Biomass pyrolysis gas self-heating type carbon catalytic reforming gasification furnace and synthesis gas production method

Abstract

The invention provides a biomass pyrolysis gas self-heating type carbon catalytic reforming gasification furnace and a synthesis gas production method, and relates to the technical field of catalytic reforming. The gasification furnace comprises a carbonization section and a gasification section which are connected in series, the carbonization section is provided with a plurality of tubes which are vertically and annularly distributed, an outer cavity of the carbonization section is filled with a biomass raw material, and an inner cavity serves as a gas channel and is provided with a gas collection assembly; a grate is arranged at the bottom of the gasification section, a high-temperature biochar layer is filled above the grate, and a nozzle for introducing a pure oxygen-steam mixed gasification agent and an ash outlet are formed in the grate. Biomass is pyrolyzed in the carbonization section to generate pyrolysis gas and biochar, the pyrolysis gas downwards penetrates through a high-temperature biochar layer for carbon in-situ catalytic reforming to remove tar, synthesis gas generated in the gasification section ascends to supply heat to the carbonization section, and heat energy self-circulation and tar in-situ purification are achieved. The design solves the problems of high tar content and low heat energy utilization rate of the traditional gasification furnace and carbonization furnace, and is suitable for preparing clean synthesis gas.

Description

Technical Field

[0001] This invention relates to the field of catalytic reforming technology, and more specifically, to a biomass pyrolysis gas self-heating carbon catalytic reforming gasifier and a syngas production method. Background Technology

[0002] Traditional biomass gasification and carbonization technologies have significant drawbacks, posing a bottleneck in environmental pollution control. In conventional fixed-bed continuous gasification or carbonization using a gasifying agent, the biomass and the gasifying agent exchange heat in opposite directions. During the drying, pyrolysis, and carbonization process in the low-temperature zone, water vapor, acetic acid, light tar, and heavy tar generated are carried out of the gasifier by the hot gas flow. Upon cooling, these substances precipitate as wood vinegar and tar, causing equipment blockage, environmental pollution, and reduced gas production, resulting in resource waste. The high-temperature cooling of water vapor, acetic acid, light tar, and heavy tar also releases a large amount of sensible heat, leading to heat waste. Existing gasification or carbonization processes struggle to address both pollutant control and energy utilization. The tar concentration produced by biomass pyrolysis is generally higher than 1 g / Nm³. 3 Acidic components such as wood vinegar require additional purification equipment (such as scrubbing towers and catalytic cracking reactors) for removal, which not only increases the complexity of the system purification but also creates problems in treating phenol-containing wastewater. In addition, the thermal energy utilization rate of the gasification process is less than 60%, and a large amount of sensible heat is not recovered, requiring external energy to supplement operating costs.

[0003] Some of the improved technologies still have limitations. For example, although the integrated furnace described in patent CN20241069998.77 attempts to integrate carbonization and gasification functions, it relies on an external waste heat recovery device to achieve energy circulation, resulting in a long equipment process and high investment costs; moreover, tar cracking requires an independent catalytic unit, and the complexity of system operation and energy consumption problems have not been fundamentally solved. Summary of the Invention

[0004] To overcome or at least partially solve the above problems, this application provides a biomass pyrolysis gas self-heating carbon catalytic reforming gasifier, comprising a carbonization section and a gasification section. The carbonization section includes: multiple tubes arranged vertically in a triangular ring shape, the outer cavity of each tube filled with biomass feedstock, and the inner cavity of each tube serving as a gas passage; a gas collection assembly for collecting and discharging the syngas output from the inner cavity of the tubes. The gasification section includes: a grate located at the bottom of the gasification section; a high-temperature biochar layer filling the space above the grate; nozzles disposed on the grate for introducing a gasifying agent, the gasifying agent comprising air or air + steam; and an ash outlet located at the bottom of the gasification section for discharging the ash after the reaction.

[0005] In some embodiments, the gas collection assembly includes an annular gas collection box disposed at the top of the tube, an annular gas collection pipe communicating with the gas collection box, a radially extending main gas guide pipe and an annular header pipe, wherein the annular header pipe is communicating with the synthesis gas outlet.

[0006] In some embodiments, the diameter of the tubes is 57-133 mm, the spacing between adjacent tubes is not less than 3 times the diameter of the biomass raw material particles, the insertion depth of the tubes into the biochar layer is not less than 500 mm, the tubes are made of Q345R-inconel600-625-690 / Haynes233 / Haynes HR-160-alumina / silicon carbide ceramic tubes from low temperature to high temperature, and the total flow cross-sectional area of ​​all tubes accounts for more than 30% of the furnace cross-sectional area.

[0007] In some embodiments, the thickness of the high-temperature biochar layer is not less than 1000 mm, and the operating temperature is maintained at 800-1200℃.

[0008] In some embodiments, the grate is a water-cooled structure with an internal circulating water pipe. The two ends of the circulating water pipe are respectively connected to a circulating water inlet pipe and a circulating water outlet pipe provided on the furnace wall of the gasification section, and the porosity of the grate is 15-30%.

[0009] In some embodiments, a feeding component is also included;

[0010] The feeding components include a sealed hopper located on the top of the furnace, an airlock fan connected to the outlet of the hopper, and a material inlet extending to the carbonization section.

[0011] In some embodiments, a fabric component is also included;

[0012] The fabric component includes a rotatable fabric scraper, a feeder, and a drive motor that drives them to rotate, for uniformly distributing biomass raw materials in the outer cavity of the tube.

[0013] In some embodiments, an ash silo is also included, which is connected to an ash outlet and is used to collect and temporarily store ash to achieve continuous ash discharge.

[0014] This application also provides a method for producing syngas, comprising the following steps: S1, biomass feedstock moves from top to bottom in the outer cavity of the carbonization section tubes, undergoing drying, dry distillation, pyrolysis, and carbonization treatments in sequence to generate biochar and pyrolysis gas; S2, the pyrolysis gas generated in step S1 penetrates downward through the high-temperature biochar layer of the gasification section, and undergoes in-situ biochar catalytic reforming at 800-1200℃, causing tar and wood vinegar to be cracked into small molecule gases; S3, the reformed pyrolysis gas flows upward through the inner cavity of the tubes, providing a heat source for the carbonization section before being cooled and output; S4, the biochar enters the gasification section and undergoes a gasification reaction with a mixture of pure oxygen and steam as a gasifying agent to generate crude syngas; S5, the crude syngas flows upward through the inner cavity of the tubes, is cooled to 120-150℃, and is output; wherein, in step S4, the molar ratio of pure oxygen to steam is 1:1 to 1:4.

[0015] This application also provides a biomass pyrolysis gas self-heating carbon catalytic reforming carbonization and activation furnace, including a carbonization section and an activation section. The carbonization section includes: multiple tubes arranged vertically in a triangular ring shape, the outer cavity of the tubes being filled with biomass raw materials, and the inner cavity of the tubes serving as a gas passage; a gas collection assembly for collecting and discharging the synthesis gas output from the inner cavity of the tubes; the activation section includes: a spiral blade driven by a motor located below the activation section; a carbon removal scraper located at the bottom of the activation section for discharging carbon slag from the carbonization and activation furnace; a shell-and-tube heat exchanger located outside the activation section; and an oxygen-deficient combustion chamber located on the side of the shell-and-tube heat exchanger away from the activation section. Attached Figure Description

[0016] To more clearly illustrate the technical solutions of the embodiments of the present invention, the accompanying drawings used in the embodiments will be briefly introduced below. It should be understood that the following drawings only show some embodiments of the present invention and should not be regarded as a limitation on the scope. For those skilled in the art, other related drawings can be obtained based on these drawings without creative effort.

[0017] Figure 1 This is a schematic diagram of the structure of a biomass pyrolysis gas self-heating carbon catalytic reforming gasifier according to an embodiment of the present invention;

[0018] Figure 2 for Figure 1 Cross-sectional view of AA;

[0019] Figure 3 This is a schematic diagram of the structure of a biomass pyrolysis gas self-heating carbon catalytic reforming carbonization activation furnace provided in an embodiment of the present invention;

[0020] Figure 4This is a schematic diagram of the structure of a biomass pyrolysis gas self-heating carbon catalytic reforming carbonization activation gasification system provided in an embodiment of the present invention;

[0021] Figure 5 This is a schematic diagram of another biomass pyrolysis gas self-heating carbon catalytic reforming carbonization activation gasification system provided in an embodiment of the present invention.

[0022] The attached diagrams are labeled as follows: 1. Carbonization section; 11. Tube; 12. Gas collection assembly; 121. Annular gas collection box; 122. Annular gas collection pipe; 123. Main gas guide pipe; 124. Annular header pipe; 2. Gasification section; 21. Grate; 211. Circulating water pipe; 212. Circulating water inlet pipe; 213. Circulating water outlet pipe; 22. High-temperature biochar layer; 23. Nozzle; 24. Ash outlet; 3. Feeding component; 31. Sealed silo; 32. Airlock; 33. Material inlet; 4. Feeding component; 41. Feeding scraper; 42. Feeder; 43. Drive motor; 5. Ash silo; 6. Activation section; 61. Spiral blade; 62. Carbon removal scraper; 63. Shell-and-tube heat exchanger; 64. Energy supply oxygen-deficient system. Combustion chamber; 641, Cooling gas inlet; 642, Combustion pyrolysis gas inlet; 643, Combustion-supporting gas inlet; 7, Intercooler; 71, First intercooler; 72, Second intercooler; 73, Third intercooler; 74, Dust removal device; 81, Pressure swing adsorption device; 811, First pressure swing adsorption device; 812, Second pressure swing adsorption device; 821, First gas storage tank; 822, Second gas storage tank; 823, Third gas storage tank; 824, Fourth gas storage tank; 83, Proportional valve; 84, CO conversion device; 91, Biomass pyrolysis gas self-heating carbon catalytic reforming gasifier; 92, Biomass pyrolysis gas self-heating carbon catalytic reforming carbonization activation furnace; 93, First carbonization activation furnace; 94, Second carbonization activation furnace. Detailed Implementation

[0023] To make the objectives, technical solutions, and advantages of the embodiments of the present invention clearer, the technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. The components of the embodiments of the present invention described and shown in the accompanying drawings can generally be arranged and designed in various different configurations.

[0024] Figure 1 This is a schematic diagram of the structure of a biomass pyrolysis gas self-heating carbon catalytic reforming gasifier provided in an embodiment of the present invention. Figure 2 for Figure 1 Cross-sectional view of AA.

[0025] like Figure 1 and Figure 2As shown in the figure, this application provides a biomass pyrolysis gas self-heating carbon catalytic reforming gasifier, including a carbonization section 1 and a gasification section 2.

[0026] The carbonized segment 1 includes:

[0027] Multiple tubes 11 are arranged vertically and in a ring shape. The outer cavity of each tube 11 is filled with biomass feedstock, and the inner cavity of each tube 11 serves as a gas passage. The diameter of each tube 11 is 57-133 mm, and the spacing between adjacent tubes is not less than three times the diameter of the biomass feedstock particles.

[0028] Gas collection assembly 12, which is used to collect and export the synthesis gas output from the inner cavity of the tube 11;

[0029] The gasification section 2 includes:

[0030] A grate 21 is located at the bottom of the gasification section 2;

[0031] High-temperature biochar layer 22, which fills the space above the grate 21;

[0032] Nozzle 23, which is disposed on grate 21, is used to introduce a mixture of pure oxygen and steam as a gasifying agent;

[0033] Ash outlet 24, located at the bottom of gasification section 2, is used to discharge ash after reaction.

[0034] The carbonization section 1 refers to the area in the gasifier where biomass is pyrolyzed, and it consists of multiple vertically arranged annular distribution tubes 11. The tubes 11 are tubular structures made of high-temperature resistant alloys, with their outer cavity containing the biomass feedstock and their inner cavity serving as gas flow channels. The diameter of the tubes 11 is 57-133 mm, and the spacing between adjacent tubes is not less than three times the diameter of the biomass feedstock particles. The insertion depth of the tubes 11 into the biochar layer is not less than 500 mm. Different materials of the tubes 11 correspond to different temperature zones, ranging from low to high temperature: Q345R-inconel600-625-690 / Haynes233 / Haynes HR-160-alumina / silicon carbide ceramic tubes.

[0035] Gasification section 2 refers to the area in the gasifier where biochar is converted into syngas, located below carbonization section 1. The grate 21 is a supporting structure at the bottom of gasification section 2, used to support the biochar layer and distribute the gasifying agent. The high-temperature biochar layer 22 is a biochar accumulation layer filled above the grate 21, with its temperature maintained within the catalytically active range. The nozzle 23 is an injection device that introduces a mixture of pure oxygen and steam as a gasifying agent into gasification section 2.

[0036] Biomass feedstock fills the outer cavity of the tubes 11 in carbonization section 1 and moves downwards under gravity. In gasification section 2, nozzles 23 introduce a mixed gasifying agent of pure oxygen and steam above the grate 21. This gasifying agent permeates upwards through the high-temperature biochar layer 22, undergoing partial oxidation (C + O2 → CO) and water-gas reactions (C + H2O → CO + H2) with the biochar, generating crude syngas mainly composed of CO and H2. The high temperature (>1000℃) released by this reaction maintains thermal equilibrium in gasification section 2.

[0037] The crude syngas, carrying high sensible heat, rises to carbonization section 1 and flows through the inner cavity of tube 11. The high-temperature gas indirectly heats the biomass in the outer cavity through the wall of tube 11, causing it to undergo a series of processes: drying (removing moisture at 120-300℃), pyrolysis (releasing volatiles at 300-500℃), and carbonization (generating biochar and pyrolysis gas at 700-800℃). After being generated in carbonization section 1, the pyrolysis gas is driven downwards by pressure, penetrating the high-temperature biochar layer 22 (800-1000℃) in gasification section 2.

[0038] The functions of the high-temperature bio-carbon layer 22 include:

[0039] 1) Tar catalytic cracking: Tar components (such as toluene and naphthalene) in the cracked gas come into contact with active sites on the surface of biochar (—COOH / —OH and alkali metals), and are cracked into small molecule gases such as CH4, CO, and H2;

[0040] 2) Wood vinegar reforming: Oxygen-containing organic matter (such as acetic acid) decomposes into CO2 and H2 under high temperature and steam conditions;

[0041] 3) Gas-solid separation: Unreacted carbon particles are retained and continue to participate in the gasification reaction.

[0042] 4) Biochar has a specific surface area greater than 500 m2 / g, adsorbs acetic acid and tar, and promotes the purification of pyrolysis gas.

[0043] 5) The metal ions such as K / Na / Fe in biomass ash act as catalysts, reducing the activation energy of pyrolysis.

[0044] The complete decomposition of tar and wood vinegar is promoted through the synergistic effect of active site-pore adsorption-alkali metal catalysis.

[0045] The reformed pyrolysis gas mixes with the crude syngas generated in gasification section 2 and flows upward into the inner cavity of tube 11. During its ascent, the mixed gas transfers heat to the biomass in the outer cavity of tube 11, cooling itself to 120-150°C, and is finally collected and output by gas collection assembly 12. Biochar continuously falls to gasification section 2 to participate in the reaction, while residual ash is screened by grate 21 and discharged through ash outlet 24, achieving material recycling and energy self-sufficiency.

[0046] Through the integrated design of carbonization section 1 and gasification section 2 and the in-situ catalytic effect of high-temperature bio-carbon layer 22, the pyrolysis gas tar and wood vinegar are directly purified in the furnace, eliminating the need for external purification equipment; at the same time, the high-temperature syngas of gasification section 2 is used to provide a heat source for carbonization section 1, realizing heat energy self-circulation and significantly reducing system energy consumption and operating costs.

[0047] In some embodiments, the gas collection assembly 12 includes an annular gas collection box 121 disposed at the top of the tube 11, an annular gas collection pipe 122 communicating with the gas collection box, a radially extending gas guide main pipe 123 and an annular main pipe 124, wherein the annular main pipe 124 is communicating with the synthesis gas outlet.

[0048] After the syngas rises from the inner cavity of the tube 11 to the top, it first enters the annular gas collecting box 121 for initial collection; then it is guided through the annular gas collecting pipe 122 to the radially extending gas guiding main pipe 123, and finally integrated through the annular main pipe 124 before being uniformly output from the syngas outlet. This multi-stage annular gas collection structure reduces the flow resistance of the syngas, avoids localized airflow short-circuiting, ensures uniform penetration of the cracked gas through the high-temperature biochar layer 22, and improves the efficiency of tar catalytic reforming.

[0049] In some embodiments, the diameter of the tubes 11 is 57-133 mm, the spacing between adjacent tubes 11 is not less than 3 times the diameter of the biomass raw material particles, and the total flow cross-sectional area of ​​all tubes 11 accounts for more than 30% of the furnace cross-sectional area.

[0050] The tubes 11, with diameters ranging from 57 to 133 mm, are arranged in a ring at intervals no less than three times the diameter of the biomass pellets. Their total flow cross-sectional area accounts for 30% of the furnace, ensuring smooth heat transfer of the high-temperature syngas within the tubes 11 while providing sufficient heating area for the biomass outside the tubes 11. By optimizing the size and layout of the tubes 11, the biomass is heated uniformly in the carbonization section 1, preventing localized overheating and coking, and maintaining pressure balance between the gasification section 2 and the carbonization section 1.

[0051] The depth to which tube 11 is inserted into the biochar layer is not less than 500 mm.

[0052] To improve economic efficiency and reduce equipment investment, the tubes are made of different materials corresponding to the corresponding temperature zones, from low temperature to high temperature. The materials are Q345R-inconel600-625-690 / Haynes233 / Haynes HR-160-alumina / silicon carbide ceramic tubes.

[0053] In some embodiments, the thickness of the high-temperature biochar layer 22 is not less than 1000 mm, and the operating temperature is maintained at 800-1000 °C.

[0054] A high-temperature biochar layer 22 with a thickness ≥1000 mm forms a porous alkali metal K / Na / Fe catalytic bed at 800-1000℃. As the pyrolysis gas penetrates downwards, the tar components are adsorbed and pyrolyzed by the active sites (—COOH / —OH) on the biochar surface and by nanopores with a specific surface area greater than 500 m² / g. The wood vinegar decomposes in a high-temperature steam environment. By synergistically controlling the thickness of the biochar layer and the temperature, the residence time of the tar pyrolysis reaction is sufficient, achieving near-complete decomposition of the wood vinegar and eliminating wastewater discharge.

[0055] In some embodiments, the grate 21 is a water-cooled structure with an internal circulating water pipe 211. The two ends of the circulating water pipe 211 are respectively connected to a circulating water inlet pipe 212 and a circulating water outlet pipe 213 provided on the furnace wall of the gasification section 2, and the porosity of the grate 21 is 15-30%.

[0056] The water-cooled grate 21 has an internal circulating water pipe 211 that connects to the external cooling system via inlet / outlet water pipes on the furnace wall. The circulating water continuously removes heat from the gasification reaction; the 15-30% porosity ensures uniform distribution of the gasifying agent. Through the water-cooling structure and porosity design, the temperature of the grate 21 is controllable, preventing slagging and sintering of the biochar layer and maintaining the stability of the gasification reaction.

[0057] In some embodiments, the system further includes a feeding component 3, which includes a sealed hopper 31 located on the top of the furnace, a shut-off fan 32 connected to the outlet of the hopper, and a material inlet 33 extending to the carbonization section 1.

[0058] In some embodiments, a fabric component 4 is also included, which includes a rotatable fabric scraper 41, a feeder 42, and a drive motor 43 for driving its rotation, for uniformly distributing biomass raw materials in the outer cavity of the tube 11.

[0059] The drive motor 43 drives the scraper 41 and the feeder 42 to rotate, spreading the biomass feedstock input from the material inlet 33 evenly in the outer cavity of the tube 11, avoiding local accumulation or bridging. Through the forced dispersion effect of the mechanical feeding component 4, the heating area of ​​the biomass in the carbonization section 1 is maximized, eliminating the fluctuation in pyrolysis gas production caused by uneven carbonization.

[0060] In some embodiments, the system further includes an ash hopper 5, which is connected to the ash outlet 24. The ash hopper 5 is used to collect and temporarily store ash to achieve continuous ash discharge.

[0061] Furthermore, the gasifying agent can be replaced with air, air + steam, or oxygen-enriched + steam to adapt to fuels with different calorific values ​​and uses.

[0062] This application also provides a method for producing syngas, including the following steps:

[0063] S1. Biomass feedstock moves from top to bottom in the outer cavity of tube 11 in carbonization section 1, and undergoes drying, dry distillation, pyrolysis and carbonization treatment in sequence to generate biochar and pyrolysis gas.

[0064] S2. The cracked gas generated in step S1 penetrates downward through the high-temperature biochar layer 22 of the gasification section 2 and undergoes catalytic reforming at 800-1200℃. Through in-situ adsorption-catalysis synergistic effect, it promotes the decomposition of tar and wood vinegar, and cracks the tar into small molecule gas.

[0065] S3. The reformed cracked gas flows in the reverse direction through the inner cavity of tube 11 and flows upward to provide a heat source for carbonization section 1 before being cooled and output.

[0066] S4. Biochar enters gasification section 2 and reacts with pure oxygen and steam mixed gasification agent to generate crude syngas.

[0067] S5. The crude synthesis gas flows upward through the inner cavity of tube 11 and is cooled to 120-150℃ before being output.

[0068] In step S4, the molar ratio of pure oxygen to steam is 1:1 to 1:4.

[0069] Biomass feedstock is temporarily stored in the sealed hopper 31 of the feeding unit 3. After the airtightness is controlled by the airlock fan 32, it enters the outer cavity of the tube 11 of the carbonization section 1 through the material inlet 33. The drive motor 43 of the feeding unit 4 drives the feeding scraper 41 and the feeder 42 to rotate, so that the feedstock is evenly distributed in the outer cavity of the tube 11. The feedstock moves from top to bottom under the action of gravity, and successively undergoes drying, dry distillation, pyrolysis and carbonization. In the drying stage, moisture is removed at 120-300℃, and the heat comes from the high-temperature gas rising in the inner cavity of the tube 11; in the dry distillation stage, volatiles are released at 300-500℃ to generate pyrolysis gas; in the carbonization stage, biochar is generated at 700-800℃.

[0070] The generated pyrolysis gas penetrates downwards through the high-temperature biochar layer 22 (thickness ≥1000 mm, temperature 800-1000℃) of the gasification section 2. Through adsorption-catalysis synergy at the active sites (—COOH / —OH) on the biochar surface, porous adsorption, and alkali metal catalysis, the tar and wood vinegar in the pyrolysis gas are decomposed into CH4 / CO / H2, and the wood vinegar is reformed into CO2 / H2O. The reformed gas flows upwards through the inner cavity of tube 11, providing heat to the carbonization section 1 before cooling to 120-150℃.

[0071] Simultaneously, biochar falls above grate 21 (water-cooled structure, porosity 15-30%) in gasification section 2. A mixture of pure oxygen and steam (O2 / H2O molar ratio 1:1 to 1:4) is introduced through nozzle 23, undergoing partial oxidation (C+O2→CO) and a water-gas reaction (C+H2O→CO+H2) with the biochar to generate crude syngas (CO+H2≥85%). This crude syngas rises into the inner cavity of tube 11 and mixes with the reformed pyrolysis gas before being output. Residual ash is screened by grate 21 and discharged from ash outlet 24 into ash silo 5 for temporary storage.

[0072] Figure 3 This is a schematic diagram of the structure of a biomass pyrolysis gas self-heating carbon catalytic reforming carbonization activation furnace 92 provided in an embodiment of the present invention.

[0073] like Figure 3 As shown in the illustration, this application also provides a biomass pyrolysis gas self-heating carbon catalytic reforming carbonization and activation furnace 92, including a carbonization section 11 and an activation section 6.

[0074] The carbonized segment 11 includes:

[0075] Multiple tubes 11 are arranged vertically and in a triangular ring shape. The outer cavity of each tube 11 is filled with biomass raw materials, and the inner cavity of each tube 11 serves as a gas channel.

[0076] Gas collection assembly 12, which is used to collect and export the synthesis gas output from the inner cavity of the tube 11;

[0077] The activation segment 6 includes:

[0078] Spiral blade 61, which is driven by a motor located below the activation section 6;

[0079] Carbon removal scraper 62 is located at the bottom of the activation section 6 and is used to remove carbon slag from the carbonization activation furnace.

[0080] Shell-and-tube heat exchanger 63, which is disposed outside the activation section 6;

[0081] An oxygen-deficient combustion chamber 64 is provided, which is located on the side of the shell-and-tube heat exchanger 63 away from the activation section 6.

[0082] In some embodiments, the oxygen-deficient combustion chamber 64 is provided with three inlets: a cooling gas inlet 641, a combustion cracking gas inlet 642, and a combustion-supporting gas inlet 643.

[0083] In some embodiments, the carbonization section 11 of the biomass pyrolysis gas self-heating carbon catalytic reforming carbonization activation furnace 92 has the same structure as the carbonization section 11 of the biomass pyrolysis gas self-heating carbon catalytic reforming gasification furnace 91.

[0084] The biomass pyrolysis gas self-heating carbon catalytic reforming carbonization activation furnace is used to produce porous carbon and anode materials.

[0085] Figure 4 This is a schematic diagram of a biomass pyrolysis gas self-heating carbon catalytic reforming carbonization activation gasification system provided in an embodiment of the present invention.

[0086] like Figure 4 As shown in the embodiments of this application, a biomass pyrolysis gas self-heating carbon catalytic reforming carbonization activation gasification system is also provided, including the biomass pyrolysis gas self-heating carbon catalytic reforming gasification furnace 91 as described in any of the preceding claims, and the aforementioned biomass pyrolysis gas self-heating carbon catalytic reforming carbonization activation furnace 92, further comprising:

[0087] Intercooler 7, the air inlet of which is connected to the syngas outlet of the biomass pyrolysis gas self-heating carbon catalytic reforming gasifier 91.

[0088] Pressure swing adsorption device 81, the inlet of the pressure swing adsorption device 81 is connected to the outlet of the intercooler 7, one outlet of the pressure swing adsorption device 81 is connected to the first gas storage tank 821, and the other outlet is connected to the second gas storage tank 822. The first gas storage tank 821 is used to store CO2-rich oxidizing gas, and the second gas storage tank 822 is used to store CO+H2-rich gas.

[0089] Both the first gas storage tank 821 and the second gas storage tank 822 are equipped with proportional valves 83 at their outlets, and the proportional valves 83 are connected to the cooling gas inlet 641 of the energy-supplying oxygen-deficient combustion chamber 64.

[0090] The combustion pyrolysis gas inlet 642 of the energy-supplying oxygen-deficient chamber is connected to the gas outlet of the intercooler 7 and the gas collection component 12 of the biomass pyrolysis gas self-heating carbon catalytic reforming carbonization activation furnace 92.

[0091] One or more embodiments of this application also provide a method for the self-heating carbon catalytic reforming carbonization activation gasification of biomass pyrolysis gas, which is applied to... Figure 4 The system includes the following steps:

[0092] S1. In the gasifier, the biomass feedstock moves from top to bottom in the outer cavity of the carbonization section tubes and undergoes drying, dry distillation, pyrolysis and carbonization in sequence to generate biochar and pyrolysis gas.

[0093] S2. The cracked gas penetrates downward through the high-temperature biochar layer of the gasification section and undergoes in-situ biochar catalytic reforming at 800-1200℃, causing the tar and wood vinegar to be cracked into small molecule gases.

[0094] S3. The reformed cracked gas flows in the reverse direction through the inner cavity of the tube and flows upward to provide a heat source for the carbonization section before being cooled and output as syngas.

[0095] S4. Biochar enters the gasification section and reacts with the gasification agent to generate crude syngas.

[0096] S5. The crude syngas flows upward through the inner cavity of the tube and is output after cooling.

[0097] S6. The output synthesis gas is purged by a dust removal device and cooled by an intercooler.

[0098] S7. The cooled gas enters the pressure swing adsorption device and is separated into CO2-rich gas and CO+H2-rich gas.

[0099] S8. CO2-rich gas is stored in the first gas storage tank, and CO+H2-rich gas is stored in the second gas storage tank.

[0100] S9. Adjust the ratio of CO2-rich gas and CO+H2-rich gas by using a proportional valve, and introduce the mixed gas as a cooling gas into the oxygen-deficient chamber at the bottom of the carbonization and activation furnace.

[0101] S10, the energy-deficient oxygen chamber receives combustion and cracking gas from the intercooler outlet and the carbonization and activation furnace gas collection assembly for combustion.

[0102] The high-temperature syngas output from the gasifier is cooled by an intercooler and then enters a pressure swing adsorption unit, where it is separated into CO2-rich gas and CO+H2-rich gas, which are stored in the first and second gas storage tanks, respectively. The ratio of the two gases is dynamically adjusted by a proportional valve to form a mixed cooling gas with specific components, which is then introduced into the oxygen-deficient chamber at the bottom of the carbonization and activation furnace. At the same time, the combustion and cracking gas inlet of the oxygen-deficient chamber receives the residual gas from the outlet of the intercooler and the cracking gas produced by the carbonization and activation furnace itself, and releases heat through combustion in an oxygen-deficient environment to provide heat for the carbonization and activation process.

[0103] By utilizing the full components of syngas in a graded manner and implementing closed-loop control, the waste heat of the gasifier (high-temperature syngas) is converted into an effective heat source for the carbonization and activation furnace, eliminating the need for external heating equipment. The CO2-rich gas is used as a diluent to participate in oxygen-deficient combustion, precisely controlling the combustion temperature to avoid overburning in the activation section, while eliminating direct CO2 emissions, thus achieving a synergistic effect of improving system energy efficiency and reducing carbon emissions.

[0104] Figure 5 This is a schematic diagram of another biomass pyrolysis gas self-heating carbon catalytic reforming carbonization activation gasification system provided in an embodiment of the present invention.

[0105] like Figure 5 As shown in the embodiments of this application, another biomass pyrolysis gas self-heating carbon catalytic reforming carbonization activation gasification system is also provided, including a biomass pyrolysis gas self-heating carbon catalytic reforming gasification furnace 91 as described in any of the preceding claims, and two of the aforementioned biomass pyrolysis gas self-heating carbon catalytic reforming carbonization activation furnaces 92. The biomass pyrolysis gas self-heating carbon catalytic reforming carbonization activation furnace includes a first carbonization activation furnace 93 and a second carbonization activation furnace 94. The biomass pyrolysis gas self-heating carbon catalytic reforming carbonization activation gasification system further includes:

[0106] The first pressure swing adsorption device 811, the gas collection component 12 of the first carbonization activation furnace 93 passes through the dust removal device 74 and the first intercooler 71, and is connected to the air inlet of the first pressure swing adsorption device 811 and the combustion cracking gas inlet 642 of the oxygen-deficient combustion chamber of the first carbonization activation furnace 93; one outlet of the first pressure swing adsorption device 811 is connected to the first gas storage tank 821, and the other outlet is connected to the second gas storage tank 822. The first gas storage tank 821 is used to store CO2-rich oxidizing gas, and the second gas storage tank 822 is used to store CO+H2-rich gas; the outlets of the first gas storage tank 821 and the second gas storage tank 822 are each equipped with a first proportional valve 83, and the first proportional valve 83 is connected to the cooling gas inlet 641 of the oxygen-deficient combustion chamber 64 of the first carbonization activation furnace 93.

[0107] CO conversion device 84, the inlet of the CO conversion device 84 is connected to the first proportional valve 83, the inlet of the CO conversion device 84 is connected to the syngas outlet of the biomass pyrolysis gas self-heating carbon catalytic reforming gasification furnace 91 through the second intercooler 72, and the inlet of the CO conversion device 84 is connected to the syngas outlet of the biomass pyrolysis gas self-heating carbon catalytic reforming carbonization activation furnace 92 through the third intercooler 73.

[0108] The second pressure swing adsorption device 812 has its inlet connected to the outlet of the CO conversion device 84. One outlet of the second pressure swing adsorption device 812 is connected to the third gas storage tank 823, and the other outlet is connected to the fourth gas storage tank 824. The third gas storage tank 823 is used to store CO2-rich oxidizing gas, and the fourth gas storage tank 824 is used to store H2. The outlets of the third gas storage tank 823 and the fourth gas storage tank 824 are each equipped with a second proportional valve 83. The second proportional valve 83 is connected to the cooling gas inlet 641 of the oxygen-deficient combustion chamber 64 of the second carbonization activation furnace 94.

[0109] The gas collection assembly 12 of the second carbonization activation furnace 94 is connected to the combustion pyrolysis gas inlet 642 of the energy supply oxygen-deficient chamber.

[0110] When the carbonization activation furnace 92 includes a first carbonization activation furnace 93 and a second carbonization activation furnace 94, the biomass pyrolysis gas self-heating carbon catalytic reforming carbonization activation gasification method is applied. Figure 5 In addition to steps S1-S10, the system also includes the following steps:

[0111] S11. The gas generated by the first carbonization and activation furnace is cooled by the first intercooler, and part of it enters the first pressure swing adsorption device for separation, while part of it enters the oxygen-deficient combustion chamber for energy supply.

[0112] S12. The CO2-rich gas separated by the first pressure swing adsorption device is stored in the first gas storage tank, and the CO+H2-rich gas is stored in the second gas storage tank.

[0113] S13. The ratio is adjusted by the first proportional valve, and the mixed gas is introduced into the oxygen-deficient chamber of the first carbonization and activation furnace for cooling.

[0114] The syngas from S14, the gasifier, and the second carbonization and activation furnace are processed by a CO conversion unit.

[0115] The gas after S15 and CO conversion is separated into CO2-rich gas and H2 gas by the second pressure swing adsorption device; the CO2-rich gas is stored in the third gas storage tank and the H2 gas is stored in the fourth gas storage tank.

[0116] S16. The ratio is adjusted by the second proportional valve, and the mixed gas is introduced into the oxygen-deficient chamber of the second carbonization and activation furnace for cooling.

[0117] S17. Combustion cracking gas and pure oxygen support combustion flue gas are controlled by a proportional valve to achieve CO2 / CO+H2 cooling balance. The flue gas is used as an activator to produce carbon materials.

[0118] When the system includes a first and a second carbonization activation furnace, the pyrolysis gas from the first carbonization activation furnace is cooled by a first intercooler. Part of the gas then enters a first pressure swing adsorption unit to separate CO2-rich gas (stored in the first gas storage tank) and CO+H2-rich gas (stored in the second gas storage tank). The remaining gas is directly fed into its own oxygen-deficient chamber for combustion. A first proportional valve adjusts the gas ratio between the two gas storage tanks, and the mixture is then fed into the oxygen-deficient chamber of the first carbonization activation furnace for temperature control. The syngas from the gasification furnace and the second carbonization activation furnace is converted from CO to H2 by a CO conversion device, and then separated by a second pressure swing adsorption unit to separate CO2-rich gas (stored in the third gas storage tank) and high-purity H2 (stored in the fourth gas storage tank). A second proportional valve adjusts the gas ratio between the two gases, and the mixture is then fed into the oxygen-deficient chamber of the second carbonization activation furnace.

[0119] Through two-stage gas separation and directional distribution, the first carbonization and activation furnace exclusively produces biochar and medium-calorific-value gas (rich in CO and H2), while the second carbonization and activation furnace co-produces high-purity H2 and carbon materials. The system simultaneously outputs energy (syngas and H2), materials (biochar), and carbon sink carrier (rich in CO2 gas for temperature-controlled combustion), achieving multi-product co-production and maximizing resource utilization. Independent gas control of the two furnaces avoids component interference and ensures operational stability under complex operating conditions.

[0120] In some embodiments, the porous carbon material may be air-purifying activated carbon, supercapacitor carbon, medical slow-release carbon, or hard carbon.

[0121] In Example 1, bamboo is first cut, dried, and crushed, then fed into a self-heating carbon catalytic reforming furnace for carbonization activation. Carbonization and activation are performed at 850°C for 180 minutes using a specific burner (center vented with cracked gas, middle ring vented with pure oxygen, and outer ring vented with CO2-rich gas), generating cracked carbonization activation gas and activated carbon. The exiting cracked carbonization activation gas is dedusted by a dust collector; 40% is used for combustion and energy supply, and 60% is cooled by an intercooler to obtain purified gas. This purified gas is then separated into CO2-rich and reducing gas by a PSA (Power Separator). The CO2-rich gas is introduced into the outer ring of the energy-supplying burner, mixing with the central combustion gas and the middle ring pure oxygen to form a mixed flue gas at 1400°C. This forms a high-temperature activation flue gas with a specific CO2:H2O ratio of 8:2-7:3. This flue gas is cooled to 850°C and then fed into the self-heating carbon catalytic reforming furnace for carbonization activation. Under micro-positive pressure and online monitoring and control of the CO2 / H2O partial pressure, the material is activated, ultimately yielding a material with a specific surface area of ​​3300 m². 2 / g, micropore volume 0.95cm³ 3 Air purification activated carbon products with a density of / g, pore size of 1.2-1.8nm, micropores >70%, and ash content of 2.3%.

[0122] Example 2: Crushed and dried bamboo granules are fed into a self-heating carbon catalytic reforming carbonization activation furnace (activated at 850℃ for 240 minutes) to produce pyrolysis carbonization activation gas and carbon-based materials. After dust removal by a dust removal device, 40% of the carbonization activation gas (CO 37%, H2 22%, CH4 13%, CO2 28%) is used for combustion to provide energy, and 60% is cooled by an intercooler. The gas was separated by PSA into 92% CO2-rich oxidizing gas and ≥85% CO+H2-rich reducing gas. The CO2-rich gas was burned with some fuel gas and pure oxygen in a combustion chamber at 2000℃. Superheated steam (450℃) was added to form activated flue gas at 850℃ (CO2:H2O=5:1). The flue gas was then activated in an activation furnace at a constant temperature for 240 minutes. The pore size distribution (micropores >90%) was controlled by adjusting the gas-fuel ratio using online mass spectrometry to obtain supercapacitor carbon with a specific surface area of ​​2000-2500 m2 / g, an iodine value of 1400-1600 mg / g, an electrical conductivity ≥10 S / cm, and an organic capacitance ≥200 F / g.

[0123] Example 3

[0124] Raw material preparation: Pine sawdust is used as the biomass raw material, with a moisture content of 25%, a particle size range of 5-20 mm, and a natural bulk density of approximately 200 kg / m³. 3 .

[0125] Step 1: Pine wood chips are continuously fed into the outer cavity of the carbonization section 111 tubes 1111 through the feeding component 3, and slowly move downwards under the action of gravity. Biomass undergoes a drying stage, a dry distillation stage, and a pyrolysis carbonization stage in the outer cavity of the tubes 1111 to generate pyrolysis gas, and the residual solid phase is converted into biochar.

[0126] Step 2: The pyrolyzed gas penetrates the high-temperature biochar layer 22 (1500 mm thick, 900 °C) in the gasification section 2. Under the synergistic effect of adsorption-catalysis through the active sites (—COOH / —OH) on the biochar surface, porous carbon adsorption, and alkali metal catalysis, the tar components are pyrolyzed into small molecule gases such as CH4, CO, and H2, while the wood vinegar is reformed by steam into CO2 and H2O.

[0127] Step 3: The reformed pyrolysis gas flows upward into the inner cavity of tube 1111, transferring heat to the biomass feedstock in the outer cavity of tube 1111, and cooling itself to 135°C.

[0128] Step 4: The biochar generated from carbonization falls into gasification section 2, where it mixes with the pure oxygen-steam mixed gasification agent (O2 / H2O molar ratio 1:2.5, flow rate 3 Nm³). 3 The biomass ( / kg) undergoes a reaction, including partial oxidation and water-gas reaction, to generate crude syngas and maintain the temperature of gasification section 2 at 900℃. The residual solid phase after gasification is ash.

[0129] Step 5: The crude synthesis gas rises and flows through the inner cavity of tube 1111, and after being cooled to 135°C, it is output by gas collection assembly 1212.

[0130] Example 4

[0131] Raw material preparation: Rice husks are used as biomass raw material, with a moisture content of 25%, a particle size range of 1-5 mm, and a natural bulk density of approximately 200 kg / m³. 3 .

[0132] Step 1: Rice husks are continuously fed into the outer cavity of the carbonization section 111 tubes through the feeding component 3, and slowly move downwards under the action of gravity. Biomass undergoes a drying stage, a dry distillation stage, and a pyrolysis carbonization stage in sequence in the outer cavity of the tubes 1111, and the residual solid phase is converted into biocarbon.

[0133] Step 2: The pyrolysis gas penetrates the high-temperature biochar layer 22 (thickness 400 mm, temperature 1250 °C) in the gasification section 2. The biochar surface active sites (—COOH / —OH), porous carbon adsorption, and alkali metal catalysis promote the decomposition of tar and wood vinegar through adsorption-catalysis synergy. The tar components are decomposed into small molecule gases such as CH4, CO, and H2, while the wood vinegar is decomposed into CO2 and H2O through steam reforming.

[0134] Step 3: The reformed pyrolysis gas flows upward into the inner cavity of tube 1111, transferring heat to the biomass feedstock in the outer cavity of tube 1111, and cooling itself to 135°C.

[0135] Step 4: The bio-carbon generated by carbonization falls into gasification section 2 and reacts with the pure oxygen-steam mixed gasification agent (pure oxygen purity ≥99.5%, steam pressure 0.3MPa, O2 / H2O molar ratio 1:3) to generate crude syngas and maintain the temperature of gasification section 2 at 1250℃.

[0136] Step 5: The crude synthesis gas rises and flows through the inner cavity of tube 1111, and after being cooled to 135°C, it is output by gas collection assembly 1212.

[0137] In Example 3, when pine sawdust was used, the syngas composition consisted of 38% H2, 45% CO, 5% CH4, and 12% CO2, with a calorific value of 11.2 MJ / Nm³. 3 Tar content 28mg / Nm 3 The biomass carbon yield was 28%. This result verifies the high efficiency of the gasifier with wood-based raw materials: the total CO+H2 content met the requirements of chemical synthesis (>80%), and the tar content was much lower than that of traditional processes (<50mg / Nm³). 3 The 28% biocarbon yield reflects the sufficiency of the carbonization stage 111.

[0138] In Example 4, when rice husks were used for operation, the syngas contained 42.3% H2, 38.1% CO, and 5.2% CH4, with a calorific value of 11.3 MJ / Nm³. 3 Tar content 32mg / Nm 3 The high-ash raw materials maintain low tar characteristics even at a gasification temperature of 1250℃ and a biochar layer of 400mm. The increased H2 content is due to the increased steam ratio (O2 / H2O = 1:3), which promotes water-gas conversion. The water-cooled grate design effectively avoids slagging.

[0139] This gasifier, through pure oxygen-steam gasification, in-situ catalysis with a high-temperature bio-carbon layer 22, and a self-circulating thermal energy design, can stably output tar <50mg / Nm³ from both wood and agricultural waste. 3 Calorific value > 11 MJ / Nm 3The high-quality syngas systematically solves the shortcomings of traditional processes, such as high tar content, low calorific value, and insufficient energy efficiency.

[0140] Although preferred embodiments of the present application have been described, those skilled in the art, upon learning the basic inventive concept, can make other changes and modifications to these embodiments. Therefore, the appended claims are intended to be interpreted as including the preferred embodiments as well as all changes and modifications falling within the scope of the embodiments of the present application.

[0141] Finally, it should be noted that in this document, relational terms such as "first" and "second" are used only to distinguish one entity or operation from another, and do not necessarily require or imply any such actual relationship or order between these entities or operations. Furthermore, the terms "comprising," "including," or any other variations thereof are intended to cover non-exclusive inclusion, such that a process, method, article, or terminal device that comprises a list of elements includes not only those elements but also other elements not expressly listed, or elements inherent to such a process, method, article, or terminal device. Without further limitations, an element defined by the phrase "comprising one..." does not exclude the presence of other identical elements in the process, method, article, or terminal device that includes said element.

[0142] The above provides a detailed description of a transformer fault monitoring device and its monitoring method provided in this application. Specific examples have been used to illustrate the principles and implementation methods of this application. The description of the above embodiments is only for the purpose of helping to understand the method and core ideas of this application. At the same time, for those skilled in the art, there will be changes in the specific implementation methods and application scope based on the ideas of this application. Therefore, the content of this specification should not be construed as a limitation of this application.

Claims

1. A biomass pyrolysis gas self-heating carbon catalytic reforming gasifier, characterized in that, Includes carbonization section and gasification section, The carbonization segment includes: Multiple tubes are arranged vertically in a triangular ring shape. The outer cavity of each tube is filled with biomass raw material, and the inner cavity of each tube serves as a gas channel. A gas collection assembly for collecting and discharging synthesis gas output from the tube end cavity; The gasification section includes: A grate, located at the bottom of the gasification section; A high-temperature biochar layer is filled above the grate; A nozzle, which is disposed on the grate, is used to introduce a gasifying agent, the gasifying agent including air or air + steam; Ash outlet, located at the bottom of the gasification section, is used to discharge the ash after the reaction.

2. The biomass pyrolysis gas self-heating carbon catalytic reforming gasifier according to claim 1, characterized in that, The gas collection assembly includes an annular gas collection box located at the top of the tube, an annular gas collection pipe connected to the gas collection box, a radially extending main gas guide pipe, and an annular main pipe, wherein the annular main pipe is connected to the synthesis gas outlet.

3. The biomass pyrolysis gas self-heating carbon catalytic reforming gasifier according to claim 1, characterized in that, The diameter of the tubes is 57-133mm, the spacing between adjacent tubes is not less than 3 times the diameter of the biomass raw material particles, the insertion depth of the tubes into the biochar layer is not less than 500mm, and the tubes are made of Q345R-inconel600-625-690 / Haynes233 / Haynes HR-160-alumina / silicon carbide ceramic tubes from low temperature to high temperature, and the total flow cross-sectional area of ​​all tubes accounts for more than 30% of the furnace cross-sectional area.

4. The biomass pyrolysis gas self-heating carbon catalytic reforming gasifier according to claim 1, characterized in that, The thickness of the high-temperature biochar layer is not less than 1000 mm, and the operating temperature is maintained at 800-1200℃.

5. The biomass pyrolysis gas self-heating carbon catalytic reforming gasifier according to claim 1, characterized in that, The grate is a water-cooled structure with an internal circulating water pipe. The two ends of the circulating water pipe are respectively connected to a circulating water inlet pipe and a circulating water outlet pipe located on the furnace wall of the gasification section, and the porosity of the grate is 15-30%.

6. The biomass pyrolysis gas self-heating carbon catalytic reforming gasifier according to claim 1, characterized in that, It also includes the feeding component; The feeding components include a sealed hopper located on the top of the furnace, an airlock fan connected to the outlet of the hopper, and a material inlet extending to the carbonization section.

7. The biomass pyrolysis gas self-heating carbon catalytic reforming gasifier according to claim 1, characterized in that, It also includes fabric components; The fabric component includes a rotatable fabric scraper, a feeder, and a drive motor that drives them to rotate, for uniformly distributing biomass raw materials in the outer cavity of the tube.

8. The biomass pyrolysis gas self-heating carbon catalytic reforming gasifier according to claim 1, characterized in that, It also includes an ash silo, which is connected to the ash outlet. The ash silo is used to collect and temporarily store ash to achieve continuous ash discharge.

9. A method for producing syngas, characterized in that, Includes the following steps: S1. Biomass feedstock moves from top to bottom in the outer cavity of the carbonization section tubes and undergoes drying, dry distillation, pyrolysis and carbonization in sequence to generate biochar and pyrolysis gas. S2. The cracked gas generated in step S1 penetrates the high-temperature biochar layer in the gasification section and undergoes in-situ biochar catalytic reforming at 800-1200℃, causing the tar and wood vinegar to be cracked into small molecule gases. S3. The reformed cracked gas flows in the reverse direction through the inner cavity of the tube and flows upward to provide a heat source for the carbonization section before being cooled and output. S4. Biochar enters the gasification section and reacts with pure oxygen and steam mixed gasification agent to generate crude syngas. S5. The crude syngas flows upward through the inner cavity of the tube and is cooled to 120-150℃ before being output. In step S4, the molar ratio of pure oxygen to steam is 1:1 to 1:

4.

10. A biomass pyrolysis gas self-heating carbon catalytic reforming carbonization activation furnace, characterized in that, Includes carbonization and activation sections. The carbonization segment includes: Multiple tubes are arranged vertically in a triangular ring shape. The outer cavity of each tube is filled with biomass raw material, and the inner cavity of each tube serves as a gas channel. A gas collection assembly for collecting and discharging synthesis gas output from the tube end cavity; The activation segment includes: A spiral blade, the spiral blade being driven by a motor located below the activation section; Carbon removal scraper, which is located at the bottom of the activation section, is used to remove carbon slag from the carbonization activation furnace; A shell-and-tube heat exchanger, wherein the shell-and-tube heat exchanger is disposed outside the activation section; An oxygen-deficient combustion chamber is provided, which is located on the side of the shell-and-tube heat exchanger away from the activation section. Self-heating carbon catalytic reforming carbonization and activation furnace carbonization and activation production method: S21. In the carbonization and activation furnace, the biomass raw material moves from top to bottom in the outer cavity of the carbonization section tubes and undergoes drying, dry distillation, pyrolysis and carbonization treatment in sequence to generate biochar and pyrolysis gas. S22. The cracked gas penetrates downward through the high-temperature biochar layer of the gasification section and undergoes in-situ biochar catalytic reforming at 800-1200℃, causing the tar and wood vinegar to be cracked into small molecule gases. S23. The reformed cracked gas flows in the reverse direction through the inner cavity of the tube and flows upward to provide a heat source for the carbonization section before being cooled and output as syngas. S24. Biochar enters the activation section and reacts with the mixed activator provided by the combustion chamber to generate crude syngas. S25. The crude synthesis gas flows upward through the inner cavity of the tube and is output after cooling.

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