CN114744264B - Multi-combined supply system based on biomass gasification and solid oxide fuel cell - Google Patents
Multi-combined supply system based on biomass gasification and solid oxide fuel cell Download PDFInfo
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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
- H01M8/10—Fuel cells with solid electrolytes
- H01M8/12—Fuel cells with solid electrolytes operating at high temperature, e.g. with stabilised ZrO2 electrolyte
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K25/00—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for
- F01K25/08—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours
- F01K25/10—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours the vapours being cold, e.g. ammonia, carbon dioxide, ether
- F01K25/103—Carbon dioxide
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B33/00—Steam-generation plants, e.g. comprising steam boilers of different types in mutual association
- F22B33/18—Combinations of steam boilers with other apparatus
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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
- H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
- H01M8/04007—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids related to heat exchange
- H01M8/04014—Heat exchange using gaseous fluids; Heat exchange by combustion of reactants
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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
- H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
- H01M8/04007—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids related to heat exchange
- H01M8/04067—Heat exchange or temperature measuring elements, thermal insulation, e.g. heat pipes, heat pumps, fins
- H01M8/04074—Heat exchange unit structures specially adapted for fuel cell
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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
- H01M8/0662—Treatment of gaseous reactants or gaseous residues, e.g. cleaning
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0916—Biomass
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- 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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Abstract
The application relates to a multi-combined supply system based on biomass gasification and a solid oxide fuel cell, which comprises a gasification furnace, the solid oxide fuel cell, a second air heat exchanger and a fourth heat exchanger, wherein an anode tail gas outlet of the solid oxide fuel cell is sequentially connected with the fourth heat exchanger and the gasification furnace, the gasification furnace is provided with a biomass inlet, a synthesis gas outlet of the gasification furnace is connected with the second air heat exchanger, and a synthesis gas outlet of the air heat exchanger is connected with an anode inlet of the solid oxide fuel cell; the cathode tail gas outlet of the solid oxide fuel cell is sequentially connected with the fourth heat exchanger and the gasification furnace, and the cathode tail gas outlet of the gasification furnace is sequentially connected with the supercritical carbon dioxide recompression power circulation system and the kalina circulation system. Solves the clean and efficient energy conversion problem. The full recycling of the waste heat of the flue gas is realized.
Description
Technical Field
The application belongs to the technical field of metal material preparation, and particularly relates to a multi-combined supply system based on biomass gasification and a solid oxide fuel cell.
Background
The disclosure of this background section is only intended to increase the understanding of the general background of the application and is not necessarily to be construed as an admission or any form of suggestion that this information forms the prior art already known to those of ordinary skill in the art.
With the rapid development of socioeconomic performance, humans are consuming a large amount of fossil energy such as coal and petroleum at a high speed. However, fossil energy is not renewable, and with the increasing consumption, fossil energy has become a scarce energy source, and the cost of developing and using fossil energy has increased. Therefore, the need for efficient, low-cost, clean energy conversion technologies using renewable energy as fuel is a major problem that is urgently needed to be solved in countries around the world.
The solid oxide fuel cell is a high-efficiency power generation device for directly converting chemical energy of fuel into electric energy, and has high energy conversion efficiency because the device is not limited by Carnot cycle, and the reaction product is mainly H 2 O and CO 2 And H is 2 O has no pollution, CO 2 Is also much lower than the common method, and is a clean energy source in the true sense.
Biomass is a renewable energy source, and biomass and a solid oxide fuel cell are used for generating electricity, but clean and efficient energy conversion is not realized.
Disclosure of Invention
In view of the above problems in the prior art, it is an object of the present application to provide a multi-combined supply system based on biomass gasification and solid oxide fuel cells.
In order to solve the technical problems, the technical scheme of the application is as follows:
a multi-combined supply system based on biomass gasification and a solid oxide fuel cell comprises a gasification furnace, the solid oxide fuel cell, a second air heat exchanger and a fourth heat exchanger, wherein an anode tail gas outlet of the solid oxide fuel cell is sequentially connected with the fourth heat exchanger and the gasification furnace, the gasification furnace is provided with a biomass inlet, a synthesis gas outlet of the gasification furnace is connected with the second air heat exchanger, and a synthesis gas outlet of the air heat exchanger is connected with an anode inlet of the solid oxide fuel cell;
the cathode tail gas outlet of the solid oxide fuel cell is sequentially connected with the fourth heat exchanger and the gasification furnace, and the cathode tail gas outlet of the gasification furnace is sequentially connected with the supercritical carbon dioxide recompression power circulation system and the kalina circulation system.
The application relates to a multi-combined supply system based on biomass gasification and a solid oxide fuel cell, wherein the biomass gasification system is combined with the solid oxide fuel cell system, and the anode exhaust gas of the solid oxide fuel cell system enters the gasification system to be used as biomass gasification to provide gasifying agent, and the synthetic gas obtained by biomass is used as fuel of the anode of the solid oxide fuel cell system to realize effective utilization of biomass as renewable energy; meanwhile, cathode gas waste heat obtained by the solid oxide fuel cell is effectively utilized through a supercritical carbon dioxide recompression power circulation system and a kalina circulation system, so that the system efficiency is improved; and fully recovering waste heat through the second air heat exchanger and the fourth heat exchanger.
One or more of the technical schemes of the application has the following beneficial effects:
the biomass gasification system and the solid oxide fuel cell system are combined, so that full utilization of renewable energy sources of biomass is realized, and meanwhile, the chemical energy of the solid oxide fuel cell is fully utilized to be converted into electric energy for high-efficiency utilization, and the clean and high-efficiency energy conversion problem is solved.
Through the reasonable arrangement of the heat exchangers (AH 1, AH2, AH3 and AH 4), the full recycling of the waste heat of the flue gas is realized, the power generation efficiency and the combined supply efficiency of the system are improved to a greater extent, the cascade utilization of heat is realized, and the carbon dioxide trapping is facilitated.
The exhaust of the anode tail gas of the SOFC and the oxygen are burnt and are divided into two parts, and one part of the exhaust is used as a gasifying agent to be sent into the gasifier to fully react with biomass, so that the effect of using the exhaust of the anode tail gas as the gasifying agent is realized, and part of heat is provided for the reaction in the gasifier.
The top circulation SOFC system, the supercritical carbon dioxide recompression power circulation system and the kalina circulation system are combined to realize further deep recycling of exhaust gas, so that the whole system has a function of power and heat combined supply, meanwhile, near zero emission of carbon dioxide can be realized, and the efficiency of the whole system is further improved.
Drawings
The accompanying drawings, which are included to provide a further understanding of the application and are incorporated in and constitute a part of this specification, illustrate embodiments of the application and together with the description serve to explain the application.
FIG. 1 is a diagram of a multi-gang supply system based on biomass gasification and solid oxide fuel cells;
wherein, 1, air, 2-compressed air; 3-first preheated air; 4-second preheated air; 5-third preheated air; 6-cathode mixed gas; 7-cathode tail gas; 8-heating cathode tail gas; 9-first cooling cathode tail gas; 10-second cooling cathode tail gas; 11-third cooling cathode tail gas; 12-fourth cooling cathode tail gas; 13-first venting to atmosphere; 14-biomass; 15-synthesis gas; 16-nitrogen; 17-fuel gas; 18-compressing the fuel gas; 19-preheating the fuel gas; 20-anode mixed gas; 21-anode tail gas; 21 a-anode tail gas first shunt; 21 b-anode tail gas second shunt; 22-primary flue gas; 23-cooling the flue gas; 24 a-first flue gas; 24 b-second flue gas; 25-first cooling flue gas; 26-first depressurization of flue gas; 27-second venting to atmosphere; 28-oxygen; 29-eighth fluid; 30-carbon dioxide working medium; 31-sixth fluid; 32-a third fluid; 33-a first fluid; 34-a second fluid; 35-cooling fluid; 36-compressing a fluid; 37-low temperature pre-heating fluid; 38-fourth fluid; 39-a fifth fluid; 40-seventh fluid; 41-a first preheating fluid; 42-a second preheating fluid; 43-high temperature ammonia vapor; 44-ammonia rich vapor; 45-weak ammonia solution; 46-low temperature weak ammonia solution; 47-low pressure weak ammonia solution; 48-mixing the fluid; 49-liquid alkaline solution; 50-high pressure alkaline ammonia solution; 51-ammonia-rich fluid; 52-external water; 53-heating water; an AB-combustion chamber; an AC-air compressor; AH 1-a first air preheater; AH 2-second air preheater; AH 3-third air preheater; AH 4-fourth heat exchanger; COOL-coolers; a COND-condenser; an FC-fuel compressor; GAS-gasifier; HE-hot water heat exchanger; an HR-regenerator; HRVG 1-carbon dioxide first boiler; HRVG 2-carbon dioxide second boiler; HTR-high temperature regenerator; LTR-low temperature regenerator; m1-a first mixer; m2-a second mixer; m3-third mixer; MC main compressor; a P-pump; PRE-solution preheater; an RC-recompressor; RE-regenerator; SEP 1-a first purification separation device; SEP 2-a second purification separation device; SOFC-solid oxide fuel cells; t1-a first turbine; t2-a second turbine; t3-a third turbine; v-throttle valve; SCRPC-supercritical carbon dioxide recompression power cycle; KSC-kalina cycle.
Detailed Description
It should be noted that the following detailed description is illustrative and is intended to provide further explanation of the application. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this application belongs.
It is noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of exemplary embodiments according to the present application. As used herein, the singular is also intended to include the plural unless the context clearly indicates otherwise, and furthermore, it is to be understood that the terms "comprises" and/or "comprising" when used in this specification are taken to specify the presence of stated features, steps, operations, devices, components, and/or combinations thereof.
A multi-combined supply system based on biomass gasification and a solid oxide fuel cell comprises a gasification furnace, the solid oxide fuel cell, a second air heat exchanger and a fourth heat exchanger, wherein an anode tail gas outlet of the solid oxide fuel cell is sequentially connected with the fourth heat exchanger and the gasification furnace, the gasification furnace is provided with a biomass inlet, a synthesis gas outlet of the gasification furnace is connected with the second air heat exchanger, and a synthesis gas outlet of the air heat exchanger is connected with an anode inlet of the solid oxide fuel cell;
the cathode tail gas outlet of the solid oxide fuel cell is sequentially connected with the fourth heat exchanger and the gasification furnace, and the cathode tail gas outlet of the gasification furnace is sequentially connected with the supercritical carbon dioxide recompression power circulation system and the kalina circulation system.
The anode of the solid oxide fuel cell generates flue gas which enters the gasification furnace to provide activated gas for biomass gasification, and the biomass can generate synthesis gas such as hydrogen, methane, carbon monoxide and the like under the action of the gasifying agent. The synthesis gas enters a solid oxide fuel cell as fuel, the conversion of biomass renewable energy sources is realized, and the product of the solid oxide fuel cell is mainly H 2 O and CO 2 Clean energy conversion is realized.
The cathode exhaust gas of the solid oxide fuel cell enters a supercritical carbon dioxide recompression power circulation system and a kalina circulation system for deep utilization, so that the flue gas waste heat is deeply recovered.
In the fourth heat exchanger, the anode tail gas exchanges heat with the cathode tail gas to improve the temperature of the cathode tail gas, then the cathode tail gas enters the gasification furnace to provide heat, and then the anode tail gas enters the second heat exchanger to exchange heat with air to improve the temperature of the air. The full recovery of the waste heat of the anode tail gas is realized.
In some embodiments of the present application, the gasification furnace further comprises a first purification and separation device and a fuel compressor, wherein the synthesis gas outlet of the gasification furnace is connected with the purification and separation device and the fuel compressor in sequence, and the fuel compressor outlet is connected with the second air heat exchanger. The synthesis gas discharged from the gasification furnace is subjected to impurity and nitrogen separation by a first purification and separation device, and then is compressed by a fuel compressor and then is sent to a solid oxide fuel cell.
In some embodiments of the application, the gasification furnace further comprises a first air preheater, wherein the first air preheater is provided with an air inlet and an air outlet, the air outlet of the first air preheater is connected with the second air preheater, and the cathode gas outlet of the gasification furnace is connected with the first air preheater. And after the cathode tail gas enters the gasification furnace to provide heat, the cathode tail gas enters the first air preheater to preheat air.
In some embodiments of the application, the air preheater comprises a first air preheater, and the air preheater comprises a second air preheater.
In some embodiments of the application, the solid oxide fuel cell further comprises a third air preheater, an air outlet of the second air heat exchanger is connected with the third air preheater, an air outlet of the third air preheater is connected with a cathode inlet of the solid oxide fuel cell, and an anode gas outlet of the fourth heat exchanger is connected with the third air preheater. The first air preheater provides the first preheating of air, then gets into second air preheater, third air preheater in proper order and preheats, has realized the cascade utilization of tail gas heat.
In some embodiments of the present application, the method further comprises the step of connecting the third air preheater and the cathode gas outlet of the solid oxide fuel cell to the inlet of the first mixer, respectively, and connecting the outlet of the first mixer to the cathode inlet of the solid oxide fuel cell.
In some embodiments of the application, the solid oxide fuel cell further comprises a combustion chamber, the anode gas outlet of the solid oxide fuel cell is connected to the combustion chamber, the outlet of the combustion chamber is connected to the fourth preheater, and the combustion chamber is provided with an oxygen inlet. Burning with oxygen in a combustion chamber to make the main component of the flue gas after the anode tail gas is burnt be CO 2 And H 2 And O is beneficial to providing gasified activated gas for biomass into the gasifier.
In some embodiments of the application, the method further comprises a second mixer, the synthesis gas outlet of the first air preheater being connected to the second mixer, the synthesis gas outlet of the second mixer being connected to the anode inlet of the solid oxide fuel cell, the anode outlet of the solid oxide fuel cell being connected to the inlet of the second mixer.
In some embodiments of the application, the supercritical carbon dioxide recompression power cycle system comprises a carbon dioxide first boiler, the kalina cycle system comprises a carbon dioxide second boiler, and a cathode gas outlet of the first air preheater is sequentially connected with the carbon dioxide first boiler and the carbon dioxide second boiler.
In some embodiments of the application, the carbon dioxide boiler further comprises a hot water heat exchanger, the circulating gas outlet of the carbon dioxide second boiler is connected with the hot water heat exchanger, and the hot water heat exchanger is provided with a water inlet.
The kalina cycle and the supercritical carbon dioxide recompression power cycle and the hot water heat exchanger sequentially carry out deep recovery of waste heat on cathode exhaust. The cathode tail gas firstly supplies heat for supercritical carbon dioxide and then compresses power to circulate through a first boiler comprising carbon dioxide, then preheats for kalina circulation through a second boiler comprising carbon dioxide, and finally supplies water heat, thereby realizing the cascade recovery of the waste heat of the cathode tail gas.
In some embodiments of the present application, the supercritical carbon dioxide recompression power cycle system further includes a first turbine, a high temperature regenerator, a low temperature regenerator, a cooler, a main compressor, and a recompression device, wherein a carbon dioxide working medium outlet of the carbon dioxide first boiler is connected with the first turbine, a carbon dioxide working medium outlet of the first turbine is sequentially connected with the high temperature regenerator and the low temperature regenerator, a carbon dioxide working medium outlet of the low temperature regenerator is respectively connected with the cooler and the recompression device, an outlet of the cooler is connected with the main compressor, an outlet of the main compressor is sequentially connected with the low temperature regenerator, the high temperature regenerator, and the carbon dioxide first boiler, and an outlet of the recompression device is sequentially connected with the high temperature regenerator and the carbon dioxide first boiler.
In some embodiments of the application, the kalina cycle system further comprises a second turbine and a solution preheater, and an anode gas outlet of the third air preheater is connected with the third turbine and the solution preheater in sequence.
In some embodiments of the application, the kalina cycle system further comprises a second purifying and separating device, a second turbine, a third mixer, a condenser and a regenerator, wherein a steam outlet of the carbon dioxide second boiler is connected with the second purifying and separating device, an ammonia-rich outlet of the second purifying and separating device is sequentially connected with the second turbine and the third mixer, a weak ammonia outlet of the second purifying and separating device is sequentially connected with the regenerator and the third mixer, and an outlet of the third mixer is sequentially connected with the condenser, the regenerator, the solution preheater and a solution inlet of the carbon dioxide second boiler.
Example 1
Anode flue gas recovery circuit: biomass 14 and a portion of the released heat solid oxide fuel cell SOFC cathode tail gas (CO 2 And H 2 O) the synthesis GAS 15 generated by chemical reaction in the gasification furnace GAS is separated from the nitrogen 16 by the first purifying and separating device SEP1, the separated fuel GAS 17 is sent to the fuel compressor FC for compression, the compressed fuel GAS 18 is sent to the second mixer M2 for mixing with the anode reflux GAS 21b after releasing heat by the second air preheater AH2, and then the anode mixed GAS 20 is sent to the SOFC anode. In the SOFC, the anode mixture 20 and the cathode mixture 6 electrochemically react to generate electric energy. The anode tail gas 21 from the SOFC anode is divided into two paths, and the anode tail gas second branch 21b is communicatedReturning the excessive reflux to the second mixer M2; the anode tail gas first branch 21a is directly sent into a combustion chamber AB to be burnt with oxygen 28, and primary flue gas 22 is obtained after the combustion, the primary flue gas 22 becomes cooling flue gas 23 after passing through a fourth heat exchanger, and first flue gas 24a (mainly CO 2 And H 2 O), the first cooled flue gas 25 is formed after passing through the third air preheater AH3, then the first cooled flue gas 26 is formed after passing through the third turbine T3, the second discharged air 27 is formed after the solution preheater PRE exchanges heat and cools, and the second flue gas 24b enters the biomass furnace.
Cathode flue gas recovery circuit: compressed air 2 passes through a first air preheater AH1, then enters a second air preheater AH2 as first preheated air 3, enters a third air preheater AH3 as second preheated air 4, then enters a first mixer M1 as third preheated air 5, is heated to the inlet temperature of SOFC, is sent to SOFC cathode, and is subjected to electrochemical reaction with anode mixed GAS 20, and cathode tail GAS 7 is heated by a fourth heat exchanger AH4, is heated to become heated cathode tail GAS 8 and is sent to a high-temperature gasifier GAS to release heat. The first cooled cathode tail GAS 9 from GAS then passes through the first air preheater AH1 in sequence, then enters the carbon dioxide first boiler HRVG1 as the second cooled cathode tail GAS 10, then enters the carbon dioxide second boiler HRVG2 as the third cooled cathode tail GAS 11, then enters the hot water heat exchanger HE as the fourth cooled cathode tail GAS 12 to release heat, and finally is first exhausted to the atmosphere 13. The hot water heat exchanger enters the external water 52 and then discharges the heated water 53
Supercritical carbon dioxide recompression power cycle:
the carbon dioxide working medium 30 in the supercritical state sequentially enters the high-temperature heat regenerator HTR after being expanded and acting by the first turbine T1, the low-temperature heat regenerator LTR is precooled, the first fluid 33 after being cooled is divided into two paths, the second fluid 34 is cooled by the cooler COOL and becomes a cooling fluid 35 to flow into the main compressor MC for compression, then becomes a compression fluid 36, and is preheated by the third fluid 32 through the low-temperature heat regenerator LTR to become a low-temperature preheating fluid 37. The fourth fluid 38 is compressed by the recompressor RC and then merges with the low temperature preheating fluid 37 into a mixed fluid 39, then the fifth fluid 39 is heated by the sixth fluid 31 by the high temperature regenerator HTR, then the seventh fluid 40 flows out and then into the eighth fluid 29 to be sent into the carbon dioxide first boiler HRVG1 to be heated by the top cycle second cooled cathode exhaust gas 10 and become the carbon dioxide working fluid 30, thereby completing one cycle.
Kalina (KSC) cycle:
the high pressure alkaline ammonia solution 50 at the pump outlet is first preheated in the regenerator HR and solution preheater PRE in sequence and then enters the carbon dioxide second boiler HRVG2 to absorb the heat released by the top cycle cathode exhaust and convert it to high temperature ammonia vapor 43. The steam is then separated in a second purification and separation device SEP2 into ammonia rich steam 44 and weak ammonia solution 45. The ammonia-rich steam enters a second turbine T2 to be expanded and work done, and becomes an expanded ammonia-rich fluid 51. The weak ammonia solution is passed through a regenerator to release heat, and becomes low temperature weak ammonia solution 46, which is throttled to low pressure by throttle valve V to become low pressure weak ammonia solution 47. The two liquids are then mixed in the third mixer M3 to form a mixed fluid 48, which is condensed in the condenser COND to form a low-pressure alkaline ammonia solution 49, which is then fed into the regenerator by the pump P to form a high-pressure alkaline ammonia solution 50, which is then fed into the second preheating fluid 42 through the solution preheater PRE to form the first preheating fluid 41.
The above description is only of the preferred embodiments of the present application and is not intended to limit the present application, but various modifications and variations can be made to the present application by those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present application should be included in the protection scope of the present application.
Claims (7)
1. A biomass gasification and solid oxide fuel cell based multi-cogeneration system, characterized in that: the device comprises a gasification furnace, a solid oxide fuel cell, a second air heat exchanger and a fourth heat exchanger, wherein an anode tail gas outlet of the solid oxide fuel cell is sequentially connected with the fourth heat exchanger and the gasification furnace, the gasification furnace is provided with a biomass inlet, a synthesis gas outlet of the gasification furnace is connected with the second air heat exchanger, and a synthesis gas outlet of the air heat exchanger is connected with an anode inlet of the solid oxide fuel cell;
the cathode tail gas outlet of the solid oxide fuel cell is sequentially connected with a fourth heat exchanger and a gasification furnace, and the cathode tail gas outlet of the gasification furnace is sequentially connected with a supercritical carbon dioxide recompression power circulation system and a kalina circulation system;
the supercritical carbon dioxide recompression power circulation system comprises a carbon dioxide first boiler, the kalina circulation system comprises a carbon dioxide second boiler, and a cathode gas outlet of the first air preheater is sequentially connected with the carbon dioxide first boiler and the carbon dioxide second boiler;
further, the device also comprises a hot water heat exchanger, a circulating gas outlet of the carbon dioxide second boiler is connected with the hot water heat exchanger, and the hot water heat exchanger is provided with a water inlet;
the supercritical carbon dioxide recompression power circulation system further comprises a first turbine, a high-temperature heat regenerator, a low-temperature heat regenerator, a cooler, a main compressor and a recompression machine, wherein a carbon dioxide working medium outlet of the carbon dioxide first boiler is connected with the first turbine, a carbon dioxide working medium outlet of the first turbine is sequentially connected with the high-temperature heat regenerator and the low-temperature heat regenerator, a carbon dioxide working medium outlet of the low-temperature heat regenerator is respectively connected with the cooler and the recompression machine, an outlet of the cooler is connected with the main compressor, an outlet of the main compressor is sequentially connected with the low-temperature heat regenerator, the high-temperature heat regenerator and the carbon dioxide first boiler, and an outlet of the recompression machine is sequentially connected with the high-temperature heat regenerator and the carbon dioxide first boiler;
the kalina circulating system also comprises a second turbine and a solution preheater, and an anode gas outlet of the third air preheater is sequentially connected with the third turbine and the solution preheater;
the kalina circulating system comprises the following specific circulating processes: the high-pressure alkaline ammonia solution at the outlet of the pump is firstly preheated in the regenerator and the solution preheater in sequence, then enters the carbon dioxide second boiler to absorb heat released by the top circulation cathode exhaust gas and is converted into high-temperature ammonia steam; then separating the steam into ammonia-rich steam and weak ammonia solution in a second purifying and separating device; the steam rich in ammonia enters a second turbine for expansion and work to become an expanded ammonia-rich fluid; the weak ammonia solution flows through a regenerator to release heat, and becomes low-temperature weak ammonia solution, and the low-temperature weak ammonia solution is throttled to low pressure through a throttle valve to become low-pressure weak ammonia solution; then, the two liquids are mixed in a third mixer to become mixed fluid, then condensed into low-pressure alkaline ammonia solution in a condenser, and the low-pressure alkaline ammonia solution is made into high-pressure alkaline ammonia solution after the action of a pump to enter a regenerator, and the high-pressure alkaline ammonia solution becomes first preheating fluid and becomes second preheating fluid after the solution preheater.
2. The biomass gasification and solid oxide fuel cell based multiple supply system according to claim 1, wherein: the gasification furnace further comprises a first purification and separation device and a fuel compressor, a synthesis gas outlet of the gasification furnace is sequentially connected with the purification and separation device and the fuel compressor, and an outlet of the fuel compressor is connected with the second air heat exchanger.
3. The biomass gasification and solid oxide fuel cell based multiple supply system according to claim 1, wherein: the gasification furnace further comprises a first air preheater, wherein the first air preheater is provided with an air inlet and an air outlet, the air outlet of the first air preheater is connected with the second air preheater, and the cathode gas outlet of the gasification furnace is connected with the first air preheater.
4. The biomass gasification and solid oxide fuel cell based multiple supply system according to claim 1, wherein: the solid oxide fuel cell also comprises a third air preheater, an air outlet of the second air heat exchanger is connected with the third air preheater, an air outlet of the third air preheater is connected with a cathode inlet of the solid oxide fuel cell, and an anode gas outlet of the fourth heat exchanger is connected with the third air preheater.
5. The biomass gasification and solid oxide fuel cell based multiple supply system according to claim 4, wherein: the solid oxide fuel cell also comprises a first mixer, wherein the third air preheater and a cathode gas outlet of the solid oxide fuel cell are respectively connected with an inlet of the first mixer, and an outlet of the first mixer is connected with a cathode inlet of the solid oxide fuel cell.
6. The biomass gasification and solid oxide fuel cell based multiple supply system according to claim 1, wherein: the solid oxide fuel cell also comprises a combustion chamber, an anode gas outlet of the solid oxide fuel cell is connected with the combustion chamber, an outlet of the combustion chamber is connected with the fourth preheater, and an oxygen inlet is arranged in the combustion chamber.
7. The biomass gasification and solid oxide fuel cell based multiple supply system according to claim 5, wherein: the system also comprises a second mixer, wherein the synthesis gas outlet of the first air preheater is connected with the second mixer, the synthesis gas outlet of the second mixer is connected with the anode inlet of the solid oxide fuel cell, and the anode outlet of the solid oxide fuel cell is connected with the inlet of the second mixer.
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| CN111900432A (en) * | 2020-06-11 | 2020-11-06 | 山东大学 | Solid oxide fuel cell system, power-cooling combined supply system and method thereof |
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