Device and method for preparing green hydrogen by biomass pyrolysis gasification

Abstract

The application discloses a device and method for preparing green hydrogen through biomass pyrolysis and gasification, relates to the technical field of green hydrogen preparation, and solves the problems of blockage and corrosion caused by ash melting and slagging in the pure oxygen gasification process, and the problem of low energy utilization rate. The device for preparing green hydrogen through biomass pyrolysis and gasification comprises a pyrolysis reaction device, and the pyrolysis reaction device comprises a pyrolysis reaction tank connected with a high-temperature heat carrier conveying spiral, a biomass raw material storage bin, a biomass raw material conveying spiral and a pyrolysis solid-phase product conveying spiral. In the application, biomass raw materials are converted into biochar and pyrolysis oil gas through pyrolysis technology, the biomass ash is effectively cut, and problems such as blockage and corrosion caused by ash melting and slagging in the pure oxygen gasification process are effectively avoided; the high-temperature pyrolysis oil gas is directly subjected to pure oxygen gasification reaction through gasification technology, the sensible heat and latent heat in the pyrolysis oil gas are fully utilized, and the energy utilization rate is high.

Description

Technical Field

[0001] This invention relates to the field of green hydrogen production technology, specifically to an apparatus and method for producing green hydrogen through biomass pyrolysis and gasification. Background Technology

[0002] Hydrogen is clean, low-carbon, high in calorific value, diverse in sources, and flexible in storage and transportation, making it a promising candidate to become the "ultimate energy source" of the 21st century. Green hydrogen is hydrogen produced using renewable energy sources such as solar, wind, nuclear, and biomass energy. Currently, green hydrogen primarily originates from "solar / wind power generation - water electrolysis to produce hydrogen."

[0003] Biomass energy, characterized by its abundant resources and wide distribution, is one of the most promising renewable energy sources. The production of green hydrogen from biomass has attracted significant attention across various sectors due to the wide availability of raw materials and high hydrogen yield. Currently, the mainstream technologies for producing green hydrogen from biomass are bio-fermentation hydrogen production and direct biomass gasification hydrogen production. Biomass fermentation hydrogen production technology primarily targets organic waste liquids and agricultural waste rich in carbohydrates such as glucose, starch, and cellulose. However, raw materials containing lignin, such as straw and forestry waste, are more difficult to utilize, requiring strict control over the types of raw materials used.

[0004] However, this green hydrogen production device has the following drawbacks in practical use:

[0005] 1. Existing green hydrogen production devices generally employ a method of mixed pyrolysis of a solid heat carrier and biomass feedstock to obtain gaseous pyrolysis volatiles and solid pyrolysis materials. The solid pyrolysis materials are then mixed with the solid heat carrier and combusted to heat the solid heat carrier. The gaseous pyrolysis volatiles enter a catalytic bed for reforming to produce high-purity hydrogen. However, because biomass ash has a low melting point, generally below 900℃, direct biomass gasification technology uses a gasification temperature higher than the biomass ash melting point to reduce tar, hydrocarbons, methane, and other components in the gaseous products. This results in ash melting, which easily adheres to the reactor, affecting the continuous operation of the system.

[0006] 2. In existing green hydrogen production facilities, tar-like substances are present in the gaseous products. The mass transfer power of the pyrolysis oil and gas generally relies on the exhaust fan at the back end of the process or is entirely provided by the pressure boosting of the front-end pyrolysis unit. Traditional solutions typically use a back-end exhaust fan, which means that the gasification conversion, reforming catalysis, and other units operate under slightly positive or negative pressure, which is not conducive to the forward progress of the reforming hydrogen production reaction. If the pressure is provided by increasing the reaction pressure of the front-end pyrolysis unit, it places higher demands on the pyrolysis reactor, pyrolysis feed system, etc., increasing the equipment complexity and cost.

[0007] 3. Existing green hydrogen production facilities produce pyrolysis gaseous products containing impurities such as tar, dust, and hydrogen sulfide. Traditional methods typically employ catalytic reforming to treat these impurities. However, in practice, the catalyst is prone to problems such as carbon buildup, coking, poisoning, and deactivation. Furthermore, the system suffers from significant catalyst loss, poor process continuity, and high costs, making it unsuitable for large-scale application. Summary of the Invention

[0008] The purpose of this invention is to provide an apparatus and method for preparing green hydrogen by biomass pyrolysis and gasification, so as to solve the problems mentioned in the background art.

[0009] To achieve the above-mentioned objectives, the present invention adopts the following technical solution:

[0010] This invention provides an apparatus for producing green hydrogen through biomass pyrolysis and gasification, comprising a pyrolysis reaction device. The pyrolysis reaction device includes: a pyrolysis reactor connected to a high-temperature heat carrier conveying screw, a biomass feedstock storage silo, a biomass feedstock conveying screw, and a pyrolysis solid-phase product conveying screw; a pyrolysis acceleration structure disposed inside the pyrolysis reaction reactor; and a pyrolysis heating assembly disposed outside the pyrolysis acceleration structure.

[0011] The pyrolysis acceleration structure includes: a rotary lifting assembly installed inside the pyrolysis reactor; an intermediate shaft connected to the rotary lifting assembly and movably disposed at the center of the pyrolysis reactor; a stirring and mixing assembly installed at the center of the outer side of the intermediate shaft; a conical body installed on the stirring and mixing assembly; a feed pipe installed at the center of the top of the pyrolysis reactor by screws; and an oblique channel formed on the inner wall of the feed pipe and located outside the conical body.

[0012] The feed pipe is connected to the biomass raw material storage silo, a sealing rubber ring is fitted on the outer side of the cone, the intermediate shaft is slidably connected to the inside of the upper top frame, and the upper top frame is installed on the inner top of the pyrolysis reaction tank.

[0013] As a preferred embodiment of the present invention, the pyrolysis reactor includes: an outer protective tank; a pyrolysis tank installed inside the outer protective tank; a first input pipe connected to one side of the pyrolysis tank and extending to the outside of the outer protective tank; a side pipe connected to the other side of the pyrolysis tank and extending to the other side of the outside of the outer protective tank; and an output pipe disposed at the bottom of the pyrolysis tank and extending to the outside of the bottom of the outer protective tank.

[0014] The pyrolysis tank has a feed pipe installed at the top center, a pyrolysis acceleration structure is movable inside the pyrolysis tank, and pyrolysis heating components extending to the outside of the outer protective tank are provided on the outer side of the pyrolysis tank and the inner side of the outer protective tank.

[0015] As a preferred embodiment of the present invention, the rotary lifting assembly includes: a bottom support installed at the bottom of the pyrolysis tank; a bottom protective cover installed at the center of the bottom of the bottom support; a lifting drive source installed at the bottom of the bottom protective cover; a lifting connecting plate connected to the output end of the lifting drive source and slidably connected inside the bottom protective cover; a lifting rotating rod rotatably connected to the lifting connecting plate and installed at the bottom of the intermediate shaft; a vertical groove formed 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 meshing with the first gear and rotatably connected inside the bottom protective cover; and a rotary drive source connected to the second gear and installed at an eccentric position inside the bottom protective cover.

[0016] As a preferred embodiment of the present invention, the mixing assembly includes: mixing spiral blades installed on the upper and lower sides of the outside of the intermediate shaft; a movable turntable disposed between the two mixing spiral blades and installed on the outside of the intermediate shaft; an eccentric stop rod rotatably connected to the inside of the movable turntable; mixing blades rotatably connected to the top of the eccentric stop rod; and a telescopic spring installed inside the eccentric stop rod and extending to the inside of the movable turntable at the eccentric position.

[0017] As a preferred embodiment of the present invention, the pyrolysis heating assembly includes: a heating unit disposed on the outside of the outer protective tank; and a spiral heating pipe connected to the heating unit and disposed on the outside of the pyrolysis tank and the inside of the outer protective tank.

[0018] As a preferred embodiment of the present invention, the apparatus for preparing green hydrogen further includes: a combustion blower, a fluidized bed heating and lifting device, a high-temperature heat carrier storage silo, a primary cyclone dust collector for pyrolysis gaseous products, a carbon bin for the primary cyclone dust collector for pyrolysis gaseous products, a secondary cyclone dust collector for pyrolysis gaseous products, a carbon bin for the secondary cyclone dust collector for pyrolysis gaseous products, a traction-type gasification conversion burner, a gasification conversion device, an ash storage silo, a waste heat boiler, a spray purification tower spray pump, a compressor, and a hydrogen extraction device.

[0019] The combustion blower, fluidized bed heating lifting device, high-temperature heat carrier storage silo, high-temperature heat carrier conveying screw, pyrolysis reaction device, and pyrolysis solid product conveying screw are connected in sequence. The biomass raw material storage silo, biomass raw material conveying screw, and pyrolysis reaction device are connected in sequence. The pyrolysis reaction device, pyrolysis gas phase product primary cyclone dust collector, pyrolysis gas phase product secondary cyclone dust collector, induced draft 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 primary cyclone dust collector and the pyrolysis gas phase product primary cyclone dust collector carbon bin are connected. The pyrolysis gas phase product secondary cyclone dust collector and the pyrolysis gas phase product secondary cyclone dust collector carbon bin are connected. The gasification conversion device and ash storage silo are connected.

[0020] As a preferred embodiment of the present invention, the extraction-type gasification conversion burner comprises a 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 phase product inlet, a steam injection pipe, a reduced diameter steam injection pipe, a central oxygen support frame, a burner conical tube, a burner throat, and a burner expansion tube.

[0021] The suction steam inlet is located at the end of the suction-type gasification conversion burner, and the central oxygen inlet is located along the central axis of the suction-type gasification conversion burner. The end of the steam injection pipe has a reduced diameter, and the steam reaches its maximum flow velocity at the reduced diameter location. The outer shell of the suction-type gasification conversion burner consists of a burner conical tube, a burner throat, and a burner expansion tube. The suction steam inlet has four sets of channels, which, from the inside out, are respectively configured as a central oxygen inlet channel, a pyrolysis gas phase product inlet channel, an outer ring oxygen inlet channel, a cooling circulating water inlet, and a cooling circulating water outlet.

[0022] The gasification device interface flange is located in the straight pipe section of the induced gasification converter burner, and a central oxygen support frame is provided in the central oxygen inlet of the induced gasification converter burner.

[0023] As a preferred embodiment of the present invention, the gasification conversion device comprises a gasification interface flange, a gasification chamber, an upper swirl-type steam jet throat, a conversion chamber, a steam inlet of the upper swirl-type steam jet throat, a lower swirl-type steam jet throat, a slag discharge pipe, a bottom slag discharge port of the gasification device, a gas outlet of the gasification device, a refractory lining of the gasification device, a heat insulation layer of the gasification device, and a thermal insulation layer of the gasification device.

[0024] 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 region of the gasification conversion device, and the conversion chamber is located in the lower region of the gasification conversion device. The gasification chamber and the conversion chamber are isolated by an upper swirl-type steam jet throat. A lower swirl-type steam jet throat and a slag discharge pipe are sequentially arranged in the lower part of the conversion chamber. The bottom slag discharge port of the gasification device is located in the bottom region of the gasification conversion device. The gas outlet of the gasification device is located on the side of the gasification conversion device. The gas outlet of the gasification device is located below the lower swirl-type steam jet throat and above the outlet of the slag discharge pipe. The gasification conversion device consists of a refractory lining, a heat insulation layer, and a thermal insulation layer from the inside to the outside. The steam inlet of the upper swirl-type steam jet throat is located at one end of the upper swirl-type steam jet throat, and the steam inlet of the lower swirl-type steam jet throat is located at one end of the lower swirl-type steam jet throat.

[0025] As a preferred embodiment of the present invention, the upper swirl-type steam jet throat is composed of an upper swirl-type steam jet throat steam nozzle and an upper swirl-type steam jet throat steam chamber.

[0026] The lower swirl steam jet throat consists of a lower swirl steam jet throat steam nozzle and a lower swirl steam jet throat steam chamber.

[0027] This invention also provides a method for preparing green hydrogen through biomass pyrolysis and gasification, comprising the following steps:

[0028] S1. Biomass raw materials are pre-treated by crushing and grinding to obtain raw materials with a particle size ≤10mm;

[0029] S2. Raw materials with a particle size ≤10mm enter the drying system to reduce the moisture content of the raw materials to below 5%, and the drying heat source is the waste heat flue gas of the system;

[0030] S3. Raw materials with a moisture content of ≤5% after drying are transported to the biomass raw material storage silo. The dried raw materials are then transported to the pyrolysis reaction device via a biomass raw material conveying screw. At the same time, the high-temperature heat carrier located in the high-temperature heat carrier storage silo is transported to the pyrolysis reaction device via a high-temperature heat carrier conveying screw. The biomass raw materials and the high-temperature heat carrier undergo full mass and heat transfer in the pyrolysis reaction device to obtain high-temperature biochar and pyrolysis oil and gas.

[0031] S4. The mixture of high-temperature biochar and medium-temperature heat carrier is conveyed into the fluidized heating and lifting device via a pyrolysis solid product conveying screw conveyor. At the same time, air is introduced. The high-temperature biochar is fully combusted in the fluidized heating and lifting device, which raises the temperature of the medium-temperature heat carrier to obtain a high-temperature heat carrier. The heat carrier is then lifted to the high-temperature heat carrier storage silo. The flue gas is used for raw material drying.

[0032] S5. Pyrolysis oil and gas are sequentially treated by a primary cyclone dust collector and a secondary cyclone dust collector for pyrolysis gas phase products before entering the induced draft gasification converter burner. The mass transfer power of the pyrolysis oil and gas is mainly provided by the negative pressure formed by the injection of steam into the induced draft gasification converter burner. Oxygen enters the induced draft gasification converter burner in two streams: central oxygen and annular oxygen. The pyrolysis oil and gas, steam, and oxygen undergo a gasification reaction in the gasification chamber of the gasification converter to obtain gasified syngas. The gasified syngas passes through the upper swirl-type steam injection throat area and is injected by a swirling steam stream. The gasified syngas and steam undergo a water-gas shift reaction to obtain hydrogen-rich gas. The hydrogen-rich gas passes through the lower swirl-type steam injection throat area and is injected by a swirling steam stream. 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 converter through the ash discharge pipe.

[0033] S6. Hydrogen-rich gas is sequentially processed through a waste heat boiler for heat exchange, a spray purification tower for cooling and purification, a compressor for compression, and a hydrogen extraction unit for further hydrogen extraction to obtain high-purity hydrogen product. The steam generated by the waste heat boiler is used to power the induced draft gasification converter burners and the gasification conversion unit.

[0034] Compared with existing technologies, one or more of the above technical solutions have the following beneficial effects:

[0035] 1. In the apparatus and method for producing green hydrogen from biomass pyrolysis gasification, to address the issue of ash melting during the biomass thermochemical conversion process, pyrolysis is used to solidify the biomass ash in biochar. For the pyrolysis oil and gas, a two-stage dust removal system is employed to reduce the content of biochar impurities. To address the small amount of ash melting present during the gasification stage of the pyrolysis oil and gas, a multi-stage steam swirl jet is used to reduce the ash content below its melting point, forming a solid particle removal system, thus solving the ash melting problem. Simultaneously, a uniquely designed extraction-type gasification conversion burner is used to address the characteristics of pyrolysis oil in the gas being prone to condensation and coking. This design not only ensures effective discharge of pyrolysis oil and gas from the pyrolysis section but also enables positive pressure gasification conversion operation within the gasification conversion unit. This reduces the equipment processing difficulty and cost of the pyrolysis system and pyrolysis feeding system while ensuring the full progress of the gasification conversion reaction.

[0036] 2. In the apparatus and method for producing green hydrogen through biomass pyrolysis gasification, a pyrolysis oil and gas gasification conversion device was invented for the high-temperature pyrolysis oil and gas gasification hydrogen production process. The entire process does not require the addition of a catalyst. Furthermore, the gasification conversion device adopts a multi-stage throat design, with multiple steam nozzles at the throat positions, which facilitates the forward reaction of the water-gas transformation, resulting in a greater yield of hydrogen. Compared to traditional methods of producing green hydrogen, this process offers advantages such as low loss, continuous operation, and low cost, making it suitable for large-scale application.

[0037] 3. In the apparatus and method for producing green hydrogen through biomass pyrolysis and gasification, a combination of "pyrolysis + gasification conversion" is adopted. Biochar and pyrolysis oil and gas are obtained through biomass pyrolysis, and biomass ash remains in the biochar, realizing ash separation in biomass and avoiding the impact of ash melting and slagging on the continuous operation of the process. For pyrolysis oil and gas, the impurity content of biochar is reduced by two-stage cyclone separation. The gasification conversion unit is equipped with a multi-stage water vapor cyclone jet device to reduce the temperature of hydrogen-rich conversion gas below the ash melting point, avoiding the impact of molten ash on the unit.

[0038] 4. In the apparatus and method for preparing green hydrogen by biomass pyrolysis and gasification, when the raw materials (high-temperature solid heat carrier and bamboo chips) are mixed and pyrolyzed, the raw materials can be conveyed by a cutting method and driven to contact in the vortex generated outside the intermediate shaft by the rotating intermediate shaft. While ensuring the contact area of ​​the raw materials (high-temperature solid heat carrier and bamboo chips) during pyrolysis and mixing, the irregularly shaped vortex (through the rotating stirring blades in the middle) can ensure that the raw materials are heated evenly during the mixing process, avoiding local overheating or undercooling, which can significantly improve the effect and efficiency of pyrolysis.

[0039] 5. In the apparatus and method for producing green hydrogen through biomass pyrolysis and gasification, when the intermediate shaft is driven to rotate and move up and down to achieve the mixing and pyrolysis of raw materials (high-temperature solid heat carrier and bamboo chips), the up and down 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 through multiple oblique channels opened on its outer wall, and fall to the eccentric part 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. Attached Figure Description

[0040] The accompanying drawings, which form part of this invention, are used to provide a further understanding of the invention. The illustrative embodiments of the invention and their descriptions are used to explain the invention and do not constitute an improper limitation of the invention.

[0041] Furthermore, the terms "installation," "setup," "equipped with," "connection," "linking," and "socketing" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral structure; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium, or an internal connection between two devices, components, or parts. Those skilled in the art can understand the specific meaning of these terms in this application based on the specific circumstances.

[0042] Figure 1 This is a flowchart of the overall process of this invention;

[0043] Figure 2 This is a schematic diagram of the pyrolysis reaction apparatus of the present invention;

[0044] Figure 3 This is a cross-sectional schematic diagram of the pyrolysis reaction apparatus of the present invention;

[0045] Figure 4 This is a schematic diagram of the pyrolysis reaction apparatus of the present invention in a cross section;

[0046] Figure 5 This is a schematic diagram showing the cross-sectional view of the connection between the pyrolysis reaction vessel and the pyrolysis heating assembly of the present invention;

[0047] Figure 6 This is a schematic diagram of the pyrolysis acceleration structure of the present invention;

[0048] Figure 7 This is a cross-sectional structural schematic diagram of the connection between the rotary lifting assembly and the intermediate shaft of the present invention;

[0049] Figure 8 This is the present invention. Figure 7 Enlarged structural diagram of region A in the middle;

[0050] Figure 9 This is a schematic diagram of the connection between the intermediate shaft and the mixing assembly of the present invention;

[0051] Figure 10 This is a cross-sectional structural diagram showing the connection between the intermediate shaft and the feed pipe of the present invention;

[0052] Figure 11 This is a schematic diagram of the gasification conversion device of the present invention;

[0053] Figure 12 This is a schematic diagram of the structure of the extraction-type gasification conversion burner of the present invention;

[0054] Figure 13 This is a schematic diagram of the front section of the upper swirling steam jet throat of the present invention;

[0055] Figure 14 This is a top-section structural diagram of the upper swirling steam jet throat of the present invention;

[0056] Figure 15 This is a schematic diagram of the cross-section of the lower swirling steam jet throat of the present invention;

[0057] Figure 16 This is a schematic diagram of the structure of the lower swirling steam jet throat of the present invention (top section).

[0058] In the picture:

[0059] 1. Combustion blower; 2. Fluidized bed heating lifting device; 3. High-temperature heat carrier storage silo; 4. High-temperature heat carrier conveying screw; 5. Biomass raw material storage silo; 6. Biomass raw material conveying screw; 7. Pyrolysis reaction device; 8. Pyrolysis solid phase product conveying screw; 9. Primary cyclone dust collector for pyrolysis gas phase products; 10. Carbon bin for primary cyclone dust collector for pyrolysis gas phase products; 11. Secondary cyclone dust collector for pyrolysis gas phase products; 12. Carbon bin for secondary cyclone dust collector for pyrolysis gas phase products; 13. Extraction-type gasification conversion burner; 14. Gasification conversion device; 15. Ash and slag storage silo; 16. Waste heat boiler; 17. Spray purification tower; 18. Spray pump; 19. Compressor; 20. Hydrogen extraction device;

[0060] 1301. 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 phase product inlet; 1308. Steam injection pipe; 1309. Steam injection pipe reducer; 1310. Central oxygen support frame; 1311. Burner conical tube; 1312. Burner throat; 1313. Burner expansion tube;

[0061] 1401. Gasification interface flange; 1402. Gasification chamber; 1403. Upper swirl-type steam jet throat; 1404. Conversion chamber; 1405. Steam inlet of upper swirl-type steam jet throat; 1406. Lower swirl-type steam jet throat; 1407. Steam inlet of lower swirl-type steam jet throat; 1408. Ash discharge pipe; 1409. Ash discharge port at the bottom of the gasification unit; 1410. Gas outlet of the gasification unit; 1411. Refractory lining of the gasification unit; 1412. Heat insulation layer of the gasification unit; 1413. Thermal insulation layer of the gasification unit;

[0062] 140301, Upper swirl-type steam jet throat steam nozzle; 140302, Upper swirl-type steam jet throat steam chamber;

[0063] 140601, Lower swirl-type steam jet throat steam nozzle; 140602, Lower swirl-type steam jet throat steam chamber;

[0064] 70. Pyrolysis reaction vessel; 7001. Outer protective vessel; 7002. Pyrolysis vessel body; 7003. First input pipe; 7004. Side pipe; 7005. Output pipe;

[0065] 80. Pyrolysis acceleration structure; 801. Rotary lifting assembly; 802. Intermediate shaft; 8021. Upper top frame; 803. Agitating and mixing assembly; 804. Conical body; 8041. Sealing rubber ring; 805. Feed pipe; 806. Inclined channel;

[0066] 8011, Bottom bracket; 8012, Bottom protective cover; 8013, Lifting drive source; 8014, Lifting connecting plate; 8015, Lifting rotating rod; 8016, Vertical groove; 8017, First gear; 8018, Second gear; 8019, Rotation drive source;

[0067] 8031. Agitator blades; 8032. Movable turntable; 8033. Deflector lever; 8034. Agitator blades; 8035. Telescopic spring;

[0068] 90. Pyrolysis heating assembly; 901. Heating unit; 902. Spiral heating pipe;

[0069] 100. Discharge cooling assembly; 1001. Cooling unit; 1002. Cooling spiral tube. Detailed Implementation

[0070] To enable those skilled in the art to better understand the present application, the technical solutions in the embodiments of the present application will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present application, and not all embodiments. Based on the embodiments in the present application, all other embodiments obtained by those of ordinary skill in the art without creative effort should fall within the scope of protection of the present application. Example 1

[0071] Please see Figures 1-16 An apparatus for producing green hydrogen through biomass pyrolysis and gasification includes a pyrolysis reaction unit 7. The pyrolysis reaction unit 7 comprises: a pyrolysis reactor 70 connected to a high-temperature heat carrier conveying spiral 4, a biomass raw material storage silo 5, a biomass raw material conveying spiral 6, and a pyrolysis solid product conveying spiral 8; a pyrolysis acceleration structure 80 disposed inside the pyrolysis reactor 70; and a pyrolysis heating assembly 90 disposed outside the pyrolysis acceleration structure 80. The pyrolysis acceleration structure 80 includes: a rotary lifting assembly 801 installed inside the pyrolysis reactor 70; and a movably disposed at the center inside the pyrolysis reactor 70, connected to the rotary lifting assembly 801. The intermediate shaft 802; the stirring and mixing assembly 803 installed at the center of the outside of the intermediate shaft 802; the conical body 804 installed on the stirring and mixing assembly 803; the feed pipe 805 installed at the center of the top of the pyrolysis reactor 70 by screws; the inclined channel 806 opened on the inner wall of the feed pipe 805 and located outside the conical body 804, wherein the feed pipe 805 is connected to the biomass raw material storage bin 5, the outer side of the conical body 804 is fitted with a sealing rubber ring 8041, the intermediate shaft 802 is slidably connected to the inside of the upper top frame 8021, and the upper top frame 8021 is installed on the inner top of the pyrolysis reactor 70.

[0072] In this invention, the pyrolysis reaction vessel 70 includes: an outer protective vessel 7001; a pyrolysis vessel 7002 installed inside the outer protective vessel 7001; a first input pipe 7003 connected to one side of the pyrolysis vessel 7002 and extending to the outside of the outer protective vessel 7001; a side pipe 7004 connected to the other side of the pyrolysis vessel 7002 and extending to the other side of the outer protective vessel 7001; and an output pipe 7005 disposed at the bottom of the pyrolysis vessel 7002 and extending to the outside of the bottom of the outer protective vessel 7001. A feed pipe 805 is installed at the center of the top of the pyrolysis vessel 7002, a pyrolysis acceleration structure 80 is movably disposed inside the pyrolysis vessel 7002, and pyrolysis heating components 90 extending to the outside of the outer protective vessel 7001 are disposed on the outside of the pyrolysis vessel 7002 and the inside of the outer protective vessel 7001.

[0073] The working principle described above is as follows: By installing a rotating intermediate shaft 802 (driven by a rotating lifting assembly 801) that can be raised and lowered inside the pyrolysis reactor 70, the various raw materials (high-temperature solid heat carrier and bamboo chips) entering the pyrolysis reactor 70 can be accelerated to mix, increasing the contact area and uniformity of the mixing and pyrolysis reaction, thereby improving the efficiency of the pyrolysis reaction. Simultaneously, while the intermediate shaft 802 is rotating and raised / lowered, the material inside the feed pipe 805 will intermittently move through the inclined channel 806 or the bottom channel of the feed pipe 805, ensuring that the bamboo chip raw material can enter the pyrolysis reactor 7002 in an irregular moving and conveying manner, further increasing the contact area with the pyrolysis reactor 7002, and achieving more efficient raw material pyrolysis.

[0074] For details, please refer to the following: Figure 7 and Figure 8 The rotary lifting assembly 801 includes: a bottom support 8011 installed at the bottom of the pyrolysis tank 7002; a bottom protective cover 8012 installed at the center of the bottom of the bottom support 8011; a lifting drive source 8013 installed at the bottom of the bottom protective cover 8012; a lifting connecting plate 8014 connected to the output end of the lifting drive source 8013 and slidably connected inside the bottom protective cover 8012; a lifting rotating rod 8015 rotatably connected to the lifting connecting plate 8014 and installed at the bottom of the intermediate shaft 802; a vertical groove 8016 formed 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 meshing with the first gear 8017 and rotatably connected inside the bottom protective cover 8012; and a rotary drive source 8019 connected to the second gear 8018 and installed at an eccentric position inside the bottom protective cover 8012.

[0075] In the biomass pyrolysis gasification apparatus for producing green hydrogen of the present invention, when the intermediate shaft 802 is rotated and moved up and down to mix the raw materials and carry out 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, and the first gear 8017 meshing with the side of the second gear 8018 will rotate. When the first gear 8017 rotates, the vertical groove 8016 on its inner side can drive the lifting rod 8015 to rotate without affecting the up and down movement of the lifting rod 8015, thereby driving the intermediate shaft 802 connected to the lifting rod 8015 to rotate. At the same time, the lifting drive source 8013 can be activated to drive the lifting rod 8015 and the intermediate shaft 802, which are rotatably connected to the output end of the lifting drive source 8013 through the lifting connecting plate 8014, to move up and down, thereby accelerating the efficiency of raw material mixing and pyrolysis reaction.

[0076] For details, please refer to the following: Figure 9 The mixing assembly 803 includes: mixing spiral blades 8031 ​​installed on the upper and lower sides of the outside of the intermediate shaft 802; a movable turntable 8032 disposed between the two mixing spiral blades 8031 ​​and installed on the outside of the intermediate shaft 802; an eccentric stop bar 8033 rotatably connected to the eccentric part inside the movable turntable 8032; mixing blades 8034 rotatably connected to the top of the eccentric stop bar 8033; and a telescopic spring 8035 installed inside the eccentric stop bar 8033 and extending to the eccentric part inside the movable turntable 8032.

[0077] In the biomass pyrolysis gasification apparatus for producing green hydrogen of the present invention, when the intermediate shaft 802 rotates, the movable turntable 8032 and the stirring spiral blade 8031 ​​mounted on its outer side rotate synchronously. Through the structural shape of the stirring spiral blade 8031, a vortex is formed on the outside, ensuring that the raw materials are thoroughly mixed together. Simultaneously, the centrifugal force generated when the movable turntable 8032 rotates causes the deflection baffle 8033 and the stirring blade 8034 to have an outward tendency, increasing the size of the vortex in the central mixing and pyrolysis zone. Through irregular pyrolysis and mixing vortices, the efficiency of the pyrolysis reaction is improved.

[0078] For details, please refer to the following: Figure 5 The pyrolysis heating assembly 90 includes: a heating unit 901 disposed on the outside of the outer protective tank 7001; and a spiral heating pipe 902 connected to the heating unit 901 and disposed on the outside of the pyrolysis tank 7002 and the inside of the outer protective tank 7001. Example 2

[0079] Please see Figures 1-16A device for producing green hydrogen through biomass pyrolysis and gasification, comprising: a combustion blower 1, a fluidized bed heating and lifting device 2, a high-temperature heat carrier storage silo 3, a primary cyclone dust collector 9 for pyrolysis gaseous products, a carbon bin 10 for the primary cyclone dust collector 11 for pyrolysis gaseous products, a carbon bin 12 for the secondary cyclone dust collector 11 for pyrolysis gaseous products, a traction-type gasification conversion burner 13, a gasification conversion device 14, an ash storage silo 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, fluidized bed heating and lifting device 2, high-temperature heat carrier storage silo 3, high-temperature heat carrier conveying screw 4, pyrolysis reaction device 7, and... The pyrolysis solid product conveying screw 8 is connected in sequence. The biomass raw material storage silo 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 primary cyclone dust collector 9, the pyrolysis gas phase product secondary cyclone dust collector 11, the induced draft 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 phase product primary cyclone dust collector 9 and the pyrolysis gas phase product primary cyclone dust collector carbon bin 10 are connected. The pyrolysis gas phase product secondary cyclone dust collector 11 and the pyrolysis gas phase product secondary cyclone dust collector carbon bin 12 are connected. The gasification conversion device 14 and the ash and slag storage silo 15 are connected.

[0080] For details, please refer to the following: Figure 12The extraction-type gasification conversion burner 13 consists 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 reducer 1309, a central oxygen support frame 1310, a burner conical tube 1311, a burner throat 1312, and a burner expansion tube 1313. The extraction steam inlet 1301 is located at the end of the extraction-type gasification conversion burner 13, and the central oxygen inlet 1302 is located along the central axis of the extraction-type gasification conversion burner 13. The end of the steam injection pipe 1308 is provided with a steam injection pipe reducer 1309. The steam reaches its maximum flow velocity at the constriction point 1309 of the steam injection pipe. The outer shell of the extraction gasification conversion burner 13 consists of a burner cone tube 1311, a burner throat 1312, and a burner expansion tube 1313. The extraction steam inlet 1301 is provided with four sets of channels, which are respectively configured 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 circulating water inlet 1304, and a cooling circulating water outlet 1306 channel. The gasification device interface flange 1305 is located in the straight pipe section of the extraction gasification conversion burner 13. A central oxygen support frame 1310 is provided in the central oxygen inlet 1302 of the extraction gasification conversion burner 13.

[0081] Preferably, the diameter of the straight section of the steam injection pipe 1308 is a, the diameter of the reduced diameter steam injection pipe 1309 is b, the height of the reduced diameter steam injection pipe 1309 is h1, and the distance between the straight section of the reduced diameter steam injection pipe 1309 and the center line of the suction steam inlet 1301 is h2; the diameter of the straight section of the burner pyrolysis gas phase 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 conical pipe 1311 is H1, the length of the burner throat 1312 is H2, and the length of the burner expansion pipe 1313 is H3.

[0082] Preferably, a / b = 1.5 to 4, a / b = 1.5 to 2.5.

[0083] Preferably, h2 / h1 = 5 to 10, a / b = 6 to 8.

[0084] Preferably, h1 = (1.0~1.5) * b.

[0085] Preferably, A / B = 1.2 to 2.5, A / B = 1.5 to 2.

[0086] Preferably, C / A = 1.2 to 2, C / A = 1.2 to 1.5.

[0087] Preferably, H3 / H2 = 1.0 to 2.5, H3 / H2 = 1.2 to 1.5.

[0088] Preferably, H1 / H2 = 0.2 to 1.5, H1 / H2 = 0.5 to 0.8.

[0089] For details, please refer to the following: Figure 11 , Figure 13 , Figure 14 , Figure 15 and Figure 16 The gasification conversion unit 14 comprises a gasification interface flange 1401, a gasification chamber 1402, an upper swirl-type steam jet throat 1403, a conversion chamber 1404, an upper swirl-type steam jet throat steam inlet 1405, a lower swirl-type steam jet throat 1406, a lower swirl-type steam jet throat steam inlet 1407, a slag discharge pipe 1408, a bottom slag discharge port 1409, a gas outlet 1410, a refractory lining 1411, a heat insulation layer 1412, and a thermal insulation layer 1413. The gasification interface flange 1401 of the gasification conversion unit 14 is connected to the extraction-type gasification conversion burner 13. The gasification chamber 1402 is located in the upper region of the gasification conversion unit 14, and the conversion chamber 1404 is located in the lower region of the gasification conversion unit 14. The gasification chamber 1402 and the conversion chamber 1404 are connected by an upper swirl-type steam jet throat. The steam jet throat 1403 is isolated. The lower part of the conversion chamber 1404 is sequentially provided with a lower swirl steam jet throat 1406 and a slag discharge 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 outlet 1410 of the gasification device is located on the side of the gasification conversion device 14. The gas outlet 1410 of the gasification device is located below the lower swirl steam jet throat 1406 and above the outlet of the slag discharge pipe 1408. The gasification conversion device 14 consists of a gasification device refractory lining 1411, a gasification device heat insulation layer 1412, and a gasification device thermal insulation layer 1413 from the inside to the outside. The steam inlet 1405 of the upper swirl steam jet throat is located at one end of the upper swirl steam jet throat 1403, and the steam inlet 1407 of the lower swirl steam jet throat is located at one end of the lower swirl steam jet throat 1406.

[0090] In this design, the upper swirl-type steam jet throat 1403 consists of an upper swirl-type steam jet throat steam nozzle 140301 and an upper swirl-type steam jet throat steam chamber 140302, while the lower swirl-type steam jet throat 1406 consists of a lower swirl-type steam jet throat steam nozzle 140601 and a lower swirl-type steam jet throat steam chamber 140602.

[0091] Preferably, the height-to-diameter ratio of the gasification chamber 1402 is 8:1 to 4:1; and the height-to-diameter ratio of the conversion chamber 1404 is 10:1 to 4:1.

[0092] Preferably, the steam nozzles 140301 of the upper swirl steam jet throat are arranged in a ring and uniformly around the upper swirl steam jet throat 1403.

[0093] Preferably, the number of vertical layers of the upper swirl-type steam jet throat steam nozzle 140301 is n, where n = 8 to 20 layers;

[0094] Preferably, the horizontal angle between the upper swirl-type steam jet throat steam nozzle 140301 and the radial angle between the nozzle and the gasification conversion device 14 is α, where α = 0 to 60°.

[0095] Preferably, the number of horizontally arranged steam nozzles 140301 in the upper swirl-type steam jet throat is m, and n = 12 to 24 (m is an even number).

[0096] Preferably, the horizontal angle between the steam inlet of the upper swirl-type steam jet throat 1403 and the radial angle between the steam inlet and the gasification conversion device 14 is δ, where δ = 0 to 60°.

[0097] Preferably, the steam nozzles 140601 of the lower swirl steam jet throat are arranged in a ring and uniformly around the lower swirl steam jet throat 1406.

[0098] Preferably, the number of vertical layers of the lower swirl-type steam jet throat steam nozzle 140601 is k, where k = 8 to 20 layers;

[0099] Preferably, the horizontal angle between the lower swirl-type steam jet throat steam nozzle 140601 and the radial angle between the nozzle and the gasification conversion device 14 is β, where β = 0 to 60°.

[0100] Preferably, the number of horizontally arranged steam nozzles 140601 at the lower swirl-type steam jet throat is l, where l = 12 to 24 (m is an even number).

[0101] Preferably, the horizontal angle between the steam inlet 1407 of the lower swirl steam jet throat and the radial angle between the steam inlet 14 and the gasification conversion device 14 is γ, where γ = 0 to 60°. Example 3

[0102] Please see Figures 1-16 This includes the following steps:

[0103] S1. Biomass raw materials are pre-treated by crushing and grinding to obtain raw materials with a particle size ≤10mm;

[0104] S2. Raw materials with a particle size ≤10mm enter the drying system to reduce the moisture content of the raw materials to below 5%, and the drying heat source is the waste heat flue gas of the system;

[0105] S3. Raw materials with a moisture content of ≤5% after drying are transported to the biomass raw material storage silo 5. The dried raw materials are transported to the pyrolysis reaction device 7 via the biomass raw material conveying screw 6. At the same time, the high-temperature heat carrier located in the high-temperature heat carrier storage silo 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 undergo full mass and heat transfer in the pyrolysis reaction device 7 to obtain high-temperature biochar and pyrolysis oil and gas.

[0106] S4. The mixture of high-temperature biochar and medium-temperature heat carrier is conveyed into the fluidized heating and lifting device 2 through the pyrolysis solid product conveying screw 8. At the same time, air is introduced. The high-temperature biochar is fully combusted in the fluidized heating and lifting device 2, so that the medium-temperature heat carrier can be heated to obtain the high-temperature heat carrier. At the same time, the heat carrier is lifted to the high-temperature heat carrier storage silo 3. The flue gas is used for raw material drying.

[0107] S5. Pyrolysis oil and gas are successively treated by the primary cyclone dust collector 9 and the secondary cyclone dust collector 11 of pyrolysis gas phase products, and then enter the induced draft gasification conversion burner 13. The mass transfer power of the pyrolysis oil and gas is mainly provided by the negative pressure formed by the injection of steam into the induced draft gasification conversion burner 13. Oxygen enters the induced draft 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 gasified syngas. The gasified syngas passes through the upper swirl-type steam injection throat area 1403 and is injected by steam swirl. The gasified syngas and steam undergo a water-gas conversion reaction to obtain hydrogen-rich gas. The hydrogen-rich gas passes through the lower swirl-type steam injection throat area 1406 and is injected by steam swirl. 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 ash discharge pipe 1408.

[0108] S6. The hydrogen-rich gas is successively heat-exchanged by the waste heat boiler 16, sprayed and cooled by the spray purification tower 17, compressed by the compressor 19, and treated by the hydrogen extraction device 20 to obtain high-purity hydrogen product; the steam generated by the waste heat boiler 16 is used for the extraction gasification conversion burner 13 and the gasification conversion device 14. Example 4

[0109] For details, please refer to the following: 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, and the cooling unit 1001 and the cooling spiral tube 1002 are connected.

[0110] In the biomass pyrolysis gasification apparatus for producing green hydrogen of the present invention, the cooling medium circulating inside the cooling spiral tube 1002 can perform preliminary cooling treatment (cooling to ambient temperature) on materials at a high temperature, carbonizing the biomass, which facilitates the storage, utilization, and stacking of this material. Example 5

[0111] Bamboo shavings, with an average moisture content of 45%, are dried using waste heat flue gas to obtain bamboo shavings with a moisture content ≤5%. The bamboo shavings are then transported to the biomass raw material storage silo 5. The high-temperature solid heat carrier (650℃) in the high-temperature heat carrier storage silo 3, along with the bamboo shavings, are transported to the pyrolysis reactor 7 via the high-temperature heat carrier conveying screw 4 and the biomass raw material conveying screw 6, respectively. The mass ratio of the high-temperature solid heat carrier to the biomass raw material is 10:1, and the reaction pressure in the pyrolysis reactor 7 is 10 kPa. The resulting biochar and the medium-temperature heat carrier (520℃) are transported to the fluidized bed heating and lifting device 2 via the pyrolysis solid phase product conveying screw 8 for combustion and lifting (reaction temperature: 850℃). The pyrolysis oil and gas are treated by the primary cyclone dust collector 9 and the secondary cyclone dust collector 11 for pyrolysis gas phase products, and then transported to the gasification conversion device 14 under negative pressure created by the suction-type gasification conversion burner 13. Pyrolysis oil gas, water vapor, and oxygen undergo a gasification conversion reaction in gasification chamber 1402 to obtain gasified syngas (reaction temperature of gasification chamber 1402: 1350℃). The gasified syngas is injected with steam through the upper swirl-type steam jet throat 1403 and then enters the conversion chamber 1404 for a transformation reaction to obtain hydrogen-rich gas (reaction temperature of conversion chamber 1404: 1100℃). The hydrogen-rich gas is injected with steam through the lower swirl-type steam jet throat 1406 and then cooled to 900℃. After waste heat recovery by waste heat boiler 16, spray cooling by spray purification tower 17, compression by compressor 19, and hydrogen extraction by hydrogen extraction device 20, high-purity hydrogen gas (purity ≥99.9%) is obtained.

[0112] Therefore, any equivalent substitutions or modifications made by those skilled in the art within the scope of the technology disclosed in this invention, based on the technical solution and inventive concept of this invention, should be covered within the protection scope of this invention.

Claims

1. A device for preparing green hydrogen by biomass pyrolysis gasification, comprising a pyrolysis reaction device (7), characterized in that: The pyrolysis reaction device (7) comprises a pyrolysis reaction tank (70) connected with the high-temperature heat carrier conveying screw (4), the biomass raw material storage bin (5), the biomass raw material conveying screw (6) and the pyrolysis solid 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), The pyrolysis acceleration structure (80) comprises a rotating lifting assembly (801) mounted inside the pyrolysis reaction tank (70); an intermediate shaft (802) connected with the rotating lifting assembly (801) and movably arranged at the center inside the pyrolysis reaction tank (70); a stirring and mixing assembly (803) mounted at the center outside the intermediate shaft (802); a conical body (804) mounted on the stirring and mixing assembly (803); a feeding pipe (805) mounted at the center of the top of the pyrolysis reaction tank (70) through screws; an inclined channel (806) opened at the inner wall of the feeding pipe (805) and located outside the conical body (804), The feeding pipe (805) is connected with the biomass raw material storage bin (5), the outside of the conical body (804) is sleeved with a sealing rubber ring (8041), the intermediate shaft (802) is slidingly connected inside an upper top frame (8021), and the upper top frame (8021) is mounted at the inner top of the pyrolysis reaction tank (70), The pyrolysis reaction tank (70) comprises an outer protective tank body (7001); a pyrolysis tank body (7002) mounted inside the outer protective tank body (7001); a first input pipe (7003) in communication with one side of the pyrolysis tank body (7002) and extending to one side outside the outer protective tank body (7001); a side pipe (7004) in communication with 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), The top center of the pyrolysis tank body (7002) is provided with the feeding pipe (805), the inside of the pyrolysis tank body (7002) is movably provided with the pyrolysis acceleration structure (80), and the outside of the pyrolysis tank body (7002) and the inside of the outer protective tank body (7001) are provided with the pyrolysis heating assembly (90) extending to the outside of the outer protective tank body (7001), The rotating lifting assembly (801) comprises: a bottom support (8011) mounted on the bottom of the pyrolysis tank body (7002); a bottom protective cover (8012) mounted at the center of the bottom of the bottom support (8011); a lifting drive source (8013) mounted at the bottom of the bottom protective cover (8012); a lifting connecting disc (8014) connected with the output end of the lifting drive source (8013) and slidingly connected inside the bottom protective cover (8012); a lifting rotating shaft (8015) rotatably connected with the lifting connecting disc (8014) and mounted at the bottom of the intermediate shaft (802); a vertical groove (8016) formed in the outer surface of the lifting rotating shaft (8015); a first gear (8017) connected with the lifting rotating shaft (8015) through the vertical groove (8016); a second gear (8018) rotatably connected with the first gear (8017) and mounted inside the bottom protective cover (8012); and a rotating drive source (8019) connected with the second gear (8018) and mounted at the eccentric position inside the bottom protective cover (8012), The stirring and mixing assembly (803) comprises: stirring spiral blades (8031) mounted on the upper and lower sides of the outer side of the intermediate shaft (802); a movable rotating disc (8032) arranged between the two stirring spiral blades (8031) and mounted on the outer side of the intermediate shaft (802); an eccentricity bar (8033) rotatably connected at the eccentric position inside the movable rotating disc (8032); a stirring blade (8034) rotatably connected at the top of the eccentricity bar (8033); and an extension spring (8035) mounted inside the eccentricity bar (8033) and extending to the eccentric position inside the movable rotating disc (8032).

2. The device for preparing green hydrogen by biomass pyrolysis gasification according to claim 1, characterized in that: The pyrolysis heating assembly (90) comprises: a heating unit (901) arranged on the outer side of the outer protective tank body (7001); and a spiral heating pipeline (902) connected with the heating unit (901) and arranged on the outer side of the pyrolysis tank body (7002) and the inner side of the outer protective tank body (7001).

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

4. The device for preparing green hydrogen by biomass pyrolysis gasification according to claim 3, characterized in that: The suction gasification conversion burner (13) is composed of suction steam inlet (1301), center oxygen inlet (1302), outer ring oxygen inlet (1303), cooling circulating water inlet (1304), gasification device interface flange (1305), cooling circulating water outlet (1306), pyrolysis gas phase product inlet (1307), steam jet pipe (1308), steam jet pipe reducing (1309), center oxygen support frame (1310), burner conical pipe (1311), burner throat (1312) and burner expansion pipe (1313), The suction steam inlet (1301) is arranged at the end side of the suction gasification conversion burner (13), the center oxygen inlet (1302) is arranged in the center axis direction of the suction gasification conversion burner (13), the line end of the steam jet pipe (1308) is provided with the steam jet pipe reducing (1309), and the steam reaches the maximum flow rate at the position of the steam jet pipe reducing (1309), the shell part of the suction gasification conversion burner (13) is composed of the burner conical pipe (1311), the burner throat (1312) and the burner expansion pipe (1313), the suction steam inlet (1301) is provided with four groups of channels, and the four groups of channels are arranged from inside to outside as the center oxygen inlet (1302) channel, the pyrolysis gas phase product inlet (1307) channel, the outer ring oxygen inlet (1303) channel, the cooling circulating water inlet (1304) and the cooling circulating water outlet (1306) channel, Wherein, the gasification device interface flange (1305) is arranged in the straight pipe section of the suction gasification conversion burner (13), and the center oxygen support frame (1310) is arranged in the center oxygen inlet (1302) of the suction gasification conversion burner (13).

5. The device for preparing green hydrogen by biomass pyrolysis gasification according to claim 3, characterized in that: The gasification conversion device (14) is composed of a gasification interface flange (1401), a gasification chamber (1402), an upper cyclone steam injection throat (1403), a conversion chamber (1404), an upper cyclone steam injection throat steam inlet (1405), a lower cyclone steam injection throat (1406), a lower cyclone steam injection throat steam inlet (1407), a slag falling pipe (1408), a gasification device bottom slag discharge port (1409), a gasification device gas outlet (1410), a gasification device refractory lining (1411), a gasification device heat insulation layer (1412), and a gasification device heat preservation layer (1413), The gasification interface flange (1401) of the gasification conversion device (14) is connected with the suction gasification conversion burner (13), the gasification chamber (1402) is located in the upper region of the gasification conversion device (14), the conversion chamber (1404) is located in the lower region of the gasification conversion device (14), the gasification chamber (1402) and the conversion chamber (1404) are isolated by the upper cyclone steam injection throat (1403), the lower part of the conversion chamber (1404) is sequentially provided with the lower cyclone steam injection throat (1406) and the slag falling pipe (1408), the gasification device bottom slag discharge port (1409) is located in the bottom region of the gasification conversion device (14), the gasification device gas outlet (1410) is provided on the side of the gasification conversion device (14), the gasification device gas outlet (1410) is located on the lower side of the lower cyclone steam injection throat (1406) and the upper region of the outlet of the slag falling pipe (1408), the gasification conversion device (14) is composed of the gasification device refractory lining (1411), the gasification device heat insulation layer (1412), and the gasification device heat preservation layer (1413) from inside to outside, the upper cyclone steam injection throat steam inlet (1405) is provided at one end of the upper cyclone steam injection throat (1403), and the lower cyclone steam injection throat steam inlet (1407) is provided at one end of the lower cyclone steam injection throat (1406).

6. The device for preparing green hydrogen by biomass pyrolysis gasification according to claim 5, characterized in that: The upper cyclone steam injection throat (1403) is composed of an upper cyclone steam injection throat steam nozzle (140301) and an upper cyclone steam injection throat steam chamber (140302), The lower cyclone steam injection throat (1406) is composed of a lower cyclone steam injection throat steam nozzle (140601) and a lower cyclone steam injection throat steam chamber (140602).

7. A method for producing green hydrogen by biomass pyrolysis gasification, for the device for producing green hydrogen by biomass pyrolysis gasification according to any one of claims 1-6, characterized in that, The method comprises the following steps: S1, the biomass raw material is pretreated by crushing and pulverizing to obtain raw material with a particle size of ≤10 mm; S2, the raw material with a particle size of ≤10 mm enters the drying system, and the moisture of the raw material is reduced to below 5%, wherein the drying heat source uses the waste heat flue gas of the system; S3, the raw material with moisture content of less than 5% after drying is transported to the biomass raw material storage (5), and the dried raw material is transported to the pyrolysis reaction device (7) through the biomass raw material conveying screw (6); at the same time, the high-temperature heat carrier 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 and the high-temperature heat carrier are fully mass transfer and heat transfer in the pyrolysis reaction device (7) to obtain high-temperature biochar and pyrolysis oil gas; S4, the mixture of high-temperature biochar and medium-temperature heat carrier is transported into the fluidized heating lifting device (2) through the pyrolysis solid product conveying screw (8), and air is introduced at the same time, the high-temperature biochar is fully combusted in the fluidized heating lifting device (2), so that the medium-temperature heat carrier is heated, and the high-temperature heat carrier is obtained, and the heat carrier is lifted to the high-temperature heat carrier storage (3); the flue gas is used for raw material drying treatment; S5, the pyrolysis oil gas is treated by dust removal in turn through the pyrolysis gas phase product primary cyclone dust collector (9) and the pyrolysis gas phase product secondary cyclone dust collector (11), and then enters the induced gasification conversion burner (13), the mass transfer power of the pyrolysis oil gas is mainly provided by the negative pressure formed by the steam injection into the induced gasification conversion burner (13); the oxygen gas enters the induced gasification conversion burner (13) in two ways, which are central oxygen and annular oxygen, the pyrolysis oil gas, steam and oxygen gas occur gasification reaction in the gasification chamber (1402) of the gasification conversion device (14), and the gasification synthesis gas is obtained; the gasification synthesis gas is injected by steam cyclone through the upper swirl type steam injection throat (1403) area, and the gasification synthesis gas and steam occur water gas shift reaction to obtain hydrogen-rich gas; the hydrogen-rich gas is injected by steam cyclone through the lower swirl type steam injection throat (1406) area, and the temperature of the hydrogen-rich gas is reduced below the ash melting point, and the solid ash is discharged to the bottom of the gasification conversion device (14) through the ash discharge pipe (1408); S6, the hydrogen-rich gas is treated by heat exchange through the waste heat boiler (16), spray cooling and purification through the spray purification tower (17), compression through the compressor (19), and hydrogen extraction through the hydrogen extraction device (20) to obtain high-purity hydrogen gas product; the steam generated by the waste heat boiler (16) is used for the induced gasification conversion burner (13) and the gasification conversion device (14).

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