Device and method for preparing green hydrogen through biomass pyrolysis gasification

Abstract

The invention discloses a device and a method for preparing green hydrogen through biomass pyrolysis gasification, relates to the technical field of green hydrogen preparation, solves the problems of blockage and corrosion caused by ash melting and slagging in a pure oxygen gasification process, and also solves the problem of low energy utilization rate. The device for preparing green hydrogen through biomass pyrolysis gasification comprises a pyrolysis reaction device, and the pyrolysis reaction device comprises a pyrolysis reaction tank connected with a high-temperature heat carrier conveying screw, a biomass raw material storage bin, a biomass raw material conveying screw and a pyrolysis solid-phase product conveying screw. According to the invention, biomass raw materials are converted into biochar and pyrolysis oil gas by adopting a pyrolysis technology, so that effective cutting of biomass ash is realized, and the problems of blockage, corrosion and the like caused by ash melting and slagging in a pure oxygen gasification process are effectively avoided; the gasification technology is adopted to directly carry out pure oxygen gasification reaction on high-temperature pyrolysis oil gas, sensible heat and latent heat in the pyrolysis oil gas are fully utilized, and the energy utilization rate is high.

Description

Technical Field

[0001] The present invention relates to the technical field of green hydrogen preparation, and specifically to a device and method for preparing green hydrogen by pyrolysis and gasification of biomass. Background Art

[0002] Hydrogen, with its clean, low-carbon nature, high calorific value, diverse sources, and flexible storage and transportation, is poised to become the "ultimate energy source" of the 21st century. Green hydrogen is produced using renewable energy sources (such as solar, wind, nuclear, and biomass). Currently, green hydrogen is primarily produced through the electrolysis of water using solar / wind power generation.

[0003] Biomass energy is rich in resources and widely distributed, making it the most promising renewable energy source. The production of green hydrogen from biomass has attracted much attention from various fields due to its wide range of raw materials and high hydrogen yield. At present, the mainstream technologies for producing green hydrogen from biomass are mainly bio-fermentation hydrogen production technology and biomass direct gasification hydrogen production technology. Among them, biomass fermentation hydrogen production technology mainly targets organic waste liquids and agricultural wastes rich in carbohydrates such as glucose, starch, and cellulose, while lignin-containing raw materials such as straw and forestry waste are more difficult to use and have strict requirements on the type of raw materials. However, the green hydrogen production device has the following defects when used: 1. Existing green hydrogen production devices generally use a method of mixing solid heat carriers with biomass raw materials for pyrolysis to obtain gaseous pyrolysis volatiles and solid pyrolysis materials. The solid pyrolysis materials are mixed with the solid heat carrier and burned to heat the solid heat carrier; the gaseous pyrolysis volatiles enter the catalytic bed for reforming reaction to obtain high-purity hydrogen. Among them, since the melting point of biomass ash is relatively low, generally below 900°C, in order to reduce the tar, hydrocarbons, methane and other components in the gas phase products, the gasification temperature in the biomass direct gasification technology is higher than the melting point of the biomass ash. This causes the ash to melt and easily adhere to the reactor, affecting the continuous operation of the system. 2. In existing green hydrogen production devices, tar substances exist in the gas phase products, and the power for pyrolysis oil and gas mass transfer generally relies on the exhaust fan at the back end of the process or is completely provided by the pressure increase of the front end pyrolysis process unit. Traditional solutions generally use exhaust fans at the back end, and the gasification conversion, reforming catalysis and other units are operated at slightly positive or negative pressure, which is not conducive to the forward progress of the reforming hydrogen production reaction. If it relies on the increased reaction pressure of the front end pyrolysis unit, higher requirements will be placed on the pyrolysis reactor, pyrolysis feed system, etc., and the equipment difficulty and cost will increase; 3. When existing green hydrogen production equipment produces green hydrogen, the pyrolysis gas products contain impurities such as tar, dust, and hydrogen sulfide. At this time, the traditional solution generally uses catalytic reforming to deal with these impurities. However, when the catalyst is actually used, it is prone to problems such as carbon deposition, coking, and poisoning and deactivation. At the same time, the catalyst loss in the system is large, the process continuity is poor, and the cost is high, making it unsuitable for large-scale use. Summary of the Invention

[0004] The object of the present invention is to provide a device and method for producing green hydrogen by pyrolysis and gasification of biomass, so as to solve the problems raised in the above background technology.

[0005] In order to achieve the above-mentioned object of the invention, the present invention adopts the following technical solutions: The present invention provides a device for preparing green hydrogen by pyrolysis and gasification of biomass, comprising a pyrolysis reaction device, wherein the pyrolysis reaction device comprises: a pyrolysis reaction tank connected to a high-temperature heat carrier conveying screw, a biomass raw material storage bin, a biomass raw material conveying screw, and a pyrolysis solid phase product conveying screw; a pyrolysis acceleration structure arranged inside the pyrolysis reaction tank; and a pyrolysis heating assembly arranged outside the pyrolysis acceleration structure. The pyrolysis acceleration structure includes: a rotating lifting assembly installed inside the pyrolysis reaction tank; an intermediate shaft connected to the rotating lifting assembly and movably arranged at the center of the interior of the pyrolysis reaction tank; a stirring and mixing assembly installed at the center outside the intermediate shaft; a cone installed on the stirring and mixing assembly; a feed pipe installed at the center of the top of the pyrolysis reaction tank by screws; and an oblique channel opened on the inner wall of the feed pipe and located outside the cone. The feed pipe is connected to the biomass raw material storage bin, a sealing rubber ring is sleeved on the outer side of the cone, the intermediate shaft is slidably connected to the inside of the upper frame, and the upper frame is installed on the inner top of the pyrolysis reaction tank.

[0006] As a preferred embodiment of the present invention, the pyrolysis reaction tank includes: an outer protective tank body; a pyrolysis tank body installed inside the outer protective tank body; a first input pipe connected to one side of the pyrolysis tank body and extending to one side outside the outer protective tank body; a side pipe connected to the other side of the pyrolysis tank body and extending to the other side outside the outer protective tank body; an output pipe arranged at the bottom of the pyrolysis tank body and extending to the outside of the bottom of the outer protective tank body. Among them, a feeding pipe is installed at the top center of the pyrolysis tank body, a pyrolysis acceleration structure is provided inside the pyrolysis tank body, and a pyrolysis heating component extending to the outside of the outer protective tank body is provided on the outside of the pyrolysis tank body and the inside of the outer protective tank body.

[0007] As a preferred embodiment of the present invention, the rotary lifting assembly includes: a bottom bracket installed at the bottom of the pyrolysis tank body; a bottom protective cover installed at the bottom center of the bottom bracket; a lifting drive source installed at the bottom of the bottom protective cover; a lifting connection plate connected to the output end of the lifting drive source and slidingly connected to the inside of the bottom protective cover; a lifting rotating rod rotatably connected to the lifting connection plate and installed at the bottom of the intermediate shaft; a vertical groove provided on the outer surface of the lifting rotating rod; a first gear connected to the lifting rotating rod through the vertical groove; a second gear meshingly connected to the first gear and rotatably connected to the inside of the bottom protective cover; and a rotary driving source connected to the second gear and installed at an eccentric position inside the bottom protective cover.

[0008] As a preferred embodiment of the present invention, the stirring and mixing assembly includes: stirring spiral blades installed on the upper and lower sides of the outside of the intermediate shaft; a movable turntable arranged between the two stirring spiral blades and installed on the outside of the intermediate shaft; a skewed gear lever rotatably connected to the eccentric position inside the movable turntable; a stirring blade rotatably connected to the top of the skewed gear lever; and a telescopic spring installed inside the skewed gear lever and extending to the eccentric position inside the movable turntable.

[0009] As a preferred embodiment of the present invention, the pyrolysis heating assembly includes: a heating unit arranged outside the outer protective tank; and a spiral heating pipe connected to the heating unit and arranged outside the pyrolysis tank and inside the outer protective tank.

[0010] As a preferred embodiment of the present invention, the device for preparing green hydrogen further comprises: a combustion blower, a fluidized heating lifting device, a high-temperature heat carrier storage bin, a first-level cyclone dust collector for pyrolysis gas phase products, a charcoal bin for a first-level cyclone dust collector for pyrolysis gas phase products, a second-level cyclone dust collector for pyrolysis gas phase products, a charcoal bin for a second-level cyclone dust collector for pyrolysis gas phase products, an extraction-type gasification conversion burner, a gasification conversion device, an ash storage bin, a waste heat boiler, a spray purification tower spray pump, a compressor, and a hydrogen extraction device. Among them, the combustion blower, fluidized heating lifting device, high-temperature heat carrier storage bin, high-temperature heat carrier conveying screw, pyrolysis reaction device and pyrolysis solid phase product conveying screw are connected in sequence, the biomass raw material storage bin, biomass raw material conveying screw and pyrolysis reaction device are connected in sequence, the pyrolysis reaction device, pyrolysis gas phase product first-level cyclone dust collector, pyrolysis gas phase product second-level cyclone dust collector, extraction type gasification conversion burner, gasification conversion device, waste heat boiler, spray purification tower, spray pump, compressor and hydrogen extraction device are connected in sequence, the pyrolysis gas phase product first-level cyclone dust collector and the pyrolysis gas phase product first-level cyclone dust collector charcoal bin are connected, the pyrolysis gas phase product second-level cyclone dust collector and the pyrolysis gas phase product second-level cyclone dust collector charcoal bin are connected, and the gasification conversion device and the ash storage bin are connected.

[0011] As a preferred embodiment of the present invention, the extraction type gasification conversion burner is composed of an extraction steam inlet, a central oxygen inlet, an outer ring oxygen inlet, a cooling circulating water inlet, a gasification device interface flange, a cooling circulating water outlet, a pyrolysis gas product inlet, a steam injection pipe, a steam injection pipe reduction, a central oxygen support frame, a burner tapered pipe, a burner throat and a burner expansion pipe. The suction steam inlet is arranged at the end side of the extraction type gasification conversion burner, the central oxygen inlet is arranged in the central axis direction of the extraction type gasification conversion burner, the linear end of the steam injection pipe is provided with a steam injection pipe reduction, and the steam reaches the maximum flow rate at the position of the steam injection pipe reduction, the outer shell of the extraction type gasification conversion burner is composed of a burner tapered tube, a burner throat and a burner expansion tube, the suction steam inlet is provided with four groups of channels, and the four groups of channels are respectively arranged from the inside to the outside as a central oxygen inlet channel, a pyrolysis gas product inlet channel, an outer ring oxygen inlet channel, a cooling circulating water inlet and a cooling circulating water outlet channel. The gasification device interface flange is arranged on the straight pipe section of the extraction-type gasification conversion burner, and a central oxygen support frame is arranged in the central oxygen inlet of the extraction-type gasification conversion burner.

[0012] As a preferred embodiment of the present invention, the gasification conversion device is composed of a gasification interface flange, a gasification chamber, an upper swirl steam injection throat, a conversion chamber, an upper swirl steam injection throat steam inlet, a lower swirl steam injection throat, a lower swirl steam injection throat steam inlet, a slag drop pipe, a slag discharge port at the bottom of the gasification device, a gasification device gas outlet, a gasification device refractory lining, a gasification device thermal insulation layer, and a gasification device thermal insulation layer. The gasification interface flange of the gasification conversion device is connected to the extraction type gasification conversion burner, the gasification chamber is located in the upper area of ​​the gasification conversion device, and the conversion chamber is located in the lower area of ​​the gasification conversion device. The gasification chamber and the conversion chamber are isolated by an upper swirl steam injection throat, and the lower part of the conversion chamber is sequentially provided with a lower swirl steam injection throat and a slag dropping pipe, the bottom slag discharge port of the gasification device is located in the bottom area of ​​the gasification conversion device, the gasification device air outlet is arranged on the side of the gasification conversion device, the gasification device air outlet is located on the lower side of the lower swirl steam injection throat and in the upper area of ​​the slag dropping pipe outlet, the gasification conversion device is respectively composed of a refractory lining of the gasification device, a thermal insulation layer of the gasification device and a thermal insulation layer of the gasification device from the inside to the outside, the steam inlet of the upper swirl steam injection throat is arranged at one end of the upper swirl steam injection throat, and the steam inlet of the lower swirl steam injection throat is arranged at one end of the lower swirl steam injection throat.

[0013] As a preferred embodiment of the present invention, the upper swirl steam injection throat is composed of an upper swirl steam injection throat steam nozzle and an upper swirl steam injection throat steam chamber. Wherein, the lower swirl steam injection throat is composed of a lower swirl steam injection throat steam nozzle and a lower swirl steam injection throat steam chamber.

[0014] The present invention also provides a method for preparing green hydrogen by pyrolysis and gasification of biomass, comprising the following steps: S1. The biomass raw materials are crushed and pulverized to obtain raw materials with a particle size of ≤10mm; S2. Raw materials with a particle size of ≤10mm enter the drying system to reduce the moisture content of the raw materials to below 5%. The drying heat source is the waste heat flue gas of the system; S3. The dried raw materials with a moisture content of ≤5% are transported to the biomass raw material storage bin. The dried raw materials are transported to the pyrolysis reaction device via the biomass raw material conveying screw. Simultaneously, the high-temperature heat carrier located in the high-temperature heat carrier storage bin is transported to the pyrolysis reaction device via the high-temperature heat carrier conveying screw. The biomass raw materials and the high-temperature heat carrier are fully transferred to the pyrolysis reaction device to obtain high-temperature biochar and pyrolysis oil and gas. S4. The mixture of high-temperature biochar and medium-temperature heat carrier is transported into the fluidized heating and lifting device through the pyrolysis solid phase product conveying screw. Air is introduced at the same time. The high-temperature biochar is fully burned in the fluidized heating and lifting device, causing the medium-temperature heat carrier to be heated to obtain a high-temperature heat carrier. At the same time, the heat carrier is lifted to the high-temperature heat carrier storage bin; the flue gas is used for raw material drying. S5. After the pyrolysis oil and gas are dust-removed by the first-level cyclone dust collector for the pyrolysis gas phase product and the second-level cyclone dust collector for the pyrolysis gas phase product, they enter the extraction-type gasification conversion burner. The mass transfer power of the pyrolysis oil and gas is mainly provided by the negative pressure formed by the steam injection into the extraction-type gasification conversion burner. The oxygen enters the extraction-type gasification conversion burner in two ways, namely central oxygen and annular oxygen. The pyrolysis oil and gas, steam and oxygen undergo a gasification reaction in the gasification chamber of the gasification conversion device to obtain a gasification synthesis gas. The gasification synthesis gas passes through the upper cyclonic steam injection throat area and is injected by the steam cyclone. The gasification synthesis gas and steam undergo a water-gas shift reaction to obtain hydrogen-rich gas. The hydrogen-rich gas passes through the lower cyclonic steam injection throat area and is injected by the steam cyclone. The temperature of the hydrogen-rich gas drops below the ash melting point, and the solid ash is discharged to the bottom of the gasification conversion device through the slag drop pipe. S6. The hydrogen-rich gas is sequentially processed through waste heat boiler heat exchange, spray purification tower cooling and purification, compressor compression, and hydrogen extraction treatment in a hydrogen extraction device to obtain high-purity hydrogen product; the steam generated by the waste heat boiler is used to supply the induced gasification conversion burner and gasification conversion device. Compared with the existing technology, one or more of the above technical solutions have the following beneficial effects: 1. In the device and method for preparing green hydrogen by pyrolysis and gasification of biomass, in view of the melting of ash during the thermochemical conversion of biomass, pyrolysis is used to solidify the ash of biomass in biochar. A two-stage dust removal method is used to reduce the content of biochar impurities in pyrolysis oil and gas. In view of the small amount of ash melting contained in the gasification stage of pyrolysis oil and gas, multi-stage water vapor swirl injection is used to reduce the ash content to below the ash melting point to form a solid particle removal system, thereby solving the problem of ash melting. At the same time, a uniquely designed extraction-type gasification conversion burner is used to address the characteristics of pyrolysis oil in pyrolysis oil and gas that are prone to condensation and coking. This can not only meet the effective discharge of pyrolysis oil and gas in the pyrolysis section, but also realize positive pressure gasification conversion operation in the gasification conversion device, reducing the equipment processing difficulty and cost of the pyrolysis system and the pyrolysis feed system, and realizing the full progress of the gasification conversion reaction. 2. In the device and method for preparing green hydrogen by pyrolysis and gasification of biomass, a pyrolysis oil and gas gasification conversion device has been invented for the high-temperature pyrolysis oil and gas gasification hydrogen production process. The entire process does not require the addition of a catalyst to the reaction. In addition, the gasification conversion device adopts a multi-stage throat design, and multi-stage water vapor nozzles are set at the throat position, which helps the water gas conversion reaction to proceed in the positive direction and obtain more hydrogen products. At the same time, compared with the traditional method of preparing green hydrogen, this process has the advantages of low loss, continuous process and low cost, and is suitable for large-scale promotion and use; 3. In the device and method for producing green hydrogen by pyrolysis and gasification of biomass, a "pyrolysis + gasification conversion" combination is adopted. Biomass pyrolysis is used to obtain biochar and pyrolysis oil and gas. The biomass ash remains in the biochar, achieving ash separation in the biomass, avoiding conditions such as ash melting and slagging that affect the continuous operation of the process. The pyrolysis oil and gas are separated by two-stage cyclones to reduce the biochar impurity content. The gasification conversion device is equipped with a multi-stage water vapor cyclone injection device to reduce the temperature of the hydrogen-rich conversion gas to below the ash melting point, avoiding the impact of molten ash and slag on the device. 4. In the device and method for producing green hydrogen by pyrolysis and gasification of biomass, when the raw materials (high-temperature solid heat carrier and bamboo chips) are mixed and pyrolyzed, the raw materials can be transported in a cut-in manner and driven by the rotating intermediate shaft to contact the raw materials in the vortex generated on the outside of the intermediate shaft. While ensuring the contact area for pyrolysis and mixing of the raw materials (high-temperature solid heat carrier and bamboo chips), the irregularly structured vortex (through the central rotating stirring blades) can ensure that the raw materials are evenly heated during the mixing process, avoiding local overheating or overcooling, and significantly improving the effect and efficiency of the pyrolysis. 5. In the device and method for preparing green hydrogen by pyrolysis and gasification of biomass, when the intermediate shaft is driven to rotate and move up and down to achieve the mixing and pyrolysis operations of the raw materials (high-temperature solid heat carrier and bamboo chips), the lifting and lowering movement of the intermediate shaft will intermittently open the channel at the bottom of the feed pipe. When the channel at the bottom of the feed pipe is sealed, the raw materials (bamboo chips) can enter the interior of the pyrolysis tank from the multiple oblique channels opened on its outer wall, and fall at the eccentric point of the inner wall of the pyrolysis tank, further increasing the contact area of ​​the raw materials (high-temperature solid heat carrier and bamboo chips) during mixing and pyrolysis, and ensuring the uniformity of mixing and pyrolysis. BRIEF DESCRIPTION OF THE DRAWINGS

[0015] The accompanying drawings, which constitute a part of the present invention, are used to provide a further understanding of the present invention. The exemplary embodiments of the present invention and their descriptions are used to explain the present invention and do not constitute improper limitations on the present invention.

[0016] Furthermore, the terms "installed," "disposed," "provided with," "connected," "connected," and "socketed" should be interpreted broadly. For example, they can refer to fixed connections, removable connections, or integral structures; mechanical connections or electrical connections; direct connections, indirect connections through an intermediary, or internal communication between two devices, elements, or components. Those skilled in the art will understand the specific meanings of these terms in this application based on the specific circumstances.

[0017] Figure 1 It is a process flow chart of the present invention as a whole; Figure 2 It is a structural schematic diagram of the pyrolysis reaction device of the present invention; Figure 3 It is a schematic structural diagram of a pyrolysis reaction device of the present invention in cross section; Figure 4 This is a schematic diagram of the cross-section of the pyrolysis reaction device of the present invention; Figure 5 This is a schematic structural diagram of the cross-section of the connection between the pyrolysis reaction tank and the pyrolysis heating assembly of the present invention; Figure 6 It is a structural schematic diagram of the pyrolysis acceleration structure of the present invention; Figure 7 This is a schematic structural diagram of a cross-sectional view of the connection between the rotary lifting assembly and the intermediate shaft of the present invention; Figure 8 This invention Figure 7 Schematic diagram of the structure of the enlarged area A in the middle; Figure 9 This is a schematic structural diagram of the connection between the intermediate shaft and the stirring and mixing assembly of the present invention; Figure 10 This is a schematic structural diagram of a cross-sectional view of the connection between the intermediate shaft and the feed pipe of the present invention; Figure 11 It is a structural schematic diagram of the gasification conversion device of the present invention; Figure 12 This is a schematic structural diagram of the extraction type gasification conversion burner of the present invention; Figure 13 This is a schematic structural diagram of the cross-section of the upper swirl steam injection throat of the present invention; Figure 14 2. It is a schematic diagram of the cross-section of the upper swirl steam injection throat of the present invention; Figure 15 This is a schematic structural diagram of the cross-section of the lower swirl steam injection throat of the present invention; Figure 16 2. It is a schematic diagram of the cross-section of the lower swirl steam injection throat of the present invention; In the picture: 1. Combustion blower; 2. Fluidized heating lifting device; 3. High-temperature heat carrier storage bin; 4. High-temperature heat carrier conveying screw; 5. Biomass raw material storage bin; 6. Biomass raw material conveying screw; 7. Pyrolysis reaction device; 8. Pyrolysis solid product conveying screw; 9. First-stage cyclone dust collector for pyrolysis gas phase products; 10. Charcoal bin for first-stage cyclone dust collector for pyrolysis gas phase products; 11. Second-stage cyclone dust collector for pyrolysis gas phase products; 12. Charcoal bin for second-stage cyclone dust collector for pyrolysis gas phase products; 13. Extraction-type gasification conversion burner; 14. Gasification conversion device; 15. Ash storage bin; 16. Waste heat boiler; 17. Spray purification tower; 18. Spray pump; 19. Compressor; 20. Hydrogen extraction device; 1301, suction steam inlet; 1302, central oxygen inlet; 1303, outer ring oxygen inlet; 1304, cooling circulating water inlet; 1305, gasification unit interface flange; 1306, cooling circulating water outlet; 1307, pyrolysis gas product inlet; 1308, steam injection pipe; 1309, steam injection pipe reduction; 1310, central oxygen support frame; 1311, burner tapered tube; 1312, burner throat; 1313, burner expansion tube; 1401, gasification interface flange; 1402, gasification chamber; 1403, upper swirl steam injection throat; 1404, conversion chamber; 1405, upper swirl steam injection throat steam inlet; 1406, lower swirl steam injection throat; 1407, lower swirl steam injection throat steam inlet; 1408, slag drop pipe; 1409, bottom slag discharge port of gasification device; 1410, gasification device gas outlet; 1411, gasification device refractory lining; 1412, gasification device thermal insulation layer; 1413, gasification device thermal insulation layer; 140301. Upper swirl steam injection throat steam nozzle; 140302. Upper swirl steam injection throat steam chamber; 140601. Steam nozzle for lower swirl steam injection throat; 140602. Steam chamber for lower swirl steam injection throat; 70. Pyrolysis reaction tank; 7001. Outer protective tank; 7002. Pyrolysis tank; 7003. First input pipeline; 7004. Side pipeline; 7005. Output pipeline; 80. Pyrolysis acceleration structure; 801. Rotating lifting assembly; 802. Intermediate shaft; 8021. Upper frame; 803. Stirring and mixing assembly; 804. Conical body; 8041. Sealing rubber ring; 805. Feeding pipe; 806. Oblique channel; 8011, bottom bracket; 8012, bottom protective cover; 8013, lifting drive source; 8014, lifting connection plate; 8015, lifting rotating rod; 8016, vertical groove; 8017, first gear; 8018, second gear; 8019, rotation drive source; 8031, stirring spiral blade; 8032, movable turntable; 8033, deflection lever; 8034, stirring blade; 8035, telescopic spring; 90. Pyrolysis heating assembly; 901. Heating unit; 902. Spiral heating pipe; 100. Discharge cooling assembly; 1001. Cooling unit; 1002. Cooling spiral tube. DETAILED DESCRIPTION

[0018] In order to enable those skilled in the art to better understand the present invention, the following will clearly and completely describe the technical solutions in the embodiments of the present invention in conjunction with the drawings in the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments in the present invention, all other embodiments obtained by ordinary technicians in this field without making creative efforts should fall within the scope of protection of this application. Example 1

[0019] See also Figures 1-16A device for preparing green hydrogen by pyrolysis and gasification of biomass includes a pyrolysis reaction device 7, which includes: a pyrolysis reaction tank 70 connected to a high-temperature heat carrier conveying screw 4, a biomass raw material storage bin 5, a biomass raw material conveying screw 6, and a pyrolysis solid phase product conveying screw 8; a pyrolysis acceleration structure 80 arranged inside the pyrolysis reaction tank 70; a pyrolysis heating assembly 90 arranged outside the pyrolysis acceleration structure 80, and the pyrolysis acceleration structure 80 includes: a rotating lifting assembly 801 installed inside the pyrolysis reaction tank 70; a rotating lifting assembly 801 connected to the rotating lifting assembly 801 and movably arranged at the center of the pyrolysis reaction tank 70. An intermediate shaft 802; a stirring and mixing assembly 803 installed at the outer center of the intermediate shaft 802; a cone 804 installed on the stirring and mixing assembly 803; a feed pipe 805 installed at the top center of the pyrolysis reaction tank 70 by screws; an oblique channel 806 opened on the inner wall of the feed pipe 805 and located on the outside of the cone 804, wherein the feed pipe 805 is connected to the biomass raw material storage bin 5, and a sealing rubber ring 8041 is provided on the outer side of the cone 804, and the intermediate shaft 802 is slidably connected to the inside of the upper frame 8021, and the upper frame 8021 is installed on the inner top of the pyrolysis reaction tank 70.

[0020] In the present invention, the pyrolysis reaction tank 70 includes: an outer protective tank body 7001; a pyrolysis tank body 7002 installed inside the outer protective tank body 7001; a first input pipe 7003 connected to one side of the pyrolysis tank body 7002 and extending to the outside of the outer protective tank body 7001; a side pipe 7004 connected to the other side of the pyrolysis tank body 7002 and extending to the other side of the outside of the outer protective tank body 7001; an output pipe 7005 arranged at the bottom of the pyrolysis tank body 7002 and extending to the outside of the bottom of the outer protective tank body 7001, wherein a feeding pipe 805 is installed at the top center of the pyrolysis tank body 7002, a pyrolysis acceleration structure 80 is movably provided inside the pyrolysis tank body 7002, and a pyrolysis heating assembly 90 extending to the outside of the outer protective tank body 7001 is provided on the outside of the pyrolysis tank body 7002 and the inside of the outer protective tank body 7001.

[0021] The above-described operating principle: By disposing a rotating intermediate shaft 802 (driven by a rotating lifting assembly 801) within the pyrolysis reaction tank 70 and capable of lifting and moving, the various raw materials (high-temperature solid heat carrier and bamboo chips) entering the pyrolysis reaction tank 70 are accelerated to mix, increasing the contact area and uniformity of the mixing of the various raw materials and the pyrolysis reaction, thereby improving the efficiency of the pyrolysis reaction. Simultaneously, as the intermediate shaft 802 is driven to rotate and lift, the material within the feed pipe 805 intermittently moves through the oblique channel 806 or the bottom channel of the feed pipe 805, ensuring that the bamboo chips can enter the pyrolysis tank 7002 in an irregular manner, further increasing the contact area with the pyrolysis tank 7002, and achieving a more efficient raw material pyrolysis operation.

[0022] Specific reference Figure 7 and Figure 8 The rotary lifting assembly 801 includes: a bottom bracket 8011 installed at the bottom of the pyrolysis tank 7002; a bottom protective cover 8012 installed at the bottom center of the bottom bracket 8011; a lifting drive source 8013 installed at the bottom of the bottom protective cover 8012; a lifting connection plate 8014 connected to the output end of the lifting drive source 8013 and slidingly connected to the inside of the bottom protective cover 8012; a lifting rotating rod 8015 rotatably connected to the lifting connection plate 8014 and installed at the bottom of the intermediate shaft 802; a vertical groove 8016 provided on the outer surface of the lifting rotating rod 8015; a first gear 8017 connected to the lifting rotating rod 8015 through the vertical groove 8016; a second gear 8018 meshingly connected to the first gear 8017 and rotatably connected to the inside of the bottom protective cover 8012; and a rotary driving source 8019 connected to the second gear 8018 and installed at an eccentric position inside the bottom protective cover 8012.

[0023] In the biomass pyrolysis and gasification device for producing green hydrogen of the present invention, when driving the intermediate shaft 802 to rotate and lift for mixing the raw materials and conducting the pyrolysis reaction, the rotation drive source 8019 can be activated to drive the second gear 8018 connected to the output end of the rotation drive source 8019 to rotate, causing the first gear 8017, which is meshed with the side of the second gear 8018, to rotate. As the first gear 8017 rotates, the vertical groove 8016 on its inner surface cooperates with the rotation of the lifting rod 8015, without affecting the lifting movement of the lifting rod 8015. This in turn drives the intermediate shaft 802 connected to the lifting rod 8015 to rotate. Simultaneously, the operation of the lifting drive source 8013 drives the lifting rod 8015 and the intermediate shaft 802, which are rotatably connected to the output end of the lifting drive source 8013 via the lifting connection plate 8014, to lift and lower, thereby accelerating the efficiency of the raw material mixing and pyrolysis reaction.

[0024] Specific reference Figure 9 The stirring and mixing component 803 includes: stirring spiral blades 8031 ​​installed on the upper and lower sides of the outside of the intermediate shaft 802; a movable turntable 8032 arranged between the two stirring spiral blades 8031 ​​and installed on the outside of the intermediate shaft 802; a skewed gear rod 8033 rotatably connected to the eccentric position inside the movable turntable 8032; a stirring blade 8034 rotatably connected to the top of the skewed gear rod 8033; and a telescopic spring 8035 installed inside the skewed gear rod 8033 and extending to the eccentric position inside the movable turntable 8032.

[0025] In the biomass pyrolysis and gasification device for producing green hydrogen according to the present invention, when the intermediate shaft 802 rotates, the movable turntable 8032 and stirring spiral blades 8031 ​​mounted on its outer side rotate synchronously. The structural shape of the stirring spiral blades 8031 ​​creates an external vortex, ensuring that the raw materials are thoroughly mixed. Simultaneously, the centrifugal force generated by the rotation of the movable turntable 8032 causes the deflection lever 8033 and stirring blades 8034 to move outward, increasing the size of the vortex within the central mixing and pyrolysis region. This, through the irregular pyrolysis and mixing vortexes, improves the efficiency of the pyrolysis reaction.

[0026] Specific reference Figure 5 The pyrolysis heating assembly 90 includes: a heating unit 901 arranged on the outside of the outer protective tank 7001; and a spiral heating pipe 902 connected to the heating unit 901 and arranged on the outside of the pyrolysis tank 7002 and the inside of the outer protective tank 7001. Example 2

[0027] See also Figures 1-16, a device for preparing green hydrogen by pyrolysis and gasification of biomass, the device for preparing green hydrogen also includes: a combustion blower 1, a fluidized heating and lifting device 2, a high-temperature heat carrier storage bin 3, a first-level cyclone dust collector for pyrolysis gas phase products 9, a first-level cyclone dust collector charcoal bin 10 for pyrolysis gas phase products, a second-level cyclone dust collector 11 for pyrolysis gas phase products, a second-level cyclone dust collector charcoal bin 12 for pyrolysis gas phase products, an extraction type gasification conversion burner 13, a gasification conversion device 14, an ash storage bin 15, a waste heat boiler 16, a spray purification tower 17, a spray pump 18, a compressor 19 and a hydrogen extraction device 20, wherein the combustion blower 1, the fluidized heating and lifting device 2, the high-temperature heat carrier storage bin 3, the high-temperature heat carrier conveying screw 4, the pyrolysis reaction device 7 and The pyrolysis solid product conveying screw 8 is connected in sequence, the biomass raw material storage bin 5, the biomass raw material conveying screw 6 and the pyrolysis reaction device 7 are connected in sequence, the pyrolysis reaction device 7, the pyrolysis gas product first-level cyclone dust collector 9, the pyrolysis gas product second-level cyclone dust collector 11, the extraction type gasification conversion burner 13, the gasification conversion device 14, the waste heat boiler 16, the spray purification tower 17, the spray pump 18, the compressor 19 and the hydrogen extraction device 20 are connected in sequence, the pyrolysis gas product first-level cyclone dust collector 9 and the pyrolysis gas product first-level cyclone dust collector charcoal bin 10 are connected, the pyrolysis gas product second-level cyclone dust collector 11 and the pyrolysis gas product second-level cyclone dust collector charcoal bin 12 are connected, and the gasification conversion device 14 and the ash storage bin 15 are connected.

[0028] Specific reference Figure 12The extraction type gasification conversion burner 13 is composed of an extraction steam inlet 1301, a central oxygen inlet 1302, an outer ring oxygen inlet 1303, a cooling circulating water inlet 1304, a gasification device interface flange 1305, a cooling circulating water outlet 1306, a pyrolysis gas product inlet 1307, a steam injection pipe 1308, a steam injection pipe reduction 1309, a central oxygen support frame 1310, a burner tapered pipe 1311, a burner throat 1312 and a burner expansion pipe 1313. The extraction steam inlet 1301 is arranged at the end side of the extraction type gasification conversion burner 13, the central oxygen inlet 1302 is arranged in the central axis direction of the extraction type gasification conversion burner 13, and the end of the steam injection pipe 1308 is provided with a steam injection pipe reduction 1309. , and the steam reaches the maximum flow rate at the position of the steam injection pipe reduction 1309. The outer shell of the extraction type gasification conversion burner 13 is composed of a burner tapered tube 1311, a burner throat 1312 and a burner expansion tube 1313. The suction steam inlet 1301 is provided with four groups of channels, and the four groups of channels are respectively provided as the central oxygen inlet 1302 channel, the pyrolysis gas product inlet 1307 channel, the outer ring oxygen inlet 1303 channel, the cooling circulating water inlet 1304 and the cooling circulating water outlet 1306 from the inside to the outside. Among them, the gasification device interface flange 1305 is provided on the straight pipe section of the extraction type gasification conversion burner 13, and a central oxygen support frame 1310 is provided in the central oxygen inlet 1302 of the extraction type gasification conversion burner 13.

[0029] Preferably, the diameter of the straight pipe section of the steam injection pipe 1308 is a, the diameter of the steam injection pipe reduction 1309 is b, the height of the steam injection pipe reduction 1309 is h1, and the center line distance between the straight pipe section of the steam injection pipe reduction 1309 and the suction steam inlet 1301 is h2; the diameter of the straight pipe section of the burner pyrolysis gas product channel is A, the diameter of the burner throat 1312 is B, the diameter of the burner expansion pipe 1313 is C, the length of the burner tapered tube 1311 is H1, the length of the burner throat 1312 is H2, and the length of the burner expansion pipe 1313 is H3.

[0030] Preferably, a / b=1.5~4, a / b=1.5~2.5.

[0031] Preferably, h2 / h1=5-10, a / b=6-8.

[0032] Preferably, h1=(1.0~1.5)*b.

[0033] Preferably, A / B=1.2~2.5, A / B=1.5~2.

[0034] Preferably, C / A=1.2~2, C / A=1.2~1.5.

[0035] Preferably, H3 / H2=1.0~2.5, H3 / H2=1.2~1.5.

[0036] Preferably, H1 / H2=0.2~1.5, H1 / H2=0.5~0.8.

[0037] Specific reference Figure 11 、 Figure 13 、 Figure 14 、 Figure 15 and Figure 16 The gasification conversion device 14 is composed of a gasification interface flange 1401, a gasification chamber 1402, an upper swirl steam injection throat 1403, a conversion chamber 1404, an upper swirl steam injection throat steam inlet 1405, a lower swirl steam injection throat 1406, a lower swirl steam injection throat steam inlet 1407, a slag drop pipe 1408, a slag discharge port 1409 at the bottom of the gasification device, a gasification device gas outlet 1410, a gasification device refractory lining 1411, a gasification device thermal insulation layer 1412 and a gasification device thermal insulation layer 1413. The gasification interface flange 1401 of the gasification conversion device 14 is connected to the extraction type gasification conversion burner 13. The gasification chamber 1402 is located in the upper area of ​​the gasification conversion device 14, and the conversion chamber 1404 is located in the lower area of ​​the gasification conversion device 14. The gasification chamber 1402 and the conversion chamber 1404 are connected by an upper swirl. The steam injection throat 1403 is isolated, and the lower part of the conversion chamber 1404 is sequentially provided with a lower swirl steam injection throat 1406 and a slag dropping pipe 1408. The bottom slag discharge port 1409 of the gasification device is located in the bottom area of ​​the gasification conversion device 14, and the gasification device air outlet 1410 is provided on the side of the gasification conversion device 14. The gasification device air outlet 1410 is located on the lower side of the lower swirl steam injection throat 1406 and the upper area of ​​the slag dropping pipe 1408 outlet. From the inside to the outside of the gasification conversion device 14, respectively, are the gasification device refractory lining 1411, the gasification device thermal insulation layer 1412 and the gasification device thermal insulation layer 1413. The upper swirl steam injection throat steam inlet 1405 is provided at one end of the upper swirl steam injection throat 1403, and the lower swirl steam injection throat steam inlet 1407 is provided at one end of the lower swirl steam injection throat 1406.

[0038] In this scheme, the upper swirl steam injection throat 1403 is composed of an upper swirl steam injection throat steam nozzle 140301 and an upper swirl steam injection throat steam chamber 140302, wherein the lower swirl steam injection throat 1406 is composed of a lower swirl steam injection throat steam nozzle 140601 and a lower swirl steam injection throat steam chamber 140602.

[0039] Preferably, the height-to-diameter ratio of the gasification chamber 1402 is 8:1 to 4:1; the height-to-diameter ratio of the conversion chamber 1404 is 10:1 to 4:1; Preferably, the upper swirl steam injection throat steam nozzles 140301 are evenly arranged in a ring around the upper swirl steam injection throat 1403; Preferably, the number of vertical layers of the upper swirl steam injection throat steam nozzle 140301 is n, where n=8 to 20 layers; Preferably, the horizontal direction of the upper swirl steam injection throat steam nozzle 140301 and the radial angle of the gasification conversion device 14 are α, α = 0 ~ 60 degrees; Preferably, the number of upper swirl steam injection throat steam nozzles 140301 arranged in the horizontal direction is m, n=12 to 24 (m is an even number); Preferably, the horizontal direction of the steam inlet of the upper swirl steam injection throat 1403 and the radial cutting angle of the gasification conversion device 14 are δ, δ = 0 ~ 60 degrees.

[0040] Preferably, the lower swirl steam injection throat steam nozzles 140601 are evenly arranged in a ring around the lower swirl steam injection throat 1406; Preferably, the number of vertical layers of the lower swirl steam injection throat steam nozzle 140601 is k, k=8 to 20 layers; Preferably, the horizontal direction of the lower swirl steam injection throat steam nozzle 140601 and the radial cutting angle of the gasification conversion device 14 are β, β = 0 ~ 60 degrees; Preferably, the number of the lower swirl steam injection throat steam nozzles 140601 arranged horizontally is l, where l=12 to 24 (m is an even number); Preferably, the horizontal direction of the steam inlet 1407 of the lower swirl steam injection throat and the radial cutting angle of the gasification conversion device 14 are γ, γ = 0 ~ 60 degrees. Example 3

[0041] See also Figures 1-16 , including the following steps: S1. The biomass raw materials are crushed and pulverized to obtain raw materials with a particle size of ≤10mm; S2. Raw materials with a particle size of ≤10mm enter the drying system to reduce the moisture content of the raw materials to below 5%. The drying heat source is the waste heat flue gas of the system; S3. The dried raw materials with a moisture content of ≤5% are transported to the biomass raw material storage bin 5. The dried raw materials are transported to the pyrolysis reaction device 7 via the biomass raw material conveying screw 6. Simultaneously, the high-temperature heat carrier in the high-temperature heat carrier storage bin 3 is transported to the pyrolysis reaction device 7 via the high-temperature heat carrier conveying screw 4. The biomass raw materials and the high-temperature heat carrier are fully transferred to the pyrolysis reaction device 7 to obtain high-temperature biochar and pyrolysis oil and gas. S4. The mixture of high-temperature biochar and medium-temperature heat carrier is transported into the fluidized heating and lifting device 2 via the pyrolysis solid phase product conveying screw 8. Air is introduced at the same time. The high-temperature biochar is fully burned in the fluidized heating and lifting device 2, causing the medium-temperature heat carrier to be heated to obtain a high-temperature heat carrier. The heat carrier is then lifted to the high-temperature heat carrier storage bin 3. The flue gas is used for drying the raw materials. S5. After the pyrolysis oil and gas are dust-removed by the first-level cyclone dust collector 9 and the second-level cyclone dust collector 11 of the pyrolysis gas phase product, they enter the extraction-type gasification conversion burner 13. The mass transfer power of the pyrolysis oil and gas is mainly provided by the negative pressure formed by the steam injection into the extraction-type gasification conversion burner 13. The oxygen enters the extraction-type gasification conversion burner 13 in two ways, namely central oxygen and annular oxygen. The pyrolysis oil and gas, steam and oxygen undergo a gasification reaction in the gasification chamber 1402 of the gasification conversion device 14 to obtain a gasified synthesis gas. The gasified synthesis gas passes through the upper cyclonic steam injection throat 1403 area and is injected by the steam cyclone. The gasified synthesis gas and steam undergo a water-gas shift reaction to obtain hydrogen-rich gas. The hydrogen-rich gas passes through the lower cyclonic steam injection throat 1406 area and is injected by the steam cyclone. The temperature of the hydrogen-rich gas drops below the ash melting point, and the solid ash is discharged to the bottom of the gasification conversion device 14 through the slag drop pipe 1408. S6. The hydrogen-rich gas is sequentially processed through the waste heat boiler 16 for heat exchange, the spray purification tower 17 for spray cooling and purification, the compressor 19 for compression, and the hydrogen extraction device 20 for hydrogen extraction to obtain a high-purity hydrogen product; the steam generated by the waste heat boiler 16 is used for the extraction-type gasification conversion burner 13 and the gasification conversion device 14. Example 4

[0042] Specific reference Figure 5 A discharge cooling assembly 100 is provided on the outer side of the bottom of the pyrolysis tank 7002. The discharge cooling assembly 100 consists of a cooling unit 1001 and a cooling spiral tube 1002. The cooling unit 1001 and the cooling spiral tube 1002 are connected.

[0043] In the device for preparing green hydrogen by pyrolysis and gasification of biomass of the present invention, the cooling medium circulating inside the cooling spiral tube 1002 can perform preliminary cooling treatment (cooling to ambient temperature) on the material at a relatively high temperature state, carbonize the biomass, and facilitate the storage, utilization, and stacking of this part of the material. Example 5

[0044] The bamboo chips are dried by using the system waste heat flue gas, and the average moisture content of the raw material is 45%. The bamboo chips with a moisture content of ≤5% are obtained. The bamboo chips are transported to the biomass raw material storage 5; the high-temperature solid heat carrier (650℃) in the high-temperature heat carrier storage 3 is transported to the pyrolysis reaction device 7 through the high-temperature heat carrier conveying screw 4 and the biomass raw material conveying screw 6, respectively, wherein the mass ratio of the high-temperature solid heat carrier to the biomass raw material is 10:1, and the reaction pressure of the pyrolysis reaction device 7 is 10kPa. The biochar obtained by the reaction and the medium-temperature heat carrier (520℃) are transported to the fluidized heating lifting device 2 through the pyrolysis solid product conveying screw 8 for combustion and lifting (reaction temperature: 850℃). The pyrolysis oil gas is treated by dust removal through the pyrolysis gas product primary cyclone dust collector 9 and the pyrolysis gas product secondary cyclone dust collector 11, and then is transported to the gasification conversion device 14 by the negative pressure formed by the suction gasification conversion burner 13. The pyrolysis oil gas, water vapor and oxygen are subjected to gasification conversion reaction in the gasification chamber 1402 to obtain the gasification synthesis gas (reaction temperature of the gasification chamber 1402 is 1350℃); the gasification synthesis gas is sprayed into steam through the upper swirl steam injection throat 1403, and then enters the conversion chamber 1404 to be subjected to change reaction to obtain the hydrogen-rich gas (reaction temperature of the conversion chamber 1404 is 1100℃); the hydrogen-rich gas is sprayed into steam through the lower swirl steam injection throat 1406 to be cooled to 900℃, and then is subjected to waste heat recovery through the waste heat boiler 16, spray cooling through the spray cleaning tower 17, compression through the compressor 19, and hydrogen extraction through the hydrogen extraction device 20 to obtain high-purity hydrogen gas (purity ≥99.9%).

[0045] Therefore, any person skilled in the art should understand that, within the technical scope of the present application, any equivalent replacement or change made to the technical solutions and the inventive concept of the present application should be covered by the protection scope of the present application.

Claims

1. A device for producing green hydrogen by pyrolysis and gasification of biomass, comprising a pyrolysis reaction device (7), characterized in that: The pyrolysis reaction device (7) comprises: a pyrolysis reaction tank (70) connected to a high-temperature heat carrier conveying screw (4), a biomass raw material storage bin (5), a biomass raw material conveying screw (6), and a pyrolysis solid phase product conveying screw (8); a pyrolysis acceleration structure (80) disposed inside the pyrolysis reaction tank (70); and a pyrolysis heating assembly (90) disposed outside the pyrolysis acceleration structure (80). The pyrolysis acceleration structure (80) includes: a rotating lifting component (801) installed inside the pyrolysis reaction tank (70); an intermediate shaft (802) connected to the rotating lifting component (801) and movably arranged at the center of the inside of the pyrolysis reaction tank (70); a stirring and mixing component (803) installed at the center outside the intermediate shaft (802); a cone (804) installed on the stirring and mixing component (803); a feed pipe (805) installed at the center of the top of the pyrolysis reaction tank (70) by screws; and an oblique channel (806) opened on the inner wall of the feed pipe (805) and located outside the cone (804). The feed pipe (805) is connected to the biomass raw material storage bin (5), the outer side of the cone (804) is provided with a sealing rubber ring (8041), the intermediate shaft (802) is slidably connected to the inside of the upper frame (8021), and the upper frame (8021) is installed on the inner top of the pyrolysis reaction tank (70).

2. The device for producing green hydrogen by pyrolysis and gasification of biomass according to claim 1, characterized in that: The pyrolysis reaction tank (70) comprises: an outer protective tank body (7001); a pyrolysis tank body (7002) installed inside the outer protective tank body (7001); a first input pipe (7003) connected to one side of the pyrolysis tank body (7002) and extending to one side outside the outer protective tank body (7001); a side pipe (7004) connected to the other side of the pyrolysis tank body (7002) and extending to the other side outside the outer protective tank body (7001); and an output pipe (7005) arranged at the bottom of the pyrolysis tank body (7002) and extending to the outside of the bottom of the outer protective tank body (7001). A feed pipe (805) is installed at the top center of the pyrolysis tank body (7002), a pyrolysis acceleration structure (80) is movably provided inside the pyrolysis tank body (7002), and a pyrolysis heating component (90) extending to the outside of the outer protective tank body (7001) is provided on the outside of the pyrolysis tank body (7002) and the inside of the outer protective tank body (7001).

3. The device for producing green hydrogen by pyrolysis and gasification of biomass according to claim 2, characterized in that: The rotary lifting assembly (801) comprises: a bottom bracket (8011) mounted on the bottom of the pyrolysis tank (7002); a bottom protective cover (8012) mounted at the bottom center of the bottom bracket (8011); a lifting drive source (8013) mounted on the bottom of the bottom protective cover (8012); a lifting connection plate (8014) connected to the output end of the lifting drive source (8013) and slidably connected to the inside of the bottom protective cover (8012); a lifting connection plate (8014) rotatably connected to the lifting connection plate (8014) and mounted on the intermediate shaft. A lifting rod (8015) at the bottom of the rod (802); a vertical groove (8016) provided on the outer surface of the lifting rod (8015); a first gear (8017) connected to the lifting rod (8015) via the vertical groove (8016); a second gear (8018) meshingly connected to the first gear (8017) and rotationally connected to the inside of the bottom protective cover (8012); and a rotation drive source (8019) connected to the second gear (8018) and installed at an eccentric position inside the bottom protective cover (8012).

4. The device for producing green hydrogen by pyrolysis and gasification of biomass according to claim 1, characterized in that: The stirring and mixing assembly (803) comprises: stirring spiral blades (8031) mounted on the upper and lower sides of the exterior of the intermediate shaft (802); a movable turntable (8032) disposed between the two stirring spiral blades (8031) and mounted on the exterior of the intermediate shaft (802); a skewed gear lever (8033) rotatably connected to an eccentric position inside the movable turntable (8032); a stirring blade (8034) rotatably connected to the top of the skewed gear lever (8033); and a telescopic spring (8035) mounted inside the skewed gear lever (8033) and extending to an eccentric position inside the movable turntable (8032).

5. The device for producing green hydrogen by pyrolysis and gasification of biomass according to claim 2, characterized in that: The pyrolysis heating assembly (90) comprises: a heating unit (901) arranged outside the outer protective tank (7001); and a spiral heating pipe (902) connected to the heating unit (901) and arranged outside the pyrolysis tank (7002) and inside the outer protective tank (7001).

6. The device for producing green hydrogen by pyrolysis and gasification of biomass according to claim 1, characterized in that: The device for preparing green hydrogen further comprises: a combustion blower (1), a fluidized heating and lifting device (2), a high-temperature heat carrier storage bin (3), a pyrolysis gas phase product primary cyclone dust collector (9), a pyrolysis gas phase product primary cyclone dust collector charcoal bin (10), a pyrolysis gas phase product secondary cyclone dust collector (11), a pyrolysis gas phase product secondary cyclone dust collector charcoal bin (12), an extraction type gasification conversion burner (13), a gasification conversion device (14), an ash storage bin (15), a waste heat boiler (16), a spray purification tower (17), a spray pump (18), a compressor (19) and a hydrogen extraction device (20). The combustion blower (1), the fluidized heating lifting device (2), the high-temperature heat carrier storage bin (3), the high-temperature heat carrier conveying screw (4), the pyrolysis reaction device (7) and the pyrolysis solid phase product conveying screw (8) are connected in sequence, the biomass raw material storage bin (5), the biomass raw material conveying screw (6) and the pyrolysis reaction device (7) are connected in sequence, the pyrolysis reaction device (7), the pyrolysis gas phase product first-stage cyclone dust collector (9), the pyrolysis gas phase product second-stage cyclone dust collector (11), the extraction type gasification conversion device (12) and the pyrolysis reaction device (13) are connected in sequence. The burner (13), the gasification conversion device (14), the waste heat boiler (16), the spray purification tower (17), the spray pump (18), the compressor (19) and the hydrogen extraction device (20) are connected in sequence, the pyrolysis gas phase product first-stage cyclone dust collector (9) is connected to the pyrolysis gas phase product first-stage cyclone dust collector charcoal bin (10), the pyrolysis gas phase product second-stage cyclone dust collector (11) is connected to the pyrolysis gas phase product second-stage cyclone dust collector charcoal bin (12), and the gasification conversion device (14) is connected to the ash storage bin (15).

7. The device for producing green hydrogen by pyrolysis and gasification of biomass according to claim 6, characterized in that: The extraction type gasification conversion burner (13) is composed of an extraction steam inlet (1301), a central oxygen inlet (1302), an outer ring oxygen inlet (1303), a cooling circulating water inlet (1304), a gasification device interface flange (1305), a cooling circulating water outlet (1306), a pyrolysis gas phase product inlet (1307), a steam injection pipe (1308), a steam injection pipe reduction (1309), a central oxygen support frame (1310), a burner tapered pipe (1311), a burner throat (1312) and a burner expansion pipe (1313). The suction steam inlet (1301) is arranged at the end side of the extraction type gasification conversion burner (13), the central oxygen inlet (1302) is arranged in the central axis direction of the extraction type gasification conversion burner (13), the line end of the steam injection pipe (1308) is provided with a steam injection pipe reduction (1309), and the steam reaches the maximum flow rate at the position of the steam injection pipe reduction (1309), the outer shell of the extraction type gasification conversion burner (13) is composed of a burner tapered tube (1311), a burner throat (1312) and a burner expansion tube (1313), the suction steam inlet (1301) is provided with four groups of channels, and the four groups of channels are respectively arranged from the inside to the outside as a central oxygen inlet (1302) channel, a pyrolysis gas phase product inlet (1307) channel, an outer ring oxygen inlet (1303) channel, a cooling circulation water inlet (1304) and a cooling circulation water outlet (1306) channel. The gasification device interface flange (1305) is provided on the straight pipe section of the extraction-type gasification conversion burner (13), and a central oxygen support frame (1310) is provided in the central oxygen inlet (1302) of the extraction-type gasification conversion burner (13).

8. The device for producing green hydrogen by pyrolysis and gasification of biomass according to claim 6, characterized in that: The gasification conversion device (14) is composed of a gasification interface flange (1401), a gasification chamber (1402), an upper swirl steam injection throat (1403), a conversion chamber (1404), an upper swirl steam injection throat steam inlet (1405), a lower swirl steam injection throat (1406), a lower swirl steam injection throat steam inlet (1407), a slag drop pipe (1408), a slag discharge port at the bottom of the gasification device (1409), a gasification device gas outlet (1410), a gasification device refractory lining (1411), a gasification device thermal insulation layer (1412) and a gasification device thermal insulation layer (1413). The gasification interface flange (1401) of the gasification conversion device (14) is connected to the extraction type gasification conversion burner (13), the gasification chamber (1402) is located in the upper area of ​​the gasification conversion device (14), and the conversion chamber (1404) is located in the lower area of ​​the gasification conversion device (14). The gasification chamber (1402) and the conversion chamber (1404) are separated by an upper swirl steam injection throat (1403). The lower part of the conversion chamber (1404) is sequentially provided with a lower swirl steam injection throat (1406) and a slag drop pipe (1408). The bottom slag discharge port (1409) of the gasification device is located in the bottom area of ​​the gasification conversion device (14). The gas port (1410) is arranged on the side of the gasification conversion device (14), and the gasification device gas outlet (1410) is located on the lower side of the lower swirl steam injection throat (1406) and the upper area of ​​the slag drop pipe (1408) outlet. The gasification conversion device (14) comprises, from the inside to the outside, a gasification device refractory lining (1411), a gasification device thermal insulation layer (1412) and a gasification device thermal insulation layer (1413). The upper swirl steam injection throat steam inlet (1405) is arranged at one end of the upper swirl steam injection throat (1403), and the lower swirl steam injection throat steam inlet (1407) is arranged at one end of the lower swirl steam injection throat (1406).

9. The device for producing green hydrogen by pyrolysis and gasification of biomass according to claim 8, characterized in that: The upper swirl steam injection throat (1403) is composed of an upper swirl steam injection throat steam nozzle (140301) and an upper swirl steam injection throat steam chamber (140302). Wherein, the lower swirl steam injection throat (1406) is composed of a lower swirl steam injection throat steam nozzle (140601) and a lower swirl steam injection throat steam chamber (140602).

10. A method for producing green hydrogen by pyrolysis and gasification of biomass, with reference to the device for producing green hydrogen by pyrolysis and gasification of biomass according to any one of claims 1 to 9, characterized in that: The following steps are involved: S1. The biomass raw materials are crushed and pulverized to obtain raw materials with a particle size of ≤10mm; S2. Raw materials with a particle size of ≤10mm enter the drying system to reduce the moisture content of the raw materials to below 5%. The drying heat source is the waste heat flue gas of the system; S3, after drying, the raw materials with a moisture content of ≤5% are transported to the biomass raw material storage bin (5), and the dried raw materials are transported to the pyrolysis reaction device (7) through the biomass raw material conveying screw (6); at the same time, the high-temperature heat carrier located in the high-temperature heat carrier storage bin (3) is transported to the pyrolysis reaction device (7) through the high-temperature heat carrier conveying screw (4), and the biomass raw materials and the high-temperature heat carrier are fully transferred in the pyrolysis reaction device (7) to obtain high-temperature biochar and pyrolysis oil and gas; S4, the mixture of high-temperature biochar and medium-temperature heat carrier is transported into the fluidized heating and lifting device (2) through the pyrolysis solid phase product conveying screw (8), and air is introduced at the same time. The high-temperature biochar is fully burned in the fluidized heating and lifting device (2), so that the medium-temperature heat carrier is heated to obtain a high-temperature heat carrier, and the heat carrier is lifted to the high-temperature heat carrier storage bin (3); the flue gas is used for drying the raw materials; S5, the pyrolysis oil and gas are sequentially dusted by the first-stage cyclone dust collector (9) and the second-stage cyclone dust collector (11) of the pyrolysis gas phase product, and then enter the extraction type gasification conversion burner (13). The mass transfer power of the pyrolysis oil and gas is mainly provided by the negative pressure formed by the steam sprayed into the extraction type gasification conversion burner (13); the oxygen enters the extraction type gasification conversion burner (13) in two ways, namely central oxygen and annular oxygen. The pyrolysis oil and gas, steam and oxygen enter the gasification chamber of the gasification conversion device (14). A gasification reaction occurs in (1402) to obtain gasified synthesis gas; the gasified synthesis gas passes through the upper cyclonic steam injection throat (1403) area and is injected by the steam cyclone, and the gasified synthesis gas and steam undergo a water-gas shift reaction to obtain hydrogen-rich gas; the hydrogen-rich gas passes through the lower cyclonic steam injection throat (1406) area and is injected by the steam cyclone, and the temperature of the hydrogen-rich gas drops below the ash melting point, and the solid ash is discharged to the bottom of the gasification conversion device (14) through the slag drop pipe (1408); S6, the hydrogen-rich gas is sequentially subjected to heat exchange in the waste heat boiler (16), spray cooling and purification in the spray purification tower (17), compression in the compressor (19), and hydrogen extraction treatment in the hydrogen extraction device (20) to obtain a high-purity hydrogen product; the steam generated by the waste heat boiler (16) is used for the supply of the induced gasification conversion burner (13) and the gasification conversion device (14).

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