Biomass carbonization and pyrolysis gasification reaction device

Abstract

The invention provides a biomass carbonization and pyrolysis gasification reaction device, which comprises a carbonization unit, a gasification unit and a chilling unit, and is characterized in that the carbonization unit comprises a pyrolysis gas channel and a carbonization channel which are adjacently arranged in parallel; the gasification unit comprises a gasification chamber, a synthesis gas cooling section arranged at the top of the gasification chamber, a pyrolysis gas input section arranged in the middle of the gasification chamber, and a biomass carbon powder input section and an oxygen input section which are arranged at the bottom of the gasification chamber; a pyrolysis gas outlet in the top of the gasification chamber is communicated with a gas inlet of the pyrolysis gas channel, and the carbonization channel is communicated with the pyrolysis gas input section, so that a pyrolysis gas circulation channel is formed between the carbonization unit and the gasification unit; a carbon powder outlet of the carbonization channel is communicated with the biomass carbon powder input section, and the bottom of the gasification chamber is in butt joint with the top of the chilling unit. The method has the advantages of improving the energy utilization rate, improving the synthesis gas quality and the like.

Description

Technical Field

[0001] This invention relates to the field of biomass energy conversion technology, and in particular to a biomass carbonization and pyrolysis gasification reaction device. Background Technology

[0002] With the development of biomass energy utilization technology, biomass pyrolysis, carbonization, and gasification are the core technological pathways for realizing the resource conversion of biomass. Currently, biomass pyrolysis and gasification equipment typically falls into two categories: 1. Separate equipment: The pyrolysis and carbonization unit and the gasification unit are independent of each other, connected by pipelines to transport materials and gases. The separate design requires the high-temperature pyrolysis gas (usually 300-500℃) generated by pyrolysis and carbonization to be transported to the gasification unit or other utilization equipment through long-distance pipelines. This results in a large amount of heat loss of the 400℃ high-temperature pyrolysis gas generated by carbonization during pipeline transportation, and some combustible components in the pyrolysis gas do not fully participate in the reaction. The thermal and chemical energy of the pyrolysis gas is not fully utilized, resulting in low energy utilization (less than 60%).

[0003] II. The simple integrated device that physically integrates two units shortens the material transport path, but it has the following problems: (1) The pyrolysis gas flow path does not form a closed loop circulation system or a structured collaboration, so the pyrolysis gas cannot be recycled. Some of the pyrolysis gas that does not participate in the reaction is directly discharged or inefficiently burned, which causes energy loss and environmental risks. (2) There is no independent channel or heat insulation measures inside the pyrolysis carbonization unit. The pyrolysis gas flow channel is in direct contact with the biomass carbonization channel. Heat crosstalk causes fluctuations in carbonization temperature and unstable pyrolysis gas composition, which in turn affects the efficiency of subsequent gasification reaction. The pyrolysis temperature is difficult to control accurately and affects the stability of the reaction. (3) The gasification chamber has a single gas inlet layout. The carbon powder, oxygen and pyrolysis gas are not mixed evenly, resulting in incomplete gasification reaction and low content of effective components in syngas. (4) The quenching component uses a single cooling medium. Its cooling efficiency is low and the cooling rate is slow. Ash and slag are easy to stick and block the pipes, affecting the continuous operation of the device. Summary of the Invention

[0004] The technical problem to be solved by the present invention is to overcome the shortcomings of the prior art and provide a biomass carbonization and pyrolysis gasification reaction device that improves energy utilization and syngas quality.

[0005] To solve the above-mentioned technical problems, the technical solution proposed by this invention is as follows: A biomass carbonization and pyrolysis gasification reactor includes a carbonization unit, a gasification unit, and a quenching unit. The carbonization unit comprises a pyrolysis gas channel and a carbonization channel arranged adjacent to each other in parallel. The gasification unit includes a gasification chamber, a syngas cooling section at the top of the gasification chamber, a pyrolysis gas input section in the middle of the gasification chamber, a biomass carbon powder input section at the bottom of the gasification chamber, and an oxygen input section. The pyrolysis gas outlet at the top of the gasification chamber is connected to the inlet of the pyrolysis gas channel, and the carbonization channel is connected to the pyrolysis gas input section, forming a pyrolysis gas circulation channel between the carbonization unit and the gasification unit. The carbon powder outlet of the carbonization channel is connected to the biomass carbon powder input section, and the bottom of the gasification chamber is connected to the top of the quenching unit.

[0006] As a further improvement to the above technical solution: The syngas cooling section includes a syngas cooling ring that runs through the side wall of the gasification chamber. The input end of the syngas cooling section is connected to a cooling gas input channel for providing low-temperature syngas. The temperature of the syngas after quenching is 800-900℃, so that the syngas produced by gasification is cooled to below the ash melting point of biomass. The output end of the syngas cooling section is provided with a cooling gas nozzle that is inclined downwards.

[0007] The syngas cooling section further includes a gas ring channel and multiple guide vanes. The cooling gas input channel is connected to the outside of the gas ring channel. There are multiple cooling gas nozzles, which are evenly arranged along the inner circumference of the gas ring channel and connected to the gas ring channel. The guide vanes are arranged between adjacent cooling gas nozzles and are arranged parallel to the cooling gas nozzles.

[0008] The biomass carbon powder input section and the oxygen input section are located in the same plane of the gasification chamber. The biomass carbon powder input section and the oxygen input section are multiple syngas input channels arranged side by side. The syngas input channels and the pyrolysis gas input section are evenly distributed along the outer periphery of the gasification chamber. The biomass carbon powder input section and the pyrolysis gas input section are equipped with spiral nozzles with an upward tilt angle to form an upward jetting swirling flow field.

[0009] The carbonization unit also includes a heat exchange baffle plate disposed between the carbonization channel and the pyrolysis gas channel. The pyrolysis gas channel is located in the middle of the carbonization channel and the two are arranged concentrically. The conveying directions of the pyrolysis gas channel and the carbonization channel are the same.

[0010] The carbonization unit also includes multiple screen plates with varying angles. The multiple screen plates are arranged in an inclined and staggered manner along the length of the carbonization channel. The screen plates are provided with through-holes. The inclination angle of the screen plates gradually increases along the conveying direction of the carbonization channel to form a curved drying carbonization channel that slows down the falling speed of the raw materials. A fluidization separation zone with screen plates arranged in parallel is provided below the curved drying carbonization channel.

[0011] Along the conveying direction of the carbonization channel, the aperture of the screen holes gradually decreases.

[0012] The carbonization unit also includes a carbonization furnace. At both ends of the carbonization furnace are a raw material input area and a biochar production area that are connected to the carbonization channel. The raw material input area is connected to a biomass input channel. The biochar production area is connected to the biomass carbon powder input section through a biochar discharge channel. Both the raw material input area and the biochar production area are connected to a nitrogen purging channel to prevent blockage.

[0013] The quenching unit includes a quenching chamber and a dual-medium quenching assembly for rapid quenching. The dual-medium quenching assembly includes a purified water cooling channel and a circulating water channel. The two ends of the circulating water channel are respectively connected to the upper and lower ends of the quenching chamber to form a circulating cooling channel in the quenching chamber. The output end of the circulating water channel is provided with a downward-spraying cooling water nozzle. The input ends of the purified water cooling channel and the circulating water channel are located at the upper end of the quenching chamber.

[0014] The bottom of the quench chamber is equipped with an ash collection unit for collecting ash slag after quenching. The ash collection unit includes an ash collector, a pressure regulating slag lock hopper, and a slag pool connected in sequence. A control valve is provided between the ash collector and the pressure regulating slag lock hopper. When the ash collector is full of solid slag, the pressure regulating slag lock hopper is pressured to the same level as the internal pressure of the ash collector. The control valve opens when the pressure of the ash collector and the pressure regulating slag lock hopper are the same and closes when the solid slag is discharged into the pressure regulating slag lock hopper. After the control valve is closed, the pressure regulating slag lock hopper is released to atmospheric pressure and the slag is discharged into the slag pool.

[0015] Compared with the prior art, the advantages of the present invention are as follows: This invention innovatively adopts a closed-loop architecture of "directional circulation of pyrolysis gas and energy self-sufficiency". It uses the heat of gasification syngas to carbonize biomass. At the same time, the pyrolysis gas and carbon powder formed during the biomass carbonization process enter the gasification unit for gasification, forming an integrated gasification and biomass carbonization system. This greatly reduces the dependence on external components for energy supply and effectively breaks through the bottleneck of low energy utilization in existing solutions.

[0016] The carbonization unit includes adjacent parallel pyrolysis gas channels and carbonization channels. The pyrolysis gas outlet at the top of the gasification chamber is connected to the inlet of the pyrolysis gas channel, and the carbonization channel is connected to the pyrolysis gas input section of the gasification unit, forming a pyrolysis gas circulation channel between the carbonization and gasification units. This allows for closed-loop circulation of the high-temperature pyrolysis gas generated by the carbonization unit between the two units, achieving efficient utilization of the high-temperature syngas. Simultaneously, the carbon powder outlet of the carbonization channel is connected to the biomass carbon powder input section, enabling the biomass carbon powder produced during carbonization to be input into the gasification unit as a reaction source for the gasification reaction. This achieves synergistic reaction between the pyrolysis gas and the carbon powder, as well as closed-loop energy recovery, ensuring full utilization of the thermal and chemical energy of the pyrolysis gas and solving the problem of wasted heat and chemical energy in existing equipment.

[0017] The high-temperature syngas produced by the gasification unit is transported to the pyrolysis gas channel, providing a stable heat source for carbonization, thus replacing traditional electric / gas-fired heating. The outlet of the carbonization channel is connected to the pyrolysis gas input section, allowing the pyrolysis gas produced by biomass carbonization to participate in the gasification reaction, replacing the need for additional energy supply for gasification and ensuring full utilization of pyrolysis gas energy. This invention achieves bidirectional coupling utilization of pyrolysis gas, constructing a bidirectional closed-loop processing system where "the gasification unit produces pyrolysis gas, the carbonization unit supplies energy, and the gasification unit returns the pyrolysis gas to participate in the reaction." This forms an integrated system of gasification and biomass carbonization, significantly reducing dependence on external components for energy supply, optimizing energy utilization, and effectively improving the system's energy self-sufficiency rate.

[0018] (2) The present invention is configured in the gasification chamber with a syngas cooling section, a pyrolysis gas input section, a biomass carbon powder input section and an oxygen input section. The syngas cooling section is located at the top of the gasification chamber, the pyrolysis gas input section is located in the middle of the gasification chamber, and the biomass carbon powder input section and the oxygen input section are located at the bottom of the gasification chamber. The multi-segment gas-solid mixing structure effectively achieves uniform mixing of carbon powder, oxygen and pyrolysis gas. At this time, the pyrolysis gas input section located at the top produces excess pyrolysis gas after the biomass is carbonized. The pyrolysis gas contains the formaldehyde contained in the biomass. The pyrolysis gas, containing methane, olefins, and a certain amount of moisture, utilizes the high temperature generated by the reaction of biomass carbon powder and oxygen input in the lower biomass carbon powder input section and oxygen input section to reform methane, olefins, and water vapor. This further increases the content of carbon monoxide and hydrogen, enhances the content of effective components in the syngas (such as H2 and CO), effectively improves the gasification reaction conversion rate, effectively improves the mixing effect between materials and gases, significantly enhances the sufficiency of the gasification reaction, and improves the quality of the syngas.

[0019] (3) This invention connects the carbonization unit, gasification unit, and quenching unit to form an integrated structure, realizing the seamless connection of the "carbonization-gasification-quenching" function. It shortens and simplifies the transmission and flow path of materials (carbon powder) and gases (pyrolysis gas, syngas) to the greatest extent, and eliminates the heat loss risk of split equipment from the structure. That is, the combination of the integrated structure and the closed-loop flow structure of pyrolysis gas effectively avoids the heat loss of pipeline transmission in split equipment, and the energy utilization rate is greatly improved compared with the existing technology. At the same time, it greatly reduces the overall space occupied by the equipment and simplifies the installation process. Attached Figure Description

[0020] The invention will now be described in more detail with reference to embodiments and the accompanying drawings. Figure 1 This is a schematic diagram of the biomass carbonization and pyrolysis gasification reaction device of the present invention; Figure 2 This is a schematic diagram of the carbonization unit of the present invention; Figure 3 This is a schematic diagram of the synthesis gas cooling ring of the present invention; Figure 4 This is a schematic diagram of the structure of the sieve plate of the present invention.

[0021] The labels in the diagram represent: 1. Carbonization unit; 11. Pyrolysis gas channel; 12. Carbonization channel; 13. Heat exchange baffle; 14. Sieve plate; 141. Sieve hole; 15. Fluidized separation zone; 16. Carbonization furnace; 161. Raw material input zone; 162. Biochar production zone; 163. Gas inlet pipe interface; 17. Biomass input channel; 18. Biochar discharge channel; 19. Nitrogen purging channel; 2. Gasification unit; 21. Gasification chamber; 211. Pyrolysis gas outlet; 22. Combined 1. Gasification cooling section; 221. Gas ring channel; 222. Cooling gas input channel; 223. Guide vane; 224. Gas nozzle; 23. Pyrolysis gas input section; 24. Biomass carbon powder input section; 25. Oxygen input section; 26. Guide channel; 3. Quenching unit; 31. Quenching chamber; 32. Purified water cooling channel; 33. Circulating water channel; 4. Ash and slag collection unit; 41. Ash and slag collector; 42. Pressure regulating slag lock hopper; 43. Slag pool; 44. Control valve. Detailed Implementation

[0022] The present invention will now be described in further detail with reference to the accompanying drawings and specific embodiments, but this does not limit the scope of protection of the present invention.

[0023] Figure 1 and Figure 2An embodiment of the biomass carbonization and pyrolysis gasification reactor of the present invention is shown, which is applicable to the energy utilization of various biomass raw materials such as agricultural waste and forestry residues. In this embodiment, the device includes a carbonization unit 1, a gasification unit 2, and a quenching unit 3. The carbonization unit 1 includes adjacent parallel pyrolysis gas channels 11 and carbonization channels 12; the gasification unit 2 includes a gasification chamber 21, a syngas cooling section 22, a pyrolysis gas input section 23, a biomass carbon powder input section 24, and an oxygen input section 25. The syngas cooling section 22 is located at the top of the gasification chamber 21, the pyrolysis gas input section 23 is located in the middle of the gasification chamber 21, the biomass carbon powder input section 24 and the oxygen input section 25 are located at the bottom of the gasification chamber 21, the pyrolysis gas outlet 211 at the top of the gasification chamber 21 is connected to the air inlet of the pyrolysis gas channel 11, and the carbonization channel 12 is connected to the pyrolysis gas input section 23 to form a closed-loop pyrolysis gas flow channel; the carbon powder outlet of the carbonization channel 12 is connected to the biomass carbon powder input section 24, and the bottom of the gasification chamber 21 is connected to the top of the quench unit 3.

[0024] This invention innovatively adopts a closed-loop architecture of "directional circulation of pyrolysis gas and energy self-sufficiency". It uses the heat of gasification syngas to carbonize biomass. At the same time, the pyrolysis gas and carbon powder formed during the biomass carbonization process enter the gasification unit 2 for gasification, forming an integrated gasification and biomass carbonization system. This greatly reduces the dependence on external components for energy supply and effectively breaks through the bottleneck of low energy utilization in existing solutions.

[0025] The carbonization unit 1 includes adjacent parallel pyrolysis gas channels 11 and carbonization channels 12. The pyrolysis gas outlet 211 at the top of the gasification chamber 21 is connected to the inlet of the pyrolysis gas channel 11, and the carbonization channel 12 is connected to the pyrolysis gas input section 23 of the gasification unit 2, forming a pyrolysis gas circulation channel between the carbonization unit 1 and the gasification unit 2. This allows the high-temperature pyrolysis gas generated by the carbonization unit 1 to circulate in a closed loop between the carbonization unit 1 and the gasification unit 2, achieving efficient utilization of the high-temperature syngas. Simultaneously, the carbon powder outlet of the carbonization channel 12 is connected to the biomass carbon powder input section 24, allowing the biomass carbon powder generated during carbonization to be input into the gasification unit 2 as a reaction source for the gasification reaction. This enables synergistic reaction between the pyrolysis gas and the carbon powder, as well as closed-loop energy recovery, ensuring full utilization of the thermal and chemical energy of the pyrolysis gas and solving the problem of wasted heat and chemical energy in existing equipment. Specifically: The high-temperature syngas produced by gasification unit 2 is transported to pyrolysis gas channel 11, providing a stable heat source for carbonization, replacing traditional electric / gas heating. The outlet of carbonization channel 12 is connected to pyrolysis gas input section 23, allowing pyrolysis gas produced by biomass carbonization to participate in the gasification reaction, replacing the need for additional energy supply for gasification and ensuring full utilization of pyrolysis gas energy. This invention achieves bidirectional coupling utilization of pyrolysis gas, constructing a bidirectional closed-loop processing system where "gasification unit 2 produces pyrolysis gas, carbonization unit 1 provides energy, and the gas is returned to gasification unit 2 to participate in the reaction." This forms an integrated system of gasification and biomass carbonization, greatly reducing dependence on external components for energy supply, optimizing energy utilization, and effectively improving the system's energy self-sufficiency rate. Specifically: First, the high-temperature pyrolysis gas generated by gasification unit 2 is precisely cooled by syngas cooling section 22 to avoid excessive cooling and energy loss. Then, it is directed to the pyrolysis gas channel 11 of carbonization unit 1 to provide a stable heat source for carbonization, replacing traditional electric / gas heating. The carbonized pyrolysis gas then flows back to the pyrolysis gas input section 23 of gasification unit 2 to participate in the gasification reaction and generate high-value syngas, replacing the method of requiring additional energy for gasification, so that the energy of pyrolysis gas is fully utilized. This invention achieves bidirectional coupled utilization of pyrolysis gas: a bidirectional closed-loop processing system is constructed sequentially, consisting of "pyrolysis gas production in gasification unit 2, precise temperature control via liquid supercooling, energy supply from carbonization unit 1, and participation in the reaction in reflux gasification unit 2." This forms a pyrolysis gas cycle integrating biomass carbonization, pyrolysis gasification, and energy recycling, creating an energy closed loop of energy supply, gas production, and re-energy supply. This effectively eliminates dependence on external heating, optimizes energy utilization, and significantly improves the system's energy self-sufficiency rate. It effectively solves the core problem of "deep coupling of carbonization and pyrolysis gasification," greatly improving the system's adaptability and application limitations. Simultaneously, the coordinated control of carbonization, gasification, and recycling significantly increases the system's continuous operation cycle and greatly reduces costs.

[0026] Secondly, existing carbonization components typically only gasify carbon powder or methane, while the carbonization unit 1 of this invention combines the gasification of pyrolysis gas and biomass carbonization on the basis of carbon powder gasification, so as to effectively adapt to the conversion needs of multiple biomass as raw materials. It can be effectively applied to carbon powder and waste (biomass) pyrolysis gas, avoiding the problem of narrow adaptability when used only for a single raw material, and greatly improving the range of raw material adaptability.

[0027] Meanwhile, the greatest advantage of using pyrolysis gas in gasification is that it contains a large amount of tar, methane, and olefins. At high temperatures (such as above 1250℃), the mixed gas and water vapor can undergo effective reforming, resulting in complete tar cracking and the generation of carbon monoxide and hydrogen. This increases the proportion of hydrogen in the syngas, resulting in a high effective gas content, which is well-suited for chemical synthesis. Simultaneously, it effectively reduces carbon dioxide emissions and conversion costs, avoiding the conventional process of separating and treating tar, methane, and olefins in the syngas, thus significantly reducing costs. Furthermore, the participation of pyrolysis gas in gasification allows moisture to reform with methane and olefins at high temperatures, enabling moisture to participate in the reaction as a gasifying agent, greatly reducing the requirements for raw material moisture and particle size.

[0028] This invention features a multi-segmented gas-solid mixing structure within a gasification chamber 21, comprising a syngas cooling section 22, a pyrolysis gas input section 23, a biomass carbon powder input section 24, and an oxygen input section 25. The syngas cooling section 22 is located at the top of the gasification chamber 21, the pyrolysis gas input section 23 is located in the middle of the gasification chamber 21, and the biomass carbon powder input section 24 and the oxygen input section 25 are located at the bottom of the gasification chamber 21. This multi-segmented gas-solid mixing structure effectively achieves uniform mixing of carbon powder, oxygen, and pyrolysis gas. At this time, the pyrolysis gas input section 23, located at the top, produces excess pyrolysis gas after biomass carbonization. The pyrolysis gas contains methane, olefins, and a certain amount of moisture from biomass. The high temperature generated by the reaction of biomass carbon powder input into the lower biomass carbon powder input section 24 and oxygen input section 25 with oxygen reforms the methane, olefins, and water vapor, thereby further increasing the content of carbon monoxide and hydrogen. This increases the content of effective components in the syngas (such as H2 and CO), effectively improving the gasification reaction conversion rate, improving the mixing effect between materials and gas, and significantly enhancing the sufficiency of the gasification reaction. The increased content of effective components in the syngas (such as H2 and CO) further improves the quality of the syngas.

[0029] This invention connects the carbonization unit 1, gasification unit 2, and quenching unit 3 into an integrated structure, achieving seamless integration of the "carbonization-gasification-quenching" function. It significantly shortens and simplifies the transmission and flow path of materials (carbon powder) and gases (pyrolysis gas, syngas), structurally eliminating the heat loss risks inherent in split-type equipment. The combination of the integrated structure and the closed-loop flow structure for pyrolysis gas effectively avoids heat loss during pipeline transmission in split-type equipment, resulting in a substantial improvement in energy utilization compared to existing technologies. Simultaneously, it significantly reduces the overall footprint of the equipment and simplifies the installation process.

[0030] Furthermore, such as Figure 3As shown, the syngas cooling section 22 includes a syngas cooling ring, which is disposed through the side wall of the gasification chamber 21. The input end of the syngas cooling section 22 is connected to the cooling gas input channel 222. The cooling gas input channel 222 is used to provide low-temperature syngas. After quenching, the temperature of the syngas is 800-900℃, so that the syngas generated by gasification is cooled to below the ash melting point of biomass.

[0031] Although the temperature of the pyrolysis gas ejected from the pyrolysis gas input section 23 decreases after reforming, it will not fall below 1200℃, which is still higher than the ash melting point of biomass. At this temperature, there is a risk of liquid slag and easy pipe blockage. In this embodiment, a syngas cooling section 22 with instantaneous quenching is provided. The set temperature of the low-temperature syngas is 150~180℃. At this time, the input low-temperature syngas effectively cools the reformed syngas, reducing its temperature to 800~900℃. At this point, the liquid slag becomes solid slag, effectively avoiding the phenomenon of pipe blockage due to adhesion. It also allows the syngas entering the downstream to be effectively used for subsequent biomass carbonization by utilizing the preheating of the syngas. It can be seen that the present invention controls the quenching temperature below the ash melting point, ensuring that the high-temperature syngas without liquid slag achieves heat exchange in the carbonization unit while preventing blockage. In this embodiment, the cooling gas input channel 222 can be connected to the low-temperature syngas purification unit that generates the downstream syngas.

[0032] Meanwhile, the output end of the syngas cooling section 22 is equipped with a cooling gas nozzle 224, which is inclined downwards. This effectively cools the high-temperature syngas while simultaneously backflushing the fly ash downwards to prevent it from being carried into the downstream channel and affecting subsequent reactions. Preferably, the downward inclination angle of the cooling gas nozzle 224 can be set to 10~30°.

[0033] Furthermore, the syngas cooling section 22 also includes an air ring channel 221 and multiple guide vanes 223. The cooling gas input channel 222 is connected to the outside of the air ring channel 221; multiple cooling gas nozzles 224 are evenly arranged along the inner circumference of the air ring channel 221 and are connected to the air ring channel 221; the guide vanes 223 are arranged between adjacent cooling gas nozzles 224 and parallel to them, thereby guiding the cooling gas downwards to form an annular water curtain. This allows for sufficient and effective initial cooling of the syngas generated by gasification in the gasification chamber 21, as well as fly ash backflushing, ensuring safe subsequent transmission. Furthermore, its structure is simple, compact, and occupies little space.

[0034] Furthermore, the biomass carbon powder input section 24 and the oxygen input section 25 are located in the same plane of the gasification chamber 21. The biomass carbon powder input section 24 and the oxygen input section 25 are multiple syngas input channels arranged side by side, so that the biomass carbon powder and oxygen (gasifying agent) are simultaneously injected into the gasification chamber 21 through the same channel to react. The syngas input channel and the pyrolysis gas input section 23 are evenly distributed along the outer periphery of the gasification chamber 21, thereby generating uniform and sufficient syngas. The biomass carbon powder input section 24 and the pyrolysis gas input section 23 are equipped with spiral nozzles with an upward tilt angle to form an upward jetting swirling flow field, throwing the slag in the syngas onto the wall of the gasification chamber 21, minimizing the amount of fly ash carried downstream.

[0035] In this embodiment, nozzles are provided at the ends of both the syngas input channel and the pyrolysis gas input section 23. The syngas input channel has four nozzles evenly distributed, while the pyrolysis gas input section 23 has two nozzles symmetrically arranged. In other embodiments, the number of nozzles in the syngas input channel and the pyrolysis gas input section 23 can be adjusted according to actual needs and is not limited here. In this embodiment, the temperature of the syngas formed by the reaction of biomass carbon powder with oxygen, and the temperature of the syngas produced by the reaction with biomass carbon powder, are both 1200~1500℃.

[0036] Furthermore, such as Figure 2 As shown, the carbonization unit 1 also includes a heat exchange baffle 13. The pyrolysis gas channel 11 is located in the middle of the carbonization channel 12, and the pyrolysis gas channel 11 and the carbonization channel 12 are arranged concentrically. The heat exchange baffle 13 is located between the carbonization channel 12 and the pyrolysis gas channel 11, thereby blocking the heat crosstalk between the two channels inside the carbonization unit 1, making the carbonization temperature stable and the pyrolysis gas composition uniform, and improving the carbonization efficiency (up to 10% or more). This provides high-quality raw materials and gas for the subsequent gasification reaction, ensures the stability of the pyrolysis and gasification reaction conditions, and significantly enhances the reaction stability.

[0037] Meanwhile, the pyrolysis gas channel 11 and the carbonization channel 12 have the same conveying direction. At this time, the syngas temperature in the pyrolysis gas channel 11 reaches 900℃. The two exchange heat indirectly through the heat exchange baffle 13, which allows the biomass in the carbonization channel 12 to carbonize faster when the heat is sufficient, thereby increasing the carbonization throughput and carbonization efficiency. This effectively avoids direct contact between the raw material and the pyrolysis gas, which could lead to coking or contamination. As a result, the adjacent walls of the carbonization channel 12 and the pyrolysis gas channel 11 can transfer heat better, further ensuring that energy is accurately transferred to the entire carbonization process, and better achieving effective drying and carbonization of the moisture-containing raw materials.

[0038] The carbonization unit of this invention adopts a dual-channel configuration, combining a carbonization channel 12 and a pyrolysis gas channel 11. The two channels are arranged adjacently and parallel, forming an independently isolated layout. Heat exchange is achieved through heat exchange baffles 13, enabling indirect heat exchange between the pyrolysis gas in the pyrolysis gas channel 11 and the raw material in the carbonization channel 12. This avoids localized overheating and coking caused by direct contact between the pyrolysis gas and biomass, while ensuring precise energy transfer throughout the carbonization process. This guarantees effective drying and carbonization of the moisture-laden raw materials, preventing agglomeration. It avoids the cumbersome and costly process of drying and pulverizing raw materials, overcoming limitations in raw material compatibility and allowing direct feeding without pretreatment, significantly reducing energy consumption and saving costs.

[0039] In this embodiment, the pyrolysis gas channel 11 is a cylindrical pyrolysis gas channel, the diameter of which is adjusted according to the pyrolysis gas flow efficiency. The carbonization channel 12 is an annular carbonization channel, the width of which is adjusted according to the raw material processing volume. The edge of the heat exchange baffle 13 is welded and sealed to the inner wall of the furnace, thereby further and completely blocking heat crosstalk between the two channels from a structural perspective, achieving complete heat insulation, and further ensuring stable carbonization temperature and uniform pyrolysis gas composition.

[0040] In this embodiment, as Figure 2 and 4 As shown, the carbonization unit 1 also includes multiple screen plates 14 arranged at varying angles. These screen plates 14 are inclined and staggered along the length of the carbonization channel 12. Each screen plate 14 has through-holes 141 for screening the biomass raw materials. The inclination angle of the screen plates 14 gradually increases along the conveying direction of the carbonization channel 12, forming a curved drying and carbonization channel that slows down the falling speed of the raw materials. In this configuration, the increasing number of screen plates 14 from top to bottom effectively slows down the falling speed of the raw materials, allowing the biomass raw materials to fall slowly under the action of multiple screen plates 14, extending the residence time, and achieving uniform drying and carbonization. The curved drying and carbonization channel includes a moisture drying zone, a pre-carbonization zone, and a deep carbonization zone arranged sequentially. The moisture drying zone dries the biomass raw material, reducing the moisture content to below 10%. The pre-carbonization zone pre-carbonizes the biomass raw material, at which point the temperature of the biomass raw material is 200-400℃. The deep carbonization zone deep carbonizes the biomass raw material and generates biochar, at which point the temperature of the biomass raw material is 400-600℃, thereby further achieving the drying and carbonization of the moisture-laden raw material.

[0041] Below the curved drying and carbonization channel 12, a fluidized separation zone 15 with parallelly arranged screen plates 14 is provided to form a fluidized separation zone 15 that ensures uniform fluidization and separation of biomass carbon powder, thereby facilitating uniform fluidization and separation of biomass carbon powder. This invention further effectively dries, carbonizes, and separates multi-component biomass carbon through a sequentially arranged moisture drying zone, pre-carbonization zone, deep carbonization zone, and fluidized separation zone 15, producing primary biomass carbon, thus further effectively meeting the conversion needs of multi-component biomass as raw material.

[0042] Preferably, along the conveying direction of the carbonization channel 12, the aperture of the screen 141 gradually decreases. At this time, as the carbonization depth increases, the biomass carbon powder will gradually break down and decrease in size, thereby enabling the biomass raw material to sequentially achieve moisture removal, pre-carbonization, and deep carbonization, ensuring the smooth and reliable progress of the biomass carbonization process.

[0043] In this embodiment, the carbonization unit 1 further includes a carbonization furnace 16. The carbonization furnace 16 has a raw material input area 161 and a biochar production area 162, both connected to the carbonization channel 12, respectively. Specifically, the top of the carbonization furnace 16 has the raw material input area 161, and the bottom of the carbonization furnace 16 has the biochar production area 162. The raw material input area 161 is connected to a biomass input channel 17 for quantitative input of biomass. The biochar production area 162 is connected to a biomass carbon powder input section 24 via a biochar discharge channel 18 to input biomass carbon powder into the gasification chamber 21. Both the raw material input area 161 and the biochar production area 162 are connected to a nitrogen purging channel 19 to purge nitrogen, prevent blockage of biomass raw materials or biochar, and ensure smooth feeding and discharging, guaranteeing reliable and continuous operation of the system.

[0044] Furthermore, high-pressure nitrogen can be introduced into the carbonization furnace 16 through the nitrogen purging channel 19 to control the pressure stabilization between the carbonization furnace 16 and the synthesis gas, which can support the full range of pressure operation from 0 to 6 MPa, so that it can be used for atmospheric pressure power generation and can also be directly connected to chemical synthesis that requires high pressure (such as methanol production and ammonia synthesis).

[0045] In this embodiment, the carbonization furnace 16 can be made of stainless steel, with a sealed structure and a design pressure range of 0-6MPa to adapt to the high temperature and high pressure conditions of biomass pyrolysis.

[0046] Furthermore, the quench unit 3 includes a quench chamber 31 and a dual-medium quench assembly. The dual-medium quench assembly includes a purified water cooling channel 32 and a circulating water channel 33. The two ends of the circulating water channel 33 are respectively connected to the upper and lower ends of the quench chamber 31 to form a circulating cooling channel in the quench chamber 31. A circulating water outlet is provided on the lower side of the quench chamber 31 to discharge the used circulating water, which can be recycled and reused, reducing water consumption. The input ends of the purified water cooling channel 32 and the circulating water channel 33 are located at the upper end of the quench chamber 31, which further ensures the continuous and effective rapid cooling of the high-temperature syngas. It achieves precise control of energy loss and eliminates the complex process of combining pyrolysis gas cooling and reheating in traditional systems, thereby greatly reducing the energy consumption ratio and significantly improving the energy utilization rate of syngas.

[0047] The output end of the circulating water channel 33 is equipped with downward-spraying cooling water nozzles to form an annular quenching water curtain, further ensuring the continuous and effective rapid cooling of the high-temperature syngas. This achieves precise control of energy loss, eliminates the complex process of combining pyrolysis gas cooling and reheating in traditional systems, thereby greatly reducing the energy consumption ratio and significantly improving the energy utilization rate of syngas. In this embodiment, the spray angle of the cooling water nozzles is 10~45°.

[0048] More preferably, the temperature of the purified water source is 25℃~40℃, which cools the syngas produced by gasification below the ash melting point of biomass. Although the temperature of the high-temperature syngas containing carbon monoxide and hydrogen generated by reforming decreases, it generally does not fall below 1200℃, which is still higher than the ash melting point of biomass. At this point, there is a risk of liquid slag and easy pipe blockage. The temperature of the input purified water source effectively cools the reformed high-temperature syngas, reducing its temperature to 800~900℃. At this point, the liquid slag becomes solid slag, effectively preventing pipe blockage and allowing the high-temperature syngas to smoothly form a circulating syngas with a preset ash solidification temperature for effective biomass carbonization. In this embodiment, the temperature of the high-temperature syngas can be adjusted by controlling the amount of purified water.

[0049] In this embodiment, an air inlet pipe interface 163 is provided on the upper side of the pyrolysis gas channel 11. The air inlet pipe interface 163 is connected to the pyrolysis gas outlet 211 at the top of the gasification chamber 21 through the guide channel 26. At the same time, the carbonization channel 12 is connected to the pyrolysis gas input section 23 in the middle of the gasification chamber 21, which simplifies the pyrolysis gas flow path and improves the closed-loop efficiency.

[0050] Furthermore, the ash collection unit 4 includes an ash collector 41, a pressure regulating slag lock hopper 42, and a slag pool 43 connected in sequence. A control valve 44 is provided between the ash collector 41 and the pressure regulating slag lock hopper 42. When the ash collector 41 is full of solid slag, the pressure regulating slag lock hopper 42 is pressured to the same pressure as the inside of the ash collector 41. The control valve 44 is opened when the pressure of the ash collector 41 and the pressure regulating slag lock hopper 42 is the same, and closed when the solid slag is discharged into the pressure regulating slag lock hopper 42. After the control valve 44 is closed, the pressure regulating slag lock hopper 42 is released to atmospheric pressure and the slag is discharged into the slag pool 43. This is used to reliably and effectively remove fly ash carried by the circulating synthesis gas. The structure is simple, the operation is convenient, and the cost is low.

[0051] In this embodiment, the gasification unit 2 receives biomass carbon powder from the carbonization unit 1 and reacts it with oxygen / water vapor at high temperature to generate high-temperature syngas rich in carbon monoxide and hydrogen. The temperature of the high-temperature syngas is above 1200°C. It is initially cooled to 900°C through the quench chamber 31 to form circulating syngas. The circulating syngas carries fly ash and is ash-removed through the ash collection unit 4. At the same time, the circulating syngas enters the pyrolysis gas channel 11 of the carbonization unit 1, where the thermal energy of the syngas is used for biomass carbonization, realizing the comprehensive utilization of the thermal energy of the syngas. Meanwhile, the pyrolysis gas after biomass carbonization flows back to the pyrolysis gas input section 23 of the gasification unit 2 to participate in the gasification reaction and generate high-value syngas.

[0052] In this embodiment, the specific working process of the processing system is as follows: Raw material feeding and carbonization: Biomass enters the carbonization channel 12 through the discharge valve at the top of the carbonization unit 1, with a stable hourly feed rate. Under the action of multiple layers of screen plates 14, the biomass slowly falls, sequentially completing the drying, pre-carbonization, and deep carbonization processes to generate biomass carbon powder. The biomass carbon powder enters the gasification chamber 21 of the gasification unit 2 through the bottom of the carbonization unit 1. Nitrogen is purged into the nitrogen purging channel 19 as needed to prevent blockage.

[0053] 2) Pyrolysis Gasification and Preliminary Cooling: The pyrolysis gas containing tar, methane, olefins, and some carbon powder from the biomass carbon powder is directly fed into the gasification chamber 21 at a temperature of 350°C or higher. It combines with oxygen injected from the oxygen input section 25, and the oxygen reacts with the tar and carbon powder in the pyrolysis gas to generate pyrolysis gas containing carbon monoxide and hydrogen at 1200-1500°C. At this temperature above 1200°C, the mixed gas undergoes gasification and reforming with water vapor, ensuring complete tar cracking and resulting in a high effective gas content in the high-temperature syngas. This avoids the problem of low-temperature tar condensation during cooling, ensuring stable system operation and continuous production. Furthermore, it eliminates the need for an external purification system, reducing costs. Afterward, the high-temperature syngas from the gasification chamber 21 is cooled to 980°C via purified water cooling channel 32 and enters the quench chamber 31; simultaneously, the ash from the quench chamber 31 enters the ash collection unit 4.

[0054] 3) Circulating pyrolysis gas for energy supply: Circulating syngas is transported to the pyrolysis gas channel 11 of carbonization unit 1 to supply energy for biomass carbonization; after energy supply, the pyrolysis gas with a temperature of 400℃ returns to the gasification chamber 21 through the pyrolysis gas input section 23 to participate in the gasification reaction.

[0055] 4) Product purification and collection: A portion of the pyrolysis gas cooled to 300°C in the pyrolysis gas channel 11 of the carbonization furnace 16 passes through the gas-solid separation unit, purification unit and conversion unit in sequence and is connected to external chemical systems such as the methanol synthesis system.

[0056] This invention constructs a continuous processing system encompassing "raw material pretreatment, carbonization, gasification synergistic conversion, closed-loop energy supply from pyrolysis gas, and efficient product purification." It couples the independent processes of "biomass carbonization" and "pyrolysis gasification" into a single system. The pyrolysis gas generated within the system is cleverly recycled, serving both as a heat source for the carbonization process and being recycled back to participate in the gasification reaction. This maximizes the utilization of the system's own energy and reduces dependence on external energy sources, effectively improving energy efficiency and reducing emissions.

[0057] Although the invention has been described with reference to preferred embodiments, various modifications can be made and components can be replaced with equivalents without departing from the scope of the invention. In particular, the technical features mentioned in the various embodiments can be combined in any manner as long as there is no structural conflict. The invention is not limited to the specific embodiments disclosed herein, but includes all technical solutions falling within the scope of the claims.

Claims

1. A biomass carbonization and pyrolysis gasification reaction apparatus, characterized in that, The system includes a carbonization unit, a gasification unit, and a quenching unit. The carbonization unit comprises adjacent, parallel pyrolysis gas channels and a carbonization channel. The gasification unit includes a gasification chamber, a syngas cooling section at the top of the gasification chamber, a pyrolysis gas input section in the middle of the gasification chamber, a biomass carbon powder input section at the bottom of the gasification chamber, and an oxygen input section. The pyrolysis gas outlet at the top of the gasification chamber is connected to the inlet of the pyrolysis gas channel, and the carbonization channel is connected to the pyrolysis gas input section, forming a pyrolysis gas circulation channel between the carbonization unit and the gasification unit. The carbon powder outlet of the carbonization channel is connected to the biomass carbon powder input section, and the bottom of the gasification chamber is connected to the top of the quenching unit.

2. The biomass carbonization and pyrolysis gasification reaction apparatus according to claim 1, characterized in that, The syngas cooling section includes a syngas cooling ring that runs through the side wall of the gasification chamber. The input end of the syngas cooling section is connected to a cooling gas input channel for providing low-temperature syngas. The temperature of the syngas after quenching is 800-900℃, so that the syngas produced by gasification is cooled to below the ash melting point of biomass. The output end of the syngas cooling section is provided with a cooling gas nozzle that is inclined downwards.

3. The biomass carbonization and pyrolysis gasification reaction apparatus according to claim 2, characterized in that, The syngas cooling section further includes a gas ring channel and multiple guide vanes. The cooling gas input channel is connected to the outside of the gas ring channel. There are multiple cooling gas nozzles, which are evenly arranged along the inner circumference of the gas ring channel and connected to the gas ring channel. The guide vanes are arranged between adjacent cooling gas nozzles and are arranged parallel to the cooling gas nozzles.

4. The biomass carbonization and pyrolysis gasification reaction apparatus according to claim 1, characterized in that, The biomass carbon powder input section and the oxygen input section are located in the same plane of the gasification chamber. The biomass carbon powder input section and the oxygen input section are multiple syngas input channels arranged side by side. The syngas input channels and the pyrolysis gas input section are evenly distributed along the outer periphery of the gasification chamber. The biomass carbon powder input section and the pyrolysis gas input section are equipped with spiral nozzles with an upward tilt angle to form an upward jetting swirling flow field.

5. The biomass carbonization and pyrolysis gasification reactor according to any one of claims 1 to 4, characterized in that, The carbonization unit also includes a heat exchange baffle plate disposed between the carbonization channel and the pyrolysis gas channel. The pyrolysis gas channel is located in the middle of the carbonization channel and the two are arranged concentrically. The conveying directions of the pyrolysis gas channel and the carbonization channel are the same.

6. The biomass carbonization and pyrolysis gasification reaction apparatus according to claim 5, characterized in that, The carbonization unit also includes multiple screen plates with varying angles. The multiple screen plates are arranged in an inclined and staggered manner along the length of the carbonization channel. The screen plates are provided with through-holes. The inclination angle of the screen plates gradually increases along the conveying direction of the carbonization channel to form a curved drying carbonization channel that slows down the falling speed of the raw materials. A fluidization separation zone with screen plates arranged in parallel is provided below the curved drying carbonization channel.

7. The biomass carbonization and pyrolysis gasification reaction apparatus according to claim 6, characterized in that, Along the conveying direction of the carbonization channel, the aperture of the screen holes gradually decreases.

8. The biomass carbonization and pyrolysis gasification reaction apparatus according to claim 5, characterized in that, The carbonization unit also includes a carbonization furnace. At both ends of the carbonization furnace are a raw material input area and a biochar production area that are connected to the carbonization channel. The raw material input area is connected to a biomass input channel. The biochar production area is connected to the biomass carbon powder input section through a biochar discharge channel. Both the raw material input area and the biochar production area are connected to a nitrogen purging channel to prevent blockage.

9. The biomass carbonization and pyrolysis gasification reactor according to any one of claims 1 to 4, characterized in that, The quenching unit includes a quenching chamber and a dual-medium quenching assembly for rapid quenching. The dual-medium quenching assembly includes a purified water cooling channel and a circulating water channel. The two ends of the circulating water channel are respectively connected to the upper and lower ends of the quenching chamber to form a circulating cooling channel in the quenching chamber. The output end of the circulating water channel is provided with a downward-spraying cooling water nozzle. The input ends of the purified water cooling channel and the circulating water channel are located at the upper end of the quenching chamber.

10. The biomass carbonization and pyrolysis gasification reactor according to any one of claims 1 to 4, characterized in that, The bottom of the quench chamber is equipped with an ash collection unit for collecting ash slag after quenching. The ash collection unit includes an ash collector, a pressure regulating slag lock hopper, and a slag pool connected in sequence. A control valve is provided between the ash collector and the pressure regulating slag lock hopper. When the ash collector is full of solid slag, the pressure regulating slag lock hopper is pressured to the same level as the internal pressure of the ash collector. The control valve opens when the pressure of the ash collector and the pressure regulating slag lock hopper are the same and closes when the solid slag is discharged into the pressure regulating slag lock hopper. After the control valve is closed, the pressure regulating slag lock hopper is released to atmospheric pressure and the slag is discharged into the slag pool.

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