WO2019000623A1 - 一种甲烷化反应系统、发电厂调峰系统及发电厂 - Google Patents

一种甲烷化反应系统、发电厂调峰系统及发电厂 Download PDF

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WO2019000623A1
WO2019000623A1 PCT/CN2017/099628 CN2017099628W WO2019000623A1 WO 2019000623 A1 WO2019000623 A1 WO 2019000623A1 CN 2017099628 W CN2017099628 W CN 2017099628W WO 2019000623 A1 WO2019000623 A1 WO 2019000623A1
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power plant
methanation reaction
high pressure
boiler
carbon dioxide
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PCT/CN2017/099628
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English (en)
French (fr)
Inventor
杨豫森
崔华
徐波
谭智
陈辉
展望
陈超
朱明志
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赫普热力发展有限公司
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Publication of WO2019000623A1 publication Critical patent/WO2019000623A1/zh

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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
    • C07C1/02—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon
    • C07C1/12—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon from carbon dioxide with hydrogen

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  • the present invention relates to the field of electric energy technology, and more particularly to a methanation reaction system, and further includes a power plant peak shaving system and a power plant including the above methanation reaction system.
  • the cogeneration unit operates in a "heat-set" mode, and the peak-shaving capability is only about 10%. Difficulties in peak shaving have become the most prominent problem in grid operation.
  • the domestic thermal power flexibility peaking transformation is aimed at the winter heating unit, and how to adjust the summer peaking is a difficult problem in front of many thermal power plants. In order to meet the peak demand of the power grid and the survival needs of the power plant in the fierce competition, the depth Peaking is imperative.
  • an object of the present invention is to provide a methanation reaction system capable of utilizing the peak shaving balance of a power plant to significantly improve environmental protection and energy saving effects.
  • Another object of the present invention is to provide a power plant peak shaving system and a power plant including the above methanation reaction system, which can reasonably consume electric energy or emit carbon dioxide by providing the above methanation reaction system, thereby realizing energy integration. .
  • the present invention provides the following technical solutions:
  • a methanation reaction system comprising:
  • An electrolysis hydrogen production device connected to a power supply device of a power plant for receiving a peak-sharing balance output from a power supply device of the power plant to prepare hydrogen;
  • a methanation reaction apparatus connected to the electrolytic hydrogen production apparatus and the carbon dioxide supply source for preparing methane using hydrogen and carbon dioxide as raw materials.
  • the electrolytic hydrogen production unit is connected to the methanation reaction device through a hydrogen collection and purification device; and/or the hydrogen output line of the electrolytic hydrogen production device is connected to the hydrogen storage device.
  • a collecting control valve is disposed on the connecting line of the hydrogen output line of the electrolytic hydrogen producing device and the hydrogen storage device for connecting and closing the connecting line.
  • the oxygen discharge port of the electrolytic hydrogen production unit is connected to a boiler of a power plant to supply pure oxygen to the boiler.
  • the carbon dioxide supply source comprises:
  • a carbon dioxide capture system of a power plant for connecting a flue gas exhaust line of a boiler of a power plant to collect carbon dioxide in the flue gas discharged from the boiler;
  • the electrolytic hydrogen production device comprises an alkaline aqueous electrolytic hydrogen production device and/or a solid polymer electrolytic hydrogen production device.
  • the water source line of the electrolytic hydrogen production device is connected to the purified water preparation device of the water treatment plant; and/or the cooling water supply line of the electrolytic hydrogen production device is connected to the steam turbine condensate line of the boiler; Or, the cooling water discharge line of the electrolytic hydrogen production unit is connected to the power plant deaerator.
  • the electrolytic hydrogen production device comprises a high temperature solid oxide electrolyzed water hydrogen production device.
  • the water vapor inlet port of the high temperature solid oxide electrolysis water hydrogen plant is connected to the main steam discharge port of the boiler through an electric superheater.
  • the methanation reaction device comprises:
  • the first high pressure reaction tank for methanation reaction
  • the first high pressure reaction tank is provided with a raw material input line, and an output line of the first high pressure reaction tank is connected to a second high pressure through a high pressure waste pot for pressurization Reaction tank
  • the second high pressure reaction tank is connected to the third high pressure reaction tank through another high pressure waste pot;
  • the third high pressure reaction tank is provided with a methane output line.
  • the method further comprises:
  • a first superheater disposed on an output line of the first high pressure reaction tank to exchange and recover heat energy of the exhaust gas of the first high pressure reaction tank;
  • a boiler water preheater a gas outlet disposed at an outlet of the third high pressure reaction tank or a high pressure waste pot connected to the outlet, for superheating gas, water vapor and boiler feed water of the output of the third high pressure reaction tank Perform heat exchange.
  • the first superheater is connected to a steam turbine of a boiler of a power plant to provide thermal energy to the steam turbine; and/or
  • the liquid input end of the boiler water preheater is connected to the boiler feed water, and the liquid output end boiler steam drum is connected to the first superheater.
  • the third high-pressure reaction tank is connected to the gas-liquid separator through a gas pipeline after the boiler water preheater, and the gas-liquid separator is provided with a natural gas collection pipeline and/or a condensed water collection pipeline.
  • the condensed water collecting line is connected to a water source line of the electrolytic hydrogen producing unit for supplying condensed water to the electrolytic hydrogen producing unit.
  • the methane output line of the methanation reaction unit is connected to a natural gas pipeline network, a natural gas storage facility, and/or a burner of a boiler of the power plant.
  • a power plant peak shaving system comprising a power plant power supply device, further comprising the methanation reaction system according to any one of the above, wherein the electrolysis hydrogen plant of the methanation reaction system is connected to the power plant of the power plant, To obtain peak shaving balance.
  • the power plant power supply device includes a generator output grid and an inverter connected to the generator output grid, the inverter connecting the electrolysis hydrogen generator.
  • the method further comprises:
  • the power plant centralized control center is configured to control the peak shaving balance power, and the power plant centralized control center is connected with the power plant of the power plant and the power grid dispatching center;
  • a power grid dispatching center configured to send a peak load command to the power plant centralized control center according to the real-time power generation and peak load demand situation in the area, where the power plant centralized control center refers to the peak load reference Let the control adjust the peak shaving balance.
  • a power plant comprising the methanation reaction system of any of the above, and/or the power plant peaking system of any of the above.
  • the methanation reaction system provided by the invention can directly consume the peak shaving balance power of the power plant, indirectly utilizes the abandoned wind, abandon the light, abandon the water, and abandon the nuclear power, thereby alleviating the problem of grid balance and peak-to-valley difference, and prolonging the service life of the power plant equipment. . Since the peaking balance power is subjected to hydrogen production operation and finally methane is produced, phase storage of electric energy is realized.
  • the invention combines electrolysis hydrogen production, hydrogen and carbon dioxide to produce methane, realizes the use of power plant peak shaving balance power, facilitates the utilization of energy-saving source and energy, and provides strong support for realizing environmental protection and energy-saving industrial production.
  • the carbon dioxide recovery of the power plant is realized, which can not only reduce carbon dioxide, but also generate methane or other fuel for self-use. Or access to the natural gas pipeline network to achieve the recycling of carbon dioxide by the power plant, and reduce the carbon emission intensity of the power plant as a whole.
  • the present invention also provides a power plant peak shaving system including the above methanation reaction system and a power plant including the above methanation reaction system.
  • FIG. 1 is a schematic structural view of a methanation reaction system provided by the present invention.
  • FIG. 2 is a schematic view showing the structure of a methanation reaction apparatus provided by the present invention.
  • 1 is an electrolysis hydrogen production device
  • 101 is an alkaline aqueous solution electrolysis hydrogen production device
  • 102 is a solid polymer electrolysis hydrogen production device
  • 103 is a high temperature solid oxide electrolysis water hydrogen production device
  • 2 is carbon dioxide capture system
  • 3 boiler
  • 4 methanation reaction equipment
  • 5 is hydrogen collection and purification device
  • 6 is power plant power supply device
  • 7 is pure water preparation device
  • 8 is deaerator
  • 9 High temperature heater
  • 10 is steam turbine
  • 11 low temperature heater
  • 12 is power grid and power plant peaking control platform
  • 13 is generator;
  • 401 is a first high pressure reaction tank
  • 402 is a second high pressure reaction tank
  • 403 is a third high pressure reaction tank
  • 411 is a first superheater
  • 404 is a boiler steam drum
  • 405 is a boiler water preheater
  • 601 is an inverter
  • 602 is an electric superheater
  • 121 is the power grid dispatching center and 122 is the power plant centralized control center.
  • the core of the present invention is to provide a methanation reaction system capable of utilizing the peak shaving balance of a power plant to significantly improve environmental protection and energy saving effects.
  • FIG. 1 is a schematic structural view of a methanation reaction system provided by the present invention
  • FIG. 2 is a schematic structural view of a methanation reaction device provided by the present invention.
  • the invention provides a methanation reaction system, which mainly comprises: an electrolysis hydrogen production device 1, a carbon dioxide supply source for providing carbon dioxide, and a methanation reaction device 4.
  • the electrolysis hydrogen production device 1 is a device for preparing hydrogen by using a peak shaving balance power of a power plant as a power source.
  • the electrolysis hydrogen production device 1 may be connected to a power supply device 6 of a power plant for obtaining a power supply device of a power plant. 6
  • the peaking balance charge during the peaking process is subjected to electrolytic hydrogen production to obtain hydrogen.
  • the power plant can be a power plant of the type such as a thermal power plant.
  • the methanation reaction apparatus 4 is an apparatus for preparing methane using hydrogen and carbon dioxide as a raw material, and a methanation reaction apparatus 4 connected to an electrolytic hydrogen production apparatus 1 and a carbon dioxide supply source for preparing methane using hydrogen and carbon dioxide as raw materials.
  • the raw material input line of the methanation reaction device 4 is connected to the hydrogen output line of the electrolytic hydrogen production device 1, the carbon dioxide output line of the carbon dioxide supply source, and the methane output line of the methanation reaction device 4.
  • hydrogen is a general term for gas hydrogen and liquid hydrogen.
  • the hydrogen and carbon dioxide mentioned in the present application may be in a gaseous state, a liquid state, a gas-liquid mixed state or other forms, and the physical form of the two is not limited.
  • the electrolytic hydrogen production unit 1 referred to in the present application functions to generate hydrogen, which may be gaseous hydrogen, liquid hydrogen, or other forms of hydrogen energy.
  • the lines used to deliver hydrogen can be used to transport gases or liquids, or other delivery structures.
  • the source of carbon dioxide provides carbon dioxide, which can be other carbon dioxide gases, or it can be liquid or other forms of carbon dioxide.
  • the conduit for transporting carbon dioxide can be used to transport a gas or liquid, or other delivery structure.
  • the methanation reaction device 4 can produce methane or a methane-based flammable gas by carbon dioxide and hydrogen, under the conditions of a catalyst and high temperature and high pressure, and the invention is prepared by the electrolysis hydrogen production device 1.
  • Hydrogen and carbon dioxide are the raw materials for the methanation operation, so that a large amount of methane natural gas products can be obtained.
  • the methane natural gas products can be directly used for boiler combustion energy supply, or can be conveniently stored. Compared with electric energy, methane has Easy to store.
  • the power plant peak shaving system provided by the invention can directly consume the peak shaving balance power of the power plant, indirectly utilizes the abandoned wind, abandon the light, abandon the water and abandon the nuclear power, thereby alleviating the problem of grid balance and peak-to-valley difference, and prolonging the service life of the power plant equipment. Due to the hydrogen production operation of the peak shaving balance and the final production of methane, the phase storage of electric energy is realized, and the stable storage and effective utilization of energy is realized.
  • the invention combines electrolysis hydrogen production technology, hydrogen and carbon dioxide reaction to obtain methane and other combustible gas technologies, realizes the use of power plant peak shaving balance power, indirectly uses abandoned wind and abandoned light power, and produces gaseous fuel such as hydrogen and methane, in order to realize environmental protection. Energy-efficient industrial production provides strong support.
  • the power supply function of the power supply device 6 of the power plant may be controlled by the power grid and the power plant peaking control platform 12, according to the wind abandonment situation in the power grid region, combined with the peak load requirement of the power grid for the power plant, in the low valley electricity period A large amount of power is supplied to the electrolytic hydrogen production unit 1.
  • the hydrogen output line of the electrolytic hydrogen production device 1 is connected to the raw material delivery line of the methanation reaction device 4 through the hydrogen collection and purification device 5; and/or the hydrogen output tube of the electrolytic hydrogen production device 1
  • the road is connected to a hydrogen storage device for storing energy.
  • the electrolytic hydrogen generator 1 when the electrolytic hydrogen generator 1 produces liquid or other forms of hydrogen, the hydrogen output line, the hydrogen collection and purification device 5, and the like may perform other forms of hydrogen transport and collection.
  • a collection control valve is disposed on the connecting line between the hydrogen output line and the hydrogen storage device for connecting and closing the connecting line.
  • the electrolytic hydrogen production device 1 is provided with an oxygen discharge port for connecting the boiler 3 to provide pure oxygen, that is, the oxygen discharge port of the electrolytic hydrogen production device 1 is connected to the boiler 3 of the power plant to provide the boiler 3 with Pure oxygen.
  • the oxygen discharge port can be discharged to output oxygen or liquid oxygen.
  • the hydrogen is effectively treated by collecting and utilizing in parallel, so that the produced hydrogen has two uses, and on the other hand, it enters the methanation reaction device 4 through the purification treatment, and participates in the methanation operation;
  • the hydrogen or liquid hydrogen is stored by the hydrogen storage device, and the hydrogen or liquid hydrogen has better storage capacity than the electric energy, and the storage is more stable and less likely to be lost.
  • the invention utilizes the electrolytic hydrogen production process to realize the disguised storage of electric energy, and the hydrogen energy can be used as the future energy source, which is not only convenient to store, but also has no pollution and any carbon emission after combustion, and the hydrogen production and storage of the electric energy can ensure the preservation of the energy of the power plant.
  • the carbon dioxide supply source includes a carbon dioxide capture system 2 for connecting the power plant boiler 3, the collection boiler 3 for exhausting carbon dioxide from the flue gas, and the carbon dioxide capture system 2 is provided for use with the boiler The interface of the flue gas exhaust pipe of 3 is connected.
  • the source of carbon dioxide supply may also include a source of liquid carbon dioxide and/or a source of solid carbon dioxide.
  • the carbon dioxide capture system 2 is used for collecting carbon dioxide in the flue gas discharged from the boiler 3, and the carbon dioxide capture system 2 is connected to the flue gas discharge line of the boiler 3; the flue gas discharge line of the boiler 3 usually generates carbon dioxide such as exhaust gas, and the discharge amount is the boiler.
  • the present invention realizes the recovery of carbon dioxide emitted by the power plant by utilizing carbon dioxide in the boiler exhaust gas as an important raw material for methanation, which can not only reduce carbon dioxide, but also generate methane or other fuel for self-use or access. Natural gas pipeline network.
  • the carbon dioxide capture system of the carbon dioxide capture system 2 is provided with a carbon dioxide purification system.
  • the purification of carbon dioxide ensures sufficient reaction of the methanation equipment and purity of the methane preparation.
  • the electrolysis hydrogen production device 1 in the present application may be an alkaline aqueous electrolysis hydrogen production device 101, or may be other devices for hydrogen production in the prior art, such as solid polymer electrolysis.
  • the electrolytic hydrogen production apparatus 1 includes an alkaline aqueous electrolytic hydrogen production apparatus 101 and/or a solid polymer electrolytic hydrogen production apparatus 102. It should be noted that, referring to FIG. 1 , both the alkaline aqueous electrolytic hydrogen production device 101 and the solid polymer electrolytic hydrogen production device 102 can be powered by the power plant power supply device 6 or the inverter 601 of the power plant power supply device 6 . .
  • the alkaline aqueous electrolytic hydrogen production device 101 and the solid polymer electrolytic hydrogen production device 102 may be present at the same time, or only one of them may be included, and the specific setting may be adjusted according to actual conditions, and the hydrogen may be supplied to the hydrogen collection and purification device 5 after being used. It is collected or supplied to the methanation reaction device 4.
  • the water source line of the electrolytic hydrogen production unit 1 is connected to the purified water preparation unit 7 of the water treatment plant by the makeup water pump; and/or the cooling water supply line of the electrolytic hydrogen production unit 1 is connected.
  • the steam turbine condensate line of the boiler 3 uses the condensed water in the steam condensate line of the steam turbine as the cooling water of the electrolytic hydrogen production device 1, and the cooling water discharge line of the electrolytic hydrogen production device 1 is connected to the power plant deaerator, and the electrolytic hydrogen production device is utilized.
  • the cooling water after the intermediate temperature rise is recycled to the boiler; and/or the oxygen discharge port of the electrolytic hydrogen production unit 1 can be directly connected to the boiler 3 to supply the pure oxygen to the boiler 3.
  • the electrolytic hydrogen production device 1 can utilize a water source formed by a pure water preparation device in a chemical water treatment plant of a power plant, and the electrolytic hydrogen production device 1 can be a steam turbine 10 of the boiler 3. Condensate is used as a source of cooling water and is recycled.
  • the product of the electrolytic hydrogen production device 1 includes oxygen in addition to hydrogen, and the produced oxygen can also supply oxygen to the boiler, thereby achieving carbon neutral operation of the power plant and ensuring sufficient oxygen-rich combustion.
  • the produced oxygen can also supply oxygen to the boiler, thereby achieving carbon neutral operation of the power plant and ensuring sufficient oxygen-rich combustion.
  • three implementation manners are provided. The three methods may be combined with each other, may be set at the same time, or may include only one or two of them.
  • the water supply of the electrolytic hydrogen production unit 1 can also be supplied through a water tank or other equipment.
  • the electrolytic hydrogen production apparatus 1 includes a high temperature solid oxide electrolysis water hydrogen production unit 103, and the water vapor inlet port of the high temperature solid oxide electrolysis water hydrogen production unit 103 is connected by an electric superheater 602.
  • a high temperature solid oxide electrolysis water hydrogen production device 103 The power supply device 6 or the inverter 601 is powered by the power plant.
  • the high-temperature steam can be supplied from the main steam of the boiler 3, and specifically, the steam inlet thereof is connected to the main steam of the boiler 3 through the electric superheater 602.
  • the electric heater can be used to heat the main steam of the boiler 3, and usually can be heated to 800 degrees Celsius or higher to form high temperature steam, and is introduced into the high temperature solid oxide electrolysis water hydrogen producing device 103.
  • the high-temperature steam line of the electrolysis hydrogen-producing device 1 is connected to the main steam of the boiler 3, and then superheated to over 800 degrees by the electric superheater 602, and then enters the high-temperature solid oxide electrolyzed water hydrogen tank.
  • the above three electrolyte hydrogen devices may be combined, and the embodiment provided by the present invention includes at least four different electrolytic hydrogen production devices, wherein the high temperature solid oxide electrolysis water hydrogen production device 103 can be combined with a base.
  • the aqueous solution electrolysis hydrogen production unit 101 or the solid polymer electrolysis hydrogen production unit 102 is simultaneously disposed in the power plant system, and may include only one or two of them.
  • the methanation reaction apparatus 4 includes a first high pressure reaction tank 401, a second high pressure reaction tank 402, and a third high pressure reaction tank 403.
  • the first high pressure reaction tank 401, the second high pressure reaction tank 402 and the third high pressure reaction tank 403 are both used for the methanation reaction, and the first high pressure reaction tank 401 is provided with the raw material input line of the methanation reaction device 4, and the raw material.
  • the input line obtains hydrogen and carbon dioxide and is sent to the first high pressure reaction tank 401 for methanation reaction.
  • the outlet line of the first high pressure reaction tank 401 is connected to the second high pressure reaction tank 402 through a high pressure waste pot for pressurization.
  • the second high pressure reaction tank 402 is connected to the third high pressure reaction tank 403 through another high pressure waste pot, and the third high pressure reaction tank 403 is provided with a methane output line.
  • the above three-stage high-pressure reaction tanks are all high-temperature and high-pressure reaction tanks, and a catalyst for promoting methanation reaction may be provided.
  • the pressure of the three-stage high-pressure reaction tank can be set according to the step level, and the pressure and temperature are increased step by step.
  • the output line of the first high pressure reaction tank 401 is provided with a first superheater 411 disposed on the output line of the first high pressure reaction tank 401 to discharge the exhaust gas of the first high pressure reaction tank 401.
  • the heat is exchanged for recycling.
  • a boiler water preheater 405 is further included.
  • the boiler water preheater 405 is disposed at the outlet of the third high pressure reaction tank 403 or at the outlet of the third high pressure reaction tank 403.
  • the gas outlet of the connected high-pressure waste pot is used to exchange heat between the superheated gas and the water vapor of the output of the third high-pressure reaction tank 403 and the boiler feed water.
  • the first superheater 411 is coupled to the steam turbine 10 of the boiler 3 to provide thermal energy to the steam turbine 10.
  • the liquid input end of the boiler water preheater 405 is connected to the boiler feed water, and the liquid output end of the boiler water preheater 405 is connected to the first superheater 411 through the boiler drum 404.
  • the first high pressure reaction tank 401 is a high temperature and high pressure furnace, and the discharged methane gas or water vapor has high heat energy and pressure energy, and the energy can be used as a boiler structure.
  • the first superheater 411 is provided in the first high pressure reaction tank 401, and the first superheater 411 is used to exchange and recover the heat energy of the exhaust gas of the first high pressure reaction tank 401. Further, the thermal energy obtained by the first superheater 411 leads to the steam turbine 10 of the boiler 3 in the form of superheated steam through which the steam turbine 10 can perform work, and the above-mentioned device realizes the energy at the outlet of the first high-pressure reaction tank 401. Save on reuse.
  • a corresponding energy recovery device may also be disposed at the second high pressure reaction tank 402 and the third high pressure reaction tank 403 to utilize the energy of the reaction tank outlet.
  • the pressure of the second high pressure reaction tank 402 is greater than the pressure of the first high pressure reaction tank 401 and less than the pressure of the third high pressure reaction tank 403. And/or, the second high pressure reaction tank 402 is a high pressure reaction tank group in which at least two high pressure reaction tanks are connected in series.
  • the second high-pressure reaction tank 402 can form a step pressure with the first high-pressure reaction tank 401 and the third high-pressure reaction tank 403, respectively, so that full utilization of the reaction raw materials can be realized by continuous pressurization.
  • the second high pressure reaction tank 402 may be more than one reaction tank, that is, the methanation reaction apparatus 4 includes at least three reaction tanks.
  • the setting of the reaction tank of the above methanation reaction device 4 can be adjusted according to specific use conditions.
  • the third high pressure reaction tank 403 is connected to the gas liquid separator through a gas line behind the boiler water preheater 405, and the gas liquid separator is provided with a natural gas product collection line and/or Condensate collection line.
  • the condensed water collecting pipeline is connected to the water source pipeline of the electrolytic hydrogen generating device 1 to use the condensed water as the water source in the electrolytic hydrogen producing device 1 , and the setting realizes energy saving utilization to a large extent.
  • the methane output line of the methanation reaction unit 4 is connected to a natural gas pipeline network, a natural gas storage facility, and/or a burner of the boiler 3 of the power plant.
  • the power plant peak shaving system provided by the invention combines a conventional power plant, a hydrogen plant and a methanation reaction device 4 to heat the condensate of the power plant, and combines the feed water heating and the main steam generation with the hydrogen production and methane production process.
  • the waste heat recovery and energy cascade utilization are realized, which greatly improves the energy utilization of the power plant, not only saves effective electric energy, but also utilizes it through storage or methane production, and effectively utilizes carbon dioxide generated by the boiler to reduce power generation.
  • the plant's carbon dioxide emissions have great scientific and technological significance for environmental protection and energy conservation.
  • the present invention also provides a power plant peak shaving system including the above methanation reaction system, the system comprising a power plant power supply device 6, and a methanation reaction system provided by any of the above embodiments, a methanation reaction system
  • the electrolysis hydrogen generator 1 is connected to the power plant 6 to obtain a peak shaving balance.
  • the power plant power supply unit 6 includes a generator output grid and an inverter 601 connected to the generator output grid, and the inverter 601 is connected to the electrolysis hydrogen plant 1.
  • the generator output grid may be specifically a generator 13 .
  • the steam turbine 10 of the boiler 3 is connected to a generator 13, which serves as the main equipment of the generator plant and is the source of electrical energy during the peak shaving process.
  • the inverter 601 can supply the electric energy of the generator to the electrolysis hydrogen producing apparatus 1 for electrolysis operation.
  • the power plant centralized control center 122 for controlling the peak shaving balance power is further included, and the power plant power supply unit 6 can be connected to the power plant centralized control center, and the power plant centralized control center 122 is connected to the power grid dispatching center 121.
  • the dispatch center 121 sends a peak load command to the power plant control center 122 according to the real-time power generation and peak load demand situation in the area, and the power plant control center 122 controls and adjusts the peak balance power according to the peak load command.
  • the system includes a power grid and a power plant peaking control platform 12, the platform includes a power grid dispatching center 121 and a power plant centralized control center 122, and the power grid dispatching center 121 according to the real-time power generation and peaking load demand of the wind power photovoltaic in the area.
  • the power plant peaking command and the peak shaving load are issued to the power plant centralized control center 122, and the power plant centralized control center 122 controls the inverter 601 to control the inverter 13 by controlling the electric switch circuit connected between the generator 13 and the inverter 601.
  • the direct current is converted into an alternating current and used as a power source for the electrolytic hydrogen production apparatus 1.
  • the electrolysis hydrogen generator 1 supplies power to indirectly convert unstable wind power photovoltaic power into storable hydrogen or methane gas.
  • the flue gas discharge port of the boiler 3 of the power plant serves as a carbon dioxide supply source for the methanation reaction system, and supplies carbon dioxide for the methanation reaction, thereby realizing recovery and reuse of carbon dioxide in the boiler.
  • the present invention also provides a power plant comprising the methanation reaction system provided in the above various embodiments, or the above-mentioned power plant peak shaving system, and other structural features of the above power plant can refer to the prior art , will not repeat them here.

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Abstract

一种甲烷化反应系统，包含该甲烷化反应系统的发电厂调峰系统及发电厂。该甲烷化反应系统，包括：电解制氢装置，其连接到发电厂供电装置，用于接收发电厂供电装置输出的调峰结余电量以制备氢；二氧化碳提供源，用于提供二氧化碳；甲烷化反应设备，其连接到所述电解制氢装置和所述二氧化碳提供源，用于以氢和二氧化碳为原料制备甲烷。本发明提供的甲烷化反应系统可直接消耗发电厂的调峰结余电量，间接利用了弃风弃光弃水弃核电力，缓解了电网平衡和峰谷差问题。由于将调峰结余电量进行制氢操作，并最终制成甲烷气体，实现了电能的变相储存。

Description

一种甲烷化反应系统、发电厂调峰系统及发电厂
本申请要求于2017年06月29日提交中国专利局、申请号为201710515869.3、发明名称为“一种甲烷化反应系统、发电厂调峰系统及发电厂”的中国专利申请的优先权，其全部内容通过引用结合在本申请中。
技术领域
本发明涉及电力能源技术领域，更具体地说，涉及一种甲烷化反应系统，此外还包括一种包括上述甲烷化反应系统的发电厂调峰系统及发电厂。
背景技术
近年来，在中国三北地区电力市场容量富裕，燃机、抽水蓄能等可调峰电源稀缺，电网调峰与火电机组灵活性之间矛盾突出，电网消纳风电、光电、水电及核电等新能源的能力不足，因此，弃风、弃光、弃水和弃核现象严重。
现有技术中，热电联产机组“以热定电”方式运行，调峰能力仅为10％左右。调峰困难已经成为电网运行中最为突出的问题。目前国内火电灵活性调峰改造均针对冬季供热机组，而如何调整夏季调峰是摆在众多火电厂面前的一个难题，为了满足电网调峰需求，以及电厂在激烈竞争中的生存需要，深度调峰势在必行。
综上所述，如何避免发电厂调峰能源的浪费，是目前本领域技术人员亟待解决的问题。
发明内容
有鉴于此，本发明的目的是提供一种甲烷化反应系统，该系统能够利用发电厂的调峰结余电量，显著提升环保节能效应。
此外，本发明的另一目的是提供一种包括上述甲烷化反应系统的发电厂调峰系统和发电厂，由于设置了上述甲烷化反应系统，能够合理消耗电能或排放的二氧化碳，实现能源的整合。
为了实现上述目的，本发明提供如下技术方案：
一种甲烷化反应系统，包括：
电解制氢装置，其连接到发电厂供电装置，用于接收发电厂供电装置输出的调峰结余电量以制备氢；
二氧化碳提供源，用于提供二氧化碳；
甲烷化反应设备，其连接到所述电解制氢装置和所述二氧化碳提供源，用于以氢和二氧化碳为原料制备甲烷。
优选地，所述电解制氢装置通过氢收集净化装置连接到所述甲烷化反应设备；和/或，所述电解制氢装置的氢输出管路连接到氢贮存装置。
优选地，所述电解制氢装置的氢输出管路与氢贮存装置的连接管路上设有收集控制阀，用于连通和关闭该连接管路。
优选地，所述电解制氢装置的氧排出口连接到发电厂的锅炉，以向所述锅炉提供纯氧。
优选地，所述二氧化碳提供源包括：
发电厂的二氧化碳捕捉系统，所述二氧化碳捕捉系统用于连接发电厂的锅炉的烟气排出管路，以收集所述锅炉排出烟气中的二氧化碳；
和/或液体二氧化碳源、和/或固体二氧化碳源。
优选地，所述电解制氢装置包括碱性水溶液电解制氢装置和/或固体聚合物电解制氢装置。
优选地，所述电解制氢装置的水源管路连接水处理车间的纯净水制备装置；和/或，所述电解制氢装置的冷却水供应管路连接所述锅炉的汽轮机凝结水管路；和/或，所述电解制氢装置的冷却水排出管路连接电厂除氧器。
优选地，所述电解制氢装置包括高温固体氧化物电解水制氢装置。
优选地，所述高温固体氧化物电解水制氢装置的水蒸汽进入口通过电过热器连接所述锅炉的主蒸汽排出口。
优选地，所述甲烷化反应设备包括：
用于甲烷化反应的第一高压反应罐，所述第一高压反应罐设有原料输入管路，所述第一高压反应罐的输出管路通过用于加压的高压废锅连接第二高压反应罐；
用于甲烷化反应的第二高压反应罐，所述第二高压反应罐通过另一高压废锅连接第三高压反应罐；
第三高压反应罐，设有甲烷输出管路。
优选地，还包括：
第一过热器，设置在所述第一高压反应罐的输出管路上，将所述第一高压反应罐的排出气体的热能进行交换回收；
锅炉水预热器，设置在所述第三高压反应罐的出口或与所述出口连接的高压废锅的气体出口，用于将第三高压反应罐的输出的过热气体、水蒸气与锅炉给水进行换热。
优选地，所述第一过热器连接发电厂的锅炉的汽轮机，以便为所述汽轮机提供热能；和/或
所述锅炉水预热器的液体输入端连接锅炉给水，液体输出端锅炉汽包连接所述第一过热器。
优选地，所述第三高压反应罐通过锅炉水预热器后的气体管路连接气液分离器，气液分离器上设有天然气收集管路和/或冷凝水收集管路。
优选地，所述冷凝水收集管路连接电解制氢装置的水源管路，用于为所述电解制氢装置提供冷凝水。
优选地，所述甲烷化反应设备的甲烷输出管路连接天然气管网、天然气储存设备、和/或所述发电厂的锅炉的燃烧器。
一种发电厂调峰系统，包括发电厂供电装置，还包括上述任意一项所述的甲烷化反应系统，所述甲烷化反应系统的所述电解制氢装置与所述发电厂供电装置连接，以获得调峰结余电量。
优选地，所述发电厂供电装置包括发电机输出电网和连接所述发电机输出电网的逆变器，所述逆变器连接所述电解制氢装置。
优选地，还包括：
电厂集控中心，用于控制调峰结余电量，所述电厂集控中心与所述发电厂供电装置、电网调度中心连接；
电网调度中心，用于根据区域内实时发电和调峰负荷需求情况向所述电厂集控中心发送调峰负荷指令，所述电厂集控中心根据所述调峰负荷指 令控制调整所述调峰结余电量。
一种发电厂，包括上述任意一项所述的甲烷化反应系统和/或上述任意一项所述的发电厂调峰系统。
本发明提供的甲烷化反应系统可直接消耗发电厂的调峰结余电量，间接利用了弃风弃光弃水弃核电力，缓解了电网平衡和峰谷差问题，延长了发电厂设备的使用寿命。由于将调峰结余电量进行制氢操作，并最终制成甲烷，实现了电能的变相储存。
本发明将电解制氢、氢与二氧化碳反应制取甲烷相结合，实现了利用电厂调峰结余电量，从节能的源头和能源的利用方便，为实现环保节能的工业生产提供了强大的支撑。
在本发明一个优选的实施方式中，通过利用锅炉排烟中的二氧化碳作为甲烷化的重要原料，实现了电厂排放二氧化碳的回收，不但可以减排二氧化碳，而且可以生成甲烷或其他燃料，以便实现自用或通入天然气管网，实现电厂对废气二氧化碳的循环应用，整体减少了电厂的碳排放强度。
本发明还提供了一种包括上述甲烷化反应系统的发电厂调峰系统以及一种包括上述甲烷化反应系统的发电厂。
附图说明
为了更清楚地说明本发明实施例或现有技术中的技术方案，下面将对实施例或现有技术描述中所需要使用的附图作简单地介绍，显而易见地，下面描述中的附图仅仅是本发明的实施例，对于本领域普通技术人员来讲，在不付出创造性劳动的前提下，还可以根据提供的附图获得其他的附图。
图1为本发明所提供的甲烷化反应系统的结构示意图；
图2为本发明所提供的甲烷化反应设备的结构示意图。
图1-2中：
1为电解制氢装置、101为碱性水溶液电解制氢装置、102为固体聚合物电解制氢装置、103为高温固体氧化物电解水制氢装置；
2为二氧化碳捕捉系统、3为锅炉、4为甲烷化反应设备、5为氢收集净化装置、6为发电厂供电装置、7为纯净水制备装置、8为除氧器、9为 高温加热器、10为汽轮机、11为低温加热器、12为电网及电厂调峰控制平台、13为发电机；
401为第一高压反应罐、402为第二高压反应罐、403为第三高压反应罐、411为第一过热器、404为锅炉汽包、405为锅炉水预热器；
601为逆变器、602为电过热器；
121为电网调度中心、122为电厂集控中心。
具体实施方式
下面将结合本发明实施例中的附图，对本发明实施例中的技术方案进行清楚、完整地描述，显然，所描述的实施例仅仅是本发明一部分实施例，而不是全部的实施例。基于本发明中的实施例，本领域普通技术人员在没有做出创造性劳动前提下所获得的所有其他实施例，都属于本发明保护的范围。
本发明的核心是提供一种甲烷化反应系统，该系统能够利用发电厂的调峰结余电量，显著提升环保节能效应。
请参考图1至图2，图1为本发明所提供的甲烷化反应系统的结构示意图；图2为本发明所提供的甲烷化反应设备的结构示意图。
本发明所提供的一种甲烷化反应系统，该系统主要包括：电解制氢装置1、用于提供二氧化碳的二氧化碳提供源和甲烷化反应设备4。
其中，电解制氢装置1是以发电厂的调峰结余电量为电源制取氢的装置，可选的，电解制氢装置1可以与发电厂供电装置6连接，用以通过获取发电厂供电装置6在调峰过程中的调峰结余电量进行电解制氢操作，从而获得氢。需要说明的是，发电厂可以为火电厂等类型的发电厂。
甲烷化反应设备4是以氢和二氧化碳为原料制备甲烷的设备，甲烷化反应设备4，其连接到电解制氢装置1和二氧化碳提供源，用于以氢和二氧化碳为原料制备甲烷。可选的一种连接方式中，甲烷化反应设备4的原料输入管路连接电解制氢装置1的氢输出管路、二氧化碳提供源的二氧化碳输出管路，甲烷化反应设备4的甲烷输出管路连接天然气管网、和/或天然气储存设备、和/或发电厂的锅炉3燃料室。
需要说明的是，氢气是气体氢和液态氢的统称，本申请中提到的氢、二氧化碳均可以为气态、液态、气液混合态或者其他形态，并不限定二者的物理形态，本申请统称为氢气和二氧化碳，本申请中提到的电解制氢装置1的作用是生成氢，可以气态氢气，也可以为液态氢，或者为其他形式的氢能源。相适应的，用于输送氢的管路可以用于输送气体或液体，或者其他输送结构。二氧化碳提供源的作用是提供二氧化碳，可以为其他二氧化碳气体，也可以为液态或其他形态的二氧化碳。相适应的，用于输送二氧化碳的管路可以用于输送气体或液体，或者其他输送结构。
以现有技术为基础，甲烷化反应设备4可以通过二氧化碳和氢、以催化剂和高温高压为条件，反应制得甲烷或以甲烷为主的可燃性气体，本发明以电解制氢装置1制得的氢和二氧化碳为反应原料，进行甲烷化操作，因而能够得到大量的甲烷天然气产品，甲烷天然气产品可以直接用于锅炉燃烧供能，或者可以方便的进行储存，相比起电能而言，甲烷具有易储存性。
本发明提供的发电厂调峰系统可直接消耗电厂的调峰结余电量，间接利用了弃风弃光弃水弃核电力，缓解了电网平衡和峰谷差问题，延长了电厂设备的使用寿命。由于将调峰结余电量进行制氢操作，并最终制成甲烷，实现了电能的变相储存，实现了能源的稳定储存和有效利用。本发明将电解制氢技术、氢与二氧化碳反应制取甲烷等可燃气体技术相结合，实现了利用电厂调峰结余电量，间接利用弃风弃光电力，生产氢气和甲烷等气体燃料，为实现环保节能的工业生产提供了强大的支撑。
可选的，上述发电厂供电装置6的供电作用可以通过电网及电厂调峰控制平台12控制，根据电网区域内弃风弃光情况，结合电网对发电厂的调峰负荷要求，在低谷电时段大量给电解制氢装置1供电。
在上述实施例的基础之上，电解制氢装置1的氢输出管路通过氢收集净化装置5连接甲烷化反应设备4的原料输送管路；和/或，电解制氢装置1的氢输出管路连接用于储备能源的氢贮存装置。
可选的，电解制氢装置1制得液态或其他形态氢时，上述氢气输出管路、氢收集净化装置5等对应进行其他形态的氢的输送和收集。
可选的，氢输出管路与氢贮存装置的连接管路上设有收集控制阀，用于连通和关闭该连接管路。
可选的，电解制氢装置1设有用于连接锅炉3以提供纯氧的氧气排出口，也就是说，电解制氢装置1的氧排出口连接到发电厂的锅炉3，以向锅炉3提供纯氧。可选的，上述氧排出口可以排出可以输出氧气或液态氧。
需要说明的是，本实施例中采用收集和利用并行的方式有效地处理氢，使制得的氢具有两种用途，一方面通过净化处理进入甲烷化反应设备4，参与进行甲烷化操作；另一方面，通过氢贮存装置实现氢气或液态氢的贮存，由于氢气或液态氢相比于电能而言，具有较好的储存能力，储存更加稳定、不易流失。
本发明利用电解制氢工艺，实现了电能的变相储存，氢能作为未来能源，不但存储方便，而且其燃烧后无污染和任何碳排放，电能制氢并储存能保障电厂能量的保存。
在上述任意一个实施例的基础之上，二氧化碳提供源包括二氧化碳捕捉系统2，二氧化碳捕捉系统2用于连接发电厂锅炉3，收集锅炉3排出烟气中二氧化碳，二氧化碳捕捉系统2设有用于与锅炉3的烟气排出管路连通的接口。当然，二氧化碳提供源还可以包括液体二氧化碳源和/或固体二氧化碳源。
二氧化碳捕捉系统2用于收集锅炉3排出烟气中的二氧化碳，二氧化碳捕捉系统2与锅炉3的烟气排出管路连通；锅炉3的烟气排出管路通常产生废气二氧化碳等，其排放量是锅炉厂需要控制的环保排放指标之一。
更重要的是，本发明通过利用锅炉排烟中的二氧化碳作为甲烷化的重要原料，实现了电厂排放二氧化碳的回收，不但可以减排二氧化碳，而且可以生成甲烷或其他燃料，以便实现自用或通入天然气管网。
在上述任意一个实施例的基础之上，二氧化碳捕捉系统2的二氧化碳输出管路上设有二氧化碳提纯系统。通过二氧化碳的提纯处理能够保证甲烷化设备的充分反应以及甲烷制取的纯度。
可选的，本申请中的电解制氢装置1可以为碱性水溶液电解制氢装置101，或者可以为现有技术中其他进行制氢的装置，例如固体聚合物电解制 氢装置102或高温固体氧化物电解水制氢装置103等。
在上述任意一个实施例的基础之上，电解制氢装置1包括碱性水溶液电解制氢装置101和/或固体聚合物电解制氢装置102。需要说明的是，请参考图1，其中，碱性水溶液电解制氢装置101和固体聚合物电解制氢装置102均可以通过发电厂供电装置6或发电厂供电装置6的逆变器601进行供电。可以同时存在碱性水溶液电解制氢装置101和固体聚合物电解制氢装置102，或仅包括其中一种，具体设置可以根据实际情况进行调整，制得氢后提供给氢收集净化装置5后可用于收集或提供给甲烷化反应装置4。
在上述任意一个实施例的基础之上，电解制氢装置1的水源管路通过补水泵连接水处理车间的纯净水制备装置7；和/或，电解制氢装置1的冷却水供应管路连接锅炉3的汽轮机凝结水管路，利用汽轮机凝结水管路中的凝结水作为电解制氢装置1的冷却水，电解制氢装置1的冷却水排出管路连接电厂除氧器，利用电解制氢装置1中升温后的冷却水给锅炉循环利用；和/或，电解制氢装置1的氧排出口可以直接连接锅炉3，为锅炉3提供纯氧。
需要说明的是，本实施例中共包括三个实施方式，电解制氢装置1可以利用电厂化学水处理车间中通过纯净水制备装置形成的水源，电解制氢装置1可以以锅炉3的汽轮机10的凝结水作为冷却水供应源，并循环利用。
另外，电解制氢装置1的产品除了氢还包括氧气，制得的氧气还可以对锅炉进行供氧，可实现电厂的碳中和运行以及保证充分的富氧燃烧。当然，需要将氧气中可能存在的水蒸气进行去除。本实施例共提供了三种实施方式，这三种方式可以相互组合，可以同时设置，也可以仅包括其中一种或两种。可选的，电解制氢装置1的水源供应也可以通过水箱或其他设备提供。
在上述任意一个实施例的基础之上，电解制氢装置1包括高温固体氧化物电解水制氢装置103，高温固体氧化物电解水制氢装置103的水蒸气进汽口通过电过热器602连接锅炉3的主蒸汽排出口。
需要说明的是，请参考图1，其中高温固体氧化物电解水制氢装置103 通过发电厂供电装置6或逆变器601供电，可选的，高温水蒸汽可以由锅炉3的主蒸汽提供，具体地，其水蒸气进汽口通过电过热器602连接锅炉3的主蒸汽排出口，电加热器可用于将锅炉3的主蒸汽进行加热，通常可选择加热到800摄氏度以上形成高温蒸汽，并通入高温固体氧化物电解水制氢装置103中。连接关系中电解制氢装置1的高温水蒸汽管路连接锅炉3的主蒸汽，再经过电过热器602过热到800度以上后，再进入高温固体氧化物电解水制氢槽。
可选的，可以对上述三种电解质氢装置进行组合设置，本发明所提供的实施例中至少包括四种不同的电解制氢装置，其中，高温固体氧化物电解水制氢装置103可与碱性水溶液电解制氢装置101或固体聚合物电解制氢装置102同时设置在电厂系统里，也可以仅包括其中一个或两个。
在上述任意一个实施例的基础之上，甲烷化反应设备4包括：第一高压反应罐401、第二高压反应罐402和第三高压反应罐403。
其中，第一高压反应罐401、第二高压反应罐402和第三高压反应罐403均用于进行甲烷化反应，第一高压反应罐401设有甲烷化反应设备4的原料输入管路，原料输入管路获得氢和二氧化碳后输送到第一高压反应罐401中进行甲烷化反应，第一高压反应罐401的出气管路通过用于加压的高压废锅连接第二高压反应罐402。第二高压反应罐402通过另一个高压废锅连接第三高压反应罐403，第三高压反应罐403设有甲烷输出管路。
需要说明的是，上述三级高压反应罐均为高温高压的反应罐，其中可以设置促使甲烷化反应的催化剂。另外，三级高压反应罐的压力可以按照阶梯等级设置，逐级增大压力、温度。
在上述实施例的基础之上，第一高压反应罐401的输出管路设有第一过热器411，设置在第一高压反应罐401的输出管路上，将第一高压反应罐401的排出气体的热能进行交换回收。
在上述实施例的基础之上，还包括锅炉水预热器405，请参考图2，锅炉水预热器405设置在第三高压反应罐403的出口处或者设置在第三高压反应罐403出口连接的高压废锅的气体出口处，用于将第三高压反应罐403的输出的过热气体、水蒸气与锅炉给水进行换热。
可选的，第一过热器411连接锅炉3的汽轮机10，以便为汽轮机10提供热能。
可选的，锅炉水预热器405的液体输入端连接锅炉给水，锅炉水预热器405的液体输出端通过锅炉汽包404连接第一过热器411。
需要说明的是，第一高压反应罐401为高温高压炉，其排出的甲烷气体或水蒸气具有较高的热能和压力能，这些能量可以被用作锅炉结构上。本实施例在第一高压反应罐401设有第一过热器411，第一过热器411用于将第一高压反应罐401的排出气体的热能进行交换回收。进一步地，该第一过热器411获得的热能以过热蒸汽的形式通往锅炉3的汽轮机10，汽轮机10可通过该过热蒸汽进行做功，上述装置实现了第一高压反应罐401出口处的能源的节约再利用。
可选的，第二高压反应罐402和第三高压反应罐403处也可以设置相应的能源回收装置，以便对反应罐出口的能源加以利用。
在上述实施例的基础之上，第二高压反应罐402的压力大于第一高压反应罐401的压力，且小于第三高压反应罐403的压力。和/或，第二高压反应罐402为至少两个高压反应罐串联连接的高压反应罐组。
需要说明的是，上述第二高压反应罐402可以与第一高压反应罐401、第三高压反应罐403分别形成阶梯压力，以便通过不断的加压实现对反应原料的充分利用。另外，第二高压反应罐402可以为不止一个反应罐，也就是说，甲烷化反应设备4共包括至少三个反应罐。可选的，上述甲烷化反应设备4的反应罐的设置可以根据具体使用情况进行调整。
在上述任意一个实施例的基础之上，第三高压反应罐403通过锅炉水预热器405后的气体管路连接气液分离器，气液分离器上设有天然气产品收集管路和/或冷凝水收集管路。
可选的，冷凝水收集管路连接电解制氢装置1的水源管路，以便作为水源将冷凝水用于电解制氢装置1中，该设置较大程度的实现了能源的节约利用。
在上述任意一个实施例的基础之上，甲烷化反应设备4的甲烷输出管路连接天然气管网、天然气储存设备、和/或发电厂的锅炉3的燃烧器。
本发明所提供的发电厂调峰系统通过耦合常规发电厂、制氢装置和甲烷化反应设备4，将电厂的凝结水加热，给水加热和主蒸汽的产生与制氢和甲烷生产工艺流程相结合，实现了余热回收和能源梯级利用，极大地提升了发电厂的能源利用，不仅节约了有效的电能，可以通过存储或制甲烷加以利用，并且将锅炉产生的二氧化碳进行有效的利用，降低了发电厂的二氧化碳排放量，具有极大的环保节能的科技意义。
除了上述各个实施例所提供的甲烷化反应系统的主要结构，该甲烷化反应系统的其他各部分的结构请参考现有技术，本文不再赘述。
此外，本发明还提供了一种包括上述甲烷化反应系统的发电厂调峰系统，该系统包括发电厂供电装置6，还包括上述任意一个实施例所提供的甲烷化反应系统，甲烷化反应系统的电解制氢装置1与发电厂供电装置6连接，以获得调峰结余电量。
在一个具体的实施例中，发电厂供电装置6包括发电机输出电网和连接发电机输出电网的逆变器601，逆变器601连接电解制氢装置1。
可选的，请参考图1，发电机输出电网可以具体为发电机13。
锅炉3的汽轮机10连接发电机13，发电机作为发电机厂的主要设备，在调峰过程中是电能的源头。逆变器601可将发电机的电能输送给电解制氢装置1进行电解操作。
在一个具体的实施例中，还包括用于控制调峰结余电量的电厂集控中心122，发电厂供电装置6可以与电厂集控中心连接，电厂集控中心122与电网调度中心121连接，电网调度中心121根据区域内实时发电和调峰负荷需求情况向电厂集控中心122发送调峰负荷指令，电厂集控中心122根据调峰负荷指令控制调整调峰结余电量。
可选的，上述系统中包括电网及电厂调峰控制平台12，该平台包括电网调度中心121和电厂集控中心122，电网调度中心121根据区域内风电光伏的实时发电和调峰负荷需求情况，向电厂集控中心122下达电网调峰指令、调峰负荷，电厂集控中心122通过控制连接于发电机13和逆变器601之间的电开关电路，控制逆变器601将发电机13的直流电转化成交流电，并用做电解制氢装置1的电源。特别是在强风和高弃风弃光时段，向 电解制氢装置1供电，间接将不稳定的风电光伏发电转化为可储存的氢能或甲烷气。
此外，发电厂的锅炉3的烟气排出口作为甲烷化反应系统的二氧化碳提供源，为甲烷化反应提供二氧化碳，从而实现锅炉的二氧化碳的回收再利用。
此外，本发明还提供了一种发电厂，该发电厂包括上述各个实施例中所提供的甲烷化反应系统，或者包括上述发电厂调峰系统，上述发电厂的其他结构特征可以参考现有技术，此处不再赘述。
本说明书中各个实施例采用递进的方式描述，每个实施例重点说明的都是与其他实施例的不同之处，各个实施例之间相同相似部分互相参见即可。
以上对本发明所提供的甲烷化反应系统、发电厂调峰系统及发电厂进行了详细介绍。本文中应用了具体个例对本发明的原理及实施方式进行了阐述，以上实施例的说明只是用于帮助理解本发明的方法及其核心思想。应当指出，对于本技术领域的普通技术人员来说，在不脱离本发明原理的前提下，还可以对本发明进行若干改进和修饰，这些改进和修饰也落入本发明权利要求的保护范围内。

Claims (19)

  1. 一种甲烷化反应系统，其特征在于，包括：
    电解制氢装置(1)，其连接到发电厂供电装置(6)，用于接收发电厂供电装置(6)输出的调峰结余电量以制备氢；
    二氧化碳提供源，用于提供二氧化碳；
    甲烷化反应设备(4)，其连接到所述电解制氢装置(1)和所述二氧化碳提供源，用于以氢和二氧化碳为原料制备甲烷。
  2. 根据权利要求1所述的甲烷化反应系统，其特征在于，
    所述电解制氢装置(1)通过氢收集净化装置(5)连接到所述甲烷化反应设备(4)；和/或，所述电解制氢装置(1)的氢输出管路连接到氢贮存装置。
  3. 根据权利要求2所述的甲烷化反应系统，其特征在于，
    所述电解制氢装置(1)的氢输出管路与氢贮存装置的连接管路上设有收集控制阀，用于连通和关闭该连接管路。
  4. 根据权利要求1所述的甲烷化反应系统，其特征在于，
    所述电解制氢装置(1)的氧排出口连接到发电厂的锅炉(3)，以向所述锅炉(3)提供纯氧。
  5. 根据权利要求1所述的甲烷化反应系统，其特征在于，所述二氧化碳提供源包括：
    发电厂的二氧化碳捕捉系统(2)，所述二氧化碳捕捉系统(2)用于连接发电厂的锅炉(3)的烟气排出管路，以收集所述锅炉(3)排出烟气中的二氧化碳；
    和/或液体二氧化碳源、和/或固体二氧化碳源。
  6. 根据权利要求1至5任意一项所述的甲烷化反应系统，其特征在于，所述电解制氢装置(1)包括碱性水溶液电解制氢装置(101)和/或固体聚合物电解制氢装置(102)。
  7. 根据权利要求6所述的甲烷化反应系统，其特征在于，所述电解制氢装置(1)的水源管路连接水处理车间的纯净水制备装置(7)；和/或，所述电解制氢装置(1)的冷却水供应管路连接所述锅炉(3)的汽轮机凝 结水管路；和/或，所述电解制氢装置(1)的冷却水排出管路连接电厂除氧器。
  8. 根据权利要求1至5任意一项所述的甲烷化反应系统，其特征在于，所述电解制氢装置(1)包括高温固体氧化物电解水制氢装置(103)。
  9. 根据权利要求8所述的甲烷化反应系统，其特征在于，所述高温固体氧化物电解水制氢装置(103)的水蒸汽进入口通过电过热器(602)连接所述锅炉(3)的主蒸汽排出口。
  10. 根据权利要求1所述的甲烷化反应系统，其特征在于，所述甲烷化反应设备(4)包括：
    用于甲烷化反应的第一高压反应罐(401)，所述第一高压反应罐(401)设有原料输入管路，所述第一高压反应罐(401)的输出管路通过用于加压的高压废锅连接第二高压反应罐(402)；
    用于甲烷化反应的第二高压反应罐(402)，所述第二高压反应罐(402)通过另一高压废锅连接第三高压反应罐(403)；
    第三高压反应罐(403)，设有甲烷输出管路。
  11. 根据权利要求10所述的甲烷化反应系统，其特征在于，还包括：
    第一过热器(411)，设置在所述第一高压反应罐(401)的输出管路上，将所述第一高压反应罐(401)的排出气体的热能进行交换回收；
    锅炉水预热器(405)，设置在所述第三高压反应罐(403)的出口或与所述出口连接的高压废锅的气体出口，用于将第三高压反应罐(403)的输出的过热气体、水蒸气与锅炉给水进行换热。
  12. 根据权利要求11所述的甲烷化反应系统，其特征在于，
    所述第一过热器(411)连接发电厂的锅炉(3)的汽轮机(10)，以便为所述汽轮机(10)提供热能；和/或
    所述锅炉水预热器(405)的液体输入端连接锅炉给水，液体输出端锅炉汽包(404)连接所述第一过热器(411)。
  13. 根据权利要求11或12所述的甲烷化反应系统，其特征在于，
    所述第三高压反应罐(403)通过锅炉水预热器(405)后的气体管路连接气液分离器，气液分离器上设有天然气收集管路和/或冷凝水收集管 路。
  14. 根据权利要求13所述的甲烷化反应系统，其特征在于，
    所述冷凝水收集管路连接电解制氢装置(1)的水源管路，用于为所述电解制氢装置(1)提供冷凝水。
  15. 根据权利要求1所述的甲烷化反应系统，其特征在于，
    所述甲烷化反应设备(4)的甲烷输出管路连接天然气管网、天然气储存设备、和/或所述发电厂的锅炉(3)的燃烧器。
  16. 一种发电厂调峰系统，包括发电厂供电装置(6)，其特征在于，还包括权利要求1至15任意一项所述的甲烷化反应系统，所述甲烷化反应系统的所述电解制氢装置(1)与所述发电厂供电装置(6)连接，以获得调峰结余电量。
  17. 根据权利要求16所述的发电厂调峰系统，其特征在于，所述发电厂供电装置(6)包括发电机输出电网和连接所述发电机输出电网的逆变器(601)，所述逆变器(601)连接所述电解制氢装置(1)。
  18. 根据权利要求16或17所述的发电厂调峰系统，其特征在于，还包括：
    电厂集控中心(122)，用于控制调峰结余电量，所述电厂集控中心(122)与所述发电厂供电装置(6)、电网调度中心(121)连接；
    电网调度中心(121)，用于根据区域内实时发电和调峰负荷需求情况向所述电厂集控中心(122)发送调峰负荷指令，所述电厂集控中心(122)根据所述调峰负荷指令控制调整所述调峰结余电量。
  19. 一种发电厂，其特征在于，包括：
    权利要求1至15任意一项所述的甲烷化反应系统；和/或权利要求16至18任意一项所述的发电厂调峰系统。
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