CN109193009A - Solid oxide fuel cell composite system and application method - Google Patents

Solid oxide fuel cell composite system and application method Download PDF

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Publication number
CN109193009A
CN109193009A CN201811092130.7A CN201811092130A CN109193009A CN 109193009 A CN109193009 A CN 109193009A CN 201811092130 A CN201811092130 A CN 201811092130A CN 109193009 A CN109193009 A CN 109193009A
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carbon dioxide
reformer
absorption
gas
burner
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CN109193009B (en
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叶爽
黄伟光
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Shanghai Advanced Research Institute of CAS
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Shanghai Advanced Research Institute of CAS
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    • 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
    • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04298—Processes for controlling fuel cells or fuel cell systems
    • H01M8/04694—Processes for controlling fuel cells or fuel cell systems characterised by variables to be controlled
    • H01M8/04791—Concentration; Density
    • H01M8/04805—Concentration; Density of fuel cell exhausts
    • 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
    • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04298—Processes for controlling fuel cells or fuel cell systems
    • H01M8/04694—Processes for controlling fuel cells or fuel cell systems characterised by variables to be controlled
    • H01M8/04828—Humidity; Water content
    • H01M8/04843—Humidity; Water content of fuel cell exhausts
    • 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
    • H01M8/0625—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 in a modular combined reactor/fuel cell structure
    • H01M8/0631—Reactor construction specially adapted for combination reactor/fuel cell
    • 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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  • Life Sciences & Earth Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Manufacturing & Machinery (AREA)
  • Sustainable Development (AREA)
  • Sustainable Energy (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Electrochemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Fuel Cell (AREA)

Abstract

The present invention provides a kind of solid oxide fuel cell composite system and application method, including electricity generation system and carbon dioxide capture system, electricity generation system includes reformer, battery pile, vaporizer and burner, reformer first input end is connected to fuel feeder, the second input terminal of reformer is connected to vaporizer, and the first output end of reformer is connected to battery pile；Burner first input end is connected to fuel feeder, the second input terminal of burner and air communication；Trapping system entrance is connected to cell stack anode outlet, and trapping system outlet, which is selected from, at least one of to be connected with burner, be connected with reformer and directly empty.Combustible component and generation water in split cell heap anode exhaust gas of the present invention, realize the recycling of combustible component；The high-grade heat-driven carbon dioxide capture system of fuel gas is made full use of, the recycling of carbon dioxide is realized on the basis of low energy consumption even zero energy consumption, carbon dioxide near-zero release is realized while so that system high efficiency is generated electricity.

Description

Solid oxide fuel cell composite system and application method
Technical field
The invention belongs to fuel cell generation technical fields, multiple more particularly to a kind of solid oxide fuel cell Collaboration system and application method.
Background technique
Solid oxide fuel cell (SOFC) electricity generation system is the power generation dress for converting the chemical energy in fuel to electric energy It sets.The selectable fuel of SOFC is relatively broad, plant hydrogen, natural gas, town gas, methanol, alcohol, diesel oil and some biologies Fuel etc. can be applied in SOFC electricity generation system directly or through after simple process, thus, SOFC is acknowledged as taking Connect the bridge of Hydrogen Energy society.The another of SOFC has the prominent advantages that its efficiency is higher, and electrical efficiency is up to 55%, if realizing thermoelectricity Coproduction, efficiency is up to 80% or more, higher than any traditional generator or other types of fuel cell.
Can SOFC realize the size of higher generating efficiency Yu its fuel availability (Fuel Utilization rate) There is direct relation, i.e., the size of fuel availability determines the size (fuel of fuel cell power generation efficiency under certain condition for import Utilization rate is lower, and the content of combustible component is higher in pile anode exhaust gas).Therefore, high fuel availability is evaluation SOFC business One of important indicator of change.Method commonly used in the fuel availability of raising SOFC electricity generation system is main are as follows: (1) improves single electricity The performance of pond or pile；(2) air demand of pile is reduced.The above method (1) reaches showing for certain level in fuel cell technology Under having ready conditions, it is larger to continue to improve the performance of monocell or pile its difficulty for realizing, and then to will lead to SOFC mono- electric for method (2) Pond is since for unsaturated vapor, anode locally redox cycle occurs and failure, damage occurs.
In order to make full use of the energy of anode exhaust gas, SOFC electricity generation system is using following several modes to anode exhaust gas at present Energy using: (1) will anode exhaust gas carry out heat exchange and condensation after empty；(2) by anode exhaust gas carry out heat exchange and Burner is passed through after condensation；(3) segment anode tail gas recycle is passed through reformer.However also have with upper type respective problem with Difficult point, mode (1) and have ignored the chemical energy of combustible component in anode exhaust gas merely with the thermal energy of anode exhaust gas；Mode (2) It is heat that although not only having recycled the thermal energy of anode exhaust gas, in anode exhaust gas, the chemical energy of combustible component, which is by burning conversion, Can, and fail to be fully converted into electric energy；Mode (3) is although the thermal energy of anode exhaust gas can be recycled, and partially recycled anode tail The chemical energy of combustible component and it is used for electrochemical reaction in gas, but still there is part combustible component to be discharged, and which pair The heat-resisting quantity of reuse pump, valve etc. requires very high, it is not easy to realize.Thus, above method or anode exhaust gas is only utilized Heat or the chemical energy of combustible component in anode exhaust gas only will partially be utilized, do not filled yet for energy grade angle Divide the chemical energy for efficiently utilizing fuel.
Therefore, this field still lacks and a kind of can improve system fuel utilization simultaneously and can fill from the grade angle of energy Point using fuel chemical energy method, how to provide a kind of solid oxide fuel cell composite system and application method to solve The above problem certainly in the prior art is necessary.
Summary of the invention
In view of the foregoing deficiencies of prior art, the purpose of the present invention is to provide a kind of solid oxide fuel cell Composite system and application method, for solving in the prior art, system fuel utilization is low, energy is difficult to sufficiently in anode exhaust gas The problems such as effective use.
In order to achieve the above objects and other related objects, the present invention provides a kind of compound system of solid oxide fuel cell System, the solid oxide fuel cell composite system includes electricity generation system and carbon dioxide capture system, in which:
The electricity generation system includes reformer, battery pile, vaporizer and burner, in which:
The reformer first input end of the reformer is connected with fuel feeder, the second input terminal of reformer and institute It states vaporizer to be connected, the first output end of reformer is connected with the battery pile, and the gas supply is based on inside the reformer Vapor in fuel gas and the vaporizer in device carries out reforming reaction, and the gas reformed after internal-response It exports from first output end of reformer to the anode inlet of the battery pile；
The burner first input end of the burner is connected with the fuel feeder, the second input terminal of burner With contact air, combustible component of the burner internal based on the fuel gas, recycling in the feeder and The air inputted from second input terminal of burner is reacted and generates thermal energy；
The carbon dioxide capture system includes trapping system entrance and trapping system outlet, wherein the trapping system Entrance is connected with the anode export of battery pile described in the electricity generation system, and the trapping system outlet is selected from and the combustion Burner at least one of is connected, is connected and directly empties with the reformer.
As a kind of optinal plan of the invention, the burner further includes the first output end of burner, the burner First output end is successively connected via the reformer, the vaporizer with the trapping system entrance, by the burning The combustion tail gas generated in device is input in the carbon dioxide capture system.
As a kind of optinal plan of the invention, the carbon dioxide capture system includes carbon dioxide absorption tower, described Carbon dioxide absorption tower includes absorption tower air supply opening and absorption tower exhaust outlet, wherein is caught described in the absorption tower air supply opening conduct Collecting system entrance, the absorption tower exhaust outlet are exported as the trapping system.
As a kind of optinal plan of the invention, the carbon dioxide absorption tower successively includes absorbing tower from bottom to top Bottom, absorption tower packing layer and absorption tower spray equipment, and the absorption tower air supply opening is set to the lower section of described filler layer, In, the absorption tower spray equipment accommodates the carbon dioxide for spraying carbon dioxide absorption lean solution, the absorbing tower bottom Absorb the carbon dioxide rich solution formed after lean solution absorbing carbon dioxide.
As a kind of optinal plan of the invention, the carbon dioxide absorption tower further includes absorption tower heat-exchanger rig, described Absorption tower heat-exchanger rig is set to the bottom at the absorbing tower bottom, and the absorption tower heat-exchanger rig is by the carbon dioxide absorption The heat output generated when lean solution absorbing carbon dioxide.
As a kind of optinal plan of the invention, the carbon dioxide capture system further includes carbon dioxide absorbent solution regeneration Tower, the carbon dioxide absorbent solution regenerator include absorbing rich solution entrance and absorbing lean solution to export, the carbon dioxide absorption tower It further include absorbing lean solution entrance and absorption rich solution outlet, wherein the absorption lean solution of the carbon dioxide absorbent solution regenerator exports It is connected with the absorption lean solution entrance of the carbon dioxide absorption tower, the absorption rich solution outlet of the carbon dioxide absorption tower and institute The absorption rich solution entrance for stating carbon dioxide absorbent solution regenerator is connected.
As a kind of optinal plan of the invention, the carbon dioxide absorbent solution regenerator successively includes regeneration from bottom to top Tower tower bottom, regenerator packing layer and regenerator spray equipment, the regenerator tower bottom accommodate the carbon dioxide absorption rich solution again The carbon dioxide absorption lean solution obtained after life, the absorption rich solution entrance of the carbon dioxide absorbent solution regenerator and institute It states regenerator spray equipment to be connected, absorption lean solution outlet and the regenerator of the carbon dioxide absorbent solution regenerator Tower bottom is connected.
As a kind of optinal plan of the invention, the carbon dioxide absorption tower and the carbon dioxide absorbent solution regenerator Between be additionally provided with absorbing liquid heat-exchanger rig, the absorbing liquid heat-exchanger rig is set to the absorption rich solution outlet and the absorption In rich solution entrance and the pipeline absorbed between lean solution outlet and the absorption lean solution entrance, so as to derive from the carbon dioxide The absorption rich solution of absorption tower output carries out heat with the absorption lean solution exported from the carbon dioxide absorbent solution regenerator Amount exchange.
As a kind of optinal plan of the invention, the carbon dioxide capture system further includes reboiler, the reboiler Reboiler entrance and the liquid communication that is exported after the regenerator packing layer, the reboiler heat the titanium dioxide The absorption lean solution in carbon absorption liquid regenerator carries out air lift to generate a large amount of vapor, and keeps the carbon dioxide Temperature in regeneration of absorption solution tower.
As a kind of optinal plan of the invention, the anode export of battery pile described in the electricity generation system by into Feed channel is connected with the reboiler, and from the anode exhaust gas that the anode export exports by passing through after the reboiler Pipeline enters the trapping system entrance of the carbon dioxide capture system.
It is described between the reformer and the battery pile and the reboiler as a kind of optinal plan of the invention Admission line is connected, wherein the anode exhaust gas exported in the anode export is via the reformer and described boils again Device enters the trapping system entrance.
As a kind of optinal plan of the invention, the carbon dioxide capture system further includes vapor condensing heat exchanger, The carbon dioxide absorbent solution regenerator includes regenerator exhaust outlet, the regenerator exhaust outlet and the vapor condensing heat-exchange The condensing heat exchanger entrance of device is connected.
As a kind of optinal plan of the invention, the carbon dioxide capture system further includes gas-liquid separator, wherein institute The separator inlet for stating gas-liquid separator is connected with the outlet of the condensing heat exchanger of the vapor condensing heat exchanger.
As a kind of optinal plan of the invention, the solid oxide fuel cell composite system further includes water supplying pipe Road, with to the reformer provide reforming reaction needed for water, wherein the separation of the water supply line and the gas-liquid separator The vaporizer entrance of device outlet and the vaporizer in the electricity generation system is connected, and the water supply line is via described Vapor condensing heat exchanger, to absorb the condensation heat of the vapor condensing heat exchanger.
As a kind of optinal plan of the invention, the electricity generation system further includes an at least anode preheating device, the sun The mode of action of pole preheater includes: that the anode preheating device connection is set between the vaporizer and the reformer, In, the vapor in the vaporizer is input to the reformer via the anode preheating device, in the feeder The fuel gas be input to the reformer via the anode preheating device, alternatively, the quantity of the anode preheating device includes It two, is respectively arranged between the fuel feeder and the reformer between the vaporizer and the reformer, Gas of the output into the reformer in the fuel feeder and the vaporizer is preheated respectively.
As a kind of optinal plan of the invention, the electricity generation system further includes cathode preheater, the cathode preheater It is connected with the cathode inlet of the battery pile, air enters the cathode inlet via the cathode preheater；The battery The cathode outlet of heap is also connected via the cathode preheater with the burner.
As a kind of optinal plan of the invention, the electricity generation system further includes air supply arrangement, the air supply Equipment is connected with the burner, the anode preheating device and the cathode preheater respectively, and air is inputted respectively To the burner, the anode preheating device and the cathode preheater.
As a kind of optinal plan of the invention, the anode preheating device is connected with blower, by air via described Anode preheating device is input to the reformer, so that carrying out oxidation reaction in the reformer, (wherein, self-heating recapitalization includes that water steams Vapour is reformed and oxidation reaction is reformed) it reacts, the reaction equation of the oxidation reaction includes:
CH4(g)+3/2O2(g)→CO(g)+2H2O(g)ΔH298 0=-519kJ/mol (2)；It is also possible to:
CH4(g)+2O2(g)→CO2(g)+2H2O(g)ΔH298 0=-802kJ/mol (1) or
CH4(g)+O2(g)→CO2(g)+2H2(g)ΔH298 0=-322kJ/mol (1)
As a kind of optinal plan of the invention, control enters the fuel gas, the vapor in the reformer And the mode of the flow of the air includes: steam/hydrocarbons ratio in the control reformer between 0-3, carbon ratio is between 0- Between 2.
As a kind of optinal plan of the invention, reducing gas intake line is additionally provided on the reformer, it is described to go back Raw-gas intake line is successively passed through reducing gas into the reformer and the battery pile, to restore in the reformer Catalyst and the monocell in the battery pile anode material.
As a kind of optinal plan of the invention, the outlet of the trapping system of the carbon dioxide capture system with it is described Air pump is additionally provided on pipeline between electricity generation system.
The present invention also provides a kind of application method of solid oxide fuel cell composite system, the application method includes Step: the solid oxide fuel cell composite system as described in any one of above scheme is provided, and is filled to the gas supply It is passed through the fuel gas in setting, converts electric energy for the chemical energy of the fuel gas, and at least recycling generates two in product Carbonoxide.
As described above, solid oxide fuel cell composite system of the invention and application method, have below beneficial to effect Fruit:
The solid oxide fuel cell composite system of the invention not only combustible component in split cell heap anode exhaust gas With combustion products CO2And water, to realize the abundant recycling of combustible component, while by making full use of fuel gas Gao Pin The thermal energy of position drives, and on the basis of low energy consumption even zero energy consumption, the trapping recycling of carbon dioxide can also be realized, to make The entire SOFC electricity generation system using fossil fuel not only reaches the purpose of efficiency power generation, moreover it is possible to realize carbon dioxide near-zero release Purpose.
Detailed description of the invention
Fig. 1 is shown as the system structure diagram of solid oxide fuel cell composite system provided by the invention.
Fig. 2 is shown as the specific structure signal of the solid oxide fuel cell composite system provided in the embodiment of the present invention Figure.
Component label instructions
100 electricity generation systems
101 reformers
101a reformer first input end
The second input terminal of 101b reformer
The first output end of 101c reformer
101d reformer third input terminal
102 battery piles
102a anode inlet
102b anode export
102c cathode inlet
102d cathode outlet
103 vaporizers
104 burners
104a burner first input end
The second input terminal of 104b burner
104c burner third input terminal
105 anode preheating devices
106 cathode preheaters
107 air supply arrangements
200 carbon dioxide capture systems
200a trapping system entrance
The outlet of 200b trapping system
300 feeders
201 carbon dioxide absorption towers
2011 absorption tower spray equipments
2012 absorption tower packing layers
2013 absorbing tower bottoms
2014 absorption tower heat-exchanger rigs
201a absorbs lean solution entrance
201b absorbs rich solution outlet
202 carbon dioxide absorbent solution regenerators
2021 regenerator spray equipments
2022 regenerator packing layers
2023 regenerator tower bottom
202a absorbs rich solution entrance
202b absorbs lean solution outlet
202c regenerator exhaust outlet
205 vapor condensing heat exchangers
205a condensing heat exchanger entrance
The outlet of 205b condensing heat exchanger
206 gas-liquid separators
206a separator inlet
206b separator outlet
207 water supply lines
208 air pumps
209 condensation water channels
401-411 regulating valve
Specific embodiment
Illustrate embodiments of the present invention below by way of specific specific example, those skilled in the art can be by this specification Other advantages and efficacy of the present invention can be easily understood for disclosed content.The present invention can also pass through in addition different specific realities The mode of applying is embodied or practiced, the various details in this specification can also based on different viewpoints and application, without departing from Various modifications or alterations are carried out under spirit of the invention.
Fig. 1 is please referred to Fig. 2.It should be noted that diagram provided in the present embodiment only illustrates this in a schematic way The basic conception of invention, though only show in diagram with related component in the present invention rather than package count when according to actual implementation Mesh, shape and size are drawn, when actual implementation form, quantity and the ratio of each component can arbitrarily change for one kind, and its Assembly layout form may also be increasingly complex.
As shown in Figures 1 and 2, the present invention provides a kind of solid oxide fuel cell composite system, the solid oxidation Object fuel cell composite system includes electricity generation system 100 and carbon dioxide capture system 200, in which:
The electricity generation system 100 converts electric energy by electrochemical reaction for the chemical energy being passed through in the fuel gas of system, Including reformer 101, battery pile 102, vaporizer 103 and burner 104, in which:
The reformer 101 is including at least reformer first input end 101a, reformer the second input terminal 101b and again Whole the first output end of device 101c, wherein the reformer first input end 101a and fuel feeder 300 of the reformer 101 Be connected, and can further carry out the adjusting of flow by regulating valve 402 and flowmeter, reformer the second input terminal 101b with The vaporizer 103 is connected, and reformer the first output end 101c is connected with the battery pile 102, further with the electricity The anode inlet 102a of pond heap 102 is connected, based on the fuel in the fuel feeder 300 inside the reformer 101 Vapor in gas and the vaporizer 103 carries out reforming reaction, and the gas reformed after 101 internal-responses export to The anode inlet 102a of the battery pile 102；
The burner 104 includes at least burner first input end 104a, burner the second input terminal 104b, the combustion The burner first input end 104a of burner 104 is connected with the fuel feeder 300, and can further pass through adjusting Valve 401 and flowmeter carry out the adjusting of flow, burner the second input terminal 104b and contact air, can be blower and drive sky Gas enters, and regulating valve 404 and flowmeter progress air stream preferably can further be arranged between blower and the burner The control of amount, based on the fuel gas in the feeder 300 and from the burner inside the burner 104 The air of two input terminal 104b input is reacted and generates thermal energy；
The carbon dioxide capture system 200 includes that trapping system entrance 200a and trapping system export 200b, wherein institute It states trapping system entrance 200a to be connected with the anode export 102b of battery pile 102 described in the electricity generation system, the trapping System outlet 200b selected from be connected with the reformer 101 in the electricity generation system or the trapping system outlet The tail gas that 200b is connected with the burner 104 in the electricity generation system or the trapping system exports in 200b is straight Any two kinds or more to run in sky or aforesaid way, wherein can be and directly emptied by pipeline.It is preferred one In example, the trapping system outlet and at least one in the burner and the reformer in the electricity generation system are selected Person is connected, to realize the recycling of the middle tail gas of the carbon dioxide capture system in the power generation system.
Specifically, the present invention provides the solid oxide fuel that a kind of pair of cell stack anode tail gas can be recycled Battery composite system (SOFC electricity generation system), including electricity generation system 100 and carbon dioxide capture system 200, wherein in the present invention Be connected and be connected and can be the piping connection etc. being carried out by scheme well-known to those skilled in the art, In:
For the electricity generation system 100, can by be passed through electricity generation system in the fuel feeder 300 Chemical energy in fuel gas is converted into electric energy by electrochemical reaction, wherein the fuel gas plant hydrogen, natural gas, city Coal gas, methanol, alcohol, diesel oil and some bio-fuels etc., it is not limited to this, methane (CH is selected as in this example4).It is described Electricity generation system 100 includes at least reformer 101, battery pile 102, vaporizer 103 and burner 104.
For the reformer 101, by pipeline respectively with the fuel feeder 300, the vaporizer 103 and The anode inlet 102a of the battery pile 102 is connected, in addition, in an optional example, the reformer first input end 101a and the second input terminal of reformer 101b can be the shared same input port, as shown in Figure 2.Described heavy In whole device 101, reforming reaction can be carried out, using fuel gas as raw natural gas CH4For carrying out reforming reaction, it can use The prior art realizes, weight that common reaction temperature section carries out in 300 DEG C~600 DEG C or so, the reformer 101 It has suffered the CH that journey includes reaction equation (3), (4)4The CO conversion reaction of (natural gas) steam reforming reaction and reaction equation (5):
Methane-steam reforming:
CH4(g)+H2O(g)→CO(g)+3H2(g)ΔH298 0=206kJ/mol (3)
CH4(g)+2H2O(g)→CO2(g)+4H2(g)ΔH298 0=165kJ/mol (4)
CO conversion reaction:
CO(g)+H2O(g)→CO2(g)+H2(g)ΔH298 0=-41kJ/mol (5)
Certainly, when being passed through other fuel gas in the reformer 101, it is well known that other reforming reactions can be carried out, and It is not limited.For reformer the first output end 101c of the reformer 101, exit gas includes CO, H2、CO2And CH4、H2The complete gas of the unreacteds such as O, above-mentioned gas reaches the battery pile 102 through high temperature conduit, via the battery pile Anode inlet 102a reaches the anode in battery pile, to carry out the electrochemical reaction in battery pile.
As an example, the reformer 101 can also and contact air, so that air is input to the reformer In, such as it is connected by pipeline, so that carrying out oxidation reaction in the reformer, the reaction equation of the oxidation reaction includes:
Partial oxidation reaction of methane:
CH4(g)+3/2O2(g)→CO(g)+2H2O(g)ΔH298 0=-519kJ/mol (2)
Certainly, the reaction equation of the oxidation reaction may also is that
CH4(g)+2O2(g)→CO2(g)+2H2O (g) Δ H2980=-802kJ/mol (1)；Or
CH4(g)+O2(g)→CO2(g)+2H2(g) (1) Δ H2980=-322kJ/mol
Specifically, in one example, in the reformer 101 other than carrying out above-mentioned reforming reaction, also described in progress Oxidation reaction, wherein carry out the oxidation reaction can make up during startup reformer 101 energy deficiency situation and The heating rate for accelerating hot-zone C, at this point, a certain amount of CH can be passed through4And air, in a preferable example, described in control entrance Gas flow in reformer 101, CH4、H2The flow of O and air is controlled in following ratio: steam/hydrocarbons ratio (vapor and CH4Rub That ratio) control is between 0-3, carbon ratio (O2 and CH4Molar ratio) control between 0-2, here, steam/hydrocarbons ratio refers to entirely It is aqueous to be greater than 0 with carbon containing the ratio between mole and be less than or equal to 3 in the reformer, it is oxygen-containing to be less than with carbon containing the ratio between mole greater than 0 Equal to 2, in one example, it can be the flow of the fuel gas of fixed import, water then adjusted according to fuel gas flow The flow of steam, air.Wherein, battery pile 102, reformer 101 and connection reformer and several pipelines of battery pile and right Battery pile and reformer play support and the shell of heat insulating function is referred to as hot-zone C.
Wherein, in SOFC electricity generation system startup stage, according to conditions such as the temperature of import substance and reformer, in an example In, the reforming process carried out in the reformer 101 includes the CH of reaction equation (3), (4)4(natural gas) steam reforming reaction, The CH of at least one of reaction equation (1) and (2)4The CO conversion reaction of the oxidation reaction and reaction equation (5) of (natural gas), into The CH of at least one of the above-mentioned reaction equation (1) of row and (2)4The oxidation reaction of (natural gas), to make up the energy of reformer 101 Insufficient situation, and accelerate the heating rate of hot-zone C, CH4Reforming reaction occurs with vapor and oxygen in reformer 101, Generate H2、CO、CO2And unreacted CH4、H2O and N2Mixed gas, above-mentioned gas form reformer outlet gas.
As an example, weight of the origin of heat inside the reformer 101 required for 101 internal-response of reformer Heat, the combustion product gases heat in the burner 104 and the electrochemical reaction in the battery pile 102 that whole reaction generates At least one of heat release.
Specifically, may come from the burner 104 for the energy source that the reformer 101 is reacted Combustion product gases sensible heat, can also be the electrochemical reaction heat release in the battery pile 102, in addition, in the reformer lead to It further include the heat generated from the oxidation reaction in the case where crossing air progress oxidation reaction.
For the battery pile 102, including anode inlet 102a, anode is passed through anode via the anode inlet 102a Reaction gas, in addition, in one example, the battery pile 102 further includes cathode inlet 102c and cathode outlet 102d, In, air can enter the cathode inlet 102c via pipeline and reach the cathode of the battery pile 102, to carry out battery pile In electrochemical reaction.
For the vaporizer 103, the vaporizer 103 by pipeline is input to the reformer 101 after vaporizing water into In, wherein the water in the vaporizer can also be can use cold in the carbon dioxide capture system by externally supplying Condensate.
As an example, origin of heat required for 103 internal-response of vaporizer is in the carbon dioxide capture system In the condensation heat of water vapour condensing heat exchanger, the combustion product gases heat in the burner 104, in the battery pile 102 At least one of cathode exhaust gas waste heat in anode exhaust gas waste heat and the battery pile 102.
Specifically, can be the combustion in the burner 104 for the source of the heat needed in the vaporizer 103 Burn fume afterheat, can also be the anode exhaust gas of the anode export in the battery pile 102 preheating or the electricity The waste heat of the cathode exhaust gas of the cathode outlet in pond heap 102, in addition, containing when in the carbon dioxide capture system 200 When water vapour condensing heat exchanger, the condensation heat from water vapour condensing heat exchanger can also be.
For the burner 104, the burner 104 passes through pipeline and the fuel feeder 300 and air It is connected, is carried out instead inside the burner 104 based on the fuel gas in the feeder 300 and the air of input Thermal energy should and be generated, after the burner 104 starts, fuel gas (such as CH in fuel feeder 3004) chemistry Energy meeting continued shift is thermal energy, and a part of the heat of burner 300 (such as heat of level-one flue gas) is passed to hot-zone C, Hot-zone C constant temperature is set to rise to target temperature, another part heat (heat of such as secondary smoke) of the burner 104 continues The vaporizer 103 is heated, its constant temperature is made to rise to target temperature.Wherein, in one example in burner 104, CH4Pressure Power and flow are controlled by pressure gauge and flowmeter, and air mass flow is controlled by blower and flowmeter.
In addition, the carbon dioxide capture system 200 can trap described for the carbon dioxide capture system 200 The most carbon dioxide in anode exhaust gas in the anode export 102b of battery pile, and titanium dioxide will be absorbed Residual gas (such as H of 100 anode exhaust gas of battery pile after carbon2、CO、CH4) give from trapping system outlet 200b to reformer At least one of 101, give into burner 104 or directly empty, it preferably is selected from the trapping system outlet 200b and send to reformation It device 101 and at least one of send to burner 104, in a preferable example, at least exports 200b from the trapping system It send to the burner, to make full use of the chemical energy of combustible component.Wherein, in one example, the trapping system outlet Gas in 200b can be merely entered into the reformer 101, can also be merely entered into the burner 104, can be with It is input in the reformer 101 and the burner 104 simultaneously, in a preferable example, while being input to the reformer 101 and the burner 104 in, and the flow being input in the burner 104 accounts for the stream of trapping system outlet 200b The 20%-100% of amount, it is preferable that the temperature at least one of the reformer and the battery pile, which is less than, stablizes work Under conditions of the target temperature of work, the ratio for being input to the flow in the burner 104 is greater than 50%.I.e. in this example, institute Battery pile and burner that carbon dioxide capture system is connected to SOFC electricity generation system are stated, the anode exhaust gas for receiving battery pile is (complete Portion) and burner part combustion tail gas, and carbon dioxide therein is trapped, then according to SOFC electricity generation system to energy and energy The demand for measuring grade will absorb the residual gas after carbon dioxide and sent respectively to reformer, burner, sufficiently to recycle The chemical energy of combustible component.
Also it should be noted that in the solution of the present invention, in SOFC electricity generation system, in the fuel feeder 300 The fuel gas, such as CH4(natural gas) is directly entered SOFC electricity generation system air inlet pipe by desulfurization process from natural gas line In road.Wherein, it in the temperature-rise period of hot-zone C, can be adjusted into according to the target temperature of practical heating rate and steady operation Fuel gas (such as CH in the burner 1044) with the flow of air.In addition, in one example, in hot-zone, the temperature of C reaches After target temperature, continue to be passed through H into the reformer 101 and the battery pile 1022, to by catalyst in reformer and Nickel oxide in battery pile in the anode of SOFC monocell is reduced to W metal, further, to catalyst in the reformer 101 After being reduced sufficiently with the nickel oxide of SOFC anode in battery pile 102, a certain amount of water is passed through into the vaporizer 103, and Close H2, water is converted into vapor by vaporizer, and enter in reformer 101 (or reach target in the temperature of hot-zone C After temperature, a small amount of, a certain proportion of CH4 and vapor are directly passed through into the reformer 101).
In addition, in an optional example, when SOFC electricity generation system enters stable operation process, due to the battery pile The energy that the electrochemical reaction process carried out in 102 is released, which has been approached/is enough, realizes that the temperature of hot-zone C is constant, described at this time Burner 104 can not need burning CH4, that is, the feeder 300 stops being passed through the fuel into the burner 104 Gas, the anode exhaust gas that the combustor section is passed through from the carbon dioxide capture system 200, the burner 104 fires at this time It burns, on the one hand, by the flammable tail gas full combustion in anode exhaust gas；On the other hand, the chemical energy for discharging combustible component, makes up and is BOP system is to the total amount and grade demand of energy in uniting, and here, BOP system refers to including vaporizer, anode preheating device, cathode The system of preheater, reformer, burner etc..
As an example, the burner 104 further includes the first output end of burner 104d, first output end of burner 104d is successively connected via the reformer 101, the vaporizer 103 with the trapping system entrance 200a, will be described The combustion tail gas generated in burner 104 is input in the carbon dioxide capture system 200.
Specifically, the combustion tail gas in the burner 104 can be recycled further, and the combustion in the example Carbon dioxide in the combustion tail gas of burner 104 can be trapped partly or entirely by the carbon dioxide capture system 200, described Combustion tail gas can be connected to the trapping system entrance 200a, with the carbon dioxide being further reduced in discharge combustion tail gas. Regulating valve 411 can also be set on the pipeline between the vaporizer 103 and the trapping system entrance 200a, to realize The combustion tail gas that the burner 104 exports is exported to the control into carbon dioxide capture system 200.Certainly, the burning The combustion tail gas of device the first output end 104d output can also be connected with other waste heat utilization equipments, to realize returning for energy It receives and utilizes.
As an example, the carbon dioxide capture system 200 includes carbon dioxide absorption tower 201, the carbon dioxide is inhaled Receiving tower 201 includes absorption tower air supply opening and absorption tower exhaust outlet, wherein the absorption tower air supply opening enters as the trapping system Mouth 200a, the absorption tower exhaust outlet export 200b as the trapping system.
Specifically, carbon dioxide absorption tower 201 is arranged, for absorbing, trapping electricity in the carbon dioxide capture system Whole carbon dioxide in the anode exhaust gas of Chi Dui, wherein from the absorption tower air supply opening, i.e., the described carbon dioxide capture system The trapping system entrance 200a in, be passed through the anode exhaust gas after the battery pile 102 is reacted, the anode exhaust gas is described two It is fully absorbed in carbonoxide absorption tower 201, in one example, can be carried out two in anode exhaust gas using carbon dioxide absorbent solution The absorption of carbonoxide, then by the residual exhaust after fully absorbing, i.e., tail gas in the described carbon dioxide absorption tower is from the absorption Tower exhaust outlet, i.e., the described trapping system outlet 200b discharge, the preferably described absorption tower exhaust outlet are set to the carbon dioxide and inhale 201 top of tower is received, in one example, when the fuel gas is selected as CH4When, the trapping system exports 200b, for being discharged Anode exhaust gas has been absorbed residual gas (such as H after carbon dioxide2、CO、CH4), and the residual gas is sent respectively to described In burner 104 and/or the reformer 101 (the demand selection according to various parts to energy).
In one example, the carbon dioxide absorption tower 201 successively includes absorbing tower bottom 2013, absorption tower from bottom to top Packing layer 2012 and absorption tower spray equipment 2011, and the absorption tower air supply opening 200a is set to the absorption tower packing layer 2012 lower section, wherein the absorption tower spray equipment 2011 is for spraying carbon dioxide absorption lean solution, the absorbing tower bottom 2013 accommodate the carbon dioxide rich solution formed after the carbon dioxide absorption lean solution absorbing carbon dioxide.
Specifically, in one example, the carbon dioxide absorption tower 201 includes at least three parts, that is, absorbing tower bottom 2013, absorption tower packing layer 2012 and absorption tower spray equipment 2011, wherein inhaled for accommodating at the absorbing tower bottom 2013 Rich solution is received, the absorption rich solution, which refers to, absorbs the carbon dioxide absorbent solution of carbon dioxide, and the absorption tower packing layer 2012 is set The medium position in the carbon dioxide absorption tower 201 is set, (absorption is poor its role is to make carbon dioxide absorbent solution Liquid, i.e., not yet carry out carbon dioxide absorption absorbing liquid) with enter the carbon dioxide absorption tower in gas (such as battery pile The anode exhaust gas) there is bigger contact surface；The filler of the absorption tower packing layer can be chosen corresponding according to process requirements Material (such as ceramics, metal or plastics) and dimensions (such as specific surface area is 155,250,500).In addition, the absorption Tower spray equipment 2011, be arranged on the absorption tower packing layer 2012, for uniformly spray carbon dioxide absorption lean solution ( That is carbon dioxide absorbent solution).In addition, the absorption tower air supply opening is set to the absorption tower packing layer in an optional example The top at the absorbing tower bottom 2013 is further preferably arranged in 2012 lower section, for providing into absorption tower from electricity Carbon dioxide gas in pond heap anode exhaust gas and burner tail gas.
Wherein, in the carbon dioxide absorption tower 201, under carbon dioxide absorption lean solution is drenched from top to bottom, gas is under And upper flowing, carbon dioxide absorbent solution are contacted with the anode exhaust gas entered in absorption tower, and absorb carbon dioxide therein.Separately Outside, the carbon dioxide absorbent solution is potassium carbonate, arsenic trioxide, monoethanolamine, diethanol amine, methyl diethanolamine, amino Mixture in one of acetic acid, propene carbonate and polyethylene glycol dimethyl ether or above-mentioned each substance both at least it is water-soluble Liquid.It should be noted that the so-called absorption lean solution of the present invention and absorption rich solution, refer to, the carbon dioxide for absorbing carbon dioxide is inhaled The absorption rich solution can be become by receiving liquid, not yet absorbed carbon dioxide or the absorption rich solution carried out it is regenerated, can The absorption lean solution is properly termed as to carry out the carbon dioxide absorbent solution of carbon dioxide absorption again.
As an example, the carbon dioxide absorption tower 201 further includes absorption tower heat-exchanger rig 2014, the absorption tower heat exchange Device 2014 is set to the bottom at the absorbing tower bottom 2013, is used for the carbon dioxide absorption lean solution absorbing carbon dioxide When generate heat output.Specifically, the heat-exchanger rig 2014 can be a heat exchanger, in the carbon dioxide absorption tower 201 bottoms are equipped with heat exchanger, the heat output that generates when can be by absorbing carbon dioxide, to user's heat supply, improve heat energy utilization Rate.
As an example, the carbon dioxide capture system 200 further includes carbon dioxide absorbent solution regenerator 202, described Carbon dioxide absorbent solution regenerator 202 includes absorbing rich solution entrance 202a and absorbing lean solution to export 202b, and the carbon dioxide is inhaled Receiving tower 201 further includes absorbing lean solution entrance 201a and absorption rich solution outlet 201b, wherein the carbon dioxide absorbent solution regenerator 202 are connected with the carbon dioxide absorption tower 201, the absorption lean solution outlet of the carbon dioxide absorbent solution regenerator 202 202b is connected with the absorption lean solution entrance 201a of the carbon dioxide absorption tower 201, the carbon dioxide absorbent solution regenerator 202 absorption rich solution entrance 202a is connected with the absorption rich solution outlet 201b of the carbon dioxide absorption tower 201.
Specifically, in this example, also providing a carbon dioxide being connected with the carbon dioxide absorption tower 201 Regeneration of absorption solution tower 202, the carbon dioxide absorbent solution regenerator 202 can receive to be inhaled in the carbon dioxide absorption tower 201 Absorption rich solution after receiving carbon dioxide, and regenerate absorption rich solution sufficiently, so that the absorption become after regeneration is poor Liquid continues to supply the use of carbon dioxide absorption tower 201.Further, when including described in the carbon dioxide absorption tower 201 In the case where absorption tower spray equipment 2011 and the absorbing tower bottom 2013, the absorption of the carbon dioxide absorption tower 201 Lean solution entrance 201a is connected with the absorption tower spray equipment 2011, and the absorption rich solution of the carbon dioxide absorption tower 201 goes out Mouth 201b is connected with the absorbing tower bottom 2013.
In one example, the carbon dioxide absorbent solution regenerator 202 from bottom to top successively include regenerator tower bottom 2023, Regenerator packing layer 2022 and regenerator spray equipment 2021, it is rich that the regenerator tower bottom 2023 accommodates the carbon dioxide absorption The carbon dioxide absorption lean solution obtained after liquid regeneration, wherein the absorption of the carbon dioxide absorbent solution regenerator 202 Rich solution entrance 202a is connected with the regenerator spray equipment 2021, the carbon dioxide absorbent solution regenerator 202 it is described Lean solution outlet 202b is absorbed to be connected with the regenerator tower bottom 2023.
Specifically, in one example, the carbon dioxide absorbent solution regenerator 202 includes at least three parts, i.e. regenerator Tower bottom 2023, regenerator packing layer 2022 and regenerator spray equipment 2021, wherein the regenerator spray equipment 2021 connects Absorption rich solution outlet in 201 bottom of carbon dioxide absorption tower；At the middle part of the carbon dioxide absorbent solution regenerator 202 Equipped with the regenerator packing layer 2022, for regenerating absorption rich solution sufficiently；The carbon dioxide absorbent solution regenerator 202 bottoms are absorbing tower bottom 2023, and for accommodating the absorption lean solution after regenerating, the absorption lean solution is due to inhaling by regenerating It receives the gas concentration lwevel that contains of lean solution to substantially reduce, by pipeline by the institute of regenerator tower bottom 2023 and carbon dioxide absorption tower The connection of absorption tower spray equipment 2013 is stated, lean solution will be absorbed and sent into carbon dioxide absorption tower 201, can be re-used for absorbing dioxy Change carbon.
As an example, being also set up between the carbon dioxide absorption tower 201 and the carbon dioxide absorbent solution regenerator 202 There is absorbing liquid heat-exchanger rig 203, the absorbing liquid heat-exchanger rig 203 is set to the absorption rich solution outlet 201b and the absorption Rich solution entrance 202a and the lean solution that absorbs export on 202b and the pipeline absorbed between lean solution entrance 202a, so as to derive from The absorption rich solution that the carbon dioxide absorption tower 201 exports is exported with from the carbon dioxide absorbent solution regenerator 202 The absorption lean solution carry out heat exchange.
Specifically, as shown in Fig. 2, in the carbon dioxide absorption tower 201 and the carbon dioxide absorbent solution regenerator 202 Between be provided with absorbing liquid heat-exchanger rig 203, can be heat exchanger, for making the tower from carbon dioxide absorbent solution regenerator 202 The carbon dioxide absorbent solution and exchange heat from the carbon dioxide absorbent solution that 201 tower bottom of carbon dioxide absorption tower exports that bottom exports, Required heat when to reduce carbon dioxide absorbent solution regeneration.
As an example, the carbon dioxide capture system 200 further includes reboiler 204, and the reboiler 204 boils again Device entrance 204a and the liquid communication exported after the regenerator packing layer 2022, the reboiler 204 heat described The absorption lean solution in carbon dioxide absorbent solution regenerator carries out air lift to generate a large amount of vapor, and keeps described two Temperature in carbonoxide regeneration of absorption solution tower 202.
Specifically, in this example, one reboiler 204 is set in the bottom of the carbon dioxide absorbent solution regenerator 202, For heating the absorbent solution in regenerator tower bottom 2023, to generate a large amount of vapor for air lift, and carbon dioxide is kept Temperature in regeneration of absorption solution tower 202, thus regenerate carbon dioxide absorbent solution at high temperature, it is in one example, described The entrance of reboiler 204 is connected with the position of 2022 lower section of regenerator packing layer and 2023 top of the regenerator tower bottom Logical, the outlet of the reboiler 204 exports 202b with the absorption lean solution for being set to regenerator tower bottom and is connected.
As an example, the anode export 102b of battery pile 102 described in the electricity generation system passes through admission line simultaneously Be connected via the reboiler 204 with the trapping system entrance 200a of the carbon dioxide capture system 200, i.e., it is described Admission line is connect with the reboiler phase 204, and the anode exhaust gas exported from the anode export 102b boils again by described Enter the trapping system entrance 200a of the carbon dioxide capture system 200 after device 204 through piping.
Specifically, in this example, as shown in Fig. 2, the anode exhaust gas in the battery pile 102 is boiled via described again first Device 204, then the trapping system entrance 200a is entered by pipeline, when there are the carbon dioxide absorption tower, by described The anode exhaust gas of reboiler 204 enters the absorption tower air inlet of the carbon dioxide absorption tower 201, so as to be further ensured that The utilization of the energy of the anode exhaust gas generated in the battery pile 102 can provide energy for reboiler, realize the step benefit of energy With.
In addition, in one example, burning of the heat source required for the reboiler 204 in the burner 104 Anode exhaust gas waste heat in electrochemical reaction heat release, the battery pile 102 and institute in obvious heat of smoke, the battery pile 102 State battery pile 102 cathode exhaust gas waste heat (for the succinct purpose of drawing, only anode exhaust gas is passed into reboiler in figure, Indeed according to needs, cathode exhaust gas, which can also be first passed through after cathode preheater, to be entered back into reboiler and exchanges heat) at least One kind, i.e., the origin of heat heated in the described reboiler 204 can be any one in above-mentioned four, be also possible to above-mentioned The combination of any three in four or the combination of any the two either above-mentioned four are provided which heat, in this way, natural gas The thermal energy that chemical energy is converted is exported eventually by heat-exchanger rig 2014, guarantees the utilization of energy.
Further, in an optional example, between the reformer 101 and the battery pile 102 and the reboiler 204 The admission line be connected, wherein the anode exhaust gas exported in the anode export 102b via the reformer 101 and The reboiler 204 enters the trapping system entrance 200.
Specifically, in an optional example, when the anode export 102b passes through admission line and boils again via described When device 204 is connected with the trapping system entrance 200a, also set up a pipeline via the reformer 101, i.e., it is described The anode exhaust gas of anode export output can enter in the reformer 101, can provide heat for the reaction in reformer 101 The tail gas that the reformer 101 exports after being reacted in the reformer, then is imported into the reboiler 204 by amount Entrance enters in the reboiler 204.It can also be set on pipeline between the cell stack anode outlet and the reformer Regulating valve 403 is set, so as to realize the regulation to tail gas in the reformer is entered.Wherein, for going out from the anode The different demands of temperature can be arranged pipeline according to different components by the pipeline that mouth 102b is drawn, final realization energy Cascade utilization, because gross energy be it is constant, in this process according to different components to the temperature requirement of energy, the total amount of energy Demand takes series connection/front and back, parallel connection/shunting mode to energize, for example, the temperature of anode exhaust gas is there are about 600~700 DEG C, according to The all parts of composite system need the energy requirement of different temperatures by pipeline to different component heat supplies, such as reforming system 500 DEG C of heat, preheater need 200~300 DEG C of heat, and reboiler needs~200 DEG C of heat, and vaporizer needs~150 DEG C Heat, then the pipeline process of anode exhaust gas is arranged from high to low according to temperature, that is, from cell stack anode → reformer → Preheater → reboiler → vaporizer, certainly, also it is contemplated that identical temperature range using parallel port to distinct device simultaneously Heat supply is arranged according to actual demand.
As an example, the carbon dioxide capture system 200 further includes vapor condensing heat exchanger 205, the titanium dioxide Carbon absorption liquid regenerator 202 includes regenerator exhaust outlet 202c, and the regenerator exhaust outlet 202c is changed with vapor condensation The condensing heat exchanger entrance 205a of hot device 205 is connected.
Specifically, in one example, the carbon dioxide absorbent solution regenerator 202 includes regenerator exhaust outlet 202c, institute State the top that regenerator exhaust outlet 202c is preferably provided at the carbon dioxide absorbent solution regenerator 202, the regenerator exhaust Mouthful 202c is connected to the vapor condensing heat exchanger 205, wherein by pipeline by the suction of 201 bottom of carbon dioxide absorption tower It receives rich solution and is delivered to the regeneration that carbon dioxide absorbent solution regenerator 202 carries out absorbing liquid, after being regenerated, form gas and liquid Two-phase, wherein the main component of the gas is carbon dioxide and vapor, is exported from the regenerator exhaust outlet 202c, and supply Vapor condensing heat exchanger 205 should be given.
As an example, the carbon dioxide capture system 200 further includes gas-liquid separator 206, wherein the gas-liquid separation The separator inlet 206a of device 206 is connected with the condensing heat exchanger of the vapor condensing heat exchanger 205 outlet 205b.
Specifically, in one example, the carbon dioxide capture system 200 further includes a gas-liquid separator 206, wherein The vapor condensing heat exchanger 205 can be such that the water in mixed gas steams with the mixed gas of cooled carbon dioxide and vapor Gas is condensed into liquid water, and the gas-liquid separator 206 is connected to the vapor condensing heat exchanger 205 by pipeline, is used for Liquid water and carbon dioxide gas from vapor condensing heat exchanger 205 are separated, the liquid water of formation is stored in the gas-liquid In separator 206, the carbon dioxide gas isolated is exported, and can be recycled as needed.
Further, in one example, the solid oxide fuel cell composite system further includes water supply line 207, with Water needed for providing reforming reaction to the reformer, wherein point of the water supply line 207 and the gas-liquid separator 206 The vaporizer entrance 103a for exporting the vaporizer 103 in 206b and the electricity generation system 100 from device is connected, and described Water supply line 207 absorbs the heat production of the vapor condensing heat exchanger 205 via the vapor condensing heat exchanger 205.
Specifically, in one example, also setting up a water supply line 207, wherein the water supply line 207 and the vaporization The entrance of device 103 is connected, to provide water in the vaporizer 103, further, and in an optional example, the water supply line 207 are connected with the separator outlet 206b of the gas-liquid separator 206, and the isolated water of the gas-liquid separator 206 can be into One step is recycled in the vaporizer 103 of the electricity generation system 100 and is further utilized, furthermore it is also possible to by described Regulating valve 409 and flowmeter are set on the pipeline between gas-liquid separator 206 and the water supply line 207, pass through regulating valve 409 Control the circulating flow of cooling water.Furthermore it is preferred that the water supply line 207 is also via the vapor condensing heat exchanger 205, the part water supply line 207, i.e. the part water supply line 207 are equipped in the vapor condensing heat exchanger 205 The vapor condensing heat exchanger 205 can be passed through, water supply line described in the part can be vapor condensation cooling coil, described Flowing has heat transferring medium in cooling coil, is used as heat source to external heating after absorbing the condensation heat of mixed gas.In addition, as schemed Shown in 2, a condensation water channel 209 is also set up on the vapor condensing heat exchanger 205, the condensation water channel 209 can be with There is provided condensed water, to prevent vapor that cannot sufficiently be condensed, in addition, if can only with the condensed water in vapour liquid separator come Cool down to the mixture of CO2 and vapor, vapor is made to be condensed into water, depends primarily on the stream of water in water supply line 207 Amount and temperature control whether to open condensation water channel with temperature so as to the flow according to the water in the water supply line 207 209。
In addition, water pump can also be arranged on the water supply line 207, it is preferably provided at the vapor condensing heat exchanger On pipeline between 205 and the vaporizer 103, to be conducive to the supply for meeting the vaporizer 103.In the water supplying pipe Flowmeter and regulating valve 410 can be set in the entry position in road, to control the flow of the water of entrance.
As an example, the electricity generation system 100 further includes an at least anode preheating device 105, the anode preheating device The mode of action includes: that the connection of anode preheating device 105 is set between the vaporizer 103 and the reformer 101, In, the vapor in the vaporizer 103 is input to the reformation after being heated up via the anode preheating device 105 Device 101, the fuel gas in the feeder 300 are input to institute after being heated up via the anode preheating device 105 State reformer 101；Alternatively, the quantity of the anode preheating device 105 includes two, it is respectively arranged at the fuel feeder Between 300 and the reformer 101 between the vaporizer 103 and the reformer 101, the fuel is supplied fill respectively Gas of the output into the reformer 101 in 300 and the vaporizer 103 is set to be preheated.
Specifically, in one example, the electricity generation system 100 further includes anode preheating device 105, in a preferable example, It is preheated into the gas in the reformer 101 by the anode preheating device 105, when needing to the reformer 101 In when being passed through air, can be blower and air driven to initially enter the anode preheating device 105, entered back into after preheated described heavy In whole device 101, further, it is possible to which regulating valve 406 is arranged between blower and the anode preheating device 105, pass through regulating valve control System enters the flow of the air in reformer, in addition, can be in the anode preheating into the fuel gas in the reformer It is mixed in device with water vapour, air mixes in reformer with fuel gas, and the gas after mixing enters the reformer In, to be conducive to improve the stability to work in the reformer.
As an example, the electricity generation system 100 further includes cathode preheater 106, the cathode preheater 106 and the electricity The cathode inlet 102c of pond heap 102 is connected, and air is heated up into the cathode via the cathode preheater 106 Mouth 102c.
As an example, the cathode outlet 102d of the battery pile 102 is also via the cathode preheater 106 and the burning Device 104 is connected.
Specifically, in one example, cathode preheater 106, the cathode preheater are arranged in the electricity generation system 100 106 can be such as arranged between blower and the battery pile 102 to heat into the gas of 102 cathode of battery pile, and blower drives Air enter the battery pile cathode, further, it is possible between blower and the battery pile 102 be arranged regulating valve 405 and Flowmeter enters the flow of the air in reformer by regulating valve control.
In addition, cathode outlet 102d and 104 phase of burner in a preferable example, also through the battery pile 102 Connection, is input to burner for the cathode exhaust gas of the battery pile 102 and is recycled, it is further preferred that the yin Pole tail gas is input in the burner 104 after being heated via the cathode preheater 106 and is utilized.
As an example, the electricity generation system 100 further includes air supply arrangement 107, the air supply arrangement be can be Blower, the air supply arrangement 107 are preheated with the burner 104, the anode preheating device 105 and the cathode respectively Device 106 is connected, and air is separately input into the burner 104, the anode preheating device 105 and the cathode and is preheated Device 106.
Specifically, an air supply arrangement 107 is also set up in the electricity generation system 100 in the example, such as air Supply arrangement can be blower, and the air supply arrangement 107 can be for needing the ground of air in the entire electricity generation system 100 Side uses, i.e., multiple components for needing air share the air supply arrangement 107, so as to simplify the complexity of system, Saving system is taken up space, in addition, regulating valve can also be arranged between the air supply arrangement 107 and the burner 104 404 and flowmeter, enter flow so as to adjust air.
As an example, the trapping system outlet 200b of the carbon dioxide capture system 200 and the electricity generation system It is additionally provided with air pump 208 on pipeline between 100, is further additionally provided with flowmeter.
Specifically, the trapping system outlet 200b of the carbon dioxide capture system 200 and the electricity generation system 100 Between pipeline can be the trapping system outlet 200b and reformer in carbon dioxide capture system in one example On pipeline between 101 and trapping system outlet 200b and the burner 104, that is, can be and caught close to described The air pump 208 is arranged in the position that collecting system exports 200b, then after the air pump 208, pipeline is respectively communicated to described Reformer 101 and the burner 104, then regulating valve 408 is set on the pipeline of the air pump 208 and the burner 104 And flowmeter, regulating valve 407 is set on the pipeline of the air pump 208 and the reformer 101, passes through the opening and closing control of regulating valve Gas flow processed, wherein the air pump 208 ensure that circulating for anode exhaust gas, provide circulation power.
It should be further noted that the present invention passes through combustor burns fuel gas (such as CH4) caused by level-one flue gas Heat is provided, is maintained for hot-zone C heating starting and constant temperature, burner combustion CH4Generated secondary smoke provides heat for sun Pole preheater and vaporizer etc., so that the preheating of anode reduction, gas and steam gasification.After reformer and battery pile starting, By the recycling to combustible component in anode exhaust gas, the fuel availability of SOFC electricity generation system is increased substantially.Due to right Fuel chemical energy makes full use of, on the one hand, the CH to burn needed for burner4Amount can sharp fall, or even only by burn Combustible component in segment anode tail gas can maintain the constant temperature of SOFC electricity generation system hot-zone；On the other hand, it makes full use of slightly lower In the high-grade waste heat energy of battery pile, the temperature of reformer, to drive the trapping process for realizing carbon dioxide.During this, The reaction heat that chemical energy is converted is not consumed, and is only converted into the low temperature heat energy of grade reduction, the low temperature heat energy Temperature is higher than heat supply temperature, thus low energy consumption, even zero energy consumption dioxy may be implemented by recycling low temperature heat energy progress heat supply Change carbon capture.Simultaneously as the vapor dew point of electrochemical reaction product gas is very high, thus the vapor of system tail gas is latent Heat, generation water can recycle completely, and the efficiency of whole system can increase substantially, and water consumption can be close in zero.
In addition, the present invention also provides a kind of application method of solid oxide fuel cell composite system, the user Method is comprising steps of provide solid oxide fuel cell composite system as described in any one of above scheme, and to the confession It is passed through the fuel gas in device of air, converts electric energy for the chemical energy of the fuel gas, and at least recycling generates in product Carbon dioxide.
Specifically, the present invention also provides a kind of application methods of solid oxide fuel cell composite system, in an example In, it is CH with the fuel gas4For (natural gas), in the electricity generation system 100, CH4(natural gas) is from the feeder 300 are directly entered in SOFC electricity generation system air inlet pipeline from natural gas line by desulfurization process；
In the electricity generation system 100 starting, can be controlled respectively by pressure gauge and flowmeter into the burning The CH of device 1044Flow, wherein in the burner 104, controlled by pressure gauge, fuel control valve 303 and flowmeter Make the CH entered4Flow, while controlling by blower, air control valve 401 and flowmeter the flow of air, make burner stable Fixed burning；After the burner 104 starting, the fuel gas (CH4) chemical energy can continued shift be thermal energy, pass through flue gas The reformer 101, the anode preheating device 105, the cathode preheater 106 and institute are heated in flowing in exhaust gases passes Vaporizer 103 is stated, target temperature is made up to, can also provide energy for the carbon dioxide capture system, wherein in hot-zone C Temperature-rise period in, can be according to the target temperature of practical heating rate and steady operation, the CH being adjusted into the burner4 With the flow of air.
After above-mentioned component reaches the target temperature of steady operation, in one example, continue to be passed through to the reformer 101 H2, then H2It is also entered by pipeline in the battery pile 102, it is therefore an objective under the high temperature conditions by catalyst in reformer 101 W metal is reduced to the nickel oxide in battery pile 102 in the anode of SOFC monocell.Catalyst and battery in device 101 to be reformed After the nickel oxide of SOFC anode is reduced sufficiently in heap 102, it is passed through a certain amount of water into the vaporizer 103, and close H2, Water is converted into vapor by the vaporizer 103, and vapor enters in reformer 101, opens fuel control valve 402, presses CH is imported to reformer according to certain steam/hydrocarbons ratio of reaction requirement4, on the other hand, pass through the blower 107, air control valve 405 and the air of flowmeter control certain flow enter the cathode preheater 106, and enter further into the battery pile 102 cathode, work off one's feeling vent one's spleen (such as CO, H of the reformer 101 being heated2、CO2And CH4、H2O), air respectively enters electricity The anode and cathode of pond heap 102 heat battery pile 102, battery pile are made also to reach target temperature.
Wherein, in a preferable example, during above-mentioned hot-zone C starting, in order to make up 101 energy of reformer Insufficient situation and the heating rate deficiency ramp case for accelerating hot-zone C, at this point, can by the anode preheating device 105 to It is passed through a certain amount of air in reformer, passes through CH4Partial oxidation reaction energy is provided, carry out above-mentioned reaction equation (1) and (2).Wherein, in a preferable example, in the reformer 101, CH4、H2The flow of O and air is adjusted in following ratio: water carbon Than controlling between 0~2, carbon ratio is controlled between 0~1, and the reforming process carried out in the reformer 101 includes reaction equation (3), the CH of (4)4The oxidation reaction and reaction of (natural gas) steam reforming reaction, reaction equation (1), (2) CH4 (natural gas) The CO conversion reaction of formula (5)；Wherein, CH4Reforming reaction occurs with vapor and oxygen in reformer 101, generates H2、CO、 CO2And unreacted CH4、H2O and N2Mixed gas, above-mentioned gas forms working off one's feeling vent one's spleen for reformer 101 described in the example Body.Reaction temperature section in usual reformer is at 300~600 DEG C or so, and in one example, Metabolic weight C temperature meets target After temperature, the air being passed through in anode preheating device 105 is gradually decreased, flows into anode preheating device until completely closing as needed 105 air duct.
Further, 101 exit gas of reformer reaches battery pile, battery pile, 102 cathode gas (sky through high temperature conduit Gas) enter cathode preheater after blower and flowmeter, and enter battery pile 102 after being preheated to 200~500 DEG C, to yin, yang After pole gas enters battery pile, electrochemical reaction occurs under the conditions of 600~1000 DEG C, by chemical energy be converted into electric energy to Family power supply.In addition, emptying after the cathode exhaust gas of battery pile 102 enters residual neat recovering system, the thermal energy of cathode exhaust gas is available Come preheating cathode inlet gas, anode inlet gas, heating water to form vapor etc., can also be answered according to the temperature condition of waste heat System is filled for collecting carbonic anhydride.Demand according to system to energy and energy grade can successively pass through reformer 101, again Device 204 is boiled to provide high-grade thermal energy, and two in carbon dioxide capture system are then entered by trapping system entrance 200b Carbonoxide absorption tower 201, for absorbing, trapping carbon dioxide whole in the anode exhaust gas of battery pile.
In addition, the anode and cathode tail gas that 102d comes out from 102 anode and cathode of battery pile outlet is final in a preferable example The burner 104 is fully entered, under control of the control system, with combustor inlet CH4, air be mixed and burned, release heat Amount is further to heat entire SOFC electricity generation system.
By above-mentioned steps, (usually in 700~1000 DEG C of ranges after 102 temperature of battery pile reaches target temperature It is interior), 101 exit gas of reformer into 102 anode of battery pile and the air into 102 cathode of battery pile are in electricity Electrochemical reaction occurs in pond heap 102, the chemical energy of fuel is converted into electric energy, and with the raising of fuel availability, turn The electric energy of change is also gradually increased；In addition as the increase for the fuel gas flow being passed through is along with heat caused by electrochemical reaction Amount is also gradually increased, outside the temperature that the energy can not only maintain battery pile 102 to work normally, it may also be used for heated reformate device etc. Other components.In one example, the anode exhaust gas gas of the high temperature of the battery pile 102 initially enters the reformer 101, will High temperature energy passes to reforming reactants, and reforming reaction is promoted to carry out.At this point, the reforming process carried out in reformer includes CH4 (natural gas) steam reforming reaction and CO conversion reaction；And 101 exit gas of reformer includes CO, H2、CO2And CH4、 H2The complete gas of the unreacteds such as O reaches battery pile 100 through high temperature conduit, wherein described heavy when SOFC normal table is run The energy requirement of whole device 101 high temperature heat, burner 104 brought by the anode exhaust gas is burnt CH4Heat production and electricity The high temperature heat that heap 102 electrochemical reaction in pond is released, at this point, the reformer 101, the burner 104 and the battery pile 102 can form an entirety in structure, to promote heat transfer effect.
When SOFC electricity generation system enters stable operation process, due to the electrochemical reaction carried out in the battery pile 102 The energy that process is released, which has been approached/is enough, realizes that the temperature of hot-zone C is constant, and burner 104 can not need burning CH at this time4, The anode exhaust gas and cathode exhaust gas that combustion parts are passed through, wherein contain the unreacted oxygen in part, ratio in cathode exhaust gas Exactly corresponding to the combustible component of anode exhaust gas, i.e. air-fuel ratio is just right, therefore cathode exhaust gas is passed through burner, the purpose is to The high temperature energy of cathode exhaust gas is made full use of, at this time the burning of burner, not only sufficiently fires the flammable tail gas in anode exhaust gas It burns, also the further chemical energy of release combustible component, makes up in system BOP system to the total amount and grade demand of energy.
In one example, when SOFC electricity generation system enters stable operation process, the anode tail of the battery pile 102 Gas can adjust the flow for respectively enteing the reboiler 204 of reformer 101 and carbon dioxide capture system 200 as needed, Flow as described in can be controlled and be entered by regulating valve 403 in reformer 101, in this example, the anode exhaust gas is first Into reformer 200, will most high-grade energy transmission to reforming reaction, subsequently into carbon dioxide capture system reboiler 204, by the energy transmission of secondary level-one to reboiler 204, in addition, the heat source of the reboiler 204 can also be generated electricity using SOFC Heat release in the combustion product gases sensible heat of the burner 104 of system, the electrochemical process of the battery pile 102, for The absorbent solution in carbon dioxide absorbent solution regenerator tower bottom 202 is heated, to generate a large amount of vapor for air lift, and is kept Temperature in carbon dioxide absorbent solution regenerator 202, so that carbon dioxide absorbent solution be made to be regenerated at high temperature.In an example In, reboiler uses combustion product gases sensible heat, the heat release in battery pile electrochemical process and the anode and cathode tail of SOFC electricity generation system The waste heat of gas provides heat source and is heated, in this way, the thermal energy that the chemical energy of natural gas is converted is defeated eventually by heat exchanger 2014 Out.
In addition, entering the trapping system entrance of carbon dioxide absorption tower 201 from the anode exhaust gas that the reboiler 204 comes out 200a (absorption tower air supply opening), completes CO in carbon dioxide absorption tower 2012And after the removing of water, exported from trapping system 200b (absorption tower exhaust outlet) comes out, and further, under the control of the air pump 208 and flowmeter, residual gas is transported to In the electricity generation system 100, in one example, according to the energy requirement of SOFC electricity generation system (the i.e. described electricity generation system 100), The 104 anode exhaust gas inlet adjusting valve 408 of burner, 101 anode exhaust gas inlet adjusting valve 407 of the reformer and flow Under the collective effect of meter, the anode exhaust gas flow for entering burner 104, anode preheating device 105 is adjusted respectively.In one example, It is entered anode preheating device and then enters the anode exhaust gas ratio of reformer and be generally 0~90%, preferably 0~80%, press The total volume meter of anode exhaust gas.
Under the conditions of SOFC electricity generation system stable operation, by by the carbon dioxide capture system 200 also based on institute It states vapor condensing heat exchanger 205 and the gas-liquid separator 206 is completed to the condensation for generating water in the anode exhaust gas Recycling, thus at this time in the reformer 101 vapor needed for reforming reaction also can be recycled recycling condensed water, condensation Water supplies SOFC electricity generation system by water pump, by the Low Temperature Thermal in absorbing carbon dioxide trapping system, such as steams in the water Low temperature heat absorption is carried out in gas condensing heat exchanger 205 by way of cooling coil, wherein the mesh of absorption condensation heat here , it is to try to first promote the temperature of condensed water, to reduce the heat demand in vaporizer, further, due to by condensed water Temperature, flow restriction can be with if the tail gas (CO2+ vapor) that fruit cannot lean on sufficiently heat absorption and export regenerator is fully cooled It is cooling by 209 further progress of cooling-water duct, and the low temperature in vaporizer 103 in absorption SOFC electricity generation system Heat is evaporated to vapor, after mixing in anode preheating device 105 with fuel, eventually enters into reformer 101.
Under the conditions of SOFC electricity generation system stable operation, the cathode exhaust gas by battery pile 102 can enter yin by pipeline Pole preheater 106, the demand according to SOFC electricity generation system to energy, in conjunction with reformer 101, anode preheating device 105, vaporizer 103, waste heat recycling is realized to form vapor etc. by preheating cathode inlet gas, anode inlet gas, heating water, according to remaining The temperature condition of heat applies also for carbon dioxide capture device, finally empties to outside system.In addition, steady in SOFC electricity generation system Determine under service condition, fuel chemical energy is converted into the part of thermal energy other than being converted into electric energy, and a part passes through reforming reaction again Secondary to be applied in SOFC system, another part thermal energy is used as driving force in carbon dioxide capture system 200, realizes dioxy Change the trapping process of carbon, during this, the reaction heat that chemical energy is converted is not consumed, and is only converted into grade drop Low low temperature heat energy, the temperature of the low temperature heat energy are higher than the heat supply temperature of domestic heating system, can still pass through heat exchanger 2014 Outward supplying heat.
It should be further noted that the present invention passes through combustor burns fuel gas (such as CH4) caused by level-one flue gas Heat is provided, is maintained for hot-zone heating starting and constant temperature, burner combustion CH4Generated secondary smoke provides heat for anode Preheater and vaporizer, so that the preheating of anode reduction, gas and steam gasification.After reformer and battery pile starting, pass through Recycling to combustible component in anode exhaust gas increases substantially the fuel availability of SOFC electricity generation system.Due to fuel Chemical energy makes full use of, on the one hand, the CH to burn needed for burner4Amount can sharp fall, or even only lean on combustion parts Combustible component in anode exhaust gas can maintain the constant temperature of SOFC electricity generation system hot-zone；On the other hand, it makes full use of slightly less than electric The high-grade waste heat energy of the temperature of Chi Dui, reformer, to drive the trapping process for realizing carbon dioxide.During this, chemistry The reaction heat that can be converted is not consumed, and is only converted into the low temperature heat energy of grade reduction, the temperature of the low temperature heat energy Higher than the heat supply temperature of domestic heating system, thus heat supply is carried out by recycling the low temperature heat energy, low energy consumption, even may be implemented Zero energy consumption collecting carbonic anhydride.Simultaneously as the vapor dew point of electrochemical reaction product gas is very high, thus system tail gas Vapor latent heat, generate water can recycle completely, the efficiency of whole system can increase substantially, and water consumption can be close in Zero.
In conclusion the present invention provides a kind of solid oxide fuel cell composite system and application method, the solid Oxide fuel cell composite system includes electricity generation system and carbon dioxide capture system, in which: the electricity generation system includes weight Whole device, battery pile, vaporizer and burner, in which: the reformer first input end of the reformer is connected with feeder Logical, the second input terminal of reformer is connected with the vaporizer, and the first output end of reformer is connected with the battery pile, described Reforming reaction, and institute are carried out based on the vapor in the fuel gas and the vaporizer in the feeder inside reformer The gas after reforming internal-response is stated to export to the anode inlet of the battery pile；The burner first input end of the burner It is connected with the feeder, the second input terminal of burner and contact air, the burner internal are based on the gas supply It the fuel gas in device and is reacted from the air that second input terminal of burner inputs and generates thermal energy；It is described Carbon dioxide capture system includes trapping system entrance and trapping system outlet, wherein the trapping system entrance and the hair The anode export of battery pile described in electric system is connected, the trapping system outlet and the reformation in the electricity generation system At least one of device and the burner are connected.Through the above scheme, solid oxide fuel cell of the invention is compound System not only passes through combustible component in split cell heap anode exhaust gas and combustion products CO2 and water, thus realize it is flammable at The abundant recycling divided；It is driven simultaneously by making full use of the high-grade thermal energy of fuel gas, in low energy consumption even zero energy consumption On the basis of, it can also realize the trapping recycling of carbon dioxide；To make entirely to utilize the SOFC electricity generation system of fossil fuel not Only reach the purpose of efficiency power generation, moreover it is possible to realize the purpose of carbon dioxide near-zero release.So the present invention effectively overcome it is existing Various shortcoming in technology and have high industrial utilization value.
The above-described embodiments merely illustrate the principles and effects of the present invention, and is not intended to limit the present invention.It is any ripe The personage for knowing this technology all without departing from the spirit and scope of the present invention, carries out modifications and changes to above-described embodiment.Cause This, institute is complete without departing from the spirit and technical ideas disclosed in the present invention by those of ordinary skill in the art such as At all equivalent modifications or change, should be covered by the claims of the present invention.

Claims (21)

1. a kind of solid oxide fuel cell composite system, which is characterized in that the compound system of solid oxide fuel cell System includes electricity generation system and carbon dioxide capture system, in which:
The electricity generation system includes reformer, battery pile, vaporizer and burner, in which:
The reformer first input end of the reformer is connected with fuel feeder, the second input terminal of reformer and the vapour Change device to be connected, the first output end of reformer is connected with the battery pile, and the feeder is based on inside the reformer In fuel gas and the vaporizer in vapor carry out reforming reaction, and the gas reformed after internal-response is from institute The first output end of reformer is stated to export to the anode inlet of the battery pile；
The burner first input end of the burner is connected with the fuel feeder, the second input terminal of burner and sky Gas phase connection, combustible component of the burner internal based on the fuel gas, recycling in the feeder and from institute The air for stating the input of the second input terminal of burner is reacted and generates thermal energy；
The carbon dioxide capture system includes trapping system entrance and trapping system outlet, wherein the trapping system entrance It is connected with the anode export of battery pile described in the electricity generation system, the trapping system outlet is selected from and the burner At least one of be connected, be connected and directly empty with the reformer.
2. solid oxide fuel cell composite system according to claim 1, which is characterized in that the burner also wraps The first output end of burner is included, first output end of burner is successively caught via the reformer, the vaporizer with described Collecting system entrance is connected, and the combustion tail gas generated in the burner is input in the carbon dioxide capture system.
3. solid oxide fuel cell composite system according to claim 1, which is characterized in that the carbon dioxide is caught Collecting system includes carbon dioxide absorption tower, and the carbon dioxide absorption tower includes absorption tower air supply opening and absorption tower exhaust outlet, In, the absorption tower air supply opening is exported as the trapping system entrance, the absorption tower exhaust outlet as the trapping system.
4. solid oxide fuel cell composite system according to claim 3, which is characterized in that the carbon dioxide is inhaled Receive tower successively includes absorbing tower bottom, absorption tower packing layer and absorption tower spray equipment from bottom to top, and the absorption tower supplies Mouth is set to the lower section of described filler layer, wherein the absorption tower spray equipment is described for spraying carbon dioxide absorption lean solution Absorbing tower bottom accommodates the carbon dioxide rich solution formed after the carbon dioxide absorption lean solution absorbing carbon dioxide.
5. solid oxide fuel cell composite system according to claim 4, which is characterized in that the carbon dioxide is inhaled Receiving tower further includes absorption tower heat-exchanger rig, and the absorption tower heat-exchanger rig is set to the bottom at the absorbing tower bottom, the suction The heat output generated when receiving tower heat-exchanger rig for the carbon dioxide absorption lean solution absorbing carbon dioxide.
6. solid oxide fuel cell composite system according to claim 3, which is characterized in that the carbon dioxide is caught Collecting system further includes carbon dioxide absorbent solution regenerator, and the carbon dioxide absorbent solution regenerator includes absorbing rich solution entrance and suction Lean solution outlet is received, the carbon dioxide absorption tower further includes absorbing lean solution entrance and absorption rich solution outlet, wherein the titanium dioxide The absorption lean solution outlet of carbon absorption liquid regenerator is connected with the absorption lean solution entrance of the carbon dioxide absorption tower, the dioxy The absorption rich solution outlet for changing carbon absorption tower is connected with the absorption rich solution entrance of the carbon dioxide absorbent solution regenerator.
7. solid oxide fuel cell composite system according to claim 6, which is characterized in that the carbon dioxide is inhaled Receive liquid regenerator successively includes regenerator tower bottom, regenerator packing layer and regenerator spray equipment, the regenerator from bottom to top Tower bottom accommodates the carbon dioxide absorption lean solution obtained after the carbon dioxide absorption rich solution regeneration, wherein the titanium dioxide The absorption rich solution entrance of carbon absorption liquid regenerator is connected with the regenerator spray equipment, the carbon dioxide absorbent solution The absorption lean solution outlet of regenerator is connected with the regenerator tower bottom.
8. solid oxide fuel cell composite system according to claim 6, which is characterized in that the carbon dioxide is inhaled It receives and is additionally provided with absorbing liquid heat-exchanger rig between tower and the carbon dioxide absorbent solution regenerator, the absorbing liquid heat-exchanger rig is set Be placed in the absorption rich solution outlet and the absorptions rich solution entrance and the absorption lean solution export and the absorption lean solution entrance it Between pipeline on so that derive from the absorption rich solution of carbon dioxide absorption tower output with from the carbon dioxide absorption The absorption lean solution of liquid regenerator output carries out heat exchange.
9. solid oxide fuel cell composite system according to claim 6, which is characterized in that the carbon dioxide is caught Collecting system further includes reboiler, the reboiler entrance of the reboiler and the liquid phase exported after the regenerator packing layer Connection, the reboiler heat the absorption lean solution in the carbon dioxide absorbent solution regenerator, are steamed with generating a large amount of water Gas carries out air lift, and keeps the temperature in the carbon dioxide absorbent solution regenerator.
10. solid oxide fuel cell composite system according to claim 9, which is characterized in that the electricity generation system Described in the anode export of battery pile be connected by admission line with the reboiler, and exported from the anode export Anode exhaust gas the trapping system of the carbon dioxide capture system is eventually entered into through piping after the reboiler Entrance.
11. solid oxide fuel cell composite system according to claim 10, which is characterized in that the reformer with The admission line between the battery pile and the reboiler is connected, wherein what is exported in the anode export is described Anode exhaust gas enters the trapping system entrance via the reformer and the reboiler.
12. solid oxide fuel cell composite system according to claim 6, which is characterized in that the carbon dioxide Trapping system further includes vapor condensing heat exchanger, and the carbon dioxide absorbent solution regenerator includes regenerator exhaust outlet, wherein The regenerator exhaust outlet is connected with the condensing heat exchanger entrance of the vapor condensing heat exchanger.
13. solid oxide fuel cell composite system according to claim 12, which is characterized in that the carbon dioxide Trapping system further includes gas-liquid separator, wherein the separator inlet of the gas-liquid separator and the vapor condensing heat-exchange The condensing heat exchanger outlet of device is connected.
14. solid oxide fuel cell composite system according to claim 13, which is characterized in that the solid oxidation Object fuel cell composite system further includes water supply line, with to the reformer provide reforming reaction needed for water, wherein it is described The vaporizer of water supply line and the vaporizer in the separator outlet of the gas-liquid separator and the electricity generation system enters Mouthful it is connected, and the water supply line is via the vapor condensing heat exchanger, to absorb the vapor condensing heat exchanger Condensation heat.
15. solid oxide fuel cell composite system according to claim 1, which is characterized in that the electricity generation system It further include an at least anode preheating device, the mode of action of the anode preheating device includes: the anode preheating device connection setting Between the vaporizer and the reformer, wherein the vapor in the vaporizer is via the anode preheating device It is input to the reformer, the fuel gas in the feeder is input to the reformation via the anode preheating device Device, alternatively, the quantity of the anode preheating device includes two, be respectively arranged at the fuel feeder and the reformer it Between between the vaporizer and the reformer, respectively to output in the fuel feeder and the vaporizer to described Gas in reformer is preheated.
16. solid oxide fuel cell composite system according to claim 15, which is characterized in that the electricity generation system It further include cathode preheater, the cathode preheater is connected with the cathode inlet of the battery pile, and air is via the cathode Preheater enters the cathode inlet；The cathode outlet of the battery pile is also via the cathode preheater and the burner phase Connection.
17. solid oxide fuel cell composite system according to claim 16, which is characterized in that the electricity generation system Further include air supply arrangement, the air supply arrangement respectively with the burner, the anode preheating device and the yin Pole preheater is connected, and air is separately input into the burner, the anode preheating device and the cathode preheater.
18. solid oxide fuel cell composite system according to claim 15, which is characterized in that the anode preheating Device is connected with blower, and air is input to the reformer via the anode preheating device so that in the reformer into Row oxidation reaction, the oxidation reaction include:
Partial oxidation reaction of methane:
CH4(g)+3/2O2(g)→CO(g)+2H2O(g)ΔH298 0=-519kJ/mol (2)
19. solid oxide fuel cell composite system according to claim 18, which is characterized in that described in control enters The mode of the flow of the fuel gas, the vapor and the air in reformer includes: in the control reformer Steam/hydrocarbons ratio between 0-3, carbon ratio is between 0-2.
20. solid oxide fuel cell composite system described in any one of -19 according to claim 1, which is characterized in that Be additionally provided with reducing gas intake line on the reformer, the reducing gas intake line successively to the reformer and It is passed through reducing gas in the battery pile, to restore the sun of the catalyst in the reformer and the monocell in the battery pile Pole material；The trapping system of the carbon dioxide capture system is exported to be also set up on the pipeline between the electricity generation system There is air pump.
21. a kind of application method of solid oxide fuel cell composite system, which is characterized in that the application method includes step It is rapid: to provide solid oxide fuel cell composite system as described in any one of claim 1-20, and to the fuel It is passed through the fuel gas in feeder, converts electric energy for the chemical energy of the fuel gas, and at least recycling generates product In carbon dioxide.
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CN114976151A (en) * 2022-07-13 2022-08-30 浙江浙能技术研究院有限公司 System multi-physical-domain simulation method considering heat transfer among hot-zone components
CN114976151B (en) * 2022-07-13 2024-04-02 浙江浙能技术研究院有限公司 System multi-physical-domain simulation method considering heat transfer among hot-zone components
CN116544449A (en) * 2023-07-03 2023-08-04 磐动(浙江)电气科技有限公司 Low-carbon-emission fuel cell system and heat management method
CN116544449B (en) * 2023-07-03 2023-09-15 磐动(浙江)电气科技有限公司 Low-carbon-emission fuel cell system and heat management method
CN116808785A (en) * 2023-08-30 2023-09-29 山东保蓝环保有限公司 High-efficiency carbon capturing and energy-saving regeneration device based on biphasic ion solution
CN116808785B (en) * 2023-08-30 2024-01-05 山东保蓝环保有限公司 High-efficiency carbon capturing and energy-saving regeneration device based on biphasic ion solution

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