transportation system on ocean | |
| CN216215922U (en) | Marine hydrogen production ammonia production storage tank platform based on wind power | |
| CN114142791A (en) | All-weather light-heat-electricity combined supply system for ship with multiple complementary functions | |
| CN215904702U (en) | Marine hydrogen manufacturing system methyl alcohol storage tank platform based on wind power | |
| EP3919369A1 (en) | Vessel for desalinating salt water, converting same into drinking water and generating electrical energy | |
| CN215907999U (en) | Marine hydrogen production system methyl alcohol storage tank platform based on nuclear power, wind-powered electricity generation combine together | |
| CN105757978B (en) | A kind of boat-carrying heat pump water heater system and heating method | |
| US20230041653A1 (en) | Offshore production facility arrangement | |
| CN114909871B (en) | Method and device for preparing liquid hydrogen by offshore off-grid superconducting wind power | |
| CN117105242A (en) | Floating wind power platform off-grid system for preparing green ammonia and preparation process thereof | |
| CN215911912U (en) | Marine hydrogen production and ammonia production storage cabin platform based on combination of nuclear power and wind power | |
| CN114893156B (en) | Offshore wind power hydrogen production coupled combustible ice exploitation, storage and transportation system and method | |
| CN113479905B (en) | Self-deoxidization ammonia synthesis tower and renewable energy source ammonia synthesis system | |
| KR101788743B1 (en) | Fuel cell system for ship | |
| CN115354345A (en) | Photovoltaic photo-thermal coupling co-electrolysis combined garbage power generation comprehensive energy system and process method thereof | |
| KR102190948B1 (en) | Ship | |
| KR20180075263A (en) | Ship | |
| CN218089824U (en) | Floating device for producing hydrogen by electrolyzing water to synthesize green ammonia | |
| CN216185896U (en) | Marine hydrogen production ammonia production storage cabin platform based on nuclear power |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |