Biomass fuel-solid oxide fuel cell comprehensive energy system with CO2 trapping function

Abstract

The invention discloses a biomass fuel-solid oxide fuel cell comprehensive energy system with a CO2 trapping function. The biomass fuel-solid oxide fuel cell comprehensive energy system comprises a top circulation system and a bottom circulation system, the top circulation system comprises a solid oxide fuel cell, a cathode inlet of the solid oxide fuel cell is communicated with outside air, an anode inlet of the solid oxide fuel cell is communicated with biomass gas and water, a cathode outlet of the solid oxide fuel cell is communicated with a permeation side of the water-gas replacement membrane reactor, and an anode outlet of the solid oxide fuel cell is communicated with a supply side of the water-gas replacement membrane reactor; the supply side of the water-gas replacement membrane reactor is communicated with the combustion chamber; the combustion chamber is directly connected with external oxygen; the bottom circulation system comprises a transcritical carbon dioxide cycle, a Kalina cycle, a humidifier-dehumidifier and an organic Rankine cycle; the combined supply of various energies and substances such as fresh water, carbon dioxide, electric power, cold energy and the like can be ensured while gradient recovery of tail gas waste heat of the solid oxide fuel cell and cold energy of liquefied petroleum and natural gas is realized.

Description

Technical Field

[0001] The present invention belongs to the technical field of energy systems, and in particular relates to a biomass fuel-solid oxide fuel cell integrated energy system with a CO2 capture function. Background Art

[0002] Solid oxide fuel cells have significant advantages in energy conversion efficiency because they can directly convert the chemical energy in the fuel into electrical energy efficiently. In addition, solid oxide fuel cells have a wide range of adaptability in fuel use and are compatible with biomass gas fuels. This feature makes the biomass fuel-solid oxide fuel cell system show great potential in industrial applications. Furthermore, solid oxide fuel cells operate under high temperature and high pressure conditions, which makes their tail gas have a high recycling value. There are some obvious deficiencies in the existing technical solutions for tail gas treatment of biomass fuel-solid oxide fuel cell systems, such as low waste heat recovery efficiency, single product form, and high energy consumption and cost of carbon dioxide capture. These problems limit the overall efficiency and economy of solid oxide fuel cell systems and hinder their application and promotion in a wider range of fields. Summary of the invention

[0003] In order to solve the existing technical problems, the present invention provides a biomass fuel-solid oxide fuel cell integrated energy system with CO2 capture function, which adopts oxygen-enriched combustion, water-gas replacement membrane reactor and liquefied petroleum natural gas cold energy utilization technology, which can greatly increase the concentration of carbon dioxide, facilitate low-energy carbon dioxide capture, and greatly reduce the oxygen consumption and corresponding costs required for oxygen-enriched combustion. In addition, by coordinating transcritical carbon dioxide cycle, Kalina cycle, humidifier-dehumidifier and organic Rankine cycle, it is possible to achieve the cascade recovery of solid oxide fuel cell tail gas waste heat and liquefied petroleum natural gas cold energy, while ensuring the joint supply of multiple energies and materials such as fresh water, carbon dioxide, electricity, and cold.

[0004] In order to achieve the above object, the present invention adopts the following technical solution:

[0005] A biomass fuel-solid oxide fuel cell integrated energy system with CO2 capture function, including a top circulation system and a bottom circulation system;

[0006] The top circulation system comprises a solid oxide fuel cell, wherein the cathode inlet is connected to the outside air, the anode inlet is connected to the biomass gas and water, the cathode outlet is connected to the permeate side of the water gas exchange membrane reactor, and the anode outlet is connected to the supply side of the water gas exchange membrane reactor; the supply side of the water gas exchange membrane reactor is connected to the combustion chamber, and the combustion chamber is directly connected to the outside oxygen;

[0007] The bottoming cycle system includes a transcritical carbon dioxide cycle, a Kalina cycle, a humidifier-dehumidifier, and an organic Rankine cycle;

[0008] The transcritical carbon dioxide cycle recovers the solid oxide fuel cell anode flue gas waste heat and liquefied petroleum natural gas cold energy through the first boiler and the first condenser respectively;

[0009] The Kalina cycle further recovers the waste heat of the anode flue gas of the solid oxide fuel cell and the cold energy of the liquefied petroleum natural gas through the second boiler and the second condenser respectively;

[0010] The humidifier-dehumidifier deeply recovers the waste heat of the anode flue gas of the solid oxide fuel cell through the third boiler, and condenses and removes the moisture in the flue gas;

[0011] The organic Rankine cycle recovers the waste heat of the cathode flue gas of the solid oxide fuel cell and the cold energy of the liquefied petroleum natural gas through the fourth boiler and the third condenser respectively;

[0012] The dehydrated flue gas is compressed by the carbon dioxide compressor and coupled with the cold energy of liquefied petroleum natural gas through the first heat exchanger to capture carbon dioxide;

[0013] The liquefied petroleum natural gas cold energy is coupled with the external cooling unit through the second heat exchanger to meet the user's cooling needs.

[0014] The solid oxide fuel cell anode is also provided with an anode flue gas loop.

[0015] The air in the top cycle is compressed by the first air compressor and then reacts with the biomass in the biomass gasifier to produce a high-temperature raw material synthesis product. Then, the impurities and nitrogen are removed by the first separator to obtain pure synthesis gas. Subsequently, the air is introduced into the fuel compressor to increase the pressure after releasing heat through the third air preheater. After that, the air is mixed with the water vapor that is pressurized and heated by the water pump and the water preheater in the mixer, and finally sent to the anode of the solid oxide fuel cell; the gas coming out of the anode of the solid oxide fuel cell is sent to the supply side of the water gas exchange membrane reactor. Under the action of the partial pressure difference on both sides of the membrane, the water gas exchange membrane reactor selectively extracts hydrogen from the synthesis gas on the supply side to the permeate side, so that the equilibrium of the water gas exchange reaction moves toward the product direction;

[0016] The hydrogen-depleted synthesis gas from the supply side of the water-gas exchange membrane reactor is introduced into the combustion chamber for stoichiometric combustion with oxygen to ensure that the combustion product has a high carbon dioxide concentration;

[0017] The high-temperature combustion products coming out of the combustion chamber release heat through the first air preheater and the water preheater in sequence, and then drive the transcritical carbon dioxide cycle and the Kalina cycle through the first boiler and the second boiler to generate additional electricity; then, the humidifier-dehumidifier is driven by the third boiler to produce fresh water, and the water vapor contained in the flue gas is also condensed and separated in this process; finally, the dehydrated flue gas is pressurized by the carbon dioxide compressor, condensed and liquefied by the low-temperature liquefied petroleum natural gas in the first heat exchanger, and then sent to the CO2 tank.

[0018] The cathode of the solid oxide fuel cell is provided with a cathode flue gas loop, in which the air is pressurized by the second air compressor, and then heated by the first air preheater, the second air preheater and the third air preheater in sequence, and then sent to the cathode of the solid oxide fuel cell;

[0019] The gas at the cathode outlet of the solid oxide fuel cell is sent to the permeate side of the water-gas exchange membrane reactor to react with the hydrogen from the supply side of the water-gas exchange membrane reactor to increase the energy quality, and then passes through the gas turbine to perform work externally and the second air preheater to release heat, and finally is discharged into the atmosphere after driving the organic Rankine cycle through the fourth boiler.

[0020] The liquefied petroleum natural gas is provided with a cold energy cascade recovery circuit. After the low-temperature liquefied petroleum natural gas is pressurized by the fourth working fluid pump, it passes through the third condenser, the first heat exchanger, the first condenser, the second condenser and the second heat exchanger in sequence to cool down other working fluids, and at the same time it is heated itself and supplied to users.

[0021] Compared with the prior art, the present invention has the following beneficial effects:

[0022] (1) The system of the present invention combines solid oxide fuel cells, water-gas exchange membrane reactors, oxygen-enriched combustion and liquefied petroleum and natural gas cold energy utilization technologies, and fully recovers substances and energy in the system exhaust gas through the reasonable arrangement of heat exchangers, thereby achieving low-energy carbon dioxide capture.

[0023] (2) The system of the present invention realizes cascade recovery of the cathode and anode flue gas waste heat of the solid oxide fuel cell through transcritical carbon dioxide cycle, Kalina cycle, humidifier-dehumidifier, and organic Rankine cycle, which can ensure that the system can achieve multiple energy and material supplies while generating electricity efficiently.

[0024] (3) The system of the present invention can improve the power generation efficiency of the system and reduce the power consumption of carbon dioxide capture while realizing the cascade recovery of liquefied petroleum and natural gas cold energy through the reasonable arrangement of the organic Rankine cycle, the first heat exchanger, the transcritical carbon dioxide cycle, the Kalina cycle and the second heat exchanger. BRIEF DESCRIPTION OF THE DRAWINGS

[0025] Figure 1This is a schematic diagram of the structure of the biomass fuel-solid oxide fuel cell integrated energy system with CO2 capture function of the present invention;

[0026] Among them, AB: combustion chamber; AC-I: first air compressor; AC-II: second air compressor; APH-I: first air preheater; APH-II: second air preheater; APH-III: third air preheater; CC: carbon dioxide compressor; COND-I: first condenser; COND-II: second condenser; COND-III: third condenser; DEH: dehumidifier; FC: fuel compressor; GAS: biomass gasifier; GT: gas turbine; HDH: humidifier-dehumidifier; HE-I: first heat exchanger; HE-II: second heat exchanger; HRVG-I: first boiler; HRVG-II: second boiler; HRVG-III: third boiler; HRVG-IV: fourth boiler furnace; HUM: humidifier; Inv: inverter; KC: Kalina cycle; LNG: liquefied petroleum natural gas; M: mixer; ORC: organic Rankine cycle; PI: first working fluid pump; P-II: second working fluid pump; P-III: third working fluid pump; P-IV: fourth working fluid pump; RE-I: first regenerator; RE-II: second regenerator; RE-III: third regenerator; SEP-I: first separator; SEP-II: second separator; SOFC: solid oxide fuel cell; TI: first turbine; T-II: second turbine; T-III: third turbine; TRCC: transcritical carbon dioxide cycle; TV: throttle valve; WGSMR: water gas displacement membrane reactor; WP: water pump; WPH: water preheater. DETAILED DESCRIPTION

[0027] The present invention will be further described below in conjunction with the accompanying drawings and embodiments.

[0028] It should be noted that the following detailed descriptions are illustrative and intended to provide further explanation of the present invention. Unless otherwise specified, all technical and scientific terms used in the present invention have the same meanings as those commonly understood by those skilled in the art to which the present invention belongs.

[0029] It should be noted that the terms used herein are only for describing specific embodiments and are not intended to limit exemplary embodiments according to the present invention. As used herein, unless the context clearly indicates otherwise, the singular form is also intended to include the plural form. In addition, it should be understood that when the terms "comprising" and / or "including" are used in this specification, it indicates the presence of features, steps, operations, devices, components and / or combinations thereof.

[0030] Example 1

[0031] A biomass fuel-solid oxide fuel cell integrated energy system with CO2 capture function, referring to Figure 1 The system consists of two parts: the top circulation system and the bottom circulation system. The system can ensure the cascade recovery of solid oxide fuel cell SOFC tail gas waste heat and liquefied petroleum natural gas cold energy while realizing the joint supply of fresh water, carbon dioxide, electricity, cold capacity and other energy and materials.

[0032] The top circulation system includes a solid oxide fuel cell SOFC, whose cathode inlet is connected to the outside air, the anode inlet is connected to the biomass gas and water, the cathode outlet is connected to the permeate side of the water gas displacement membrane reactor WGSMR, and the anode outlet is connected to the supply side of the water gas displacement membrane reactor WGSMR; the supply side of the water gas displacement membrane reactor WGSMR is connected to the combustion chamber AB, and the combustion chamber AB is directly connected to the outside oxygen;

[0033] The bottom cycle system includes the transcritical carbon dioxide cycle TRCC, Kalina cycle KC, humidifier-dehumidifier HDH, and organic Rankine cycle ORC;

[0034] The transcritical carbon dioxide cycle TRCC recovers the solid oxide fuel cell SOFC anode flue gas waste heat and liquefied petroleum natural gas cold energy through the first boiler HRVG-I and the first condenser COND-I respectively;

[0035] The Kalina cycle KC further recovers the solid oxide fuel cell SOFC anode flue gas waste heat and liquefied petroleum natural gas cold energy through the second boiler HRVG-II and the second condenser COND-II respectively;

[0036] The humidifier-dehumidifier HDH deeply recovers the waste heat of the anode flue gas of the solid oxide fuel cell SOFC through the third boiler HRVG-III, and condenses and removes the moisture in the flue gas;

[0037] The organic Rankine cycle ORC recovers the solid oxide fuel cell SOFC cathode flue gas waste heat and liquefied petroleum natural gas cold energy through the fourth boiler HRVG-IV and the third condenser COND-III respectively;

[0038] After being compressed by the carbon dioxide compressor CC, the dehydrated flue gas is coupled with the cold energy of liquefied petroleum gas through the first heat exchanger HE-I to capture carbon dioxide;

[0039] The cold energy of liquefied petroleum gas is coupled with the external cooling unit through the second heat exchanger HE-II to meet the user's cooling needs.

[0040] Specifically, the top cycle includes a first air compressor AC-I, a second air compressor AC-II, a water pump WP, a fuel compressor FC, a biomass gasifier GAS, a first separator SEP-I, a first air preheater APH-I, a second air preheater APH-II, a third air preheater APH-III, a water preheater WPH, a mixer M, a combustion chamber AB, a solid oxide fuel cell SOFC, a water gas exchange membrane reactor WGSMR, an inverter Inv, and a gas turbine GT;

[0041] The bottom cycle includes a transcritical carbon dioxide cycle TRCC, a Kalina cycle KC, a humidifier-dehumidifier HDH, an organic Rankine cycle ORC, a first heat exchanger HE-I, a second heat exchanger HE-II, a carbon dioxide compressor CC, a carbon dioxide tank, and a fourth working fluid pump P-IV;

[0042] The transcritical carbon dioxide cycle TRCC includes a first boiler HRVG-I, a first turbine TI, a first regenerator RE-I, a first working fluid pump PI, and a first condenser COND-I;

[0043] The Kalina cycle KC includes the second boiler HRVG-II, the second turbine T-II, the second regenerator RE-II, the second mass pump P-II, the second condenser COND-II, the second separator SEP-II, and the throttle valve TV;

[0044] The humidifier-dehumidifier HDH includes the third boiler HRVG-III, the humidifier HUM, and the dehumidifier DEH;

[0045] The organic Rankine cycle ORC includes the fourth boiler HRVG-IV, the third turbine T-III, the third regenerator RE-III, the third working fluid pump P-III, and the third condenser COND-III;

[0046] The first air compressor AC-I is connected to the biomass gasifier GAS, biomass is put into the biomass gasifier GAS, the biomass gasifier GAS is connected to the first separator SEP-I, and the first separator SEP-I discharges impurities and waste gas and is connected to the third air preheater APH-III;

[0047] The second air compressor AC-II is connected to the first air preheater APH-I, the first air preheater APH-I is connected to the second air preheater APH-II and the water preheater WPH respectively, and the second air preheater APH-II is connected to the third air preheater APH-III;

[0048] The water pump WP is also connected to the water preheater WPH, the third air preheater APH-III is connected to the fuel compressor FC, the fuel compressor FC and the water preheater WPH are both connected to the mixer M, the third air preheater APH-III and the mixer M are both connected to the solid oxide fuel cell SOFC, the other end of the solid oxide fuel cell SOFC is connected to the water gas displacement membrane reactor WGSMR, the water gas displacement membrane reactor WGSMR is also connected to the gas turbine GT and the combustion chamber AB respectively, the other end of the gas turbine GT is connected to the second air preheater APH-II; the second air preheater APH-II is also connected to the fourth boiler HRVG-IV in the organic Rankine cycle ORC, and oxygen is added to the combustion chamber AB, and it is also connected to the first air preheater APH-I;

[0049] The fourth boiler HRVG-IV is also connected to the third turbine T-III and the third reheater RE-III respectively. The third turbine T-III is connected to the third reheater RE-III. The third reheater RE-III is connected to the third working fluid pump P-III. The third working fluid pump P-III is also connected to the third condenser COND-III. The third condenser COND-III is connected to the fourth working fluid pump P-IV. The fourth working fluid pump P-IV is connected to the external LNG. The third condenser COND-III is also connected to the first heat exchanger HE-I. The first heat exchanger HE-I is connected to the CO2 tank. The first heat exchanger HE-I is also connected to the carbon dioxide compressor CC. The carbon dioxide compressor CC is connected to the third boiler HRVG-III in the humidifier-dehumidifier HDH. The third boiler HRVG-III, the humidifier HUM and the dehumidifier DEH are connected to each other. The dehumidifier DEH is connected to the external seawater.

[0050] The third boiler HRVG-III is also connected to the second boiler HRVG-II in the Kalina cycle KC, the second boiler HRVG-II is connected to the second separator SEP-II, the second separator SEP-II is also connected to the second turbine T-II and the second regenerator RE-II respectively, the second regenerator RE-II is connected to the throttle valve TV, the throttle valve TV and the second turbine T-II are both connected to the second condenser COND-II, the second condenser COND-II is also connected to the second regenerator RE-II through the second mass pump P-II, the second regenerator RE-II is connected to the second boiler HRVG-II, the second condenser COND-II is connected to the second heat exchanger HE-II, and the second heat exchanger HE-II is connected to the outside;

[0051] The second boiler HRVG-II is also connected to the first boiler HRVG-I in the transcritical carbon dioxide cycle TRCC, the first boiler HRVG-I is connected to the first turbine TI, the first turbine TI is connected to the first reheater RE-I, the first reheater RE-I is connected to the first boiler HRVG-I, the first reheater RE-I is also connected to the first working fluid pump PI, the first working fluid pump PI is connected to the first condenser COND-I; the first condenser COND-I is also respectively connected to the second condenser COND-II and the first heat exchanger HE-I.

[0052] This system divides the gas flow process into an anode flue gas recovery loop and a cathode flue gas recovery loop according to the different arrangements of the cathode and anode stages of the solid oxide fuel cell. The anode of the solid oxide fuel cell SOFC is provided with an anode flue gas loop. Specifically, the anode flue gas recovery loop is as follows:

[0053] After being compressed by the first air compressor AC-I, the air 2 reacts with the biomass 1 to undergo a gasification reaction in the biomass gasifier GAS to produce a high-temperature raw material synthesis product 4. Then, the impurities and nitrogen are removed by the first separator SEP-I to obtain a pure synthesis gas 5. Subsequently, the air is introduced into the fuel compressor FC to increase the pressure after releasing heat through the third air preheater APH-III. After that, the air is mixed with the water vapor 31 pressurized and heated by the water pump WP and the water preheater WPH in the mixer M, and finally sent to the anode of the solid oxide fuel cell SOFC. The anode gas 8 of the solid oxide fuel cell SOFC reacts electrochemically with the cathode air 23 to produce direct current, which is converted into alternating current through the inverter Inv. The anode gas 9 after the reaction is sent to the supply side of the water gas exchange membrane reactor WGSMR. Under the action of the partial pressure difference on both sides of the membrane, the water gas exchange membrane reactor WGSMR selectively extracts hydrogen from the synthesis gas on the supply side. To the permeate side, thereby shifting the equilibrium of the water-gas replacement reaction toward the product direction, then, the hydrogen-poor synthesis gas 10 is introduced into the combustion chamber for stoichiometric combustion with oxygen 32 to ensure that the combustion product 11 has a higher carbon dioxide concentration; then, the high-temperature combustion product 11 passes through the first air preheater APH-I and the water preheater WPH in turn to release heat, and then passes through the first boiler HRVG-I and the second boiler HRVG-II in turn to drive the transcritical carbon dioxide cycle TRCC and the Kalina cycle KC to generate additional electricity; then, the humidifier HUM and the dehumidifier DEH are driven by the third boiler HRVG-III to operate for seawater desalination, and in this process, the water vapor contained in the flue gas 15 is also condensed and separated; finally, the dehydrated flue gas 16 is pressurized by the carbon dioxide compressor CC, condensed and liquefied by the low-temperature liquefied petroleum natural gas 56 in the first heat exchanger HE-I, and then sent to the CO2 tank.

[0054] The cathode of the solid oxide fuel cell SOFC is provided with a cathode flue gas loop, specifically a cathode flue gas recovery loop:

[0055] After the air 19 is pressurized by the second air compressor AC-II, it is heated in sequence by the first air preheater APH-I, the second air preheater APH-II, and the third air preheater APH-III and then sent to the cathode of the solid oxide fuel cell SOFC. After the electrochemical reaction occurs, the cathode gas 24 reacts with the hydrogen from the supply side of the water gas exchange membrane reactor WGSMR on the permeation side of the water gas exchange membrane reactor WGSMR to increase the temperature, and then drives the gas turbine GT to perform external work. Then, after releasing heat through the second air preheater APH-II, it drives the organic Rankine cycle ORC to operate through the fourth boiler HRVG-IV to generate additional power, and is finally discharged into the atmosphere.

[0056] Liquefied petroleum and natural gas is equipped with a cold energy cascade recovery loop, the specific route is as follows:

[0057] After being pressurized by the fourth working fluid pump P-IV, the liquefied petroleum natural gas (LNG, -161.5°C) cools down other working fluids through the third condenser COND-III, the first heat exchanger HE-I, the first condenser COND-I, the second condenser COND-II, and the second heat exchanger HE-II in sequence. The liquefied petroleum natural gas 60 is heated to about 7°C and then supplied to users. It should be noted that the liquefied petroleum natural gas 59 cools down the external water 61 in the second heat exchanger HE-II, thereby meeting the user's cooling needs.

[0058] Transcritical CO2 cycle TRCC and organic Rankine cycle ORC operating principle:

[0059] The working principles of the transcritical carbon dioxide cycle TRCC and the organic Rankine cycle ORC are similar, but the working fluids are different. This system uses carbon dioxide and propane as the working fluids of the transcritical carbon dioxide cycle TRCC and the organic Rankine cycle ORC, respectively. The working fluid is heated by the boiler (HRVG-I and HRVG-IV), and then expanded in the turbine (TI and T-III) to provide power output; then it is precooled through the regenerator (RE-I and RE-III), and then liquefied by liquefied petroleum natural gas in the condenser (COND-I and COND-III). Subsequently, the working fluid is pressurized by the working fluid pump (PI and P-III). Finally, the working fluid is preheated by the regenerator (RE-I and RE-III) and returned to the boiler (HRVG-I and HRVG-IV).

[0060] Kalina Cycle KC Operating Principle:

[0061] The working fluid (ammonia water) of the Kalina cycle KC obtains the required energy from the high-temperature exhaust gas 14 in the second boiler HRVG-II. Subsequently, the second separator SEP-II divides the mixture 39 into two different streams, among which the saturated steam 40 drives the second turbine T-II to rotate and perform external work; the hot saturated liquid 46 enters the second regenerator RE-II to heat the outlet fluid 44 of the second working fluid pump P-II, and after being cooled, it flows to the throttle valve TV for throttling and pressure reduction, and then mixes with the fluid 41 from the second turbine T-II. Then the mixed fluid 42 is condensed and liquefied by the liquefied petroleum natural gas 58 in the second condenser COND-II, and then is pressurized and preheated by the second working fluid pump P-II and the second regenerator RE-II in turn, and then returns to the second boiler HRVG-II.

[0062] Humidifier-dehumidifier HDH operating principle:

[0063] First, the hot air flow 51 increases the temperature of the seawater 53 in the dehumidifier DEH. The preheated flow 49 reaches the highest temperature in the humidifier-dehumidifier unit to be sprayed in the humidifier HUM. The packed bed structure in the humidifier HUM helps to maintain a large contact area between the water 50 and the air 52, thereby improving heat and mass transfer. During the spraying process, a portion of the pure water evaporates from the sprayed seawater, and another portion of the brine is discharged. The incoming air flow 52 is mixed with the evaporated water and leaves the humidifier with higher humidity and temperature. Then, the humid hot air 51 enters the dehumidifier DEH to give its energy to the incoming seawater and produce fresh water.

[0064] The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. For those skilled in the art, the present invention may have various modifications and variations. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention shall be included in the protection scope of the present invention.

Claims

1. A biomass fuel-solid oxide fuel cell integrated energy system with CO2 capture function, characterized in that: Including top circulation system and bottom circulation system; The top circulation system comprises a solid oxide fuel cell, wherein the cathode inlet is connected to the outside air, the anode inlet is connected to the biomass gas and water, the cathode outlet is connected to the permeate side of the water gas exchange membrane reactor, and the anode outlet is connected to the supply side of the water gas exchange membrane reactor; the supply side of the water gas exchange membrane reactor is connected to the combustion chamber, and the combustion chamber is directly connected to the outside oxygen; The bottoming cycle system includes a transcritical carbon dioxide cycle, a Kalina cycle, a humidifier-dehumidifier, and an organic Rankine cycle; The transcritical carbon dioxide cycle recovers the solid oxide fuel cell anode flue gas waste heat and liquefied petroleum natural gas cold energy through the first boiler and the first condenser respectively; The Kalina cycle further recovers the waste heat of the anode flue gas of the solid oxide fuel cell and the cold energy of the liquefied petroleum natural gas through the second boiler and the second condenser respectively; The humidifier-dehumidifier deeply recovers the waste heat of the anode flue gas of the solid oxide fuel cell through the third boiler, and condenses and removes the moisture in the flue gas; The organic Rankine cycle recovers the waste heat of the cathode flue gas of the solid oxide fuel cell and the cold energy of the liquefied petroleum natural gas through the fourth boiler and the third condenser respectively; The dehydrated flue gas is compressed by the carbon dioxide compressor and coupled with the cold energy of liquefied petroleum natural gas through the first heat exchanger to capture carbon dioxide; The liquefied petroleum natural gas cold energy is coupled with the external cooling unit through the second heat exchanger to meet the user's cooling needs.

2. The biomass fuel-solid oxide fuel cell integrated energy system with CO2 capture function according to claim 1 is characterized in that: The solid oxide fuel cell anode is also provided with an anode flue gas loop.

3. The biomass fuel-solid oxide fuel cell integrated energy system with CO2 capture function according to claim 1 is characterized in that: The air in the top cycle is compressed by the first air compressor and then reacts with the biomass in the biomass gasifier to produce a high-temperature raw material synthesis product. Then, the impurities and nitrogen are removed by the first separator to obtain pure synthesis gas. Subsequently, the air is introduced into the fuel compressor to increase the pressure after releasing heat through the third air preheater. After that, the air is mixed with the water vapor that has been pressurized and heated by the water pump and the water preheater in the mixer, and finally sent to the anode of the solid oxide fuel cell; the gas coming out of the anode of the solid oxide fuel cell is sent to the supply side of the water gas exchange membrane reactor. Under the action of the partial pressure difference on both sides of the membrane, the water gas exchange membrane reactor selectively extracts hydrogen from the synthesis gas on the supply side to the permeate side, so that the equilibrium of the water gas exchange reaction moves toward the product direction; The hydrogen-depleted synthesis gas from the supply side of the water-gas exchange membrane reactor is introduced into the combustion chamber for stoichiometric combustion with oxygen to ensure that the combustion product has a high carbon dioxide concentration; The high-temperature combustion products coming out of the combustion chamber release heat through the first air preheater and the water preheater in sequence, and then drive the transcritical carbon dioxide cycle and the Kalina cycle through the first boiler and the second boiler to generate additional electricity; then, the humidifier-dehumidifier is driven by the third boiler to produce fresh water, and the water vapor contained in the flue gas is also condensed and separated in this process; finally, the dehydrated flue gas is pressurized by the carbon dioxide compressor, condensed and liquefied by the low-temperature liquefied petroleum natural gas in the first heat exchanger, and then sent to the CO2 tank.

4. The biomass fuel-solid oxide fuel cell integrated energy system with CO2 capture function according to claim 1 is characterized in that: The cathode of the solid oxide fuel cell is provided with a cathode flue gas loop, in which the air is pressurized by the second air compressor, and then heated by the first air preheater, the second air preheater and the third air preheater in sequence, and then sent to the cathode of the solid oxide fuel cell; The gas at the cathode outlet of the solid oxide fuel cell is sent to the permeate side of the water-gas exchange membrane reactor to react with the hydrogen from the supply side of the water-gas exchange membrane reactor to increase the energy quality, and then passes through the gas turbine to perform work externally and the second air preheater to release heat, and finally is discharged into the atmosphere after driving the organic Rankine cycle through the fourth boiler.

5. The biomass fuel-solid oxide fuel cell integrated energy system with CO2 capture function according to claim 1 is characterized in that: The liquefied petroleum natural gas is provided with a cold energy cascade recovery circuit. After the low-temperature liquefied petroleum natural gas is pressurized by the fourth working fluid pump, it passes through the third condenser, the first heat exchanger, the first condenser, the second condenser and the second heat exchanger in sequence to cool down other working fluids, and at the same time it is heated itself and supplied to users.

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