Biomass cascade pyrolysis-microwave gasification carbon-hydrogen cogeneration integrated device and method

Abstract

The present invention discloses a biomass cascade pyrolysis-microwave gasification carbon-hydrogen co-production integrated device and method, the device includes a coordinated integrated reaction system, an inner and outer radial energy supply system, and a product separation and collection system. The method includes firstly low-temperature pyrolysis of the raw material to greatly improve the wave absorption characteristics, and then microwave gasification and online reforming to prepare hydrogen-rich gas and co-produce porous carbon products, pyrolysis gas combustion to dry the raw material and provide heat for low-temperature pyrolysis reaction, hydrogen-rich gas separation and purification to prepare high-purity hydrogen products, and the separated gas is returned as a gasification agent to provide gasification reaction. The present invention adopts a multi-system collaborative integrated design, low-temperature pre-pyrolysis to improve the quality of microwave products and reaction efficiency, while greatly reducing the consumption of high-grade electricity, and self-producing low-grade heat energy for recycling and self-heating. The device of the present invention operates continuously and reliably, is compact and efficient, occupies a small volume, and has high overall economic efficiency, which solves the problems of large equipment, high cost, and difficulty in promotion of biomass pyrolysis and gasification hydrogen production technology.

Description

Technical Field

[0001] The present invention relates to the technical field of biomass carbon-hydrogen pyrolysis and gasification co-production, and in particular to a biomass cascade pyrolysis-microwave gasification carbon-hydrogen co-production integrated device and method. Background Art

[0002] Biomass resources include crop straw, livestock manure, forestry processing waste, etc., and are the world's fourth largest energy source. The rational use of biomass can promote the development of low-carbon agriculture, alleviate environmental problems, drive industrial upgrading, and increase farmers' income. Biomass gasification is a process in which raw materials react with a certain amount of oxygen, water vapor or CO2 at high temperature to produce CO and H2 (collectively known as synthesis gas) and a small amount of bio-oil and biochar. However, there are still many problems in the actual use of biomass gasification, mainly the following: low hydrogen yield, poor quality of gasified gas, low yield, high tar yield, slow gasification rate, high energy consumption, etc. Microwave heating has many advantages such as immediacy, selectivity, and penetration. When microwave energy is used for gasification reaction, the hydrogen yield is high and the processing efficiency is high.

[0003] In recent years, some research has been carried out around microwave pyrolysis and gasification technology at home and abroad. However, microwave gasification has many defects. Patent 201611065781.8 discloses a biomass microwave pyrolysis directional gasification method, which introduces a strong absorbent catalyst synthesized from multiple components to perform microwave pyrolysis and microwave gasification, but the product of this method is single, and the product quality and added value need to be improved. Patent 201811618224.3 discloses a biomass microwave gasification utilization method and system, which prepares hydrogen by comprehensive utilization of gas phase products at all levels through oxygen carrier reduction reaction, but additives are also required in the microwave reactor, and the separation of solid products and additives produced by the reaction brings challenges, thus producing multi-level solid residues, and the process is complex, energy consumption is high, and the cost is high. Patent 202110029378.4 discloses a method and system for biomass pyrolysis and gasification to produce hydrogen and co-produce biochar. In addition to the high consumption of high-grade electricity in the front stage, this method must maintain a reaction temperature of 500-800°C for reforming and 850-1000°C for the combustion reactor, which will almost consume all solid carbon products. Although this method improves the problem of single product to a certain extent, the device is complex and large, with many unit reactors and a large volume, and the overall economic efficiency still needs to be improved. The existing bottlenecks of biomass microwave pyrolysis and gasification technology can be summarized as follows: (1) Biomass raw materials have low energy density and poor molecular polarity, which makes them poor absorbers of heat and microwaves. To achieve microwave reaction conditions, a large amount of high-grade electricity is required. If additives are added to improve the material's microwave absorption capacity, it will cause the problem of solid product separation and generate solid waste residue; (2) The process products are single and have low added value; (3) The device is large, with many equipments and low efficiency. The microwave feed port is easily contaminated and often needs to be shut down for maintenance. The above problems make the overall technology of biomass microwave pyrolysis and gasification insufficiently economical under the conditions of complex process flow and high energy consumption cost, making it difficult to apply and promote on a large scale. Therefore, it is urgent to develop a low-cost, efficient, compact and integrated device technology for the co-production of high-value-added hydrocarbon products from biomass. Summary of the invention

[0004] The purpose of the present invention is to provide a biomass cascade pyrolysis-microwave gasification hydrocarbon co-production integrated device and method in view of the defects of the prior art, which has compact structure, high efficiency, cascade utilization of energy, high product yield and quality, and can be operated continuously for a long time, thereby solving the problems of large devices, high costs, single products, and poor economic efficiency in the prior art.

[0005] In order to solve the above technical problems, the present invention provides the following technical solutions:

[0006] A biomass cascade pyrolysis-microwave gasification carbon-hydrogen co-production integrated device, characterized in that it includes an integrated reaction system, an inner and outer radial energy supply system, and a product separation and collection system;

[0007] The integrated reaction system comprises a drying chamber, a low-temperature pyrolysis chamber, a microwave gasification chamber, and an online reforming reaction chamber arranged outside the low-temperature pyrolysis chamber, which are sequentially connected from top to bottom; the drying chamber is used to load and dry biomass raw materials; the low-temperature pyrolysis chamber is used to preliminarily pyrolyze and carbonize the biomass raw materials and improve the microwave absorption capacity; the microwave gasification chamber is connected to the online reforming reaction chamber through a gas phase outlet, and is used to produce high-quality gas products and porous carbon products from highly absorbing materials; the online reforming reaction chamber is connected to a product separation and collection system through a reforming gas outlet, and is used to perform online catalytic reforming of the gas products generated by microwave gasification;

[0008] The inner and outer radial energy supply system includes a combustion heat supply chamber and a gasifier chamber arranged from top to bottom on the central axis inside the integrated reaction system, and an annular direct-fed microwave generator arranged outside the microwave gasification chamber; the combustion heat supply chamber runs through the drying chamber and the low-temperature pyrolysis chamber, and the drying tail gas outlet arranged at the upper end is located between the drying chamber and the low-temperature pyrolysis chamber. The combustion tail gas used for pyrolysis gas is used for pyrolysis reaction and material drying and heat supply. The pyrolysis gas outlet is arranged at the lower end and is connected to the low-temperature pyrolysis chamber, and the blower is connected to the combustion heat supply chamber through the combustion air distribution inner pipe; the gasifier chamber is arranged at the axis of the microwave gasification chamber, and is used for the gasification reaction of the material. Its upper end is connected to the microwave gasification chamber through the first gasifier outlet, and the bottom is provided with a gasifier inlet; the annular direct-fed microwave generator is used to provide microwaves to the microwave gasification chamber;

[0009] The product separation and collection system includes a first-stage gas separation device, a second-stage purification device, a gas storage bottle, and a carbon material collection box; the first-stage gas separation device is used to receive and separate the reformed gas product and provide a gasifying agent for the gasification reaction, and is provided with a reformed gas inlet, a crude hydrogen outlet, and a second gasifying agent outlet, the reformed gas inlet is connected to the reformed gas outlet, the crude hydrogen outlet is connected to the gas storage bottle through the second-stage purification device, and the second gasifying agent outlet is connected to the gasifying agent inlet; the carbon material collection box is connected to the solid outlet at the bottom of the microwave gasification cavity.

[0010] Furthermore, the drying chamber is an inverted bucket-shaped structure that is larger at the top and smaller at the bottom, and the inner diameter ratio of the upper end to the lower end is 2:1-3:1, and the inclination angle α of the inner wall of the drying chamber is 30°-60°; the upper end of the combustion and heating chamber is a truncated cone structure, and the drying exhaust gas outlet is arranged on the truncated cone structure, the bottom diameter of the truncated cone structure is 1:2-2:3 The ratio of the diameter of the upper table of the truncated cone structure to the bottom diameter is 1:2-1:3, the ratio of the diameter of the upper table of the truncated cone structure to the height of the truncated cone structure is 1:1-1:1.5, and the ratio of the diameter of the upper table of the truncated cone structure to the inner diameter of the combustion and heating chamber is 1:1; the height ratio of the microwave gasification cavity to the low-temperature pyrolysis cavity is 2:3, and the height ratio of the online reforming reaction cavity to the low-temperature pyrolysis cavity is 4:5-1:1.

[0011] Furthermore, a first-stage wave suppression baffle and a second-stage wave suppression baffle are sequentially arranged between the low-temperature pyrolysis chamber and the microwave gasification chamber from top to bottom, one end of the first-stage wave suppression baffle is connected to the bottom of the inner wall of the low-temperature pyrolysis chamber, and the other end is inclined downward, with an inclination angle β of 20° to 45°, one end of the second-stage wave suppression baffle is connected to the outer wall of the gasifier chamber, and the other end is inclined downward, with an inclination angle γ in the range of β+15°, and the vertical distance from the outer end of the first-stage wave suppression baffle is 0 to 50 mm, and the ratio of the interval between the outer end of the second-stage wave suppression baffle and the outer wall of the microwave gasification chamber to the inner diameter of the microwave gasification chamber is 3:4.

[0012] Furthermore, the pyrolysis gas outlets are symmetrically arranged in 4 to 6 layers along the inner wall of the combustion heating chamber, with 2 to 4 outlets in each layer. A combustion nozzle is arranged on the combustion air distribution inner pipe. The combustion nozzle is located between two layers of pyrolysis gas outlets, and the diameter of the combustion nozzle is 40 mm.

[0013] Furthermore, the first gasifying agent outlets are symmetrically arranged in 4 to 6 layers along the circumferential direction of the outer wall of the gasifying agent cavity, and the number of the first gasifying agent outlets in each layer is 2 to 4.

[0014] Furthermore, a peripheral feeding port is provided on the outer wall of the microwave vaporization cavity, the annular direct-fed microwave generator is connected to the peripheral feeding port through an echo suppressor, a bottom air curtain outlet is provided at the bottom of the peripheral feeding port, and the vaporizing agent cavity is connected to the bottom air curtain outlet.

[0015] A biomass cascade pyrolysis-microwave gasification carbon-hydrogen co-production method, using the biomass cascade pyrolysis-microwave gasification carbon-hydrogen co-production integrated device according to any one of claims 1 to 6, characterized in that it comprises the following steps:

[0016] S1: The biomass raw material enters the drying chamber, is heated and dried through the drying tail gas outlet, and then enters the low-temperature pyrolysis chamber for low-temperature preliminary pyrolysis and carbonization. The pyrolysis gas product enters the combustion heating chamber through the pyrolysis gas outlet, and the remaining solid material enters the microwave gasification chamber;

[0017] S2: The material undergoes a gasification reaction with the gasifying agent in the microwave gasification cavity, and the gaseous product enters the online reforming reaction cavity through the gas phase outlet for online catalytic reforming and then enters the first-stage gas separation device, and the solid porous carbon material product enters the carbon material collection box through the solid outlet to isolate from the air and cool to below 60°C;

[0018] S3: The pyrolysis gas in step S1 is combusted with air in the combustion and heating chamber to provide heat for the low-temperature pyrolysis chamber, and the tail gas is discharged into the drying chamber through the dry tail gas outlet for drying. The reformed gas in step S2 is separated into crude hydrogen and gasifying agent through the first-stage gas separation device, and the gasifying agent returns to the microwave gasification chamber through the gasifying agent chamber to fully contact with the material for microwave gasification reaction, and forms a wind curtain on the surface of the peripheral feed port through the bottom wind curtain outlet to protect the peripheral feed port.

[0019] Furthermore, in step S1, the pyrolysis reaction temperature T1 of the low-temperature pyrolysis chamber ranges from 200 to 360°C, and T1 is adjusted according to the material and heating conditions; the gasification reaction temperature T2 of the microwave gasification chamber in step S2 ranges from 600 to 1200°C; the combustion temperature T3 in the combustion heating chamber in step S3 ranges from 900°C to 1300°C, and the excess air coefficient ranges from 1.2 to 1.5.

[0020] Furthermore, the gasifying agent in step S2 is separated carbon dioxide or a mixed gas with a small amount of other gases, which is introduced in a gaseous form, and the mass ratio of the gasifying agent to the solid product is 1:2 to 4:1.

[0021] Furthermore, in step S2, a natural catalyst and a synthetic supported catalyst having the ability to catalyze tar cracking are placed in the online reforming reaction chamber, including a nickel-based synthetic supported catalyst having γ-Al2O3 as a carrier and nano-nickel oxide as an active component. The nickel-based synthetic supported catalyst is made of nickel nitrate and γ-Al2O3 as raw materials and urea as a precipitant, and is prepared by impregnation, drying, and calcination at 400°C in an air atmosphere.

[0022] Compared with the prior art, the present invention has the following beneficial effects:

[0023] (1) In the present invention, the biomass raw material is firstly subjected to rapid low-temperature pyrolysis in a low-temperature pyrolysis chamber. The fast heating rate achieved by the low reaction temperature and the large temperature difference with the heat source can effectively remove the oxygen-containing functional groups in the biomass, thereby improving the quality of the gasified gas;

[0024] (2) In the present invention, the biomass is initially and rapidly pyrolyzed and carbonized in a low-temperature pyrolysis chamber, and its dielectric properties are greatly improved, and it has better microwave absorption capacity in a microwave cascade gasification system;

[0025] (3) The low-temperature pyrolysis chamber of the present invention uses the low-grade heat source of pyrolysis gas combustion heat to provide heat, completing the high-energy consumption biomass drying and preliminary pyrolysis, thereby reducing the input of high-grade electrical energy during the microwave gasification process;

[0026] (4) The microwave cascade gasification system of the present invention utilizes the advantages of uniform and rapid microwave heating and overall heat generation, and cooperates with low-temperature pyrolysis to improve the microwave absorption of raw materials. At the same time, the use of a counter-feed design can greatly shorten the gasification time. At the same time, the microwave energy density is high, which makes it easier to reach the reaction energy barrier and promote gas and hydrogen production. The air curtain design also effectively protects the feed port, improves the reliability of equipment operation, and avoids frequent shutdowns for cleaning and maintenance;

[0027] (5) The present invention provides a compact, integrated, continuous and efficient reaction device through the coordination of multiple functions, realizing multiple functions in one reactor, greatly reducing the equipment volume and floor space, reducing equipment costs, improving the economy of the process, and facilitating the large-scale promotion of technology. BRIEF DESCRIPTION OF THE DRAWINGS

[0028] Figure 1 This is a schematic diagram of the structure of an embodiment of a biomass cascade pyrolysis-microwave gasification carbon-hydrogen cogeneration integrated device of the present invention;

[0029] Among them: 1. Drying chamber; 2. Low-temperature pyrolysis chamber; 2-1. Pyrolysis gas outlet; 2-2. First-stage wave suppression baffle; 2-3. Second-stage wave suppression baffle; 3. Microwave gasification chamber; 3-1. Gas phase outlet; 3-2. Solid outlet; 4. Online reforming reaction chamber; 5. Combustion heating chamber; 5-1. Combustion nozzle; 5-2. Combustion air distribution inner pipe; 5-3. Dry tail gas outlet; 5-4. Blower; 5-5. Cone structure; 6. Gasification agent chamber; 6-1. Bottom 6-2, first gasifier inlet; 6-3, bottom air curtain outlet; 7, annular direct-fed microwave generator; 7-1, echo suppressor; 7-2, peripheral feed inlet; 8, first-stage gas separation device; 8-1, reformed gas inlet; 8-2, crude hydrogen outlet; 8-3, second gasifier outlet; 9, second-stage purification device; 9-1, crude hydrogen inlet; 9-2, high-purity hydrogen outlet; 10, gas storage cylinder; 11, carbon material collection box. DETAILED DESCRIPTION

[0030] In order to deepen the understanding of the present invention, the present invention will be further described in detail below with reference to the accompanying drawings. The embodiments are only used to explain the present invention and do not constitute a limitation on the protection scope of the present invention.

[0031] Figure 1 An embodiment of a biomass cascade pyrolysis-microwave gasification hydrocarbon co-production integrated device is shown, including a coordinated integrated reaction system, an inner and outer radial energy supply system, and a product separation and collection system.

[0032] The integrated reaction system includes a drying chamber 1, a low-temperature pyrolysis chamber 2, a microwave gasification chamber 3, and an online reforming reaction chamber 4 arranged outside the low-temperature pyrolysis chamber 2, which are connected in a cascade from top to bottom; the drying chamber 1 is used to dry the biomass raw materials, the low-temperature pyrolysis chamber 2 is used to preliminarily pyrolyze and carbonize the biomass raw materials to enhance the microwave absorption capacity and feed the materials into the microwave gasification chamber 3, the microwave gasification chamber 3 is used to produce high-quality gas products and porous carbon products from highly absorbing materials, and the online reforming reaction chamber 4 is used for online catalytic reforming of the gas products produced by microwave gasification.

[0033] The inner and outer radial energy supply system includes a combustion heat supply cavity 5 and a gasification agent cavity 6 arranged from top to bottom on the central axis inside the integrated reaction system, and an annular direct-feed microwave 7 arranged outside the microwave gasification cavity 3. Among them, the combustion heat supply cavity 5 is used to burn the pyrolysis gas produced by pyrolysis to provide energy for pyrolysis reaction and material drying, the gasification agent cavity 6 is used to provide gasification agent and protect the microwave feed port, and the annular direct-feed microwave 7 is used to provide microwaves for microwave gasification reaction.

[0034] The product separation and collection system includes a first-stage gas separation device 8, a second-stage purification device 9, a gas storage bottle 10, and a carbon material collection box 11. The first-stage gas separation device 8 is used to receive and separate the reformed gas product and provide a gasification agent for the gasification reaction, the second-stage purification device 9 is used to purify hydrogen, the gas storage bottle 10 is used to store high-purity hydrogen, and the carbon material collection box 11 is used to store porous carbon materials.

[0035] Specifically, the inverted bucket-shaped drying chamber 1 with a large upper part and a small lower part is directly connected to the low-temperature pyrolysis chamber 2, the ratio of the inner diameter between the upper end and the lower end of the drying chamber 1 is 2:1, and the inclination angle α of the inner wall of the drying chamber is 45°. The lower part of the low-temperature pyrolysis chamber 2 is connected to the microwave vaporization chamber 3 through the first-stage wave suppression baffle 2-2 and the second-stage wave suppression baffle 2-3. One end of the first-stage wave suppression baffle 2-2 is connected to the bottom of the inner wall of the low-temperature pyrolysis chamber 2, and the other end is tilted downward, with an inclination angle β of 30°. The ratio of the spacing between the lower end of the first-stage wave suppression baffle 2-2 and the central axis to the inner diameter of the microwave vaporization chamber 3 is 1:3. One end of the second-stage wave suppression baffle 2-3 is connected to the outer wall of the gasifier chamber 6, and the other end is tilted downward, with a vertical distance of 50 mm from the outer end of the first-stage wave suppression baffle 2-2, an inclination angle γ of 45°, and the ratio of the spacing between the outer end and the outer wall of the microwave vaporization chamber 3 to the inner diameter of the microwave vaporization chamber 3 is 3:4. The height ratio of the microwave gasification chamber 3 to the low-temperature pyrolysis chamber 2 is 2:3. The microwave gasification chamber 3 is connected to the online reforming reaction chamber 4 through the upper gas phase outlet 3-1, and the bottom is connected to the carbon material collection box 11 through the solid outlet 3-2. The online reforming reaction chamber 4 is connected to the product separation and collection system through the reforming gas outlet 4-1. The height ratio of the reforming reaction chamber 4 to the low-temperature pyrolysis chamber 2 is 4:5.

[0036] The combustion and heating chamber 5 runs through the drying chamber 1 and the low-temperature pyrolysis chamber 2. The bottom surface of the upper truncated cone structure is located between the drying chamber 1 and the low-temperature pyrolysis chamber 2. The ratio of the bottom diameter of the truncated cone structure to the inner diameter of the low-temperature pyrolysis chamber 2 is 2:3. The ratio of the top diameter of the truncated cone structure to the bottom diameter is 1:3, the ratio of the truncated cone height is 1:1, and the ratio of the inner diameter of the lower combustion chamber is 1:1. The main body of the combustion and heating chamber 5 is connected to the low-temperature pyrolysis chamber 2 through four layers of circumferentially symmetrical pyrolysis gas outlets 2-1, each layer has four pyrolysis gas outlets 2-1, and the pyrolysis gas outlet 2-1 is positioned with a combustion nozzle 5-1 with a diameter of 40 mm on the combustion air distribution inner pipe 5-2. A number of dry tail gas outlets 5-3 are arranged on the side of the upper truncated cone structure along the busbar and connected to the drying chamber 1. The blower 5-4 is connected to the combustion and heating chamber 5 through the combustion air distribution inner pipe 5-2.

[0037] The gasifier cavity 6 is located at the axis of the microwave gasification cavity 3, connected to the gasifier through the bottom gasifier inlet 6-1, connected to the microwave gasification cavity 3 through the six circumferentially symmetrical first gasifier outlets 6-2 on each layer, and the bottom wind curtain outlet 6-3 is arranged opposite to the peripheral feed port 7-2. The annular direct-fed microwave 7 is arranged on the peripheral feed port 7-2 of the microwave gasification cavity 3 through the echo suppressor 7-1.

[0038] The first-stage gas separation device 8 is connected to the reformer outlet 4-1 on the online reforming reaction chamber 4 through the reforming gas inlet 8-1, is connected to the second-stage purification device 9 through the crude hydrogen outlet 8-2, and is connected to the gasifying agent chamber 6 through the second gasifying agent outlet 8-3; the second-stage purification device 9 is connected to the crude hydrogen outlet 8-2 of the first-stage gas separation device 8 through the crude hydrogen inlet 9-1, and is connected to the gas storage bottle 10 through the high-purity hydrogen outlet 9-2.

[0039] The biomass cascade pyrolysis-microwave gasification carbon-hydrogen cogeneration method using the above-mentioned biomass cascade pyrolysis-microwave gasification carbon-hydrogen cogeneration integrated device embodiment comprises the following steps:

[0040] S1: The biomass enters the reactor from the drying chamber 1, is heated and dried through the drying tail gas outlet 5-3, and then enters the low-temperature pyrolysis chamber 2 for low-temperature preliminary pyrolysis and carbonization. The low-temperature pyrolysis temperature T1 is 350°C. The pyrolysis gas product enters the combustion heating chamber 5 through the pyrolysis gas outlet 2-1, and the remaining solid material enters the microwave gasification chamber 3 through the gap between the first-stage wave suppression baffle 2-2 and the second-stage wave suppression baffle 2-3;

[0041] S2: The material undergoes a gasification reaction in the microwave gasification cavity 3 with the separated carbon dioxide or a mixed gas gasifying agent with a small amount of other gases. The gasifying agent is introduced in a gaseous form, and the mass ratio of the gasifying agent to the solid product is 2:1. The gasification reaction temperature T2 is 900°C. The gaseous product enters the online reforming reaction cavity 4 through the upper gas phase outlet 3-1 for online catalytic reforming and then enters the first-stage gas separation device 8. The solid porous carbon material product passes through the solid outlet 3-2, is isolated from the air, is cooled to below 60°C, and enters the carbon material collection box 11;

[0042] S3: The pyrolysis gas in step S1 is combusted with air in the combustion and heating chamber 5, the combustion temperature T3 is 1000°C, the excess air coefficient is in the range of 1.2, the combustion pressure is normal pressure, and the heat generated is used to heat the low-temperature pyrolysis chamber 2. The tail gas is discharged into the drying chamber 1 through the dry tail gas outlet 5-3 for drying the biomass raw material. The reformed gas in step S2 is separated into crude hydrogen and gasifying agent through the first-stage gas separation device 8, and the gasifying agent returns to the gasifying agent chamber 6 and is discharged in both directions inside and outside to fully contact with the material for microwave gasification reaction, and forms a wind curtain on the surface of the feed port 7-2 through the bottom wind curtain outlet 6-3 to protect the feed port.

[0043] Among them, in step S2, the catalyst preparation step in the reforming reaction chamber 4 is:

[0044] (1) Select nickel nitrate as a precursor, weigh urea at a molar ratio of 1:4 to nickel nitrate, add 100 mL of deionized water, and dissolve and stir evenly;

[0045] (2) adding γ-Al2O3 powder in a molar ratio of 3:1 to nickel nitrate, stirring and shaking at a constant temperature of 60°C at a frequency of 4000 rpm for 10 hours, and then taking out and drying;

[0046] (3) Calcination was performed at 400°C for 2 hours in an air atmosphere.

[0047] The above specific implementation methods are only for illustrating the technical concept and structural features of the present invention, and the purpose is to enable relevant persons familiar with this technology to implement it. However, the above content does not limit the protection scope of the present invention. Any equivalent changes or modifications made according to the spirit of the present invention should fall within the protection scope of the present invention.

Claims

1. A biomass cascade pyrolysis-microwave gasification carbon-hydrogen cogeneration integrated device, characterized in that: It includes an integrated reaction system, internal and external radial energy supply systems, and a product separation and collection system; The integrated reaction system comprises a drying chamber (1), a low-temperature pyrolysis chamber (2), a microwave gasification chamber (3), and an online reforming reaction chamber (4) arranged outside the low-temperature pyrolysis chamber (2) in sequence from top to bottom; the drying chamber (1) is used to load and dry biomass raw materials; the low-temperature pyrolysis chamber (2) is used to preliminarily pyrolyze and carbonize the biomass raw materials and improve their microwave absorption capacity; the microwave gasification chamber (3) is connected to the online reforming reaction chamber (4) through a gas phase outlet (3-1) to produce high-quality gas products and porous carbon products from highly absorbing materials; the online reforming reaction chamber (4) is connected to a product separation and collection system through a reforming gas outlet (4-1) to perform online catalytic reforming of gas products generated by microwave gasification; The inner and outer radial energy supply system comprises a combustion heat supply chamber (5) and a gasification agent chamber (6) arranged from top to bottom on the central axis inside the integrated reaction system, and a ring-shaped direct-feed microwave generator (7) arranged outside the microwave gasification chamber (3); the combustion heat supply chamber (5) runs through the drying chamber (1) and the low-temperature pyrolysis chamber (2), and the drying tail gas outlet (5-3) arranged at the upper end is located between the drying chamber (1) and the low-temperature pyrolysis chamber (2), and the combustion tail gas used for pyrolysis gas is used for pyrolysis reaction and material drying. A pyrolysis gas outlet (2-1) is provided at the lower end and is connected to the low-temperature pyrolysis chamber (2); a blower (5-4) is connected to the combustion heat supply chamber (5) via a combustion air distribution inner pipe (5-2); the gasifier chamber (6) is provided at the axis of the microwave gasification chamber (3) and is used for the gasification reaction of the material; the upper end thereof is connected to the microwave gasification chamber (3) via a first gasifier outlet (6-2), and a gasifier inlet (6-1) is provided at the bottom thereof; the annular direct-feed microwave generator (7) is used to provide microwaves to the microwave gasification chamber (3); The product separation and collection system comprises a first-stage gas separation device (8), a second-stage purification device (9), a gas storage bottle (10), and a carbon material collection box (11); the first-stage gas separation device (8) is used to receive and separate reformed gas products and provide a gasifying agent for a gasification reaction, and is provided with a reformed gas inlet (8-1), a crude hydrogen outlet (8-2), and a second gasifying agent outlet (8-3); the reformed gas inlet (8-1) is connected to the reformed gas outlet (4-1), the crude hydrogen outlet (8-2) is connected to the gas storage bottle (10) through the second-stage purification device (9), and the second gasifying agent outlet (8-3) is connected to the gasifying agent inlet (6-1); the carbon material collection box (11) is connected to the solid outlet (3-2) at the bottom of the microwave gasification cavity (3).

2. According to claim 1, a biomass cascade pyrolysis-microwave gasification carbon-hydrogen cogeneration integrated device is characterized by: The drying chamber (1) is an inverted bucket-shaped structure with a larger top and a smaller bottom, the ratio of the inner diameter of the upper end to the lower end is 2:1 to 3:1, and the inclination angle α of the inner wall of the drying chamber is 30° to 60°; the upper end of the combustion and heating chamber (5) is a truncated cone structure (5-5), the drying tail gas outlet (5-3) is arranged on the truncated cone structure (5-5), the bottom diameter of the truncated cone structure (5-5) and the inner diameter of the low-temperature pyrolysis chamber (2) are in the ratio of 1:2 to 2:3, and the upper cone of the truncated cone structure (5-5) is 1:2 to 2:

3. The ratio of the top diameter to the bottom diameter is 1:2 to 1:3, the ratio of the upper table diameter of the truncated cone structure (5-5) to the height of the truncated cone structure (5-5) is 1:1 to 1:1.5, and the ratio of the upper table diameter of the truncated cone structure (5-5) to the inner diameter of the combustion heating chamber (5) is 1:1; the ratio of the height of the microwave gasification chamber (3) to the height of the low-temperature pyrolysis chamber (2) is 2:3, and the ratio of the height of the online reforming reaction chamber (4) to the height of the low-temperature pyrolysis chamber (2) is 4:5 to 1:

1.

3. According to claim 1, a biomass cascade pyrolysis-microwave gasification carbon-hydrogen cogeneration integrated device is characterized by: A first-stage wave suppression baffle (2-2) and a second-stage wave suppression baffle (2-3) are sequentially arranged between the low-temperature pyrolysis chamber (2) and the microwave vaporization chamber (3) from top to bottom. One end of the first-stage wave suppression baffle (2-2) is connected to the bottom of the inner wall of the low-temperature pyrolysis chamber (2), and the other end is inclined downward with an inclination angle β of 20° to 45°. One end of the second-stage wave suppression baffle (2-3) is connected to the outer wall of the vaporizing agent chamber (6), and the other end is inclined downward with an inclination angle γ in the range of β+15°. The vertical distance between the second-stage wave suppression baffle (2-3) and the outer end of the first-stage wave suppression baffle (2-2) is 0 to 50 mm. The ratio of the distance between the outer end of the second-stage wave suppression baffle (2-3) and the outer wall of the microwave vaporization chamber (3) to the inner diameter of the microwave vaporization chamber (3) is 3:

4.

4. According to claim 1, a biomass cascade pyrolysis-microwave gasification carbon-hydrogen cogeneration integrated device is characterized by: The pyrolysis gas outlets (2-1) are symmetrically arranged in 4 to 6 layers along the inner wall of the combustion and heating chamber (5), with 2 to 4 outlets in each layer. A combustion nozzle (5-1) is arranged on the combustion air distribution inner pipe (5-2). The combustion nozzle (5-1) is located between two layers of pyrolysis gas outlets (2-1), and the diameter of the combustion nozzle (5-1) is 40 mm.

5. According to claim 1, a biomass cascade pyrolysis-microwave gasification hydrocarbon co-production integrated device is characterized by: The first gasifying agent outlets (6-2) are symmetrically arranged in 4 to 6 layers along the circumferential direction of the outer wall of the gasifying agent cavity (6), with the number of the first gasifying agent outlets (6-2) being 2 to 4 in each layer.

6. The biomass cascade pyrolysis-microwave gasification hydrocarbon co-production integrated device according to claim 1, characterized in that: An outer peripheral feeding port (7-2) is provided on the outer wall of the microwave vaporization cavity (3); the annular direct-feed microwave generator (7) is connected to the outer peripheral feeding port (7-2) via an echo suppressor (7-1); a bottom air curtain outlet (6-3) is provided at the bottom of the outer peripheral feeding port (7-2); and the vaporizing agent cavity (6) is connected to the bottom air curtain outlet (6-3).

7. A biomass cascade pyrolysis-microwave gasification hydrocarbon co-production method, using the biomass cascade pyrolysis-microwave gasification hydrocarbon co-production integrated device according to any one of claims 1 to 6, characterized in that: The following steps are involved: S1: The biomass raw material enters the drying chamber (1), is heated and dried through the drying tail gas outlet (5-3), and then enters the low-temperature pyrolysis chamber (2) for low-temperature preliminary pyrolysis and carbonization. The pyrolysis gas product enters the combustion heating chamber (5) through the pyrolysis gas outlet (2-1), and the remaining solid material enters the microwave gasification chamber (3); S2: The material undergoes a gasification reaction with the gasifying agent in the microwave gasification chamber (3), and the gaseous product enters the online reforming reaction chamber (4) through the gas phase outlet (3-1) for online catalytic reforming and then enters the first-stage gas separation device (8), and the solid porous carbon material product enters the carbon material collection box (11) through the solid outlet (3-2) to be isolated from air and cooled to below 60°C; S3: The pyrolysis gas in step S1 is combusted with air in the combustion and heating chamber (5) to provide heat for the low-temperature pyrolysis chamber (2), and the tail gas is discharged into the drying chamber (1) through the dry tail gas outlet (5-3) for drying. The reformed gas in step S2 is separated into crude hydrogen and a gasifying agent through the first-stage gas separation device (8), and the gasifying agent returns to the microwave gasification chamber (3) through the gasifying agent chamber (6) to fully contact with the material for microwave gasification reaction, and forms a wind curtain on the surface of the peripheral feed port (7-2) through the bottom wind curtain outlet (6-3) to protect the peripheral feed port (7-2).

8. The method for co-production of carbon and hydrogen by biomass cascade pyrolysis-microwave gasification according to claim 7, characterized in that: In step S1, the pyrolysis reaction temperature T1 of the low-temperature pyrolysis chamber (2) ranges from 200 to 360° C., and T1 is adjusted according to the material and heating conditions; in step S2, the gasification reaction temperature T2 of the microwave gasification chamber (3) ranges from 600 to 1200° C.; in step S3, the combustion temperature T3 of the combustion heating chamber (5) ranges from 900° C. to 1300° C., and the excess air coefficient ranges from 1.2 to 1.

5.

9. The biomass cascade pyrolysis-microwave gasification hydrocarbon co-production method according to claim 7, characterized in that: The gasifying agent in step S2 is separated carbon dioxide or a mixed gas with a small amount of other gases, which is introduced in a gaseous form, and the mass ratio of the gasifying agent to the solid product is 1:2 to 4:

1.

10. The biomass cascade pyrolysis-microwave gasification hydrocarbon co-production method according to claim 7, characterized in that: In step S2, a natural catalyst and a synthetic supported catalyst capable of catalyzing tar cracking are placed in an online reforming reaction chamber (4), including a nickel-based synthetic supported catalyst with γ-Al2O3 as a carrier and nano-nickel oxide as an active component. The nickel-based synthetic supported catalyst is made of nickel nitrate and γ-Al2O3 as raw materials and urea as a precipitant, and is prepared by impregnation, drying, and calcination at 400° C. in an air atmosphere.

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