Biomass fuel-solid oxide fuel cell integrated energy system with co2 capture function

Abstract

The application discloses a biomass fuel-solid oxide fuel cell comprehensive energy system with a CO2 capture function, which comprises a top circulation system and a bottom circulation system; the top circulation system comprises a solid oxide fuel cell, the cathode inlet of the solid oxide fuel cell is communicated with external air, the anode inlet of the solid oxide fuel cell is communicated with biomass gas and water, the cathode outlet of the solid oxide fuel cell is communicated with the permeation side of a water-gas displacement membrane reactor, and the anode outlet of the solid oxide fuel cell is communicated with the supply side of the water-gas displacement membrane reactor; the supply side of the water-gas displacement membrane reactor is communicated with a combustion chamber, and the combustion chamber is directly connected with external oxygen; the bottom circulation system comprises a transcritical carbon dioxide cycle, a Kalina cycle, a humidification-dehumidification device and an organic Rankine cycle; the solid oxide fuel cell tail gas waste heat and liquefied petroleum gas cold energy can be recycled in stages, and the joint supply of fresh water, carbon dioxide, electric power, cold energy and other energy and substances can be ensured.

Description

TECHNICAL FIELD

[0001] The present application belongs to the technical field of energy systems, and particularly relates to a biomass fuel-solid oxide fuel cell comprehensive energy system with CO2 capture function. BACKGROUND

[0002] Solid oxide fuel cells have significant advantages in energy conversion efficiency because they can directly convert chemical energy in fuel into electrical energy with high efficiency. In addition, solid oxide fuel cells have wide adaptability in fuel use and can be compatible with biomass gas fuel. This feature makes the biomass fuel-solid oxide fuel cell system have great potential in industrial applications. Further, solid oxide fuel cells operate under high temperature and high pressure conditions, which makes their tail gas have high recycling value. However, 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, high energy consumption and cost of carbon dioxide capture. These problems limit the overall efficiency and economy of the solid oxide fuel cell system, hindering its application and promotion in a wider field. SUMMARY

[0003] In order to solve the existing technical problems, the present application provides a biomass fuel-solid oxide fuel cell comprehensive energy system with CO2 capture function, which adopts oxygen-enriched combustion, water-gas displacement membrane reactor and liquefied petroleum gas cold energy utilization technology, which can greatly improve the concentration of carbon dioxide, facilitate low-energy carbon dioxide capture, and greatly reduce the oxygen consumption and corresponding cost required for oxygen-enriched combustion. In addition, through the cooperation of transcritical carbon dioxide cycle, Kalina cycle, humidification-dehumidification device and organic Rankine cycle, the waste heat of the solid oxide fuel cell tail gas and the cold energy of the liquefied petroleum gas can be recovered in stages, while ensuring the joint supply of fresh water, carbon dioxide, electricity, cold energy and other energy and substances.

[0004] In order to achieve the above purpose, the present application adopts the following technical solutions:

[0005] A biomass fuel-solid oxide fuel cell comprehensive energy system with CO2 capture function, comprising a top cycle system and a bottom cycle system.

[0006] The top cycle system comprises a solid oxide fuel cell, the cathode inlet of which is in communication with the ambient air, the anode inlet of which is in communication with biomass gas and water, the cathode outlet of which is in communication with the permeation side of a water-gas displacement membrane reactor, and the anode outlet of which is in communication with the supply side of the water-gas displacement membrane reactor. The supply side of the water-gas displacement membrane reactor is in communication with a combustion chamber, and the combustion chamber is directly connected with the ambient oxygen.

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

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

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

[0010] The humidifier-dehumidifier deeply recycles the solid oxide fuel cell anode flue gas waste heat through a third boiler, while condensing and removing the moisture in the flue gas;

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

[0012] The dehydrated flue gas is compressed by a carbon dioxide compressor, coupled with the liquefied petroleum gas cold energy through a first heat exchanger, and used for capturing carbon dioxide;

[0013] The liquefied petroleum gas cold energy is coupled with an external cooling unit through a second heat exchanger, and used for meeting the refrigeration demand of users.

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

[0015] In the top cycle, air is compressed by a first air compressor, and then reacts with biomass in a biomass gasifier to produce a high-temperature raw material composition, followed by removal of impurities and nitrogen by a first separator to obtain pure synthesis gas, and then the synthesis gas is introduced into a fuel compressor after releasing heat by a third air preheater and being pressurized, and mixed with water vapor in a mixer after being pressurized and heated by a water pump and a water preheater, and finally sent to the solid oxide fuel cell anode; the gas from the solid oxide fuel cell anode is sent to the supply side of the water-gas shift membrane reactor, and under the action of the pressure difference on both sides of the membrane, the water-gas shift membrane reactor selectively extracts hydrogen from the synthesis gas on the supply side to the permeation side, so that the water-gas shift reaction equilibrium moves to the product direction;

[0016] The hydrogen-poor synthesis gas from the supply side of the water-gas shift membrane reactor is introduced into a combustion chamber and combusted with oxygen in a stoichiometric number to ensure that the combustion products have a high carbon dioxide concentration;

[0017] The high-temperature combustion products from the combustion chamber are sequentially passed through the first air preheater and the water preheater to release heat, and then sequentially passed through the first boiler and the second boiler to drive a transcritical carbon dioxide cycle and a Kalina cycle to generate additional electric power; subsequently, the water vapor contained in the flue gas is condensed and separated in the process of generating fresh water by the third boiler driving a humidifier-dehumidifier; finally, the dehydrated flue gas is pressurized by the carbon dioxide compressor, condensed and liquefied by the low-temperature liquefied petroleum 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 circuit, in which air is pressurized by a second air compressor, heated by a first air preheater, a second air preheater and a third air preheater in sequence, and then sent to the cathode of the solid oxide fuel cell.

[0019] The cathode outlet gas of the solid oxide fuel cell is sent to the water-gas shift membrane reactor on the permeation side to react with hydrogen from the water-gas shift membrane reactor on the supply side to improve the energy grade, and then sequentially passed through a gas turbine to do work and a second air preheater to release heat, and finally driven by an organic Rankine cycle through a fourth boiler to be discharged to the atmosphere.

[0020] The liquefied petroleum gas is provided with a cold energy cascade recovery circuit, and the low-temperature liquefied petroleum gas is pressurized by a fourth working medium pump, sequentially passed through a third condenser, a first heat exchanger, a first condenser, a second condenser and a second heat exchanger to cool other working media, and at the same time, the low-temperature liquefied petroleum gas is warmed up and supplied to users.

[0021] Compared with the prior art, the beneficial effects of the present application are:

[0022] (1) The system of the present application combines solid oxide fuel cells, water-gas shift membrane reactors, oxygen-enriched combustion and liquefied petroleum gas cold energy utilization technology, and fully recovers the substances and energy in the tail gas of the system through reasonable arrangement of the heat exchangers, so as to realize low-energy-consumption carbon dioxide capture.

[0023] (2) The system of the present application realizes cascade recovery of the anode and cathode flue gas waste heat of the solid oxide fuel cell through transcritical carbon dioxide cycle, Kalina cycle, humidifier-dehumidifier, organic Rankine cycle, which can ensure efficient power generation and supply of multiple energy and substances.

[0024] (3) The system of the present application can realize cascade recovery of the cold energy of liquefied petroleum gas, improve the power generation efficiency of the system and reduce the power consumption of carbon dioxide capture through 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 DRAWINGS

[0025] Figure 1is a schematic structural diagram of a biomass fuel-solid oxide fuel cell comprehensive energy system with CO2 capture function of the present application;

[0026] 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: humidification-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; HUM: humidifier; Inv: inverter; KC: Kalina cycle; LNG: liquefied petroleum gas; M: mixer; ORC: organic Rankine cycle; P-I: first working medium pump; P-II: second working medium pump; P-III: third working medium pump; P-IV: fourth working medium 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; T-I: first turbine; T-II: second turbine; T-III: third turbine; TRCC: transcritical carbon dioxide cycle; TV: throttle valve; WGSMR: water-gas shift membrane reactor; WP: water pump; WPH: water preheater. DETAILED DESCRIPTION

[0027] The present application is further described below in conjunction with the accompanying drawings and examples.

[0028] It should be noted that the following detailed description is exemplary in nature and is intended to provide further description of the application. Unless otherwise defined, 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.

[0029] It is also to be understood that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting, as the scope of the exemplary embodiments of this application will be limited only by the appended claims. As used herein, unless the context clearly dictates otherwise, the use of the singular herein is intended to include the plural. Furthermore, to the extent that any term is used in the singular herein, we also intend that to include plural forms.

[0030] Example 1

[0031] The application discloses a biomass fuel-solid oxide fuel cell comprehensive energy system with CO2 capture function. Figure 1 The system is composed of a top cycle system and a bottom cycle system.

[0032] The top cycle system comprises a solid oxide fuel cell (SOFC), the cathode inlet of which is communicated with external air, the anode inlet of which is communicated with biomass gas and water, the cathode outlet of which is communicated with a water-gas shift membrane reactor (WGSMR) permeation side, and the anode outlet of which is communicated with a water-gas shift membrane reactor (WGSMR) supply side.

[0033] The bottom cycle system comprises a transcritical carbon dioxide cycle (TRCC), a Kalina cycle (KC), a humidification-dehumidification device (HDH) and an organic Rankine cycle (ORC).

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

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

[0036] The humidification-dehumidification device (HDH) deeply recycles the solid oxide fuel cell (SOFC) anode flue gas waste heat through a third boiler (HRVG-III) and removes the water in the flue gas.

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

[0038] The dehydrated flue gas is compressed by a carbon dioxide compressor (CC) and coupled with the liquefied petroleum gas cold energy through a first heat exchanger (HE-I) to capture carbon dioxide.

[0039] The liquefied petroleum gas cold energy is coupled with an external cooling unit through a second heat exchanger (HE-II) to meet the refrigeration demand of a user.

[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 shift membrane reactor WGSMR, an inverter Inv, a gas turbine GT;

[0041] The bottom cycle includes a transcritical carbon dioxide cycle TRCC, a Kalina cycle KC, a humidification-dehumidification device 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 T-I, a first regenerator RE-I, a first working fluid pump P-I, and a first condenser COND-I;

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

[0044] The humidification-dehumidification device HDH includes a third boiler HRVG-III, a humidifier HUM, and a dehumidifier DEH;

[0045] The organic Rankine cycle ORC includes a fourth boiler HRVG-IV, a third turbine T-III, a third regenerator RE-III, a third working fluid pump P-III, and a 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 is connected to the third air preheater APH-III after discharging impurities and waste gas;

[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 with the water preheater WPH, the third air preheater APH-III is connected with the fuel compressor FC, the fuel compressor FC and the water preheater WPH are connected with the mixer M, the third air preheater APH-III and the mixer M are connected with the solid oxide fuel cell SOFC, the solid oxide fuel cell SOFC is connected with the water gas shift membrane reactor WGSMR at the other end, the water gas shift membrane reactor WGSMR is also connected with the gas turbine GT and the combustion chamber AB, the gas turbine GT is connected with the second air preheater APH-II at the other end; the second air preheater APH-II is also connected with the fourth boiler HRVG-IV in the organic Rankine cycle ORC, at the same time, oxygen is added into the combustion chamber AB, and the combustion chamber AB is also connected with the first air preheater APH-I;

[0049] The fourth boiler HRVG-IV is also connected with the third turbine T-III and the third regenerator RE-III, the third turbine T-III is connected with the third regenerator RE-III, the third regenerator RE-III is connected with the third working medium pump P-III, the third working medium pump P-III is also connected with the third condenser COND-III, the third condenser COND-III is connected with the fourth working medium pump P-IV, and the fourth working medium pump P-IV is connected with the outside LNG; the third condenser COND-III is also connected with the first heat exchanger HE-I, the first heat exchanger HE-I is connected with the CO2 tank, the first heat exchanger HE-I is also connected with the carbon dioxide compressor CC, the carbon dioxide compressor CC is connected with the third boiler HRVG-III in the humidification-dehumidification device HDH, and the third boiler HRVG-III, the humidifier HUM and the dehumidifier DEH are connected with each other; the dehumidifier DEH is connected with the outside seawater;

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

[0051] The second boiler HRVG-II is also connected with the first boiler HRVG-I in the transcritical carbon dioxide cycle TRCC, the first boiler HRVG-I is connected with the first turbine T-I, the first turbine T-I is connected with the first regenerator RE-I, the first regenerator RE-I is connected with the first boiler HRVG-I, the first regenerator RE-I is also connected with the first working medium pump P-I, and the first working medium pump P-I is connected with the first condenser COND-I; the first condenser COND-I is also connected with the second condenser COND-II and the first heat exchanger HE-I respectively.

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

[0053] After the air 2 is compressed by the first air compressor AC-I, the air 2 is subjected to a gasification reaction with the biomass 1 in the biomass gasifier GAS to generate a high-temperature raw material synthesis product 4. Then, the impurities and nitrogen are removed by the first separator SEP-I to obtain pure synthesis gas 5. Subsequently, the synthesis gas 5 is introduced into the fuel compressor FC after releasing heat by the third air preheater APH-III and being subjected to pressure increase. The synthesis gas 5 is mixed with the water vapor 31 which is pressurized and heated by the water pump WP and the water preheater WPH in sequence in the mixer M. Finally, the synthesis gas 5 is sent to the anode of the solid oxide fuel cell SOFC. The anode gas 8 of the solid oxide fuel cell SOFC is subjected to an electrochemical reaction with the cathode air 23 to generate direct current, and the direct current is converted into alternating current by the inverter Inv. The reacted anode gas 9 is sent to the water-gas shift membrane reactor WGSMR supply side. Under the action of the pressure difference between the two sides of the membrane, the water-gas shift membrane reactor WGSMR selectively extracts hydrogen from the synthesis gas on the supply side to the permeation side, so that the water-gas shift reaction equilibrium moves to the product direction. Then, the hydrogen-depleted synthesis gas 10 is introduced into the combustion chamber to combust with the oxygen 32 in a stoichiometric amount to ensure that the combustion product 11 has a high carbon dioxide concentration. Subsequently, the high-temperature combustion product 11 is sequentially subjected to heat release by the first air preheater APH-I and the water preheater WPH, and then sequentially drives the transcritical carbon dioxide cycle TRCC and the Kalina cycle KC by the first boiler HRVG-I and the second boiler HRVG-II to generate additional power. Then, the third boiler HRVG-III drives the humidifier HUM and the dehumidifier DEH to operate, and seawater desalination is performed. 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, and then condensed and liquefied by the low-temperature liquefied petroleum gas 56 in the first heat exchanger HE-I. The dehydrated flue gas 16 is sent to the CO2 tank.

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

[0055] After being pressurized by the second air compressor AC-II, the air 19 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 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 circuit, the specific route is as follows:

[0057] After being pressurized by the fourth working fluid pump P-IV, liquefied petroleum natural gas (LNG, -161.5°C) passes 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 to cool other working fluids. The liquefied petroleum natural gas 60 is heated to approximately 7°C before being supplied to users. It should be noted that the liquefied petroleum natural gas 59 cools the external water 61 in the second heat exchanger HE-II, thereby meeting the user's cooling needs.

[0058] Operating principles of transcritical carbon dioxide cycle TRCC and organic Rankine cycle ORC:

[0059] The transcritical carbon dioxide cycle (TRCC) and the organic Rankine cycle (ORC) have similar operating principles but different working fluids. This system uses carbon dioxide and propane as the working fluids in the transcritical carbon dioxide cycle (TRCC) and the organic Rankine cycle (ORC), respectively. The working fluid is heated in boilers (HRVG-I and HRVG-IV) and expanded in turbines (TI and T-III) to provide power output. It is then precooled by regenerators (RE-I and RE-III) and liquefied by liquefied petroleum natural gas in condensers (COND-I and COND-III). Subsequently, the working fluid is pressurized by working fluid pumps (PI and P-III). Finally, the working fluid is preheated by regenerators (RE-I and RE-III) and returned to the boilers (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, then the second separator SEP-II separates the mixture 39 into two different streams, wherein the saturated steam 40 drives the second turbine T-II to rotate and do work on the outside; the hot saturated liquid 46 enters the second regenerator RE-II to heat the fluid 44 from the outlet of the second working fluid pump P-II, and after being cooled, it flows to the throttle valve TV to be throttled and depressurized, and then mixes with the fluid 41 from the second turbine T-II. The mixed fluid 42 is liquefied and condensed by the liquefied petroleum 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 returns to the second boiler HRVG-II.

[0062] The operation principle of the humidifier-dehumidifier HDH is as follows:

[0063] Firstly, the hot air stream 51 increases the temperature of the seawater 53 in the dehumidifier DEH, and the preheated stream 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, part of the pure water evaporates from the sprayed seawater, and the other part of the brine is discharged. The incoming air stream 52 mixes with the evaporated water and leaves the humidifier with higher humidity and temperature. Then, the humidified hot air 51 enters the dehumidifier DEH to give its energy to the incoming seawater and produce fresh water.

[0064] The above only describes the preferred embodiments of the present application and is not used to limit the present application. For those skilled in the art, the present application can have various modifications and changes. Any modification, equivalent replacement, improvement, etc. made within the spirit and principles of the present application shall be included in the protection scope of the present application.

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 includes 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 is used to recover the waste heat of the solid oxide fuel cell anode flue gas and the cold energy of the liquefied petroleum natural gas through the first boiler and the first condenser respectively; The Kalina cycle further recovers the waste heat of the solid oxide fuel cell anode flue gas and the cold energy of the liquefied petroleum natural gas through the second boiler and the second condenser respectively; The humidifier-dehumidifier 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; After being compressed by the CO2 compressor, the dehydrated flue gas is coupled with the cold energy of liquefied petroleum and natural gas through the first heat exchanger to capture CO2; 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: In the top cycle, air is compressed by the first air compressor and then reacts with biomass in a biomass gasifier to produce a high-temperature raw material synthesis product. Impurities and nitrogen are then removed by a first separator to obtain pure synthesis gas. The air is then introduced into a fuel compressor to increase the pressure after releasing heat through a third air preheater. The air is then mixed with water vapor that has been pressurized and heated by a water pump and a water preheater in a 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 products have a high carbon dioxide concentration; The high-temperature combustion products coming out of the combustion chamber release heat through the first air preheater and water preheater in sequence, and then drive the transcritical carbon dioxide cycle and Kalina cycle through the first boiler and the second boiler in sequence to generate additional electricity; then, the humidifier-dehumidifier is driven by the third boiler to produce fresh water. In this process, the water vapor contained in the flue gas is also condensed and separated; finally, the dehydrated flue gas is pressurized by the carbon dioxide compressor, condensed and liquefied by 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 air is pressurized by the second air compressor, heated in sequence by the first air preheater, the second air preheater and the third air preheater, 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 hydrogen from the supply side of the water-gas exchange membrane reactor to increase the energy quality. It then passes through the gas turbine to perform external work and the second air preheater to release heat. Finally, it 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 being pressurized by the fourth working fluid pump, the low-temperature liquefied petroleum natural gas 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, while the gas itself is heated and supplied to users.

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