Biomass hydrogen production coupled with carbon dioxide capture system and method

Abstract

This application relates to the field of biomass gasification technology and discloses a biomass hydrogen production coupled with carbon dioxide capture system and method. The system includes a fluidized bed pyrolysis purification coupled reactor and a hydrogen production regeneration coupled reactor. The hydrogen production regeneration coupled reactor is used to produce hydrogen and capture carbon dioxide, while the fluidized bed pyrolysis purification coupled reactor is used to provide a biomass pyrolysis gas source. The pyrolysis reactor performs a pyrolysis reaction on the biomass feedstock and discharges impurity-laden pyrolysis gas and pre-pyrolyzed biochar. The impurity-laden pyrolysis gas enters a first cyclone separator, and the pre-pyrolyzed biochar enters an axially moving bed to form a purified bed. The impurity-laden pyrolysis gas sequentially passes through the first cyclone separator and the axially moving bed to obtain clean pyrolysis gas. The clean pyrolysis gas is connected to the interior of the hydrogen production regeneration coupled reactor through a clean pyrolysis gas discharge pipe. This system fully pyrolyzes and purifies the biomass and provides clean pyrolysis gas to the hydrogen production regeneration coupled reactor, thereby achieving the acquisition of high-purity hydrogen-containing gas during the hydrogen production process.

Description

Technical Field

[0001] This application belongs to the field of biomass gasification technology, specifically relating to a biomass hydrogen production coupled carbon dioxide capture system and a method for using the system. Background Technology

[0002] Biomass gasification for hydrogen production is one of the most promising hydrogen production technologies currently available. It converts biomass pyrolysis gas into gaseous products, mainly H2, CO, CO2 and CH4, through high-temperature cracking.

[0003] In existing technologies, fluidized bed pyrolysis of biomass is commonly used. However, the biomass pyrolysis gas produced generally contains various impurities such as tar, dust, and hydrogen sulfide. Traditional technologies often rely on catalytic reforming processes for purification, but this approach faces problems such as catalyst carbonization, coking, and poisoning deactivation in practical applications, resulting in significant catalyst loss and poor operational stability within the system. Summary of the Invention

[0004] The purpose of this application is to provide a biomass hydrogen production coupled with carbon dioxide capture system, which aims to fully pyrolyze and purify biomass to obtain high-purity hydrogen-containing gas during the hydrogen production process.

[0005] To achieve the above objectives, this application provides a biomass hydrogen production coupled with carbon dioxide capture system, comprising a fluidized bed pyrolysis purification coupled reactor and a hydrogen production regeneration coupled reactor. The hydrogen production regeneration coupled reactor is used to produce hydrogen and capture carbon dioxide, and the fluidized bed pyrolysis purification coupled reactor is used to provide a biomass pyrolysis gas source and includes: The pyrolysis reactor is equipped with a gas phase outlet for discharging impurities in the pyrolysis gas and a solid phase outlet for discharging the pre-pyrolyzed biochar. A multi-mechanism coupled purifier includes a first cyclone separator and an axially moving bed arranged coaxially. The gas phase outlet is connected to the inlet of the first cyclone separator, and the solid phase outlet is connected to the axially moving bed to form a purification bed. The gas outlet of the first cyclone separator is connected to the axially moving bed. A circulating conveying assembly is used to return the preliminary pyrolytic biochar to the pyrolysis reactor, and the circulating conveying assembly is connected between the outlet of the axially moving bed and the pyrolysis reactor; A clean pyrolysis gas discharge pipe is used to connect the biomass pyrolysis gas discharged from the axially moving bed to the interior of the hydrogen production and regeneration coupling reactor.

[0006] In some embodiments, the cyclic conveying assembly includes: A spouted bed is disposed inside the pyrolysis reactor; The conveying and lifting pipe has one end connected to the outlet of the axially moving bed, and the other end extends from the bottom of the pyrolysis reactor and is connected to the inlet of the spouting bed.

[0007] In some embodiments, the fluidized bed pyrolysis purification coupled reactor further includes an ash hopper for storing solid particles separated from the first cyclone separator, the ash hopper being located at the bottom of the multi-mechanism coupled purifier.

[0008] In some embodiments, the hydrogen production-regeneration coupling reactor includes: A hydrogen production reactor for generating hydrogen gas, wherein the hydrogen production reactor is filled with a catalyst and a carbon dioxide adsorbent and is connected to the biomass pyrolysis gas source and a steam source; A regeneration reactor, located on top of the hydrogen production reactor, is used to regenerate the catalyst and the carbon dioxide adsorbent and generate carbon dioxide. A riser is used to transport the catalyst and carbon dioxide adsorbent after reaction in the hydrogen production reactor to the regeneration reactor; The stripping section is used to recover the regenerated catalyst and the carbon dioxide adsorbent. The inlet of the stripping section is connected to the regenerated solids outlet of the regeneration reactor, and the outlet of the stripping section is connected to the hydrogen production reactor.

[0009] In some embodiments, the stripping section is arranged inside the hydrogen production reactor, the bottom of the hydrogen production reactor forms a regenerated solids buffer zone and a reaction zone located radially outside the regenerated solids buffer zone, the stripping section's feed leg extends downward into the interior of the regenerated solids buffer zone, and the outlet of the regenerated solids buffer zone communicates with the reaction zone.

[0010] In some embodiments, the hydrogen production reactor is provided with a second cyclone separator for hydrogen filtration inside, the discharge pipe of the second cyclone separator extends to the outside of the hydrogen production reactor, and the cyclone separator's cyclone separator's swirl legs extend downward to the reaction zone.

[0011] In some embodiments, the regeneration reactor includes: Regenerator cylinder; A regeneration heating device is installed on the outer side of the regenerator cylinder; A regenerated gas distributor, used to supply steam and oxygen, is arranged at the bottom of the regenerator cylinder; A cyclone separator for filtering carbon dioxide includes a primary cyclone separator and a secondary cyclone separator connected in series. The discharge pipe of the secondary cyclone separator extends to the outside of the regenerator cylinder, and the cyclone separator's cyclone feed leg is connected to the inlet of the stripping section.

[0012] In some embodiments, the fluidized bed pyrolysis purification coupled reactor further includes a reaction vessel, in which the pyrolysis reactor, the multi-mechanism coupled purifier, and the circulation conveying assembly are integrated. The reaction vessel is provided with a baffle plate, which is used to divide the space inside the reaction vessel into a pyrolysis gas containing impurities zone, a clean pyrolysis gas zone, and a biochar accumulation zone from top to bottom. The clean pyrolysis gas discharge pipe is connected to the clean pyrolysis gas zone.

[0013] A second aspect of this application provides a method for biomass-based hydrogen production coupled with carbon dioxide capture, the method employing the aforementioned biomass-based hydrogen production coupled with carbon dioxide capture system, and comprising: Step 1: The biomass raw material is fed into the pyrolysis reactor, and oxygen and water vapor are introduced into the first pyrolysis gas distributor at the bottom of the pyrolysis reactor. The biomass raw material undergoes a pyrolysis reaction in the pyrolysis reactor, generating impurity-containing pyrolysis gas and preliminary pyrolysis biochar. The impurity-containing pyrolysis gas is transported to the first cyclone separator through the gas phase outlet, and the preliminary pyrolysis biochar is transported to the axial moving bed through the solid phase outlet to form a filtration and purification bed. Step 2: The impurity-containing pyrolysis gas is passed sequentially through the first cyclone separator and the axial moving bed, and then enters the interior of the hydrogen production and regeneration coupling reactor through the clean pyrolysis gas discharge pipe.

[0014] In some embodiments, the method further includes: Step 3: The clean pyrolysis gas and steam from Step 2 are introduced into the hydrogen production reactor as fluidizing gas. The fluidizing gas is mixed with the catalyst and carbon dioxide adsorbent in the hydrogen production reactor to form a fluidized mixture. Under the action of the catalyst, the biomass pyrolysis gas is converted into hydrogen, carbon monoxide and carbon dioxide. The carbon dioxide reacts with the carbon dioxide adsorbent and is converted into calcium carbonate. The hydrogen is discharged from the hydrogen production reactor. Step 4: The catalyst and carbon dioxide adsorbent after reaction in the hydrogen production reactor are transported to the regeneration reactor through the riser for high-temperature calcination, so that the carbonate is decomposed into carbon dioxide and the regenerated carbon dioxide adsorbent, while the catalyst is restored to activity, and the carbon dioxide is discharged from the regeneration reactor. Step 5: The regenerated solids discharged from the regeneration reactor are sent back to the hydrogen production reactor through the stripping section.

[0015] The biomass hydrogen production coupled carbon dioxide capture system according to the present invention includes a fluidized bed pyrolysis purification coupled reactor and a hydrogen production regeneration coupled reactor. The fluidized bed pyrolysis purification coupled reactor is used to provide a biomass pyrolysis gas source, and the hydrogen production regeneration coupled reactor is used to produce hydrogen and capture carbon dioxide. The fluidized bed pyrolysis purification coupled reactor includes a pyrolysis reactor, a multi-mechanism coupled purifier, a circulation conveying assembly, and a clean pyrolysis gas discharge pipe. The pyrolysis reactor performs a pyrolysis reaction on the biomass feedstock and discharges impurity-containing pyrolysis gas and preliminary pyrolysis biochar. The impurity-containing pyrolysis gas enters the first cyclone separator of the multi-mechanism coupled purifier, and the preliminary pyrolysis biochar enters the axial moving bed of the multi-mechanism coupled purifier to form a purified bed. The impurity-containing pyrolysis gas passes sequentially through the first cyclone separator and the axial moving bed to obtain clean pyrolysis gas. The clean pyrolysis gas is connected to the interior of the hydrogen production regeneration coupled reactor through the clean pyrolysis gas discharge pipe. By employing a fluidized bed pyrolysis purification coupled reactor to efficiently pyrolyze and finely purify biomass and provide clean biomass pyrolysis gas to the hydrogen production regeneration coupled reactor, the technology effectively avoids phenomena such as catalyst carbon buildup, coking, poisoning, and deactivation during subsequent hydrogen production processes.

[0016] Other features and advantages of the embodiments of this application will be described in detail in the following detailed description section. Attached Figure Description

[0017] The accompanying drawings are provided to further illustrate the embodiments of this application and form part of the specification. They are used together with the following detailed description to explain the embodiments of this application, but do not constitute a limitation on the embodiments of this application. For those skilled in the art, other drawings can be obtained based on the structures shown in these drawings without any inventive effort. In the drawings: Figure 1 This is a schematic diagram of the structure of the first embodiment of the biomass hydrogen production coupled carbon dioxide capture system of the present invention; Figure 2 This is a schematic diagram of another embodiment of the fluidized bed pyrolysis purification coupled reactor of the present invention; Figure 3 This is a schematic diagram of another embodiment of the fluidized bed pyrolysis purification coupled reactor of the present invention; Figure 4 This is a schematic diagram of another embodiment of the fluidized bed pyrolysis purification coupled reactor of the present invention; Figure 5 The graph shows experimental data on the separation efficiency of the multi-mechanism coupling purifier of this invention.

[0018] Explanation of reference numerals in the attached figures Biomass hydrogen production coupled with carbon dioxide capture system 100; Hydrogen production reactor 11; regenerated solid buffer zone 111; reaction zone 112; second cyclone separator 113; circulation pipe 114; circulation pipe valve 115; second pyrolysis gas distributor 116; Regeneration reactor 12; regenerator cylinder 121; regeneration heating device 122; regeneration gas distributor 123; primary cyclone separator 124; secondary cyclone separator 125; Lift pipe 13; 14 stripping section; 141 stripping section cylinder; 142 baffle; Fluidized bed pyrolysis purification coupled reactor 15; pyrolysis reactor 151; first pyrolysis gas distributor 1511; gas phase outlet 1512; solid phase outlet 1513; multi-mechanism coupled purifier 152; first cyclone separator 1521; axial moving bed 1522; buffer space 1523; conveying and lifting pipe 153; spouted bed 154; clean pyrolysis gas discharge pipe 155; reaction vessel 156; outer shell 157; upper baffle of gas chamber 158; lower baffle of gas chamber 159; ash hopper 160. Detailed Implementation

[0019] The specific embodiments of this application will be described in detail below with reference to the accompanying drawings. It should be understood that the specific embodiments described herein are for illustration and explanation only and are not intended to limit this application.

[0020] This invention proposes a biomass hydrogen production coupled carbon dioxide capture system 100, which realizes the effective utilization of carbon dioxide while producing hydrogen from biomass.

[0021] It should be noted that, unless otherwise specified, the embodiments and features described in the present invention can be combined with each other.

[0022] In the embodiments of the present invention, unless otherwise stated, directional terms such as "upper," "lower," "top," and "bottom" are generally used to describe the relative positional relationships of the components in relation to the directions shown in the accompanying drawings or in relation to the vertical, perpendicular, or gravitational directions.

[0023] To better understand the above technical solutions, the following will provide a detailed explanation of the technical solutions in conjunction with the accompanying drawings and specific implementation methods.

[0024] In some specific embodiments of the present invention, such as Figures 1 to 4 As shown, the biomass hydrogen production coupled carbon dioxide capture system 100 includes a fluidized bed pyrolysis purification coupled reactor 15 and a hydrogen production regeneration coupled reactor. The hydrogen production regeneration coupled reactor is used to produce hydrogen and capture carbon dioxide, while the fluidized bed pyrolysis purification coupled reactor 15 is used to provide a biomass pyrolysis gas source. The fluidized bed pyrolysis purification coupled reactor 15 has different implementations.

[0025] like Figure 1 As shown, in the first embodiment of the fluidized bed pyrolysis purification coupled reactor 15, the fluidized bed pyrolysis purification coupled reactor 15 includes a pyrolysis reactor 151, a multi-mechanism coupled purifier 152, a circulation conveying assembly, and a clean pyrolysis gas discharge pipe 155. The pyrolysis reactor 151 is provided with a gas phase outlet 1512 for discharging impurity-containing pyrolysis gas and a solid phase outlet 1513 for discharging partially pyrolyzed biochar. The multi-mechanism coupled purifier 152 includes a first cyclone separator 1521 and an axially moving bed 1522 arranged coaxially. The gas phase outlet 151... 2 is connected to the inlet of the first cyclone separator 1521, and the solid phase outlet 1513 is connected to the axial moving bed 1522 to form a purified bed. The gas outlet of the first cyclone separator 1521 is connected to the axial moving bed 1522. The circulation conveying assembly is used to send the pre-pyrolyzed biochar back to the pyrolysis reactor 151. The circulation conveying assembly is connected between the outlet of the axial moving bed 1522 and the pyrolysis reactor 151. The clean pyrolysis gas discharge pipe 155 is used to connect the biomass pyrolysis gas discharged from the axial moving bed 1522 to the interior of the hydrogen production and regeneration coupling reactor.

[0026] The pyrolysis reactor 151 is a fluidized bed, and the reaction temperature is maintained at 500℃~700℃. The bottom of the pyrolysis reactor 151 is equipped with a first pyrolysis gas distributor 1511 for introducing oxygen and water vapor as fluidizing gases. The pyrolysis reactor 151 is equipped with a feeding device for adding biomass, and a solid phase outlet 1513 is provided at the bottom for discharging the preliminary pyrolysis biochar. A gas phase outlet 1512 is provided on the side near the top for discharging the impurity pyrolysis gas. The components of the impurity pyrolysis gas include carbon monoxide, carbon dioxide, water, methane, small molecule hydrocarbons, tar, and biochar particles.

[0027] The multi-mechanism coupled purifier 152 includes a coaxially arranged axially moving bed 1522 and a first cyclone separator 1521 in a nested structure. The axially moving bed 1522 is located outside the first cyclone separator 1521. The height of the axially moving bed 1522 is 0.1m to 1.5m, and the thickness of the filtration and purification bed is not less than 50mm. The first cyclone separator 1521 adopts a cyclone-particle bed coupled purifier. The gas phase outlet 1512 of the pyrolysis reactor 151 is connected to the tangential inlet of the first cyclone separator 1521, and the solid phase outlet 1513 of the pyrolysis reactor 151 is connected to the moving bed hopper at the top of the multi-mechanism coupled purifier 152. The preliminary pyrolysis biochar in the moving bed hopper eventually enters the axially moving bed 1522 and serves as a filtration and purification bed for filtering impurities in the pyrolysis gas. The top central exhaust pipe of the first cyclone separator 1521 is connected to the buffer space 1523 within the multi-mechanism coupled purifier 152. The bottom feed leg of the first cyclone separator 1521 is connected to the bottom ash hopper 160, which is used to store the solid particles separated from the first cyclone separator 1521, i.e., fully pyrolyzed biochar. The bottom of the axially moving bed 1522 has multiple gas outlets arranged tangentially. The clean pyrolysis gas discharge pipe 155 is connected to the gas outlets and is used to connect the clean biomass pyrolysis gas discharged from the axially moving bed 1522 to the interior of the hydrogen production reactor 11. Furthermore, multiple multi-mechanism coupled purifiers 152 can be provided and symmetrically arranged outside the pyrolysis reactor 151. By increasing the number of multi-mechanism coupled purifiers 152 and arranging them appropriately, the purification efficiency can be improved.

[0028] To verify the separation efficiency of the multi-mechanism coupled purifier 152, a large-scale cold-state simulation experimental platform was built, and a systematic study was conducted on the core working principle, purification performance, and operational stability of the multi-mechanism coupled purifier 152. Please refer to... Figure 5 Separation efficiency experimental data show that, under different operating conditions, the separation efficiency of the multi-mechanism coupled purifier 152 for the target pollutants remains consistently above 99.3%, demonstrating strong adaptability to various operating conditions. Particularly under fixed operating conditions of inlet gas flow rate Qin = 80 m³ / h and inlet dust concentration Cin = 60 g / m³, after long-term continuous operation testing, the pressure drop fluctuation of the multi-mechanism coupled purifier 152 was controlled within a very small range, exhibiting excellent operational stability and reliability. Notably, when the bed thickness of the axially moving bed 1522 reaches the optimized design range (i.e., a thicker bed state), the separation efficiency of the multi-mechanism coupled purifier 152 can be further improved to 99.99%, meaning it can deeply remove fine dust and impurities from biomass pyrolysis gas, fully meeting the stringent requirements for gas source purity in subsequent processing and utilization of biomass pyrolysis gas, and providing key technical support for the clean and efficient conversion of biomass energy.

[0029] The circulating conveying assembly includes a conveying riser pipe 153 and a sputtering bed 154, wherein the sputtering bed 154 is disposed inside the pyrolysis reactor 151. One end of the conveying riser pipe 153 is connected to the discharge port of the axially moving bed 1522, and the other end extends from the bottom of the pyrolysis reactor 151 and is connected to the inlet of the sputtering bed 154. Specifically, the discharge cone at the bottom of the axially moving bed 1522 is connected to the riser pipe 13 and the sputtering bed 154 disposed inside the multi-mechanism coupling purifier 152 via a hopper inclined pipe. The sputtering bed 154 is also connected to the lower part of the pyrolysis reactor 151 and has an exhaust port on its side.

[0030] Furthermore, the fluidized bed pyrolysis purification coupled reactor 15 also includes an ash hopper 160 for storing solid particles separated from the first cyclone separator 1521, the ash hopper 160 being located at the bottom of the multi-mechanism coupled purifier 152.

[0031] During operation, biomass feedstock enters the pyrolysis reactor 151 through the feeding device. Oxygen and steam are introduced into the pyrolysis reactor 151 from the first pyrolysis gas distributor 1511 at the bottom as fluidizing gas and pyrolysis medium. The biomass undergoes pyrolysis to produce impurity-laden pyrolysis gas and preliminary pyrolysis biochar. The impurity-laden pyrolysis gas is discharged from the top of the pyrolysis reactor 151 and enters the first cyclone separator 1521 through a tangential inlet. Centrifugal separation is performed in the first cyclone separator 1521 to remove most of the dust. The gas flow upwards through the top central exhaust pipe into the buffer space 1523, and then the gas flow downwards into the axially moving bed 1522. Residual tar and dust are removed by the filtration and purification bed (composed of preliminary pyrolysis biochar from the pyrolysis reactor 151), resulting in clean biomass pyrolysis gas. The biomass pyrolysis gas is discharged through the gas outlet of the axially moving bed 1522 and sent to the bottom of the hydrogen production reactor 11 through the clean pyrolysis gas discharge pipe 155. The filtered biochar is discharged from the feed cone at the bottom of the axially moving bed 1522, and then sent back to the pyrolysis reactor 151 via the riser 13 and the spouted bed 154, realizing the recycling of biochar. At the same time, the biochar separated by the first cyclone separator 1521 continues to fall through the material legs separated by the first cyclone separator 1521, and finally collects in the ash hopper 160 for centralized collection and sealed storage to prevent impurities from being dispersed again.

[0032] This invention employs a fluidized bed pyrolysis purification coupled reactor 15 to prepare clean biomass pyrolysis gas. This reactor can efficiently pyrolyze biomass first, simultaneously achieving full conversion and fine purification of the pyrolysis products, thus effectively avoiding problems such as catalyst carbon buildup, coking, and poisoning deactivation during subsequent hydrogen production. This system integrates biomass adsorption-enhanced hydrogen production, in-situ carbon dioxide conversion, and catalyst / adsorbent regeneration and recycling, fully utilizing the sensible and latent heat of the pyrolysis oil and gas to form a closed-loop internal recycling system for materials and energy, ultimately producing high-quality hydrogen-rich gas, carbon dioxide-rich gas, and biochar byproducts, opening a new path for the efficient and clean utilization of biomass energy.

[0033] like Figure 2 As shown, in the second embodiment of the fluidized bed pyrolysis purification coupled reactor 15, an outer shell 157 is added to the outside of the fluidized bed pyrolysis purification reactor. In addition to basic protection and heat insulation functions, the outer shell 157 also has a clean pyrolysis gas outlet. The clean pyrolysis gas outlet is precisely connected to the clean pyrolysis gas discharge pipe 155 through a sealed connection structure, ensuring no leakage during gas transmission. The improvement of this embodiment lies in that the purified pyrolysis gas is briefly retained in a sealed cavity formed between the outer shell 157 and the reactor body before being discharged. The residual heat carried by the gas acts in reverse on the core area of ​​the fluidized bed pyrolysis reaction, forming a highly efficient heat recycling mechanism, thereby significantly reducing heat loss during operation and improving energy utilization efficiency. Simultaneously, due to the independent installation of the outer shell 157, the insulation structure can be directly integrated and installed on the outer surface or in the inner and outer layers of the outer shell 157, without requiring complex modifications to the reactor body. This not only simplifies the insulation construction process but also reduces the amount of insulation material used and construction costs through centralized insulation design, further reducing the overall operating cost of the entire device.

[0034] like Figure 3 As shown, in the third embodiment of the fluidized bed pyrolysis purification coupled reactor 15, the feed inlet of the axially moving bed 1522 is located on the side. The improvement of this embodiment is that it enables the feed flow of the axially moving bed 1522 to form a forward flow relationship with the gas flow discharged from the central exhaust pipe at the top of the first cyclone separator 1521, thereby completely avoiding airflow interference problems that may be caused by countercurrent contact. Crucially, this arrangement effectively eliminates the bridging and blockage phenomenon caused by airflow collision and particle accumulation during the transport of pre-pyrolyzed biochar in the biochar conveying pipe, ensuring the continuity and stability of material transport, and thus improving the operating efficiency of the entire reaction system.

[0035] like Figure 4As shown, in the fourth embodiment of the fluidized bed pyrolysis purification coupled reactor 15, the fluidized bed pyrolysis purification coupled reactor 15 further includes a reaction tank 156. The pyrolysis reactor 151, the multi-mechanism coupled purifier 152 and the circulation conveying assembly are integrated in the reaction tank 156. The reaction tank 156 is provided with a partition, which is used to divide the space in the reaction tank 156 into a pyrolysis gas containing impurities zone, a clean pyrolysis gas zone and a biochar accumulation zone from top to bottom. The clean pyrolysis gas discharge pipe 155 is connected to the clean pyrolysis gas zone.

[0036] Specifically, in this embodiment, the first cyclone separator 1521 adopts an axial flow cyclone separator-particle bed coupled purifier. Compared with the traditional tangential inlet cyclone separator, the axial flow structure has advantages in gas-solid separation efficiency and fluid resistance control, and can achieve efficient dust removal at a low pressure drop. It is especially suitable for compact layouts that are integrated with the axial moving bed 1522 in the same housing 157.

[0037] Meanwhile, to achieve equipment integration and improve space utilization, the pyrolysis reactor 151, the multi-mechanism coupled purifier 152, and the circulation conveying assembly are integrated into the same reaction tank 156. To clearly define functional zones and ensure the stability of each process step, an upper baffle 158 and a lower baffle 159 are added to the reaction tank 156. Through the isolation effect of the upper baffle 158 and the lower baffle 159, the space inside the reaction tank 156 is divided into three independent areas: the upper impurity-containing pyrolysis gas zone, used to temporarily store the newly generated impurity-containing pyrolysis gas carrying solid impurities; the middle clean pyrolysis gas zone, serving as a temporary storage and export area for purified and qualified gas; and the lower biochar accumulation zone, specifically used to collect biochar byproducts generated by the pyrolysis reaction. This zoning design ensures that the pyrolysis, purification, and product collection processes proceed in an orderly and efficient manner.

[0038] In this embodiment, the pyrolysis gas exhaust pipe containing impurities is located in the upper region of the pyrolysis reactor 151, used to directionally discharge the pyrolysis gas containing impurities generated in the reactor to a preset pyrolysis gas containing impurities zone. The discharged pyrolysis gas continues to descend along the axial channel of the exhaust pipe, smoothly entering the inlet pipe of the axial flow vortex separator-particle bed coupled purifier located below. Under the precise guidance and diversion effect of the guide vanes inside the inlet pipe, the pyrolysis gas containing impurities gradually forms a high-speed rotating airflow field. This airflow field, utilizing the principle of centrifugal separation, efficiently separates and removes most of the solid impurities (such as dust, carbon particles, etc.) carried in the pyrolysis gas. The separated impurities continue to fall along the feed leg under gravity, eventually collecting in the ash hopper 160 at the bottom of the fluidized bed pyrolysis purification reactor, and then being centrally collected and sealed for storage via the bottom outlet to prevent secondary dispersion of impurities.

[0039] This embodiment further enhances the integration level of the biomass pyrolysis and purification system, effectively reducing heat loss. This solution optimizes the layout of core equipment, integrates key processes of pyrolysis reaction and purification treatment, and comprehensively strengthens the overall system integration. Simultaneously, it achieves a compact design for the pyrolysis reactor 151, purification device, and supporting pipelines, and embeds a heat recovery loop, allowing each unit of the system to form a highly efficient and collaborative operating closed loop. This highly integrated design reduces heat conduction loss at equipment connection points from the source, avoiding the radiation and convection heat dissipation problems caused by airflow and equipment gaps in traditional split systems. It significantly improves thermal energy utilization efficiency, minimizes heat loss, and lays a reliable foundation for energy-saving and efficient operation of the biomass conversion process.

[0040] In some specific embodiments of this utility model, the hydrogen production and regeneration coupled reactor includes a hydrogen production reactor 11, a regeneration reactor 12, a riser 13, and a stripping section 14. The hydrogen production reactor 11 is used to generate hydrogen gas and is filled with a catalyst and a carbon dioxide adsorbent, and is connected to a biomass pyrolysis gas source and a steam source. The regeneration reactor 12 is located at the top of the hydrogen production reactor 11 and is used to regenerate the catalyst and carbon dioxide adsorbent and generate carbon dioxide. The riser 13 is used to transport the reacted catalyst and carbon dioxide adsorbent from the hydrogen production reactor 11 to the regeneration reactor 12. The stripping section 14 is used to recover the regenerated catalyst and carbon dioxide adsorbent. The inlet of the stripping section 14 is connected to the regenerated solid outlet of the regeneration reactor 12, and the outlet of the stripping section 14 is connected to the hydrogen production reactor 11.

[0041] Understandably, the biomass pyrolysis gas source can be implemented in various forms, such as a fluidized bed pyrolysis purification coupled reactor 15, a fixed bed pyrolysis reactor 151, or a moving bed pyrolysis reactor 151, as long as it can provide biomass pyrolysis gas that meets the requirements of the hydrogen production reaction. The embodiments of the present invention are illustrated using a fluidized bed pyrolysis purification coupled reactor 15 as an example, but the scope of protection of the present invention is not limited thereto.

[0042] Specifically, the hydrogen production reactor 11 is a vertical vessel, with the reaction temperature maintained at 650℃~750℃. A steam pipe and a second pyrolysis gas distributor 116 are located at the bottom of the reactor. The steam pipe is connected to an external steam source, and the inlet of the second pyrolysis gas distributor 116 is connected to an external biomass pyrolysis gas source. In one specific embodiment, the inlet of the second pyrolysis gas distributor 116 is connected to the clean pyrolysis gas outlet pipe 155 of the fluidized bed pyrolysis purification coupled reactor 15. Simultaneously, the bottom of the hydrogen production reactor 11 is filled with a catalyst and a carbon dioxide adsorbent. The catalyst has a particle size of 20μm~80μm, and the carbon dioxide adsorbent has a particle size of 80μm~200μm. The content of the catalyst and carbon dioxide adsorbent is determined by the inlet volume of biomass pyrolysis gas. A gas outlet is located near the top of the hydrogen production reactor 11, from which the hydrogen-rich synthesis gas released during the process is discharged.

[0043] The regeneration reactor 12 is located on top of the hydrogen production reactor 11, and the reaction temperature is maintained at 750℃~950℃. The bottom part of the regeneration reactor 12 extends into the interior of the hydrogen production reactor 11, achieving a compact structure. The connection between the regeneration reactor 12 and the hydrogen production reactor 11 is sealed, such as by flange connection or direct welding to form an integral unit. The regeneration reactor 12 is used to receive the spent catalyst and spent carbon dioxide adsorbent from the hydrogen production reactor 11. Taking calcium carbonate as an example, the spent carbon dioxide adsorbent is calcined at high temperature to decompose the calcium carbonate into carbon dioxide and calcium oxide. At the same time, the carbon deposits on the catalyst surface are burned off, restoring its activity. The top of the regeneration reactor 12 is provided with a gas outlet, from which the carbon dioxide-rich gas released during the process is discharged.

[0044] A circulation pipe 114 is provided on the side of the hydrogen production reactor 11. One end of the circulation pipe 114 is connected to the lower or middle part of the hydrogen production reactor 11 to draw out the spent catalyst and spent carbon dioxide adsorbent after the reaction. The inlet height of the circulation pipe 114 is set according to the fluidization layer height of the fluidized bed in the hydrogen production reactor 11 to ensure smooth drawing out of the spent solid particles. A circulation pipe valve 115 is provided on the circulation pipe 114 to control the flow rate and on / off of the spent material. The other end of the circulation pipe 114 is connected to the pre-lifting section at the lower end of the riser pipe 13. A conveying gas inlet is provided at the bottom of the pre-lifting section for introducing conveying gas. The riser pipe 13 is set vertically, and the outlet pipe of the riser pipe 13 extends into the interior of the regeneration reactor 12. During operation, the circulation pipe valve 115 is opened, and the spent catalyst and spent carbon dioxide adsorbent enter the pre-lifting section of the riser pipe 13 from the hydrogen production reactor 11 through the circulation pipe 114. Under the action of the conveying gas, they are lifted and sent into the interior of the regeneration reactor 12 for high-temperature regeneration.

[0045] The inlet of the stripping section 14 is connected to the regenerated solids outlet of the regeneration reactor 12, and the outlet of the stripping section 14 is connected to the hydrogen production reactor 11. The stripping section 14 is used to recover the regenerated catalyst and adsorbent and return them to the hydrogen production reactor 11, forming a closed loop. In some specific embodiments, the stripping section 14 is arranged inside the hydrogen production reactor 11. Specifically, the stripping section 14 is coaxially mounted inside the upper part of the hydrogen production reactor 11, with its top serving as the inlet and closely attached to the bottom of the regeneration reactor 12. The top inlet of the stripping section 14 is connected to the solids outlet of the regeneration reactor 12, and the bottom feed leg of the stripping section 14 extends downward to the lower part of the hydrogen production reactor 11. This built-in design makes the structure more compact, reduces external connection pipelines, and lowers heat loss.

[0046] This invention is implemented as follows: a hydrogen production reactor 11, a regeneration reactor 12, a riser 13, and a stripping section 14 are integrated into a single unit. Clean biomass pyrolysis gas and steam are mixed and fed into the hydrogen production reactor 11 as fluidizing gas. There, they are mixed and fluidized with the catalyst and carbon dioxide adsorbent inside the reactor, converting into hydrogen, carbon monoxide, and carbon dioxide. Carbon dioxide is adsorbed by the carbon dioxide adsorbent to form calcium carbonate, and the hydrogen-rich gas is discharged and collected from the gas outlet of the hydrogen production reactor 11. The catalyst, carbon dioxide adsorbent, and calcium carbonate remaining after the reaction in the hydrogen production reactor 11 are transported by the riser 13 to the high-temperature reaction zone 112 of the top regeneration reactor 12, where catalyst regeneration and adsorbent desorption are completed. The removed carbon dioxide-rich gas is discharged and collected from the gas outlet of the regeneration reactor 12. Subsequently, the regenerated solid material enters the lower stripping section 14 for further carbon dioxide removal and is returned to the hydrogen production reactor 11. Through this invention, the hydrogen content in the hydrogen-rich gas is not less than 85 vol.%, and the carbon dioxide enrichment concentration in the carbon dioxide-rich gas is not less than 90 vol.%.

[0047] In some implementations, such as Figures 1 to 4 As shown, a regenerated solid buffer zone 111 and a reaction zone 112 located radially outside the regenerated solid buffer zone 111 are formed at the bottom of the hydrogen production reactor 11. The feed leg of the stripping section 14 extends downward into the interior of the regenerated solid buffer zone 111, and the outlet of the regenerated solid buffer zone 111 is connected to the reaction zone 112.

[0048] Specifically, the regenerated solids buffer zone 111 is located in the central region at the bottom of the hydrogen production reactor 11, and is used to collect the regenerated solids from the stripping section 14. The reaction zone 112 is located radially outside the regenerated solids buffer zone 111, and is filled with catalyst and carbon dioxide adsorbent, and is connected to biomass pyrolysis gas and steam. The feed leg of the stripping section 14 extends downward into the interior of the regenerated solids buffer zone 111, allowing the regenerated catalyst and carbon dioxide adsorbent to fall into the regenerated solids buffer zone 111. The regenerated solids buffer zone 111 is provided with an outlet communicating with the reaction zone 112. When the regenerated solids in the regenerated solids buffer zone 111 accumulate to a certain height, they can enter the reaction zone 112 through the outlet, come into contact with the introduced biomass pyrolysis gas and steam, and undergo a hydrogen production reaction.

[0049] like Figures 1 to 4 As shown, the hydrogen production reactor 11 is equipped with a second cyclone separator 113 for hydrogen filtration inside. The discharge pipe of the second cyclone separator 113 extends to the outside of the hydrogen production reactor 11, and the cyclone separator 113's cyclone separator leg extends downward to the reaction zone 112.

[0050] Specifically, the second cyclone separator 113 is installed at the top of the hydrogen production reactor 11 to filter solid particles entrained in the hydrogen-rich synthesis gas. The discharge pipe of the second cyclone separator 113 extends upward and extends to the outside of the hydrogen production reactor 11 through the gas outlet of the hydrogen production reactor 11. The cyclone separator 113's separating legs extend downward to the reaction zone 112, ensuring that the separated solid particles (mainly catalyst and adsorbent) are returned to the reaction zone 112, thereby realizing the internal circulation of solid particles.

[0051] like Figures 1 to 4 As shown, the stripping section 14 includes a stripping section cylinder 141 and a baffle 142 disposed inside the stripping section cylinder 141. The top of the stripping section cylinder 141 is provided with an inlet that communicates with the recycled solids outlet, and the bottom of the stripping section cylinder 141 is connected to a steam source.

[0052] Specifically, the stripping section cylinder 141 is equipped with multiple layers of herringbone-shaped baffles 142. The regenerated catalyst and carbon dioxide adsorbent enter the stripping section 141 from the top inlet and flow downwards along the herringbone-shaped baffles 142 under gravity. Steam enters from the bottom of the stripping section cylinder 141 and flows upwards, thus forming a countercurrent contact with the downward-flowing regenerated solids. This displaces the residual carbon dioxide between the solid particles and in the pores, ensuring that the solids returned to the hydrogen production reactor 11 have high purity. The gas discharged from the top of the stripping section 14 is a mixture of water vapor and carbon dioxide. It can be discharged directly or sent back to the bottom of the regeneration reactor 12 as part of the fluidizing gas or condensed to obtain high-concentration carbon dioxide gas.

[0053] like Figures 1 to 4As shown, the regeneration reactor 12 includes a regenerator cylinder 121, a regeneration heating device 122, a gas distributor, and a cyclone separator. The regeneration heating device 122 is installed on the outer side of the regenerator cylinder 121. The gas distributor is used to introduce steam and oxygen and is arranged at the bottom of the regenerator cylinder 121. The cyclone separator is used to filter carbon dioxide and includes a primary cyclone separator 124 and a secondary cyclone separator 125 connected in series. The discharge pipe of the secondary cyclone separator 125 extends to the outside of the regenerator cylinder 121. The cyclone separator 124's cyclone separation leg is connected to the inlet of the stripping section 14.

[0054] Specifically, the regenerator cylinder 121 is installed at the top of the hydrogen production reactor 11, forming a closed reaction chamber. The regenerated catalyst and carbon dioxide adsorbent are transported to the bottom of the regenerator cylinder 121. Simultaneously, a gas distributor is arranged at the bottom of the regenerator cylinder 121 and connected to both a steam source and an oxygen source, respectively, to introduce steam and oxygen as fluidizing gases. The residence time of the carbon dioxide adsorbent particles in the regeneration reactor 12 is no less than 15 seconds, the operating air velocity is >6 m / s, and the steam residence time is controlled between 6 and 10 seconds to ensure effective desorption of carbon dioxide. A regeneration heating device 122 is installed on the outer side of the regenerator cylinder 121 and can be electrically heated or a hot flue gas jacket to provide the heat required for regeneration. The cyclone separator is used to filter carbon dioxide-rich gas generated during high-temperature reactions. The inlet of the primary cyclone separator 124 is located at the upper part of the regenerator cylinder 121. The gas outlet of the primary cyclone separator 124 is connected to the inlet of the secondary cyclone separator 125. The discharge pipe of the secondary cyclone separator 125 extends upwards and extends outwards through the gas outlet of the regeneration reactor 12 to the outside of the regeneration reactor 12. The cyclone separator's spooling leg extends downwards, passes through the bottom of the regenerator cylinder 121, and connects to the inlet of the stripping section 14, used to feed the separated regenerated solids into the stripping section 14. The outlet of the cyclone separator's spooling leg is located above the gas distributor.

[0055] In the above embodiments, anti-backflow cones are respectively provided at the cyclone separator 113's cyclone leg outlet, the stripping section 14's material leg outlet, and the primary cyclone separator 124's cyclone leg outlet. The anti-backflow cones can prevent gas from flowing back into the material leg, achieving a material sealing effect, and at the same time, can make the separated solid particles evenly dispersed along the cone surface, ensuring smooth discharge of solid materials.

[0056] The present invention also proposes a biomass hydrogen production coupled with carbon dioxide capture method. The method adopts the above-mentioned biomass hydrogen production coupled with carbon dioxide capture system 100. The specific structure of the biomass hydrogen production coupled with carbon dioxide capture system 100 is as described in the above embodiments. Since the present method adopts all the technical solutions of all the above embodiments, it has at least all the beneficial effects brought about by the technical solutions of the above embodiments, which will not be described in detail here.

[0057] Specifically, the biomass-based hydrogen production coupled with carbon dioxide capture method includes: Step 1: The biomass raw material is fed into the pyrolysis reactor 151. Oxygen and water vapor are introduced into the first pyrolysis gas distributor 1511 at the bottom of the pyrolysis reactor 151, so that the biomass raw material undergoes a pyrolysis reaction in the pyrolysis reactor 151, generating impurity-containing pyrolysis gas and preliminary pyrolysis biochar. The impurity-containing pyrolysis gas is transported to the first cyclone separator 1521 through the gas phase outlet 1512, and the preliminary pyrolysis biochar is transported to the axial moving bed 1522 through the solid phase outlet 1513 to form a filtration and purification bed. Step 2: The impurity-containing pyrolysis gas is passed sequentially through the first cyclone separator 1521 and the axial moving bed 1522, and then enters the interior of the hydrogen production and regeneration coupling reactor through the clean pyrolysis gas discharge pipe 155.

[0058] Specifically, the first step is to pyrolyze the biomass, and the second step is to purify the biomass, that is, to pyrolyze and purify the biomass in the fluidized bed pyrolysis and purification coupled reactor 15, and then to introduce the clean biomass pyrolysis gas into the interior of the hydrogen production and regeneration coupled reactor.

[0059] In this step, the dried and shaped biomass feedstock is fed into the pyrolysis reactor 151 by a feeding device. Oxygen and water vapor are introduced into the first pyrolysis gas distributor 1511 at the bottom of the pyrolysis reactor 151. The biomass feedstock undergoes a pyrolysis reaction within the pyrolysis reactor 151, generating impurity-containing pyrolysis gas and preliminary pyrolysis biochar. The impurity-containing pyrolysis gas is conveyed to the first cyclone separator 1521 through the gas phase outlet 1512, and the preliminary pyrolysis biochar is conveyed to the axially moving bed 1522 through the solid phase outlet 1513 to form a filtration and purification bed.

[0060] In this step, the chemical reactions that occur in the biomass in the pyrolysis reactor 151 are as follows:

[0061] The impurity-laden pyrolysis gas enters the first cyclone separator 1521 tangentially, forming a high-speed rotating flow. Utilizing the principle of centrifugal separation, most impurities are removed. The impurities fall along the feed legs to the ash hopper 160 at the bottom of the fluidized bed pyrolysis purification reactor, where they are collected and stored via the bottom outlet. The gas flow then reverses direction and rises, entering the buffer space 1523 through the central riser. Unremoved dust is evenly distributed on the particle layer of the axially moving bed 1522 due to the gas's rotational motion, and is subsequently filtered out. The clean pyrolysis gas exits through the tangential outlet and enters the lower part of the hydrogen production reactor 11 through the clean pyrolysis gas discharge pipe 155. The dust-removed biochar, conveyed by the riser 13 and the sputtering bed 154, re-enters the pyrolysis reactor 151 along the inclined pipe for further heat transfer and pyrolysis.

[0062] Step 3: The clean pyrolysis gas and steam from Step 2 are introduced into the hydrogen production reactor 11 as fluidizing gas. The fluidizing gas is mixed with the catalyst and carbon dioxide adsorbent in the hydrogen production reactor 11 to form a fluidized mixture. Under the action of the catalyst, the biomass pyrolysis gas is converted into hydrogen, carbon monoxide and carbon dioxide. The carbon dioxide reacts with the carbon dioxide adsorbent and is converted into calcium carbonate. The hydrogen is discharged from the hydrogen production reactor 11. Step 4: The catalyst and carbon dioxide adsorbent after reaction in the hydrogen production reactor 11 are transported to the regeneration reactor 12 through the riser 13 for high-temperature calcination, so that the carbonate is decomposed into carbon dioxide and regenerated carbon dioxide adsorbent, while the catalyst is restored to activity and the carbon dioxide is discharged from the regeneration reactor 12. Step 5: The regenerated solids discharged from the regeneration reactor 12 are sent back to the hydrogen production reactor 11 through the stripping section 14.

[0063] Specifically, in step three, the catalyst and carbon dioxide adsorbent are packed at the bottom of the hydrogen production reactor 11. Clean biomass pyrolysis gas is introduced into the first pyrolysis gas distributor 1511 at the bottom of the hydrogen production reactor 11, where it, along with the introduced steam, serves as a fluidizing gas and mixes with the catalyst and carbon dioxide adsorbent to form a fluidized mixture. In the fluidized mixture, the pyrolysis gas is converted into hydrogen, carbon monoxide, and carbon dioxide under the action of the catalyst. Simultaneously, the carbon dioxide adsorbent adsorbs the carbon dioxide generated in the reaction and converts it into calcium carbonate, continuously enhancing the coupling effect of hydrogen production and in-situ carbon dioxide conversion. The hydrogen-rich gas is purified by the second cyclone separator 113 at the top of the hydrogen production reactor 11 and then discharged and collected through the central discharge pipe.

[0064] In this step, the chemical reactions of biomass pyrolysis gas under the action of a catalyst include:

[0065] In step four, the separated spent catalyst and spent carbon dioxide adsorbent enter the pre-lifting section of the riser 13 via the circulation pipe 114 and circulation valve 115 on the side of the hydrogen production reactor 11. Under the action of the gas supplied in the pre-lifting section, the spent catalyst and spent carbon dioxide adsorbent enter the bed of the regeneration reactor 12 via the riser 13. Steam and pure oxygen are introduced into the regeneration gas distributor 123 of the regeneration reactor 12, causing the bottom of the regeneration reactor 12 to be in a bubbling bed flow state. Under the action of steam, the catalyst is regenerated and releases heat. Simultaneously, the regeneration heating device 122 heats the regeneration reactor 12, maintaining the reaction temperature of the regeneration reactor 12 at 750~950℃. At this temperature, carbon dioxide adsorbent undergoes carbon dioxide desorption. The regenerated catalyst and the desorbed carbon dioxide adsorbent form a gas-solid mixture with the steam, which enters the primary cyclone separator 124 of the regeneration reactor 12. The carbon dioxide-rich gas is purified by the primary cyclone separator 124 and the secondary cyclone separator 125 connected in series, and then discharged.

[0066] In this step, the chemical reaction of calcium carbonate under high temperature conditions is as follows:

[0067] In step five, the separated regenerated catalyst and adsorbent enter the lower stripping section 14. The stripping section 14 is equipped with multiple layers of herringbone-shaped baffles 142, and superheated steam is introduced to the bottom of the stripping section 14. The regenerated catalyst and carbon dioxide adsorbent flow downwards in a zigzag pattern between the baffles 142, contacting the upward-flowing steam in a counter-current manner, displacing the carbon dioxide adsorbed between the catalyst particles and in the pores. The regenerated catalyst and carbon dioxide adsorbent are discharged from the bottom feed leg of the stripping section 14 and collect in the regenerated solid buffer zone 111, forming a certain feed level. The regenerated catalyst and regenerated carbon dioxide adsorbent are discharged from the outlet of the solid buffer zone and enter the reaction zone 112 to react with steam and clean biomass pyrolysis gas.

[0068] In the description of this application, it should be understood that the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of technical features indicated. Therefore, a feature defined as "first" or "second" may explicitly or implicitly include at least one of that feature. In the description of this application, "multiple" means at least two, such as two, three, etc., unless otherwise explicitly specified.

[0069] In this application, unless otherwise expressly specified and limited, the terms "installation," "connection," "linking," and "fixing," etc., should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral part; they can refer to a mechanical connection, an electrical connection, or a connection that allows communication between components; they can refer to a direct connection or an indirect connection through an intermediate medium; they can refer to the internal communication of two components or the interaction between two components, unless otherwise expressly limited. Those skilled in the art can understand the specific meaning of the above terms in this application based on the specific circumstances.

[0070] In the description of this specification, the references to terms such as "one embodiment," "some embodiments," "example," "specific example," or "some examples," etc., refer to specific features, structures, materials, or characteristics described in connection with that embodiment or example, which are included in at least one embodiment or example of this application. In this specification, the illustrative expressions of the above terms do not necessarily refer to the same embodiment or example. Furthermore, the specific features, structures, materials, or characteristics described may be combined in any suitable manner in one or more embodiments or examples. Moreover, without contradiction, those skilled in the art can combine and integrate the different embodiments or examples described in this specification, as well as the features of different embodiments or examples.

[0071] Although embodiments of this application have been shown and described above, it is understood that the above embodiments are exemplary and should not be construed as limiting this application. Those skilled in the art can make changes, modifications, substitutions and variations to the above embodiments within the scope of this application.

Claims

1. A biomass-to-hydrogen coupled carbon dioxide capture system, comprising: It includes a fluidized bed pyrolysis purification coupled reactor (15) and a hydrogen production and regeneration coupled reactor, wherein the hydrogen production and regeneration coupled reactor is used to produce hydrogen and capture carbon dioxide, and the fluidized bed pyrolysis purification coupled reactor (15) is used to provide a biomass pyrolysis gas source and includes: The pyrolysis reactor (151) is provided with a gas phase outlet (1512) for discharging impurity pyrolysis gas and a solid phase outlet (1513) for discharging preliminary pyrolysis biochar. A multi-mechanism coupled purifier (152) includes a first cyclone separator (1521) and an axially moving bed (1522) arranged coaxially. The gas phase outlet (1512) is connected to the inlet of the first cyclone separator (1521), and the solid phase outlet (1513) is connected to the axially moving bed (1522) to form a purification bed. The gas outlet of the first cyclone separator (1521) is connected to the axially moving bed (1522). A circulating conveying assembly is used to return the preliminary pyrolytic biochar to the pyrolysis reactor (151), and the circulating conveying assembly is connected between the outlet of the axially moving bed (1522) and the pyrolysis reactor (151). A clean pyrolysis gas discharge pipe (155) is used to connect the biomass pyrolysis gas discharged from the axially moving bed (1522) to the interior of the hydrogen production and regeneration coupling reactor.

2. The system for hydrogen production from biomass coupled with carbon dioxide capture according to claim 1, wherein, The circulating conveying assembly includes: A spouted bed (154) is disposed inside the pyrolysis reactor (151); The conveying and lifting pipe (153) is connected at one end to the outlet of the axial moving bed (1522) and at the other end extends from the bottom of the pyrolysis reactor (151) and is connected to the inlet of the spouting bed (154).

3. The system for hydrogen production from biomass coupled with carbon dioxide capture of claim 1, wherein, The fluidized bed pyrolysis purification coupled reactor (15) also includes an ash hopper (160) for storing solid particles separated from the first cyclone separator (1521), the ash hopper (160) being located at the bottom of the multi-mechanism coupled purifier (152).

4. The system for hydrogen production from biomass coupled with carbon dioxide capture of claim 1, wherein, The hydrogen production and regeneration coupled reactor includes: A hydrogen production reactor (11) is used to generate hydrogen gas. The hydrogen production reactor (11) is filled with a catalyst and a carbon dioxide adsorbent and is connected to the biomass pyrolysis gas source and the steam source. A regeneration reactor (12) is located on top of the hydrogen production reactor (11). The regeneration reactor (12) is used to regenerate the catalyst and the carbon dioxide adsorbent and generate carbon dioxide. The riser (13) is used to transport the catalyst and the carbon dioxide adsorbent after reaction in the hydrogen production reactor (11) to the regeneration reactor (12). The stripping section (14) is used to recover the regenerated catalyst and the carbon dioxide adsorbent. The inlet of the stripping section (14) is connected to the regenerated solid outlet of the regeneration reactor (12), and the outlet of the stripping section (14) is connected to the hydrogen production reactor (11).

5. The biomass- to-hydrogen coupled carbon dioxide capture system of claim 4, wherein, The stripping section (14) is arranged inside the hydrogen production reactor (11). A regenerated solid buffer zone (111) and a reaction zone (112) located radially outside the regenerated solid buffer zone (111) are formed at the bottom of the hydrogen production reactor (11). The material leg of the stripping section (14) extends downward into the interior of the regenerated solid buffer zone (111). The outlet of the regenerated solid buffer zone (111) is connected to the reaction zone (112).

6. The system for hydrogen production from biomass coupled with carbon dioxide capture according to claim 5, wherein, The hydrogen production reactor (11) is provided with a second cyclone separator (113) for hydrogen filtration inside. The discharge pipe of the second cyclone separator (113) extends to the outside of the hydrogen production reactor (11), and the cyclone separator (113) swirls downward to the reaction zone (112).

7. The system for hydrogen production from biomass coupled with carbon dioxide capture of claim 4, wherein, The regeneration reactor (12) includes: Regenerator cylinder (121); A regeneration heating device (122) is installed on the outer side of the regenerator cylinder (121); A regenerated gas distributor (123) is used to supply steam and oxygen and is arranged at the bottom of the regenerator cylinder (121); A cyclone separator for filtering carbon dioxide includes a primary cyclone separator (124) and a secondary cyclone separator (125) connected in series. The discharge pipe of the secondary cyclone separator (125) extends to the outside of the regenerator cylinder (121), and the cyclone separator (124) has its cyclone leg connected to the inlet of the stripping section (14).

8. The system for hydrogen production from biomass coupled with carbon dioxide capture according to any one of claims 1 to 7, wherein, The fluidized bed pyrolysis purification coupled reactor (15) also includes a reaction tank (156). The pyrolysis reactor (151), the multi-mechanism coupled purifier (152) and the circulation conveying assembly are integrated in the reaction tank (156). The reaction tank (156) is provided with a partition. The partition is used to divide the space in the reaction tank (156) into a pyrolysis gas containing impurities zone, a clean pyrolysis gas zone and a biochar accumulation zone from top to bottom. The clean pyrolysis gas discharge pipe (155) is connected to the clean pyrolysis gas zone.

9. A method of hydrogen production from biomass coupled with carbon dioxide capture, characterized by, The method employs the biomass hydrogen production coupled carbon dioxide capture system as described in any one of claims 1 to 8, and includes: Step 1: The biomass raw material is fed into the pyrolysis reactor (151), and oxygen and water vapor are introduced into the first pyrolysis gas distributor (1511) at the bottom of the pyrolysis reactor (151). The biomass raw material undergoes a pyrolysis reaction in the pyrolysis reactor (151) to generate impurity-containing pyrolysis gas and preliminary pyrolysis biochar. The impurity-containing pyrolysis gas is transported to the first cyclone separator (1521) through the gas phase outlet (1512), and the preliminary pyrolysis biochar is transported to the axial moving bed (1522) through the solid phase outlet (1513) to form a filtration and purification bed. Step 2: The impurity-containing pyrolysis gas is passed sequentially through the first cyclone separator (1521) and the axial moving bed (1522), and then enters the interior of the hydrogen production and regeneration coupling reactor through the clean pyrolysis gas discharge pipe (155).

10. The method according to claim 9, wherein, The method further includes: Step 3: The clean pyrolysis gas and steam from Step 2 are introduced into the hydrogen production reactor (11) as fluidizing gas. The fluidizing gas is mixed with the catalyst and carbon dioxide adsorbent in the hydrogen production reactor (11) to form a fluidized mixture. Under the action of the catalyst, the biomass pyrolysis gas is converted into hydrogen, carbon monoxide and carbon dioxide. The carbon dioxide reacts with the carbon dioxide adsorbent and is converted into calcium carbonate. The hydrogen is discharged from the hydrogen production reactor (11). Step 4: The catalyst and carbon dioxide adsorbent after reaction in the hydrogen production reactor (11) are transported to the regeneration reactor (12) through the riser (13) for high-temperature calcination, so that the carbonate is decomposed into carbon dioxide and the regenerated carbon dioxide adsorbent, while the catalyst is restored to activity, and the carbon dioxide is discharged from the regeneration reactor (12). Step 5: The regenerated solids discharged from the regeneration reactor (12) are sent back to the hydrogen production reactor (11) through the stripping section (14).

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