Biomass pyrolysis gas self-heating type carbon catalytic reforming carbonization activation gasification system and biomass pyrolysis gas self-heating type carbon catalytic reforming carbonization activation gasification method

Abstract

The invention provides a biomass pyrolysis gas self-heating type carbon catalytic reforming carbonization activation gasification system and method, and relates to the technical field of catalytic reforming. The system comprises a gasification furnace and at least one carbonization activation furnace. A synthesis gas outlet of the gasification furnace is connected with the dust removal device and the intercooler; a gas outlet of the intercooler is communicated with the pressure swing adsorption device; cO2-rich gas and CO + H2-rich gas are separated by the pressure swing adsorption device and are respectively stored in a first gas storage cabinet and a second gas storage cabinet; proportional valves are arranged at gas outlets of the two gas storage cabinets, and mixed gas entering a smoke cooling balance gas inlet of a combustor of the energy-supply oxygen-deficient combustion chamber is adjusted and introduced into the energy-supply oxygen-deficient combustion chamber of the carbonization activation furnace for cooling; a combustion cracking gas inlet of a combustor of the energy supply oxygen-deficient combustion chamber is communicated with a gas outlet of the intercooler and a gas collecting assembly of the carbonization activation furnace, and a carbon material and clean fuel gas are produced by mixing an activating agent. The system realizes all-component graded utilization of synthesis gas and closed-loop recovery of heat energy, and solves the problems of waste heat waste, large carbon emission and insufficient temperature control precision in the traditional process.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of catalytic reforming, in particular to a biomass pyrolysis gas autothermal carbon catalytic reforming carbonization activation gasification system and method. BACKGROUND

[0002] The traditional biomass gasification and carbonization technology has significant defects. When using a gasification agent to continuously gasify or carbonize in a conventional fixed bed, since the biomass and the gasification agent flow in opposite directions to exchange heat, the water vapor, acetic acid, light tar and heavy tar produced during the drying, pyrolysis and carbonization processes of the biomass in the low temperature zone are carried out of the gasification furnace by the hot gas flow, and after cooling, wood vinegar and tar are formed, which causes blockage of the equipment, pollution of the environment, and reduction of the gas production rate, resulting in waste of resources. The water vapor, acetic acid, light tar and heavy tar carry out a large amount of sensible heat during high-temperature cooling, resulting in waste of heat. The existing gasification or carbonization process cannot solve the problems of pollution control and full utilization of energy. The tar concentration produced by biomass pyrolysis is generally higher than 1 g / Nm 3 , and the acidic components such as wood vinegar need to be additionally provided with a purification device (such as a washing tower and a catalytic cracking reactor) for removal, which not only increases the complexity of the system purification, but also causes the problem of phenolic wastewater treatment. In addition, the heat energy utilization rate of the gasification process is less than 60%, and a large amount of sensible heat is not recovered, which requires external energy to supplement the operating cost.

[0003] Some improved technologies still have limitations. For example, the integrated furnace described in patent CN20241069998.77 attempts to integrate carbonization and gasification functions, but relies on an external waste heat recovery device to realize energy circulation, resulting in a long equipment process, high investment cost, and the problem of system operation complexity and energy consumption is not fundamentally solved. SUMMARY

[0004] In order to overcome the above problems or at least partially solve the above problems, the present application provides a biomass pyrolysis gas autothermal carbon catalytic reforming carbonization activation gasification system, which comprises a gasification furnace and at least one carbonization activation furnace, and further comprises:

[0005] An intercooler, an inlet of the intercooler being in communication with an outlet of the synthesis gas of the gasification furnace;

[0006] A pressure swing adsorption device, an inlet of the pressure swing adsorption device being in communication with an outlet of the intercooler, one outlet of the pressure swing adsorption device being in communication with a first gas storage tank, and the other outlet being in communication with a second gas storage tank, the first gas storage tank being used to store CO2-rich gas, and the second gas storage tank being used to store CO+H2-rich gas;

[0007] The gas outlet of the first gas storage tank and the second gas storage tank is provided with a proportional valve, which is used to adjust the proportion of CO2-rich gas and CO+H2-rich gas, and to pass the mixed gas into the energy supply oxygen-lean combustion chamber burner at the bottom of the carbonization activation furnace as cooling gas;

[0008] The combustion cracking gas inlet of the energy supply oxygen-lean combustion chamber burner is in communication with the gas outlet of the intercooler and the gas collection assembly of the carbonization activation furnace.

[0009] In some embodiments, the carbonization activation furnace comprises a carbonization section and an activation section,

[0010] The carbonization section comprises:

[0011] A plurality of column tubes are vertically arranged and distributed in a triangular ring shape, the outer cavities of the column tubes are used to fill biomass raw materials, and the inner cavities of the column tubes are used as gas passages;

[0012] A gas collection assembly is used to collect and guide the synthesis gas output from the inner cavities of the column tubes;

[0013] The activation section comprises:

[0014] A spiral blade is driven by a motor arranged below the activation section;

[0015] A carbon discharge scraper is arranged at the bottom of the activation section and is used to discharge carbon residue;

[0016] A shell-and-tube heat exchanger is arranged outside the activation section;

[0017] An energy supply oxygen-lean combustion chamber is arranged on the side of the shell-and-tube heat exchanger away from the activation section.

[0018] In some embodiments, the gasification furnace comprises a carbonization section and a gasification section,

[0019] The carbonization section comprises:

[0020] A plurality of column tubes are vertically arranged and distributed in a triangular ring shape, the outer cavities of the column tubes are used to fill biomass raw materials, and the inner cavities of the column tubes are used as gas passages;

[0021] A gas collection assembly is used to collect and guide the synthesis gas output from the inner cavities of the column tubes;

[0022] The gasification section comprises:

[0023] A grate is arranged at the bottom of the gasification section;

[0024] A high-temperature biochar layer is filled above the grate;

[0025] a nozzle disposed on the grate for introducing the gasifying agent;

[0026] an ash outlet at the bottom of the gasification section for discharging the ash.

[0027] In some embodiments, the at least one carbonization activation furnace comprises a first carbonization activation furnace and a second carbonization activation furnace, and the system further comprises:

[0028] a first intercooler, the gas collection assembly of the first carbonization activation furnace being in communication with the gas inlet of the first intercooler;

[0029] a first pressure swing adsorption device, the gas inlet of the first pressure swing adsorption device being in communication with the gas outlet of the first intercooler via a dust removal device, and being in communication with the combustion pyrolysis gas inlet of the energy-supplied oxygen-depleted combustion chamber of the first carbonization activation furnace;

[0030] one gas outlet of the first pressure swing adsorption device being in communication with a first gas storage tank, and the other gas outlet being in communication with a second gas storage tank;

[0031] the gas outlets of the first gas storage tank and the second gas storage tank are each provided with a first proportional valve, the first proportional valve being used to adjust the gas ratio and to introduce the mixed gas into the cooling gas inlet of the energy-supplied oxygen-depleted combustion chamber of the first carbonization activation furnace;

[0032] a CO shift device, the gas inlet of the CO shift device being in communication with the first proportional valve, and being in communication with the syngas outlet of the gasification furnace via a second intercooler, and being in communication with the gas collection assembly of the second carbonization activation furnace via a third intercooler;

[0033] a second pressure swing adsorption device, the gas inlet of the second pressure swing adsorption device being in communication with the gas outlet of the CO shift device;

[0034] one gas outlet of the second pressure swing adsorption device being in communication with a third gas storage tank, and the other gas outlet being in communication with a fourth gas storage tank, the third gas storage tank being used to store CO2-rich gas, and the fourth gas storage tank being used to store H2 gas;

[0035] the gas outlets of the third gas storage tank and the fourth gas storage tank are each provided with a second proportional valve, the second proportional valve being used to adjust the gas ratio and to introduce the mixed gas into the cooling gas inlet of the energy-supplied oxygen-depleted combustion chamber of the second carbonization activation furnace;

[0036] the gas collection assembly of the second carbonization activation furnace being in communication with the combustion pyrolysis gas inlet of the energy-supplied oxygen-depleted combustion chamber.

[0037] In some embodiments, the gasification furnace further comprises an ash bin, the ash bin being in communication with the ash outlet and being used to collect the ash.

[0038] In some embodiments, the diameter of the column pipe is 57-133 mm, the distance between adjacent column pipes is not less than 3 times the diameter of the biomass raw material particles, the depth of the column pipe inserted into the biochar layer is not less than 500 mm, the material of the column pipe from low temperature to high temperature is Q345R-inconel600-625-690 / Haynes233 / Haynes HR-160-alumina / silicon carbide ceramic pipe, and the total flow area of all column pipes accounts for more than 30% of the cross-sectional area of the hearth.

[0039] 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°C.

[0040] In some embodiments, the grate is a water-cooled structure, and a circulating water pipe is arranged inside, both ends of the circulating water pipe are connected to a circulating water inlet pipe and a circulating water outlet pipe arranged on the wall of the gasification section, and the porosity of the grate is 15-30%.

[0041] One or more embodiments of the present application also provide a biomass pyrolysis gas self-heating carbon catalytic reforming carbonization activation gasification production method, comprising the following steps:

[0042] S1, in the gasification furnace, the biomass raw material moves from top to bottom in the outer cavity of the column pipe in the carbonization section, and is sequentially subjected to drying, dry distillation, pyrolysis and carbonization treatment to generate biochar and pyrolysis gas;

[0043] S2, the pyrolysis gas penetrates the high-temperature biochar layer of the gasification section downward, and is subjected to in-situ biochar catalytic reforming at 800-1200°C to crack tar and wood vinegar into small molecule gas;

[0044] S3, the reformed pyrolysis gas flows upward through the inner cavity of the column pipe in the reverse direction, provides heat source for the carbonization section, and outputs the synthesis gas after cooling;

[0045] S4, the biochar enters the gasification section and reacts with the gasification agent to generate crude synthesis gas;

[0046] S5, the crude synthesis gas flows upward through the inner cavity of the column pipe and is output after cooling;

[0047] S6, the output synthesis gas is dusted by a dust removal device and cooled by an intercooler;

[0048] S7, the cooled gas enters a pressure swing adsorption device to be separated into CO2-rich gas and CO+H2-rich gas;

[0049] S8, the CO2-rich gas is stored in a first gas storage tank, and the CO+H2-rich gas is stored in a second gas storage tank;

[0050] S9. Adjust the ratio of CO2-rich gas and CO+H2-rich gas by a proportional valve, and introduce the mixed gas as a cooling gas into the oxygen-deficient combustion chamber burner at the bottom of the carbonization and activation furnace.

[0051] S10, the oxygen-deficient combustion chamber burner receives combustion and cracking gas from the intercooler outlet and the carbonization and activation furnace gas collection assembly for combustion.

[0052] In some embodiments, when the system includes a first carbonization activation furnace and a second carbonization activation furnace, the following steps are further included:

[0053] 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.

[0054] 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.

[0055] S13. The ratio is adjusted by the first proportional valve, and the mixed gas is introduced into the burner of the energy-deficient combustion chamber of the first carbonization and activation furnace for cooling.

[0056] The syngas from S14, the gasifier, and the second carbonization and activation furnace are processed by a CO conversion unit.

[0057] 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.

[0058] S16. The ratio is adjusted by the second proportional valve, and the mixed gas is introduced into the oxygen-deficient combustion chamber burner of the second carbonization and activation furnace for cooling.

[0059] 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. Attached Figure Description

[0060] 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.

[0061] Figure 1 This is a schematic diagram of the structure of a gasifier according to an embodiment of the present invention;

[0062] Figure 2 for Figure 1Cross-sectional view along A-A;

[0063] Figure 3 Structure schematic view of carbonization activation furnace provided for the embodiment of the present application;

[0064] Figure 4 Structure schematic view of biomass pyrolysis gas self-heating carbon catalytic reforming carbonization activation gasification system provided for the embodiment of the present application.

[0065] Figure 5 Structure schematic view of another biomass pyrolysis gas self-heating carbon catalytic reforming carbonization activation gasification system provided for the embodiment of the present application.

[0066] Wherein, the reference signs are: 1, carbonization section; 11, tube bank; 12, gas collection assembly; 121, annular gas collecting tank; 122, annular gas collecting pipe; 123, gas guide main pipe; 124, annular mother pipe; 2, gasification section; 21, grate; 211, circulating water pipe; 212, circulating water inlet pipe; 213, circulating water outlet pipe; 22, high-temperature bio-carbon layer; 23, nozzle; 24, ash outlet; 3, feeding component; 31, sealed bunker; 32, air lock; 33, material inlet; 4, material distribution component; 41, material distribution scraper; 42, material stirrer; 43, driving motor; 5, ash bunker; 6, activation section; 61, spiral blade; 62, carbon discharging scraper; 63, tubular heat exchanger; 64, energy supply oxygen-poor combustion chamber; 641, temperature-reducing 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 shift device; 91, gasification furnace; 92, carbonization activation furnace; 93, first carbonization activation furnace; 94, second carbonization activation furnace. DETAILED DESCRIPTION

[0067] To make the objectives, technical solutions and advantages of the embodiments of the present application clearer, the technical solutions in the embodiments of the present application will be described below in connection with the drawings in the embodiments of the present application. Obviously, the described embodiments are some but not all of the embodiments of the present application. The components of the embodiments of the present application described and shown in the drawings herein can be arranged and designed in various different configurations.

[0068] Figure 1 Structure schematic view of gasification furnace provided for the embodiment of the present application. Figure 2 For Figure 1 Cross-sectional view along A-A.

[0069] As Figure 1 and Figure 2 shown, the embodiment of the present application provides a gasifier, comprising:

[0070] A gasifier, comprising a carbonization section 1 and a gasification section 2,

[0071] The carbonization section 1 comprises:

[0072] A plurality of column tubes 11, the column tubes 11 are vertically arranged and distributed in a ring shape, the outer cavity of the column tubes 11 is filled with biomass raw materials, and the inner cavity of the column tubes 11 serves as a gas passage; the diameter of the column tubes 11 is 57-133mm, and the spacing between adjacent column tubes is not less than 3 times the diameter of the biomass raw material particles

[0073] A gas collection assembly 12, which is used to collect and export the synthesis gas output from the inner cavity of the column tubes 11;

[0074] The gasification section 2 comprises:

[0075] A grate 21 located at the bottom of the gasification section 2;

[0076] A high-temperature biochar layer 22 filled above the grate 21;

[0077] A nozzle 23 provided on the grate 21 for introducing pure oxygen and steam mixed gasification agent;

[0078] An ash outlet 24 located at the bottom of the gasification section 2 for discharging the reacted ash.

[0079] The carbonization section 1 refers to the area in the gasifier where biomass is treated by pyrolysis, which is composed of a plurality of vertically arranged column tubes 11 distributed in a ring shape. The column tubes 11 are tubular structures made of high-temperature-resistant alloy, whose outer cavity contains biomass raw materials and inner cavity serves as a gas flow passage. The diameter of the column tubes 11 is 57-133mm, and the spacing between adjacent column tubes is not less than 3 times the diameter of the biomass raw material particles. The insertion depth of the column tubes 11 into the biochar layer is not less than 500mm. Different materials of the column tubes 11 correspond to 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.

[0080] The gasification section 2 refers to the area in the gasifier where biochar is converted into synthesis gas, located below the carbonization section 1. The grate 21 is a support structure provided at the bottom of the gasification section 2, used to support the biochar layer and distribute the gasification agent. The high-temperature biochar layer 22 is a biochar accumulation layer filled above the grate 21, with a temperature maintained in the catalytic activity range. The nozzle 23 is a spraying device for introducing pure oxygen and steam mixed gasification agent into the gasification section 2.

[0081] The biomass raw material is filled in the outer cavity of the column tube 11 of the carbonization section 1 and moves from top to bottom under the action of gravity. The nozzle 23 of the gasification section 2 introduces the mixed gasification agent of pure oxygen and steam above the grate 21, the gasification agent penetrates the high-temperature biochar layer 22 upwards and reacts with the biochar to generate the crude synthesis gas mainly composed of CO and H2 through partial oxidation reaction (C+O2→CO) and water gas reaction (C+H2O→CO+H2). The high temperature (>1000℃) released by the reaction maintains the heat balance of the gasification section 2.

[0082] The crude synthesis gas carrying high-temperature sensible heat rises to the carbonization section 1 and flows through the inner cavity of the column tube 11. The high-temperature gas indirectly heats the biomass in the outer cavity through the wall of the column tube 11, so that the biomass undergoes drying (removal of moisture at 120-300℃), dry distillation (release of volatile matter at 300-500℃) and carbonization (generation of biochar and cracking gas at 700-800℃) in stages. The cracking gas generated in the carbonization section 1 flows downward under the driving force of pressure and penetrates the high-temperature biochar layer 22 (800-1000℃) of the gasification section 2.

[0083] The role of the high-temperature biochar layer 22 includes:

[0084] 1) Catalytic cracking of tar: the tar components (such as toluene and naphthalene) in the cracking gas contact the active sites (—COOH / —OH and alkali metals) on the surface of the biochar and are cracked into small-molecule gases such as CH4, CO and H2;

[0085] 2) Reforming of wood vinegar: oxygen-containing organic matter (such as acetic acid) is decomposed into CO2 and H2 under high temperature and steam environment;

[0086] 3) Gas-solid separation: the carbon particles that are not completely reacted are intercepted and continue to participate in the gasification reaction.

[0087] 4) The specific surface area of the biochar is greater than 500m2 / g, which adsorbs the vinegar and tar and promotes the purification of the cracking gas.

[0088] 5) The ash of the biomass contains metal ions such as K / Na / Fe, which act as catalysts to reduce the cracking activation energy.

[0089] The tar and wood vinegar are completely decomposed through the synergistic effect of the active sites, void adsorption and alkali metal catalysis.

[0090] The reformed cracking gas is mixed with the crude synthesis gas generated in the gasification section 2 and flows upward in the inner cavity of the column tube 11. The mixed gas transfers heat to the biomass in the outer cavity of the column tube 11 during the upward flow and is cooled to 120-150℃, and is finally collected and output by the gas collection assembly 12. The biochar continuously falls to the gasification section 2 to participate in the reaction, and the residual ash is screened by the grate 21 and discharged from the ash outlet 24, realizing material circulation and energy self-sufficiency.

[0091] By the integrated design of carbonization section 1 and gasification section 2 and the in-situ catalysis of high-temperature biochar layer 22, the pyrolysis gas tar and wood vinegar are directly purified in the furnace, and external purification equipment is saved; at the same time, the high-temperature synthesis gas of gasification section 2 is used to provide heat source for carbonization section 1, heat energy is self-circulated, and the system energy consumption and operation cost are significantly reduced.

[0092] In some embodiments, the gas collection assembly 12 includes an annular gas collection box 121 arranged at the top of the column tube 11, an annular gas collection pipe 122 in communication with the gas collection box, a radially extending gas guide main pipe 123, and an annular mother pipe 124 in communication with the synthesis gas outlet.

[0093] After the synthesis gas rises to the top of the column tube 11, it first enters the annular gas collection box 121 for preliminary collection; then it is guided to the radially extending gas guide main pipe 123 through the annular gas collection pipe 122, and finally it is integrated through the annular mother pipe 124 and then uniformly output by the synthesis gas outlet. Through the multi-stage annular gas collection structure, the flow resistance of the synthesis gas is reduced, local gas flow short circuit is avoided, uniform penetration of the pyrolysis gas through the high-temperature biochar layer 22 is ensured, and the tar catalytic reforming efficiency is improved.

[0094] In some embodiments, the diameter of the column tube 11 is 57-133 mm, the distance between adjacent column tubes 11 is not less than 3 times the diameter of the biomass raw material particles, and the total flow area of all column tubes 11 accounts for more than 30% of the hearth cross-sectional area.

[0095] The column tube 11 with a diameter of 57-133 mm is arranged in a ring shape with a distance not less than 3 times the diameter of the biomass particles, and the total flow area accounts for 30% of the hearth, which ensures smooth rising of the high-temperature synthesis gas in the inner cavity of the column tube 11 for heat transfer, and provides sufficient heating area for the biomass in the outer cavity of the column tube 11. By optimizing the size and layout of the column tube 11, the biomass is uniformly heated in the carbonization section 1, local overheating and coking are avoided, and the pressure difference balance between the gasification section 2 and the carbonization section 1 is maintained.

[0096] The depth of the column tube 11 inserted into the biochar layer is not less than 500 mm.

[0097] In order to improve economic benefits and reduce equipment investment, different materials of the column tube 11 correspond to different temperature zones, and the materials from low temperature to high temperature are Q345R-inconel600-625-690 / Haynes233 / Haynes HR-160-alumina / silicon carbide ceramic tube.

[0098] 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℃.

[0099] The high-temperature biochar layer 22 with a thickness of greater than or equal to 1000 mm forms a porous alkali metal K / Na / Fe catalytic bed at 800-1000°C, and when the cracking gas penetrates downward, the tar components are adsorbed and cracked by the biochar surface active sites (—COOH / —OH) and the nanopores with a specific surface area greater than 500 m2 / g, and the wood vinegar is decomposed in a high-temperature steam environment. Through the synergistic control of the thickness and temperature of the biochar layer, the tar cracking reaction has sufficient residence time, the wood vinegar is nearly completely decomposed, and wastewater discharge is eliminated.

[0100] In some embodiments, the grate 21 is a water-cooled structure, and a circulating water pipe 211 is arranged inside the grate 21, 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 arranged on the furnace wall of the gasification section 2, and the porosity of the grate 21 is 15-30%.

[0101] The circulating water pipe 211 inside the water-cooled grate 21 is connected to an external cooling system through the water inlet / outlet pipes of the furnace wall, and the circulating water continuously carries away the heat of the gasification reaction; the porosity of 15-30% ensures uniform distribution of the gasification agent. Through the design of the water-cooled structure and the porosity, the temperature of the grate 21 can be controlled, the biochar layer is prevented from being slagged and sintered, and the stability of the gasification reaction is maintained.

[0102] In some embodiments, the gasification device further comprises a feeding component 3, the feeding component 3 comprises a sealed material bin 31 arranged on the furnace top, a damper 32 connected to the outlet of the material bin, and a material inlet 33 extending to the carbonization section 1.

[0103] In some embodiments, the gasification device further comprises a material distributing component 4, the material distributing component 4 comprises a rotatable material distributing scraper 41, a material shifter 42, and a driving motor 43 driving the rotation of the material distributing scraper 41 and the material shifter 42, which are used to uniformly distribute the biomass raw material in the outer cavity of the tube bank 11.

[0104] The driving motor 43 drives the rotation of the material distributing scraper 41 and the material shifter 42, so that the biomass raw material input through the material inlet 33 is uniformly spread in the outer cavity of the tube bank 11, avoiding local accumulation or bridging. Through the forced dispersion effect of the mechanical material distributing component 4, the heating area of the biomass in the carbonization section 1 is maximized, and the fluctuation of the cracking gas yield caused by uneven dry distillation carbonization is eliminated.

[0105] In some embodiments, the gasification device further comprises an ash bin 5, the ash bin 5 is in communication with the ash outlet 24, and the ash bin 5 is used to collect and temporarily store the ash and slag, realizing continuous ash discharge.

[0106] Further, the gasification agent can be replaced by air, air+steam, oxygen-rich+steam, to adapt to different heat values and uses of the fuel gas.

[0107] Further, the gasification section can be replaced by an activation section to form a carbonization and activation integrated furnace, producing porous carbon and negative electrode materials.

[0108] The biomass raw material is temporarily stored in the sealed bin 31 of the feeding component 3, and enters the outer cavity of the column tube 11 of the carbonization section 1 through the material inlet 33 after being controlled by the airlock 32. The driving motor 43 of the distributing component 4 drives the distributing scraper 41 and the material shifter 42 to rotate, so that the raw material is uniformly distributed in the outer cavity of the column tube 11. The raw material moves from top to bottom under the action of gravity and sequentially undergoes drying, dry distillation, cracking and carbonization. In the drying stage, water is removed at 120-300 DEG C, and the heat comes from the high-temperature gas rising in the inner cavity of the column tube 11; in the dry distillation stage, volatile components are released to generate cracking gas at 300-500 DEG C; in the carbonization stage, biochar is generated at 700-800 DEG C.

[0109] The generated cracking gas penetrates the high-temperature biochar layer 22 (thickness ≥ 1000 mm, temperature 800-1000 DEG C) of the gasification section 2 downward. Under the synergistic effect of adsorption and catalysis, the tar and wood vinegar are decomposed into CH4 / CO / H2 and CO2 / H2O, respectively, through the adsorption-catalysis synergistic effect of the active sites (—COOH / —OH) on the surface of the biochar, the porous adsorption and the alkali metal catalysis. The reformed gas flows upward through the inner cavity of the column tube 11 in a reverse direction, cools to 120-150 DEG C after supplying heat to the carbonization section 1, and then is output.

[0110] At the same time, the biochar falls onto the top of the grate 21 (water-cooled structure, porosity 15-30%) of the gasification section 2. The mixed gasification agent (O2 / H2O molar ratio 1:1-1:4) of pure oxygen and steam is introduced into the grate 21 through the nozzle 23, and reacts with the biochar to generate the crude synthesis gas (CO+H2≥85%) through partial oxidation (C+O2→CO) and water gas reaction (C+H2O→CO+H2). The crude synthesis gas rises into the inner cavity of the column tube 11 and is mixed with the reformed cracking gas and then is output. The residual ash is screened by the grate 21 and then is discharged into the ash bin 5 through the ash outlet 24.

[0111] Figure 3 A structure schematic diagram of a carbonization and activation furnace 92 provided by the embodiment of the present application is shown.

[0112] As shown in Figure 3 the embodiment of the present application further provides a carbonization and activation furnace 92, which comprises a carbonization section 11 and an activation section 6,

[0113] The carbonization section 11 comprises:

[0114] a plurality of column tubes 11, the column tubes 11 are vertically arranged and are distributed in a triangular ring shape, the outer cavity of the column tube 11 is filled with biomass raw material, and the inner cavity of the column tube 11 is used as a gas passage;

[0115] a gas collection assembly 12, which is used to collect and guide the synthesis gas output from the inner cavity of the column tube 11;

[0116] The activation section 6 comprises:

[0117] Spiral blades 61 driven by a motor arranged below the activation section 6;

[0118] Carbon discharge scraper 62 arranged at the bottom of the activation section 6 to discharge carbon residues in the carbonization activation furnace;

[0119] Tube-shell heat exchanger 63 arranged outside the activation section 6;

[0120] Energy supply lean oxygen combustion chamber 64 arranged on the side of the tube-shell heat exchanger 63 away from the activation section 6.

[0121] In some embodiments, the energy supply lean oxygen combustion chamber 64 is provided with three inlets, namely a cooling gas inlet 641, a combustion pyrolysis gas inlet 642, and a combustion-supporting gas inlet 643.

[0122] In some embodiments, the carbonization section 11 of the carbonization activation furnace 92 is completely identical in structure to the carbonization section 11 of the gasification furnace 91.

[0123] The biomass pyrolysis gas autothermal carbon catalytic reforming carbonization activation furnace is used to produce porous carbon and negative electrode materials.

[0124] Figure 4 A structural schematic diagram of a biomass pyrolysis gas autothermal carbon catalytic reforming carbonization activation gasification system is provided for the embodiments of the present application.

[0125] As shown in the accompanying drawings, Figure 4 The embodiments of the present application also provide a biomass pyrolysis gas autothermal carbon catalytic reforming carbonization activation gasification system, which comprises a gasification furnace 91 and a carbonization activation furnace 92, and further comprises:

[0126] An intercooler 7, whose gas inlet is in communication with the syngas outlet of the gasification furnace 91;

[0127] A pressure swing adsorption device 81, whose gas inlet is in communication with the gas outlet of the intercooler 7, one gas outlet of the pressure swing adsorption device 81 is in communication with a first gas storage tank 821, and the other gas outlet is in communication with a second gas storage tank 822, the first gas storage tank 821 is used to store CO2-rich gas, and the second gas storage tank 822 is used to store CO+H2-rich gas;

[0128] Proportional valves 83 are arranged at the gas outlets of the first gas storage tank 821 and the second gas storage tank 822, the proportional valves 83 are used to adjust the proportion of CO2-rich gas and CO+H2-rich gas, and the mixed gas is used as cooling gas and is introduced into the energy supply lean oxygen combustion chamber 64 at the bottom of the carbonization activation furnace 92;

[0129] The combustion cracking gas inlet 642 of the energy supply oxygen-depleted combustion chamber combustor is in communication with the gas outlet of the intercooler 7 and the gas collection assembly 12 of the carbonization activation furnace 92.

[0130] One or more embodiments of the present application also provide a biomass cracking gas autothermal carbon catalytic reforming carbonization activation gasification method, which is applied to Figure 4 The system comprises the following steps:

[0131] S1, in the gasifier, the biomass raw material moves from top to bottom in the outer cavity of the column pipe in the carbonization section, and is sequentially subjected to drying, dry distillation, cracking and carbonization treatment to generate biochar and cracking gas;

[0132] S2, the cracking gas penetrates the high-temperature biochar layer of the gasification section downward, and is subjected to in-situ biochar catalytic reforming at 800-1200℃ to crack tar and wood vinegar into small molecule gas;

[0133] S3, the reformed cracking gas flows upward through the inner cavity of the column pipe in the reverse direction, provides heat source for the carbonization section, and outputs the synthesis gas after cooling;

[0134] S4, the biochar enters the gasification section and reacts with the gasification agent to generate crude synthesis gas;

[0135] S5, the crude synthesis gas flows upward through the inner cavity of the column pipe and is output after cooling;

[0136] S6, the output synthesis gas is dusted by a dust removal device and cooled by an intercooler;

[0137] S7, the cooled gas enters a pressure swing adsorption device to be separated into CO2-rich gas and CO+H2-rich gas;

[0138] S8, the CO2-rich gas is stored in a first gas storage tank, and the CO+H2-rich gas is stored in a second gas storage tank;

[0139] S9, the proportion of the CO2-rich gas and the CO+H2-rich gas is adjusted by a proportional valve, and the mixed gas is introduced into the energy supply oxygen-depleted combustion chamber combustor at the bottom of the carbonization activation furnace as a cooling gas;

[0140] S10, the energy supply oxygen-depleted combustion chamber combustor receives the combustion cracking gas from the gas outlet of the intercooler and the gas collection assembly of the carbonization activation furnace for combustion.

[0141] The high-temperature synthesis gas output by the gasifier is cooled by the intercooler and then enters the pressure swing adsorption device, and is separated into CO2-rich gas and CO+H2-rich gas, which are stored in the first and second gas storage tanks respectively; the proportion of the two gases is dynamically adjusted by the proportional valve to form a mixed cooling gas with specific components, which is introduced into the energy supply lean oxygen combustion chamber burner at the bottom of the carbonization and activation furnace; at the same time, the combustion and cracking gas inlet of the energy supply lean oxygen combustion chamber burner receives the remaining gas from the gas outlet of the intercooler and the cracking gas produced by the carbonization and activation furnace, and burns in a lean oxygen environment to release heat and provide heat for the carbonization and activation process.

[0142] By means of full-component staged utilization of synthesis gas and closed-loop regulation, the waste heat (high-temperature synthesis gas) of the gasifier is converted into an effective heat source for the carbonization and activation furnace, and external heating equipment is saved; the CO2-rich gas participates in lean oxygen combustion as a diluent, the combustion temperature is accurately controlled to avoid over-burning in the activation section, and at the same time, direct CO2 emission is eliminated, thereby achieving the synergy of system energy efficiency improvement and carbon emission reduction.

[0143] Figure 5 Another structure schematic diagram of a biomass cracking gas self-heating type carbon catalytic reforming carbonization and activation gasification system is provided.

[0144] As shown in Figure 5 Another biomass cracking gas self-heating type carbon catalytic reforming carbonization and activation gasification system is provided, which comprises a gasifier 91 and a carbonization and activation furnace 92, the carbonization and activation furnace 92 comprises a first carbonization and activation furnace 93 and a second carbonization and activation furnace 94, and the biomass cracking gas self-heating type carbon catalytic reforming carbonization and activation gasification system further comprises:

[0145] A first pressure swing adsorption device 811, the gas collection assembly 12 of the first carbonization and activation furnace 93 is communicated with the gas inlet of the first pressure swing adsorption device 811, the combustion and cracking gas inlet 642 of the energy supply lean oxygen combustion chamber burner of the first carbonization and activation furnace 93 through a dust removal device 74 and a first intercooler 71; one gas outlet of the first pressure swing adsorption device 811 is communicated with a first gas storage tank 821, and the other gas outlet is communicated with a second gas storage tank 822, the first gas storage tank 821 is used to store CO2-rich gas, and the second gas storage tank 822 is used to store CO+H2-rich gas; the gas outlets of the first gas storage tank 821 and the second gas storage tank 822 are respectively provided with a first proportional valve 83, and the first proportional valve 83 is communicated with the cooling gas inlet 641 of the energy supply lean oxygen combustion chamber 64 of the first carbonization and activation furnace 93;

[0146] A CO shift device 84, the gas inlet of the CO shift device 84 is communicated with the first proportional valve 83, the gas inlet of the CO shift device 84 is communicated with the synthesis gas outlet of the gasifier 91 through a second intercooler 72, and the gas inlet of the CO shift device 84 is communicated with the synthesis gas outlet of the carbonization and activation furnace 92 through a third intercooler 73.

[0147] a second pressure swing adsorption device 812, an air inlet of the second pressure swing adsorption device 812 is communicated with an air outlet of the CO shift device 84, one air outlet of the second pressure swing adsorption device 812 is communicated with a third gas storage tank 823, and the other air outlet is communicated with a fourth gas storage tank 824, the third gas storage tank 823 is used to store CO2-rich gas, and the fourth gas storage tank 824 is used to store H2; the air outlets of the third gas storage tank 823 and the fourth gas storage tank 824 are respectively provided with a second proportional valve 83, and the second proportional valve 83 is communicated with the cooling gas inlet 641 of the energy supply oxygen-depleted combustion chamber 64 of the second carbonization activation furnace 94;

[0148] the gas collection assembly 12 of the second carbonization activation furnace 94 is communicated with the combustion pyrolysis gas inlet 642 of the energy supply oxygen-depleted combustion chamber burner.

[0149] When the carbonization activation furnace 92 includes the first carbonization activation furnace 93 and the second carbonization activation furnace 94, the biomass pyrolysis gas autothermal carbon catalytic reforming carbonization activation gasification method is applied to Figure 5 In addition to steps S1-S10, the system further includes the following steps:

[0150] S11, after the gas generated by the first carbonization activation furnace is cooled by the first intercooler, part of the gas enters the first pressure swing adsorption device for separation, and the other part enters the energy supply oxygen-depleted combustion chamber;

[0151] 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;

[0152] S13, the mixed gas is introduced into the energy supply oxygen-depleted combustion chamber burner of the first carbonization activation furnace for cooling by adjusting the proportion through the first proportional valve;

[0153] S14, the synthesis gas of the gasification furnace and the second carbonization activation furnace is treated by the CO shift device;

[0154] S15, the gas after CO shift 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;

[0155] S16, the mixed gas is introduced into the energy supply oxygen-depleted combustion chamber burner of the second carbonization activation furnace for cooling by adjusting the proportion through the second proportional valve.

[0156] In some embodiments, the following steps are further included:

[0157] S17, the combustion pyrolysis gas pure oxygen combustion-supporting combustion flue gas is used to balance the CO2 / CO+H2 cooling flue gas to produce carbon materials as activators.

[0158] 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 part is directly fed into the oxygen-deficient combustion chamber burner powered by the furnace itself. A first proportional valve adjusts the gas ratio between the two gas storage tanks, and the mixture is then fed into the oxygen-deficient combustion chamber burner 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 into CO2-rich gas (stored in the third gas storage tank) and high-purity H2 (stored in the fourth gas storage tank) by a second pressure swing adsorption unit. A second proportional valve adjusts the gas ratio between the two gases, and the mixture is then fed into the oxygen-deficient combustion chamber burner of the second carbonization activation furnace.

[0159] 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.

[0160] In some embodiments, the porous carbon material may be air-purifying activated carbon, supercapacitor carbon, medical slow-release carbon, or hard carbon.

[0161] Example 1: First, bamboo is cut, dried, and crushed, then fed into a self-heating carbon catalytic reforming furnace for carbonization activation. Carbonization activation is 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 energy, and 60% is cooled by an intercooler to obtain purified gas. This purified gas is then separated into CO2-rich gas 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 introduced 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%.

[0162] Example 2, the broken dry bamboo particles are sent into a self-heating carbon catalytic reforming carbonization activation furnace (850℃ activation for 240 minutes) to produce pyrolysis carbonization activation gas and carbon-based materials. After the carbonization activation gas (CO 37%, H2 22%, CH4 13%, CO2 28%) is dedusted by a dedusting device, 40% of the carbonization activation gas is used for combustion to provide energy, and 60% of the carbonization activation gas is cooled by an intercooler. The carbonization activation gas is separated by a PSA into 92% CO2-rich oxidation gas and ≥85% CO+H2-rich reduction gas; the CO2-rich gas is combusted in a combustion chamber at 2000℃ with part of the fuel gas and pure oxygen, and superheated steam (450℃) is added to form 850℃ activation flue gas (CO2:H2O=5:1), which is introduced into the activation furnace to maintain a temperature of 240 minutes, and the pore size distribution is controlled by adjusting the gas ratio by an online mass spectrometer (micropores >90%), to obtain supercapacitor carbon, with a specific surface area of 2000-2500m2 / g, an iodine value of 1400-1600mg / g, an electrical conductivity of ≥10S / cm, and an organic capacitance of ≥200F / g.

[0163] Example 3

[0164] Raw material preparation: pine sawdust is used as the biomass raw material, with a moisture content of 25%, a particle size range of 5-20mm, and a natural bulk density of about 200kg / m 3 .

[0165] Step one: the pine sawdust is continuously input into the carbonization section 111 through the feeding component 3 and slowly moves downward under the action of gravity in the outer cavity of the column tube 1111. The biomass successively experiences a drying stage, a dry distillation stage and a pyrolysis carbonization stage in the outer cavity of the column tube 1111 to generate pyrolysis gas, and the residual solid phase is converted into biochar.

[0166] Step two: the pyrolysis gas penetrates through the high-temperature biochar layer 22 (thickness 1500mm, temperature 900℃) of the gasification section 2. Under the synergistic effect of adsorption and catalysis by the active sites (—COOH / —OH) on the surface of the biochar, the porous carbon adsorption and the alkali metal catalysis, the tar components are decomposed into small molecule gases such as CH4, CO and H2, and the wood vinegar is decomposed into CO2 and H2O by steam reforming.

[0167] Step three: the reformed pyrolysis gas reversely enters the inner cavity of the column tube 1111 and flows upward, transferring heat to the biomass raw material in the outer cavity of the column tube 1111 and cooling itself to 135℃.

[0168] Step four: the biochar generated by carbonization falls into the gasification section 2 and reacts with the pure oxygen-steam mixed gasification agent (O2 / H2O molar ratio 1:2.5, flow rate 3Nm 3 / kg of biomass) introduced, including partial oxidation reaction and water gas reaction, to generate raw synthesis gas and maintain the temperature of the gasification section 2 at 900℃, and the residual solid phase after gasification is ash.

[0169] Step five, the crude synthesis gas rising through the column tube 1111 cavity, cooled to 135 ℃ by gas collection components 1212 output.

[0170] Example 4

[0171] Raw material preparation: rice husk as biomass raw material, moisture content of 25%, particle size range 1-5mm, natural bulk density of about 200kg / m 3 .

[0172] Step one, the rice husk through the feed component 3 continuous input carbonization section 111 column tube 1111 cavity, under the action of gravity slowly down. Biomass in the column tube 1111 cavity in turn through the drying stage, dry distillation stage and pyrolysis carbonization stage, the residual solid phase into biochar.

[0173] Step two, the pyrolysis gas through the gasification section 2 high temperature biochar layer 22 (thickness 400mm, temperature 1250℃). In the biochar surface active site (—COOH / —OH), porous carbon adsorption and alkali metal catalyst through the adsorption-catalysis synergistic effect to promote the decomposition of tar and wood vinegar, tar components are cracked into CH4, CO, H2 and other small molecule gas, wood vinegar is decomposed into CO2 and H2O by steam reforming.

[0174] Step three, the reformed pyrolysis gas reversely into the column tube 1111 cavity upward flow, the heat transfer to the biomass raw material in the column tube 1111 cavity, itself cooled to 135℃.

[0175] Step four, the carbonization generated biochar into the gasification section 2, with the pure oxygen-steam mixed gasification agent (pure oxygen purity ≥ 99.5%, steam pressure 0.3MPa, O2 / H2O molar ratio 1:3) to occur including partial oxidation reaction and water gas reaction, generate crude synthesis gas and maintain the temperature of the gasification section 2 1250℃.

[0176] Step five, the crude synthesis gas rising through the column tube 1111 cavity, cooled to 135 ℃ by gas collection components 1212 output.

[0177] In example 3, when using pine sawdust, the synthesis gas components H2 accounted for 38%, CO accounted for 45%, CH4 accounted for 5%, CO2 accounted for 12%, the heat value reached 11.2MJ / Nm 3 , tar content 28mg / Nm 3 , biochar yield 28%; the results verify the efficiency of the gasifier under the wood raw material: CO+H2 total amount of 83% to meet the chemical synthesis demand (>80%), tar content is far lower than the traditional process (<50mg / Nm 3 ), 28% biochar yield embodies the conversion of carbonization section 111.

[0178] In Example 4, when rice husk was used, the H2 content in the synthesis gas was 42.3%, the CO content was 38.1%, the CH4 content was 5.2%, the heat value was 11.3 MJ / Nm 3 , the tar content was 32 mg / Nm 3 ; the high-ash raw material still had low tar properties at a gasification temperature of 1250 DEG C and under a 400 mm biochar layer, and the H2 content was increased due to the increased steam ratio (O2 / H2O = 1:3) to promote water gas shift, and the grate 21 was water-cooled to effectively avoid slagging.

[0179] The gasifier can stably output high-quality synthesis gas with a tar content < 50 mg / Nm 3 and a heat value > 11 MJ / Nm 3 for wood / agricultural waste through pure oxygen-steam gasification, in-situ catalysis by a high-temperature biochar layer 22, and heat energy self-circulation design, and systematically solves the defects of high tar and low heat value and insufficient energy efficiency in traditional processes.

[0180] Although the preferred embodiments of the present application have been described, those skilled in the art who understand the basic inventive concept can make additional changes and modifications to the embodiments. Therefore, the appended claims are intended to include the preferred embodiments and all changes and modifications falling within the scope of the embodiments of the present application.

[0181] Finally, it should also be noted that, in this text, 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. Moreover, the terms "comprise", "contain" or any other variant thereof are intended to cover non-exclusive inclusion, so that a process, method, article or terminal device including a series of elements not only includes those elements, but also includes other elements not explicitly listed or inherent to such a process, method, article or terminal device. Without more limitations, the element defined by the statement "comprises a" does not exclude the presence of additional identical elements in the process, method, article or terminal device including the element.

[0182] The above provides a kind of transformer fault monitoring device and monitoring method thereof provided by the present application, specific examples are applied in this paper to explain the principle and implementation mode of the present application, the above example is only used to help understand the method of the present application and its core idea;For those skilled in the art, according to the idea of the present application, there will be changes in specific implementation mode and application range, and the above description should not be understood as limiting the present application.

Claims

1. A biomass pyrolysis gas self-heating carbon catalytic reforming carbonization activation gasification system, characterized in that, It includes a gasifier and at least one carbonization activation furnace, and also includes: An intercooler, wherein the air inlet of the intercooler is connected to the syngas outlet of the gasifier; The pressure swing adsorption device has an inlet connected to the outlet of the intercooler. One outlet of the pressure swing adsorption device is connected to a first gas storage tank, and the other outlet is connected to a second gas storage tank. The first gas storage tank is used to store CO2-rich gas, and the second gas storage tank is used to store CO+H2-rich gas. Both the first and second gas storage tanks are equipped with proportional valves at their outlets. The proportional valves are used to adjust the ratio of CO2-rich gas and CO+H2-rich gas, and to introduce the mixed gas as a cooling gas into the oxygen-deficient combustion chamber burner at the bottom of the carbonization and activation furnace. The combustion pyrolysis gas inlet of the oxygen-deficient combustion chamber burner is connected to the gas outlet of the intercooler and the gas collection assembly of the carbonization activation furnace. The mixed flue gas is used as an activator to produce carbon materials.

2. The biomass pyrolysis gas self-heating carbon catalytic reforming carbonization activation gasification system according to claim 1, characterized in that, The carbonization and activation furnace includes a carbonization section and an activation section. The carbonization segment includes: Multiple tubes are arranged vertically in a triangular ring shape. The outer cavity of each tube is used to fill biomass raw materials, and the inner cavity of each tube serves as a gas passage. A gas collection assembly for collecting and exporting synthesis gas output from the tube cavity; The activation segment includes: A spiral blade, the spiral blade being driven by a motor located below the activation section; A carbon removal scraper, located at the bottom of the activation section, is used to remove carbon residue; 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.

3. The biomass pyrolysis gas self-heating carbon catalytic reforming carbonization activation gasification system according to claim 1, characterized in that, The gasifier includes a carbonization section and a gasification section. The carbonization segment includes: Multiple tubes are arranged vertically in a triangular ring shape. The outer cavity of each tube is used to fill biomass raw materials, and the inner cavity of each tube serves as a gas passage. A gas collection assembly for collecting and exporting synthesis gas output from the tube 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; Ash outlet, located at the bottom of the gasification section, is used to discharge ash.

4. The biomass pyrolysis gas self-heating carbon catalytic reforming carbonization activation gasification system according to claim 1, characterized in that, The at least one carbonization activation furnace includes a first carbonization activation furnace and a second carbonization activation furnace, and the system further includes: The first intercooler, the gas collection component of the first carbonization activation furnace is connected to the air inlet of the first intercooler; The first pressure swing adsorption device has its inlet connected to the outlet of the first intercooler via a dust removal device, and is also connected to the combustion pyrolysis gas inlet of the oxygen-deficient combustion chamber burner of the first carbonization activation furnace. One outlet of the first pressure swing adsorption device is connected to the first gas storage tank, and the other outlet is connected to the second gas storage tank. Both the first gas storage tank and the second gas storage tank are equipped with a first proportional valve at their outlets. The first proportional valve is used to adjust the gas ratio and to introduce the mixed gas into the cooling gas inlet of the energy-supplied oxygen-deficient combustion chamber burner of the first carbonization and activation furnace. The CO conversion device has an air inlet connected to the first proportional valve, and is connected to the syngas outlet of the gasifier through the second intercooler, and is connected to the gas collection assembly of the second carbonization activation furnace through the third intercooler. The second pressure swing adsorption device has its inlet connected to the outlet of the CO conversion device. One of the gas outlets of the second pressure swing adsorption device is connected to the third gas storage tank, and the other gas outlet is connected to the fourth gas storage tank. The third gas storage tank is used to store CO2-rich gas, and the fourth gas storage tank is used to store H2 gas. The outlets of the third and fourth gas storage tanks are each equipped with a second proportional valve. The second proportional valve is used to adjust the gas ratio and to introduce the mixed gas into the cooling gas inlet of the oxygen-deficient combustion chamber burner of the second carbonization and activation furnace. The gas collection assembly of the second carbonization activation furnace is connected to the burner combustion pyrolysis gas inlet of the oxygen-deficient combustion chamber.

5. The biomass pyrolysis gas self-heating carbon catalytic reforming carbonization activation gasification system according to claim 3, characterized in that, The gasifier also includes an ash silo, which is connected to an ash outlet for collecting ash.

6. The biomass pyrolysis gas self-heating carbon catalytic reforming carbonization activation gasification system according to claim 3, 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 / Haynes 233 / 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.

7. The biomass pyrolysis gas self-heating carbon catalytic reforming carbonization activation gasification system according to claim 3, 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℃.

8. The biomass pyrolysis gas self-heating carbon catalytic reforming carbonization activation gasification system according to claim 3, 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%.

9. A method for self-heating carbon catalytic reforming carbonization activation gasification of biomass pyrolysis gas, characterized in that, Includes the following steps: 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. 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. 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. S4. Biochar enters the gasification section and reacts with the gasification agent to generate crude syngas. S5. The crude syngas flows upward through the inner cavity of the tube and is output after cooling. S6. The output synthesis gas is purged by a dust removal device and cooled by an intercooler. S7. The cooled gas enters the pressure swing adsorption device and is separated into CO2-rich gas and CO+H2-rich gas. 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. S9. Adjust the ratio of CO2-rich gas and CO+H2-rich gas by a proportional valve, and introduce the mixed gas as a cooling gas into the oxygen-deficient combustion chamber burner at the bottom of the carbonization and activation furnace. S10, the oxygen-deficient combustion chamber burner receives combustion and cracking gas from the intercooler outlet and the carbonization and activation furnace gas collection assembly for combustion.

10. The method for self-heating carbon catalytic reforming carbonization activation gasification of biomass pyrolysis gas according to claim 9, characterized in that, When the system includes a first carbonization activation furnace and a second carbonization activation furnace, the following steps are also included: 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. 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. S13. The ratio is adjusted by the first proportional valve, and the mixed gas is introduced into the burner of the energy-deficient combustion chamber of the first carbonization and activation furnace for cooling. The syngas from S14, the gasifier, and the second carbonization and activation furnace are processed by a CO conversion unit. 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. S16. The ratio is adjusted by the second proportional valve, and the mixed gas is introduced into the oxygen-deficient combustion chamber burner of the second carbonization and activation furnace for cooling.

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