CN117307426A - Power generation system - Google Patents

Power generation system Download PDF

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Publication number
CN117307426A
CN117307426A CN202311187485.5A CN202311187485A CN117307426A CN 117307426 A CN117307426 A CN 117307426A CN 202311187485 A CN202311187485 A CN 202311187485A CN 117307426 A CN117307426 A CN 117307426A
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China
Prior art keywords
gas
preheater
water
inlet
outlet
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CN202311187485.5A
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Chinese (zh)
Inventor
陈哲文
张玉明
魏俊杰
张炜
李家州
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China University of Petroleum Beijing
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China University of Petroleum Beijing
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Priority to CN202311187485.5A priority Critical patent/CN117307426A/en
Publication of CN117307426A publication Critical patent/CN117307426A/en
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F03—MACHINES OR ENGINES FOR LIQUIDS; WIND, SPRING, OR WEIGHT MOTORS; PRODUCING MECHANICAL POWER OR A REACTIVE PROPULSIVE THRUST, NOT OTHERWISE PROVIDED FOR
    • F03G—SPRING, WEIGHT, INERTIA OR LIKE MOTORS; MECHANICAL-POWER PRODUCING DEVICES OR MECHANISMS, NOT OTHERWISE PROVIDED FOR OR USING ENERGY SOURCES NOT OTHERWISE PROVIDED FOR
    • F03G6/00—Devices for producing mechanical power from solar energy
    • F03G6/06—Devices for producing mechanical power from solar energy with solar energy concentrating means
    • F03G6/068—Devices for producing mechanical power from solar energy with solar energy concentrating means having other power cycles, e.g. Stirling or transcritical, supercritical cycles; combined with other power sources, e.g. wind, gas or nuclear
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
    • F02C3/00—Gas-turbine plants characterised by the use of combustion products as the working fluid
    • F02C3/20—Gas-turbine plants characterised by the use of combustion products as the working fluid using a special fuel, oxidant, or dilution fluid to generate the combustion products
    • F02C3/22—Gas-turbine plants characterised by the use of combustion products as the working fluid using a special fuel, oxidant, or dilution fluid to generate the combustion products the fuel or oxidant being gaseous at standard temperature and pressure
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
    • F02C6/00—Plural gas-turbine plants; Combinations of gas-turbine plants with other apparatus; Adaptations of gas-turbine plants for special use
    • F02C6/18—Plural gas-turbine plants; Combinations of gas-turbine plants with other apparatus; Adaptations of gas-turbine plants for special use using the waste heat of gas-turbine plants outside the plants themselves, e.g. gas-turbine power heat plants
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F24—HEATING; RANGES; VENTILATING
    • F24S—SOLAR HEAT COLLECTORS; SOLAR HEAT SYSTEMS
    • F24S23/00—Arrangements for concentrating solar-rays for solar heat collectors
    • F24S23/70—Arrangements for concentrating solar-rays for solar heat collectors with reflectors
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
    • H01M8/0606—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants
    • H01M8/0612—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants from carbon-containing material
    • H01M8/0618—Reforming processes, e.g. autothermal, partial oxidation or steam reforming
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/10—Fuel cells with solid electrolytes
    • H01M8/12—Fuel cells with solid electrolytes operating at high temperature, e.g. with stabilised ZrO2 electrolyte
    • H01M8/1231—Fuel cells with solid electrolytes operating at high temperature, e.g. with stabilised ZrO2 electrolyte with both reactants being gaseous or vaporised
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/10—Fuel cells with solid electrolytes
    • H01M8/12—Fuel cells with solid electrolytes operating at high temperature, e.g. with stabilised ZrO2 electrolyte
    • H01M2008/1293—Fuel cells with solid oxide electrolytes
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/30—Hydrogen technology
    • Y02E60/50—Fuel cells

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Sustainable Development (AREA)
  • Sustainable Energy (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Organic Chemistry (AREA)
  • Manufacturing & Machinery (AREA)
  • Electrochemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Engine Equipment That Uses Special Cycles (AREA)

Abstract

The invention provides a power generation system, relates to the technical field of energy, and aims to solve the problems of more carbon dioxide emission and low trapping efficiency in the related art. The power generation system comprises a solar reaction device, a solid oxide fuel cell, a reaction unit and a first gas-liquid separator; the solar reaction device comprises a solar component and a solar gasifier, wherein the solar component is configured to provide heat energy for the solar gasifier through solar energy, the solar gasifier is provided with a reactant inlet and a product outlet, the reactant inlet is used for introducing gasified coal and water into the solar gasifier, the solar gasifier is configured to react the gasified coal and the water which are introduced into the solar gasifier through the received heat energy so as to generate combustible gas, the reaction unit is connected between the product outlet and the anode layer, and the solid oxide fuel cell comprises an anode layer and a cathode layer which are sequentially stacked. The invention reduces the carbon dioxide emission of gasification coal power generation and improves the capture efficiency of carbon dioxide.

Description

Power generation system
Technical Field
The invention relates to the technical field of energy, in particular to a power generation system.
Background
At present, the energy production and consumption structure in China mainly uses coal, and the main utilization mode of the coal is combustion power generation, wherein CO of a coal-fired power station 2 The emission is about CO in China 2 50% of the total amount discharged. There is a great need for coal power to evolve toward cleanliness and low carbonization, wherein CO 2 The emission reduction work is particularly important.
In the related art, CO 2 The emission reduction technology includes supercritical water gasification technology, in which supercritical water is water in a supercritical state having a temperature exceeding a critical temperature (374 degrees celsius) and a pressure exceeding a critical pressure (22.1 MPa), coal gasification is a chemical process of converting coal into synthesis gas, and supercritical water gasification technology is a gasification technology using water as a gasification medium and an environmental medium, specifically, in a gasification reaction device, coal reacts with supercritical water to generate synthesis gas containing hydrogen.
However, since the supercritical water gasification reaction is an endothermic reaction, heat needs to be supplied by an external heat source, the external heat source in the related art is supplied by the combustion heat of fuel coal, which not only increases the consumption of coal, but also the tail gas generated by the combustion of coal includes carbon dioxide, and the capturing efficiency of carbon dioxide is low.
Disclosure of Invention
The invention provides a power generation system for reducing carbon dioxide emission of gasification coal power generation and improving carbon dioxide capturing efficiency.
In order to achieve the above object, the present invention provides the following technical solutions:
the invention provides a power generation system, which comprises a solar reaction device, a solid oxide fuel cell, a reaction unit and a first gas-liquid separator;
the solar reaction apparatus includes a solar module configured to provide thermal energy to the solar gasifier through solar energy, the solar gasifier having a reactant inlet for introducing gasified coal and water into the solar gasifier and a product outlet, and the solar gasifier configured to react the gasified coal introduced into the solar gasifier with water through the received thermal energy to generate a first synthesis gas, wherein the first synthesis gas includes a combustible gas and carbon dioxide, the solid oxide fuel cell includes an anode layer, an electrolyte layer, and a cathode layer disposed in sequence, the reaction unit is connected between the product outlet and the anode layer, the reaction unit is configured to perform a reforming reaction on the combustible gas to generate a second synthesis gas, the second synthesis gas includes hydrogen and carbon monoxide; the anode layer is configured to receive the second syngas to generate electrical energy through electrochemical reactions between the second syngas and ions of the cathode layer;
the first gas-liquid separator is configured to separate and collect carbon dioxide generated by the solar gasifier and the solid oxide fuel cell.
The invention has at least the following beneficial effects:
compared with the combustion fuel coal in the related art, the solar reaction device is used as a heat source for the water gasification reaction, so that not only is the coal consumption reduced, but also CO in the combustion process of the fuel coal is avoided 2 Discharging; in addition, the pressure energy of the synthetic gas generated by the water gasification reaction is utilized and combined with the solid oxide fuel cell to generate electricity, so that the complementary electricity generation of sunlight and gasified coal light and coal is realized, the cascade utilization of energy is realized by combining the pressure energy and chemical reaction energy, and the electricity generation efficiency of the electricity generation system is improvedThe rate.
In one possible implementation, the reactant inlets include a first reactant inlet for delivering vaporized coal into the solar vaporization furnace and a second reactant inlet for delivering water into the solar vaporization furnace, and the second reactant inlet is in communication with the cathode layer such that water delivered into the solar vaporization furnace is heated by cathode gas generated by the cathode layer;
the solar module comprises an optical focusing device and a reflecting device, wherein the optical focusing device is configured to project light rays irradiated to the optical focusing device to the reflecting device, and the reflecting device reflects the light rays to the solar reaction device and provides heat energy for the solar reaction device.
In one possible implementation, the power generation system further comprises a supercritical turbine connected between the product outlet and the reaction unit for converting pressure energy of the first synthesis gas into mechanical energy for power generation.
In one possible implementation, the reaction unit includes a first preheater, a reforming reactor, a first water pump and a water supply preheater, the first preheater having a cold end, a hot end, a cold end outlet and a hot end outlet, the reforming reactor having a feed end and a discharge end, the cold end of the first preheater being in communication with the product outlet of the solar gasifier, the cold end outlet of the first preheater being in communication with the feed end of the reforming reactor;
one of the hot end of the first preheater and the reforming reactor is communicated with the anode layer so as to transfer heat from anode gas generated by the anode layer to the first synthesis gas;
the reforming reactor is provided with a liquid inlet, the water supply preheater is provided with a first water inlet, a first water outlet and a hot end inlet, the first water outlet is communicated with the liquid inlet, the hot end inlet is communicated with the discharge end of the reforming reactor, the first water pump is communicated with the first water inlet, the water supply preheater is used for preheating water from the first water pump and then conveying the water to the reforming reactor, so that the water preheated by the water supply preheater, the first synthetic gas and the anode gas are mixed and then subjected to reforming reaction, and reforming reaction products comprise carbon monoxide and hydrogen;
the first hot side inlet is for receiving the reforming reaction product.
In one possible implementation, the reaction unit further comprises a shift reactor having a first feed end, a second feed end, and a discharge end, the feed preheater further having a second water inlet, a second water outlet, and a second hot end outlet, the first feed end in communication with the second hot end outlet to receive the preheated reforming reaction product;
the second feeding end is communicated with a second water outlet of the water supply preheater so as to receive preheated water from the water supply preheater, the discharging end of the shift reactor is communicated with the anode layer, and the shift reactor is used for carrying out water gas shift reaction on the reforming reaction product and the preheated water so as to generate third synthesis gas, wherein the third synthesis gas comprises hydrogen and carbon dioxide;
the anode layer is configured to receive the third syngas to generate electrical energy via electrochemical reactions between the third syngas and ions of the cathode layer.
In one possible implementation, the power generation system further includes a fuel preheater having a first inlet end in communication with the discharge end of the shift reactor, a second inlet end in communication with the anode layer, and a first outlet end in communication with the cathode layer, the fuel preheater configured to receive the cathode gas to transfer heat to the third syngas.
In one possible implementation, the power generation system further includes a gas turbine in communication with the first preheater and having a combustion chamber therein, the combustion chamber having a fuel inlet end, an oxygen inlet end, and an outlet end, the fuel inlet end being in communication with the hot end outlet of the first preheater for receiving the anode gas;
the combustion chamber is used for enabling the anode gas to generate combustion reaction and generate combustion smoke, the gas turbine is provided with a gas inlet, a gas outlet and a power output end, the outlet end of the combustion chamber is communicated with the gas inlet of the gas turbine, the gas outlet is communicated with the inlet of the first gas-liquid separator, and the gas turbine is used for utilizing the combustion smoke to do work so that the power output end outputs mechanical energy for generating electricity.
In one possible implementation manner, a pressure reducing valve, a condenser, a second gas-liquid separator and a second preheater are further sequentially arranged between the supercritical permeable plate and the first preheater, a reactant inlet of the solar gasifier is communicated with a water supply pump, the second preheater is provided with a water inlet end, a gas inlet end, a water outlet end and a gas outlet end, an inlet end of the pressure reducing valve is communicated with a product outlet of the solar gasifier, an outlet end of the pressure reducing valve is communicated with an inlet end of the condenser, an outlet end of the condenser is communicated with an inlet end of the second gas-liquid separator, a gas outlet end of the second gas-liquid separator is communicated with the first preheater, a liquid outlet end of the second gas-liquid separator is communicated with a water inlet of the water supply pump, a water outlet of the water supply pump is communicated with a water inlet end of the second preheater, a water outlet end of the second preheater is communicated with a water inlet end of the solar gasifier, an outlet end of the second preheater is communicated with a gas inlet end of the gas turbine of the second preheater;
the second gas-liquid separator is configured to separate and convey the liquid in the combustible gas to the second preheater and to be heat-transferred by the anode gas together with the water supply of the water supply pump.
In one possible implementation manner, a third preheater is further arranged between the second preheater and the solar gasifier, the third preheater is provided with a water inlet end, a gas inlet end, a water outlet end and a gas outlet end, the water inlet end of the third preheater is communicated with the water outlet end of the second preheater, the water outlet end of the third preheater is communicated with the water inlet end of the solar gasifier, the gas inlet end of the third preheater is communicated with the gas outlet end of the fuel preheater, and the third preheater is configured to receive cathode gas passing through the fuel preheater so as to transfer heat to water supplied by the water supply pump;
and the air outlet end of the third preheater is communicated with an air turbine for recovering residual pressure energy of the cathode gas after heat transfer in the third preheater.
In one possible implementation, the power generation system further includes a heat exchanger having a cold side channel with a cold side inlet and a cold side outlet, and a hot side channel with a hot side inlet and a hot side outlet, and a first compressor in communication with the cold side inlet of the heat exchanger, the hot side inlet and the cold side outlet of the heat exchanger both in communication with the cathode layer, and the hot side inlet of the heat exchanger for ingress of cathode gas, and the hot side outlet of the heat exchanger for egress of the cathode gas;
the heat exchanger is configured to exchange heat with the cold side channel and the hot side channel to transfer heat from the cathode gas to the compressed air compressed by the first compressor.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the embodiments or the description of the prior art will be briefly described, and it is obvious that the drawings in the following description are some embodiments of the present invention, and other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
Fig. 1 is a schematic diagram of a power generation system according to an embodiment of the present invention.
Reference numerals illustrate:
100-solar energy reaction device;
110-a solar gasifier; 120-solar module; 130-a water supply pump;
121-an optical focussing device; 122-reflecting means;
200-solid oxide fuel cell;
210-an anode layer; 220-a cathode layer;
300-reaction unit;
310-a first preheater; 320-reforming reactor; 330-a feed preheater; 331-a first water pump; 332-a second water pump; a 340-shift reactor; 350-a pressure reducing valve; 360-condenser; 370-a second gas-liquid separator; 380-a second preheater;
400-a first gas-liquid separator;
500-supercritical turbines;
600-fuel preheater; 610-a third preheater; 620-air turbine;
700-gas turbine;
800-combustion chamber;
900-a first compressor; 910-a heat exchanger; 920-second compressor.
Detailed Description
As described in the background art, the carbon dioxide emission reduction work in the coal-to-electricity technology needs to be continuously focused and optimized, but when the water gasification control of carbon dioxide emission in the related technology is performed, the reaction heat source needs to be provided by means of coal combustion, and the problems of excessive carbon dioxide emission and low trapping efficiency exist. The inventor researches find that the cause of the problem is mainly that: the heat source of the water coal gasification reaction is not clean enough, and the concentration of carbon dioxide generated by the reaction is low and is generally only 13% -15% of that of the product gas, when the product gas is captured, an ethanolamine method is generally adopted, namely the ethanolamine solution is contacted with the carbon dioxide to react to absorb the carbon dioxide, but the ethanolamine solution is heated in the desorption stage to release the absorbed carbon dioxide, the heating process of the method consumes more electric energy of a coal power generation system, and the power generation efficiency of the power generation system is influenced when the carbon dioxide capturing efficiency is low.
In view of the above technical problems, embodiments of the present invention provide a power generation system, which is superior to the related art in burning fuel coalThe solar reaction device is used as a heat source for the water coal gasification reaction, so that not only is the coal consumption reduced, but also CO in the combustion process of fuel coal is avoided 2 Discharging; in addition, the pressure energy of the synthetic gas generated by the water gasification reaction is utilized and combined with the solid oxide fuel cell to generate electricity, so that the complementary electricity generation of sunlight and gasified coal light and coal is realized, the cascade utilization of energy is realized by combining the pressure energy and chemical reaction energy, and the electricity generation efficiency of the electricity generation system is improved.
In order to make the above objects, features and advantages of the embodiments of the present invention more comprehensible, the technical solutions of the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings. It will be apparent that the described embodiments are only some, but not all, embodiments of the invention. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
Referring to fig. 1, an embodiment of the present invention provides a power generation system including a solar reaction apparatus 100, a solid oxide fuel cell 200 (Solid Oxide Fuel Cell, abbreviated as SOFC), a reaction unit 300, and a first gas-liquid separator 400.
The solar reaction apparatus 100 includes a solar module 120 and a solar gasifier 110, the solar module 120 configured to provide heat energy to the solar gasifier 110 through solar energy, the solar gasifier 110 having a reactant inlet for introducing gasified coal and water into the solar gasifier and a product outlet, and the solar gasifier 110 configured to react the gasified coal introduced into the solar gasifier 110 with the water through the received heat energy to generate a first synthesis gas, a reaction unit 300 connected between the product outlet and the anode layer 210, the reaction unit 300 configured to perform a reforming reaction on the combustible gas to generate a second synthesis gas, wherein the first synthesis gas includes the combustible gas and carbon dioxide, and the second synthesis gas includes hydrogen and carbon monoxide.
The solid oxide fuel cell 200 includes an anode layer 210, an electrolyte layer, and a cathode layer 220, which are disposed in sequence, the anode layer 210 being configured to receive a second synthesis gas to generate electrical energy through an electrochemical reaction between ions of the second synthesis gas and the cathode layer 220.
The water reacted with the gasified coal is supercritical water, the gasification reaction heat of the gasification reaction of the gasified coal and the supercritical water is provided by the solar reaction device 100, the reaction temperature is 600-700 ℃, and the reaction pressure in the solar gasification furnace 110 is 220-300bar; the first synthesis gas comprises H 2 、CH 4 、CO、CO 2 And C 2 H 6 After methane reforming reaction, electrochemical reaction occurs in the anode of the solid oxide fuel cell 200, and the generated anode gas comprises H 2 、H 2 O and CO 2 Wherein the reforming reaction is an endothermic reaction at a temperature of 700-1000 ℃ and a reaction pressure of 15-30bar.
The first gas-liquid separator 400 is configured to separate and collect carbon dioxide generated from the solar gasification furnace 110 and the solid oxide fuel cell 200.
By adopting the structural design, the solar reaction device 100 is used as a heat source for the water coal gasification reaction, so that not only is the coal consumption reduced, but also CO in the combustion process of fuel coal is avoided 2 Discharging; in addition, the pressure energy of the synthetic gas generated by the water gasification reaction is utilized and combined with the solid oxide fuel cell 200 to generate power, so that the complementary power generation of sunlight and gasified coal is realized, the cascade utilization of energy is realized by combining the pressure energy and chemical reaction energy, and the power generation efficiency of a power generation system is improved.
In a possible embodiment, the reactant inlets include a first reactant inlet for delivering vaporized coal into the solar vaporization furnace and a second reactant inlet for delivering water into the solar vaporization furnace, and the second reactant inlet is in communication with the cathode layer 220 such that the water delivered into the solar vaporization furnace is heated by the cathode gas generated by the cathode layer 220, and the reaction water in the gasification furnace is preheated in advance to remove unwanted volatile components from the vaporized coal, resulting in a higher purity fuel gas for the SOFC.
The solar module 120 includes an optical concentrator 121 and a reflecting device 122, the optical concentrator 121 is configured to project light irradiated to itself to the reflecting device 122, the reflecting device 122 reflects the light to the solar reaction device 100 to provide heat energy for the solar reaction device 100, the optical concentrator 121 is illustratively a heliostat, the reflecting device 122 is a reflecting tower, and the solar gasifier 110 is provided with a solar collector, i.e. solar radiation energy is concentrated to the solar collector of the solar gasifier 110 through the heliostat and the reflecting tower.
In other possible embodiments, the power generation system further includes a supercritical turbine 500, where the supercritical turbine 500 is connected between the product outlet and the reaction unit 300 for converting the pressure energy of the first synthesis gas into mechanical energy for power generation, and it is understood that the first synthesis gas, which is the gasification product of the solar gasification furnace 110, is introduced into the supercritical turbine 500 to expand and perform work to generate energy for power generation.
As an example, the reaction unit 300 includes a first preheater 310, a reforming reactor 320, a first water pump 331 and a water supply preheater 330, the first preheater 310 having a cold end, a hot end, a cold end outlet and a hot end outlet, the reforming reactor 320 having a feed end and a discharge end, the cold end of the first preheater 310 being connected to a product outlet of the solar gasifier 110, the cold end outlet of the first preheater 310 being connected to the feed end of the reforming reactor 320;
one of the hot end of the first preheater 310 and the reforming reactor 320 is in communication with the anode layer 210 to transfer the anode gas generated by the anode layer 210 to the first synthesis gas;
the reforming reactor 320 has a liquid inlet, the water supply preheater 330 has a first water inlet, a first water outlet and a hot end inlet, the first water outlet is communicated with the liquid inlet, the hot end inlet is communicated with the discharge end of the reforming reactor 320, the first water pump 331 is communicated with the first water inlet, the water supply preheater 330 is used for preheating water from the first water pump 331 and then delivering the water to the reforming reactor 320, so that the water preheated by the water supply preheater 330 is mixed with the first synthetic gas and the anode gas and then subjected to reforming reaction to generate a reforming reaction product, and the reforming reaction product comprises carbon monoxide and hydrogen;
the first hot side inlet is for receiving a reforming reaction product.
In this way, in the cycle of the power generation system, the high-temperature anode gas generated by the SOFC is utilized to preheat the first synthesis gas in the first preheater 310 so as to meet the reaction temperature condition of the subsequent reforming reaction, and the reforming reaction is performed in the reforming reactor 320 with the water preheated by the water supply heat exchanger 910 from the first water pump 331, so that the methane is converted into the cleaner and more efficient fuel hydrogen, and the power generation efficiency of the SOFC electrochemical reaction is improved.
In other possible embodiments, the reaction unit 300 further comprises a shift reactor 340, the shift reactor 340 having a first feed end, a second feed end, and a discharge end, the feed preheater 330 further having a second water inlet, a second water outlet, and a second hot end outlet, the first feed end in communication with the second hot end outlet to receive the preheated reformate reaction product;
the second feed end is connected to the second water outlet of the water supply preheater 330 to receive the preheated water from the water supply preheater 330, the discharge end of the shift reactor 340 is connected to the anode layer 210, and the shift reactor 340 is used for generating a water gas shift reaction between the reforming reaction product and the preheated water to generate a third synthesis gas, wherein the third synthesis gas comprises hydrogen and carbon dioxide; the anode layer 210 is configured to receive the third synthesis gas to generate electric power through electrochemical reaction between the third synthesis gas and ions of the cathode layer 220, that is, the second synthesis gas generated by the reforming reaction is introduced into the feed preheater 330 to preheat the reforming reaction feed water from the first water pump 331 and the shift reaction feed water from the second water pump 332, and then introduced into the shift reactor 340 together with the shift reaction feed water to perform shift reaction, where the shift reaction equation is CO+H 2 O→H 2 +CO 2 。
In this way, the carbon monoxide generated by the reforming reaction and the water are subjected to the water gas shift reaction to generate the hydrogen with higher purity, so that the combustion efficiency of the SOFC fuel is improved, and the emission of carbon dioxide in the power generation system is reduced.
It will be appreciated that the shift reaction is exothermic, at a temperature of 200-450 ℃, at a pressure of 10-30bar, such that the shifted hydrogen-containing third synthesis gas is passed into the SOFC anode layer 210 for electrochemical reaction, wherein the SOFC reaction temperature is 800-1000 ℃, preferably 700-800 ℃, such as 700 ℃ or 750 ℃ or 800 ℃; the reaction pressure is 10 to 20bar, for example 15bar.
As yet another example, the power generation system further includes a fuel preheater 600, the fuel preheater 600 having a first inlet end, a second inlet end, and a first outlet end, the first inlet end being in communication with the outlet end of the shift reactor 340, the first outlet end being in communication with the anode layer 210, the second inlet end being in communication with the cathode layer 220, the fuel preheater 600 being configured to receive the cathode gas to transfer heat to the third syngas.
In this embodiment, the fuel preheater 600 receives the cathode gas, wherein the cathode gas includes the residual gas of the cathode reaction, steam and carbon dioxide, and the high temperature of the cathode gas is utilized to continuously and circularly heat the conversion reaction product, namely the third synthesis gas, to provide the reaction heat energy for the fuel for generating power of the next cycle of the battery, and the third synthesis gas is heated by the cathode gas and then enters the anode layer 210 to undergo the anode electrochemical reaction, and the equation is H 2 +O 2- →H 2 O+2e - Wherein electrons flow from the cathode to the anode from an external circuit of the panel, forming a circuit to generate electrical energy, illustratively yttrium stabilized zirconium dioxide.
As one possible implementation, the power generation system further includes a gas turbine 700 and a gas turbine in communication with the first preheater 310, the gas turbine having a combustion chamber 800 disposed therein, the combustion chamber 800 having a fuel inlet end, an oxygen inlet end, and an outlet end, the fuel inlet end in communication with the hot end outlet of the first preheater 310 for receiving anode gas; the combustion chamber 800 is used for generating combustion reaction of anode gas and producing combustion exhaust gas, the gas turbine 700 is provided with a gas inlet, a gas outlet and a power output end, the outlet end of the combustion chamber 800 is communicated with the gas inlet of the gas turbine 700, the gas outlet is communicated with the inlet of the first gas-liquid separator 400, and the gas turbine 700 is used for utilizing the combustion exhaust gas to do work so that the power output end outputs mechanical energy for generating electricity.
That is, the SOFC anode gas is utilized, and the fuel gas is the first synthesis gas, the second synthesis gas or the third synthesis gas and oxygen are combusted, and the combustion exhaust gas generated by the combustion is then introduced into the gas turbine 700 to perform work to drive the motor to generate power.
After the SOFC anode gas transfers heat to the first synthesis gas, the first synthesis gas is introduced into the combustion chamber 800 to perform combustion reaction with pure oxygen, and the reaction temperature in the combustion chamber 800 is 1300-1600 ℃, and the pressure is 12-40bar.
In more possible embodiments, a pressure reducing valve 350, a condenser 360, a second gas-liquid separator 370 and a second preheater 380 are further sequentially disposed between the supercritical turbine 500 and the first preheater 310, the reactant inlet of the solar gasifier 110 is communicated with the water supply pump 130, the second preheater 380 has a water inlet end, a gas inlet end, a water outlet end and a gas outlet end, the inlet end of the pressure reducing valve 350 is communicated with the product outlet of the solar gasifier 110, the outlet end of the pressure reducing valve 350 is communicated with the inlet end of the condenser 360, the outlet end of the condenser 360 is communicated with the inlet end of the second gas-liquid separator 370, the gas outlet end of the second gas-liquid separator 370 is communicated with the first preheater 310, the liquid outlet end of the second gas-liquid separator 370 is communicated with the water inlet of the water supply pump 130, the water outlet of the water supply pump 130 is communicated with the water inlet end of the second preheater 380, the water outlet end of the second preheater 380 is communicated with the water inlet end of the solar gasifier 110, the gas inlet end of the second preheater 380 is communicated with the gas outlet of the gas turbine, the outlet end of the second preheater 380 is communicated with the gas outlet of the gas turbine 700, and the second gas outlet end of the second preheater 380 is communicated with the first gas-liquid separator 400.
The second gas-liquid separator 370 is configured to separate and convey the liquid in the combustible gas to the second preheater 380, and is heat-transferred by the anode gas together with the water supply of the water supply pump 130.
In this way, the first synthesis gas in the high temperature and high pressure state is depressurized to normal pressure after being introduced into the pressure reducing valve 350, the temperature is reduced to 80-100 ℃, the synthesis gas is cooled to normal temperature through the condenser 360, the gradient depressurization and the temperature reduction of the synthesis gas are performed so as to provide condition preparation for recycling the gasified water in the first synthesis gas, and then the water is separated through the second gas-liquid separator 370 so as to be subsequently utilized together with the water supply introduced into the water supply pump 130.
On the basis of the above embodiments, it can be improved that the flue gas of the gas turbine 700 carries out a first stage preheating of the gasifier feed water in the first stage preheater. The exhaust smoke at the hot end outlet of the first-stage preheater enters a gas-liquid separator to separate CO 2 ，CO 2 After compression and capture, the outlet pressure of the second compressor 920 for carbon dioxide compression is 60-100bar, and the carbon dioxide can be finally buried.
In some embodiments, a third preheater 610 is further disposed between the second preheater 380 and the solar gasifier 110, the third preheater 610 having a water inlet end, a gas inlet end, a water outlet end, and a gas outlet end, the water inlet end of the third preheater 610 being in communication with the water outlet end of the second preheater 380, the water outlet end of the third preheater 610 being in communication with the water inlet end of the solar gasifier 110, the gas inlet end of the third preheater 610 being in communication with the gas outlet end of the fuel preheater 600, the third preheater 610 being configured to receive cathode gas passing through the fuel preheater 600 for heat transfer to the water supply of the water supply pump 130;
the air turbine 620 is connected to the air outlet end of the third preheater 610, for recovering the residual pressure energy of the cathode gas after heat transfer in the third preheater 610.
In this way, the cathode gas at 800-900 ℃ is recycled to heat the external air source of the SOFC, the combustible gas introduced into the anode layer 210 and/or the solar gasification furnace 110 in the third preheater 610, and then is discharged to the atmosphere, thereby realizing the efficient recycling of the SOFC cathode gas.
As an example, the power generation system further comprises a heat exchanger 910 and a first compressor 900, the heat exchanger 910 having a cold side channel and a hot side channel, the cold side channel having a cold side inlet and a cold side outlet, the hot side channel having a hot side inlet and a hot side outlet, the first compressor 900 being in communication with the cold side inlet of the heat exchanger 910, the hot side inlet and the cold side outlet of the heat exchanger 910 being both in communication with the cathode layer 220, and the hot side inlet of the heat exchanger 910 being for the entry of cathode gas, the hot side outlet of the heat exchanger 910 being for the exit of cathode gas.
The heat exchanger 910 is configured to exchange heat between the cold side channel and the hot side channel, and transfer the heat of the cathode gas to the compressed air compressed by the first compressor 900.
In this way, through the cooperation of the heat exchanger 910 and the first compressor 900, the oxygen as the raw material for the cathode layer 220 reaction can be pressurized and heated in advance, that is, pressurized by the first compressor 900, and preheated by the cathode gas in the heat exchanger 910, and the oxygen concentration, the activation energy and the reaction efficiency of the cathode reaction are obviously improved by utilizing the high-temperature gas produced by the cathode reaction and the residual reaction gas, and the high-energy oxygen source for further improving the high-temperature high-pressure cathode reaction, so that the energy for heating the cathode reaction gas source is saved, and it is to be noted that the cathode reaction is O 2 +e - →O 2- Illustratively, the cathode material is a Lasmaus material (Lanthanum Strontium Manganite, abbreviated LSM) composed of oxides of lanthanum, strontium, and manganese.
The embodiment of the invention at least realizes the following beneficial effects:
the introduction of solar energy can avoid the consumption of fuel coal and simultaneously avoid the CO of the combustion process of the fuel coal 2 Discharging; in addition, through the combination arrangement of a plurality of turbines, SOFC and gas turbine combustion chambers and the cooperation of a plurality of preheaters and/or heat exchangers, the comprehensive cascade utilization of the pressure energy, the heat energy and the combustion reaction chemical energy of gasification products of cathode and anode gases is realized, so that the power generation efficiency is improved; on the other hand, the combustion chamber of the combustion turbine adopts the oxygen-enriched combustion technology, so that the combustion product only contains H 2 O and CO 2 Then the CO can be realized after the temperature and the pressure are reduced 2 Compared with the prior art, the method has the advantages that compared with the prior art that more power generation power consumption of a power generation system is occupied to capture carbon dioxide by the MEI alcohol amine method, the method remarkably improves the capture efficiency of the carbon dioxide, improves the power generation efficiency of the power generation system, reduces the consumption of fossil energy, improves the power generation proportion of renewable energy, and has wide development and application prospects in the field of coal-based power generation.
Specifically, the embodiment of the invention at least comprises the following advantages:
(1) The solar energy is adopted to provide gasification reaction heat, so that the consumption of fuel coal and CO in the combustion process are avoided 2 The emission improves the power generation proportion of solar energy, and is practicalThe light coal is complementary to generate electricity.
(2) The flue gas is used for preheating the water supply of the solar gasifier through the combustion of the gas turbine, and the SOFC cathode gas is used for further heating the water supply of the solar gasifier, so that the heat load of the gasification chamber of the solar gasifier is reduced.
(3) The gasification products of the solar gasification furnace, namely the pressure energy, sensible heat and chemical energy of the synthesis gas are respectively utilized to generate power through a supercritical turbine, an SOFC and a gas turbine, so that the efficient cascade utilization of energy is realized, and the power generation efficiency is improved.
(4) The combustion chamber of the gas turbine adopts the oxygen-enriched combustion technology, and the first synthesis gas mainly consists of H 2 、CH 4 、CO、CO 2 And C 2 H 6 After reforming and conversion reaction, electrochemical reaction takes place in the SOFC anode, and the anode gas is H only 2 、H 2 O and CO 2 After cooling, the anode gas enters a combustion chamber of the gas turbine, and is combusted with pure oxygen to generate a gas mixture containing only H 2 O and CO 2 Is cooled and depressurized to realize CO 2 Is used for separating and capturing CO 2 Is provided.
In the description of the present invention, it should be understood that the terms "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", etc. indicate orientations or positional relationships based on the drawings, are merely for convenience in describing the present invention and simplifying the description, and do not indicate or imply that the devices or elements referred to must have a specific orientation, be configured and operated in a specific orientation, and thus should not be construed as limiting the present invention.
Furthermore, the terms "first," "second," and the like, are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include at least one such feature. In the description of the present invention, the meaning of "plurality" means at least two, for example, two, three, etc., unless specifically defined otherwise.
In the present invention, unless explicitly specified and limited otherwise, the terms "mounted," "connected," "secured," and the like are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally formed; can be mechanically or electrically connected; either directly or indirectly, through intermediaries, or both, may be in communication with each other or in interaction with each other, unless expressly defined otherwise. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.
In the present invention, unless expressly stated or limited otherwise, a first feature "up" or "down" a second feature may be the first and second features in direct contact, or the first and second features in indirect contact via an intervening medium. Moreover, a first feature being "above," "over" and "on" a second feature may be a first feature being directly above or obliquely above the second feature, or simply indicating that the first feature is level higher than the second feature. The first feature being "under", "below" and "beneath" the second feature may be the first feature being directly under or obliquely below the second feature, or simply indicating that the first feature is less level than the second feature.
In this specification, each embodiment or implementation is described in a progressive manner, and each embodiment focuses on a difference from other embodiments, and identical and similar parts between the embodiments are all enough to refer to each other.
It should be noted that references in the specification to "one embodiment," "an example embodiment," "some embodiments," etc., indicate that the embodiment may include a particular feature, structure, or characteristic, but every embodiment may not necessarily include the particular feature, structure, or characteristic. Moreover, such phrases are not necessarily referring to the same embodiment. Furthermore, when a particular feature, structure, or characteristic is described in connection with an embodiment, it is submitted that it is within the knowledge of one skilled in the art to effect such feature, structure, or characteristic in connection with other embodiments whether or not explicitly described.
Finally, it should be noted that: the above embodiments are only for illustrating the technical solution of the present invention, and not for limiting the same; although the invention has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical scheme described in the foregoing embodiments can be modified or some or all of the technical features thereof can be replaced by equivalents; such modifications and substitutions do not depart from the spirit of the invention.

Claims (10)

1. A power generation system is characterized by comprising a solar reaction device, a solid oxide fuel cell, a reaction unit and a first gas-liquid separator;
the solar reaction apparatus includes a solar module configured to provide thermal energy to the solar gasifier through solar energy, the solar gasifier having a reactant inlet for introducing gasified coal and water into the solar gasifier and a product outlet, and the solar gasifier configured to react the gasified coal introduced into the solar gasifier with water through the received thermal energy to generate a first synthesis gas, wherein the first synthesis gas includes a combustible gas and carbon dioxide, the solid oxide fuel cell includes an anode layer, an electrolyte layer, and a cathode layer disposed in sequence, the reaction unit is connected between the product outlet and the anode layer, the reaction unit is configured to perform a reforming reaction on the combustible gas to generate a second synthesis gas, the second synthesis gas includes hydrogen and carbon monoxide; the anode layer is configured to receive the second syngas to generate electrical energy through electrochemical reactions between the second syngas and ions of the cathode layer;
the first gas-liquid separator is configured to separate and collect carbon dioxide generated by the solar gasifier and the solid oxide fuel cell.
2. The power generation system of claim 1, wherein the reactant inlets comprise a first reactant inlet for delivering vaporized coal into the solar vaporization furnace and a second reactant inlet for delivering water into the solar vaporization furnace, and wherein the second reactant inlet is in communication with the cathode layer such that water delivered into the solar vaporization furnace is heated by cathode gas generated by the cathode layer;
the solar module comprises an optical focusing device and a reflecting device, wherein the optical focusing device is configured to project light rays irradiated to the optical focusing device to the reflecting device, and the reflecting device reflects the light rays to the solar reaction device and provides heat energy for the solar reaction device.
3. The power generation system of claim 1 or 2, further comprising a supercritical turbine coupled between the product outlet and the reaction unit for converting pressure energy of the first synthesis gas into mechanical energy for power generation.
4. The power generation system of claim 3, wherein the reaction unit comprises a first preheater, a reforming reactor, a first water pump and a water feed preheater, the first preheater having a cold end, a hot end, a cold end outlet and a hot end outlet, the reforming reactor having a feed end and a discharge end, the cold end of the first preheater being in communication with the product outlet of the solar gasifier, the cold end outlet of the first preheater being in communication with the feed end of the reforming reactor;
one of the hot end of the first preheater and the reforming reactor is communicated with the anode layer so as to transfer heat from anode gas generated by the anode layer to the first synthesis gas;
the reforming reactor is provided with a liquid inlet, the water supply preheater is provided with a first water inlet, a first water outlet and a hot end inlet, the first water outlet is communicated with the liquid inlet, the hot end inlet is communicated with the discharge end of the reforming reactor, the first water pump is communicated with the first water inlet, the water supply preheater is used for preheating water from the first water pump and then conveying the water to the reforming reactor, so that the water preheated by the water supply preheater, the first synthetic gas and the anode gas are mixed and then subjected to reforming reaction, and reforming reaction products comprise carbon monoxide and hydrogen;
the first hot side inlet is for receiving the reforming reaction product.
5. The power generation system of claim 4, wherein the reaction unit further comprises a shift reactor having a first feed end, a second feed end, and a discharge end, the feed preheater further having a second water inlet, a second water outlet, and a second hot end outlet, the first feed end in communication with the second hot end outlet to receive the preheated reformate reaction product;
the second feeding end is communicated with a second water outlet of the water supply preheater so as to receive preheated water from the water supply preheater, the discharging end of the shift reactor is communicated with the anode layer, and the shift reactor is used for carrying out water gas shift reaction on the reforming reaction product and the preheated water so as to generate third synthesis gas, wherein the third synthesis gas comprises hydrogen and carbon dioxide;
the anode layer is configured to receive the third syngas to generate electrical energy via electrochemical reactions between the third syngas and ions of the cathode layer.
6. The power generation system of claim 5, further comprising a fuel preheater having a first inlet end in communication with the discharge end of the shift reactor, a second inlet end in communication with the anode layer, and a first outlet end in communication with the cathode layer, the fuel preheater configured to receive the cathode gas to transfer heat to the third syngas.
7. The power generation system of claim 4, further comprising a gas turbine in communication with the first preheater and a combustion chamber disposed within the gas turbine, the combustion chamber having a fuel inlet end, an oxygen inlet end, and an outlet end, the fuel inlet end being in communication with the hot end outlet of the first preheater for receiving the anode gas;
the combustion chamber is used for enabling the anode gas to generate combustion reaction and generate combustion smoke, the gas turbine is provided with a gas inlet, a gas outlet and a power output end, the outlet end of the combustion chamber is communicated with the gas inlet of the gas turbine, the gas outlet is communicated with the inlet of the first gas-liquid separator, and the gas turbine is used for utilizing the combustion smoke to do work so that the power output end outputs mechanical energy for generating electricity.
8. The power generation system according to claim 7, wherein a pressure reducing valve, a condenser, a second gas-liquid separator and a second preheater are further sequentially arranged between the supercritical level and the first preheater, a reactant inlet of the solar gasifier is communicated with a water supply pump, the second preheater is provided with a water inlet end, an air inlet end, a water outlet end and an air outlet end, the inlet end of the pressure reducing valve is communicated with a product outlet of the solar gasifier, the outlet end of the pressure reducing valve is communicated with the inlet end of the condenser, the outlet end of the condenser is communicated with the inlet end of the second gas-liquid separator, the gas outlet end of the second gas-liquid separator is communicated with the first preheater, the liquid outlet end of the second gas-liquid separator is communicated with a water inlet of the water supply pump, the water outlet end of the second preheater is communicated with the water inlet end of the second preheater, the water outlet end of the second preheater is communicated with the water inlet end of the solar gasifier, the gas outlet end of the second gas turbine is communicated with the gas inlet end of the second gas-liquid separator;
the second gas-liquid separator is configured to separate and convey the liquid in the combustible gas to the second preheater and to be heat-transferred by the anode gas together with the water supply of the water supply pump.
9. The power generation system of claim 8, wherein a third preheater is further disposed between the second preheater and the solar gasifier, the third preheater having a water inlet end, a gas inlet end, a water outlet end, and a gas outlet end, the water inlet end of the third preheater being in communication with the water outlet end of the second preheater, the water outlet end of the third preheater being in communication with the water inlet end of the solar gasifier, the gas inlet end of the third preheater being in communication with the gas outlet end of the fuel preheater, the third preheater being configured to receive cathode gas passing through the fuel preheater for heat transfer to the water supply of the water supply pump;
and the air outlet end of the third preheater is communicated with an air turbine for recovering residual pressure energy of the cathode gas after heat transfer in the third preheater.
10. The power generation system of claim 1 or 2, further comprising a heat exchanger having a cold side channel and a hot side channel, the cold side channel having a cold side inlet and a cold side outlet, the hot side channel having a hot side inlet and a hot side outlet, the first compressor in communication with the cold side inlet of the heat exchanger, the hot side inlet and the cold side outlet of the heat exchanger both in communication with the cathode layer, and the hot side inlet of the heat exchanger for ingress of cathode gas, the hot side outlet of the heat exchanger for egress of the cathode gas;
the heat exchanger is configured to exchange heat with the cold side channel and the hot side channel to transfer heat from the cathode gas to the compressed air compressed by the first compressor.
CN202311187485.5A 2023-09-14 2023-09-14 Power generation system Pending CN117307426A (en)

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