Biomass gasification reaction device

Abstract

The invention provides a biomass gasification reaction device, and belongs to the field of biosynthesis, the biomass gasification reaction device comprises: a pyrolysis reactor for performing a pyrolysis reaction on a biomass raw material to obtain a pyrolysis reactant, the pyrolysis reactant comprising bio-oil and initial synthesis gas; the gasification reactor is used for carrying out gasification reaction on the pyrolysis reactant by utilizing various gasification agents to obtain target synthesis gas, and the target synthesis gas comprises H2 and CO; wherein the gasification reactor comprises a multi-stage gasification agent nozzle module; the multi-stage gasification nozzle module comprises a plurality of gasification agent nozzles and a plurality of gasification nozzles, wherein each gasification agent nozzle is used for injecting a gasification agent into the gasification reactor; the plurality of gasifying agent nozzles are axially arranged along the central axis direction of the gasification reactor; and moreover, the gasifying agent nozzles for injecting the same type of gasifying agent are positioned at the same height of the gasification reactor.

Description

Technical Field

[0001] This application belongs to the field of biosynthesis, specifically relating to a biomass gasification reaction device. Background Technology

[0002] Biomass gasification refers to the process of feeding biomass feedstock into a high-temperature gasification reactor, where, under the action of a gasification medium, the biomass undergoes drying, pyrolysis, partial oxidation, and reduction to produce a mixture of gases such as CO, H2, and CH4.

[0003] In traditional gasification processes, the control mechanism for gasifying agents is too simplistic, often employing a single gasifying agent (such as CO2 or steam), which fails to achieve coordinated control of multiple syngas, resulting in large fluctuations in the composition of the produced gas and low gasification efficiency. Summary of the Invention

[0004] This application provides a biomass gasification reactor for flexible control of the gasifying agent.

[0005] In a first aspect, a biomass gasification reactor, the reactor comprising: A pyrolysis reactor is used to pyrolyze biomass feedstock to obtain pyrolysis products, said pyrolysis products including: bio-oil and initial syngas; A gasification reactor is used to perform a gasification reaction on the pyrolysis reactants using a variety of gasifying agents to obtain a target syngas, wherein the target syngas includes H2 and CO; wherein the gasification reactor includes a multi-stage gasifying agent nozzle module; The multi-stage gasification nozzle module includes: multiple gasifying agent nozzles, each of which is used to inject a gasifying agent into the gasification reactor; The plurality of gasifying agent nozzles are axially arranged along the central axis of the gasification reactor; and the gasifying agent nozzles that inject the same type of gasifying agent are located at the same height of the gasification reactor.

[0006] In one possible implementation, each gasifying agent nozzle corresponds to a gasifying agent, and each gasifying agent participates in one stage of the gasification reaction. The axial spacing of each stage of gasifying agent nozzles is matched with the particle flow distance under the time required for the corresponding reaction stage; Wherein, the axial arrangement spacing represents the distance between the gasifying agent nozzle and the adjacent next-stage gasifying agent nozzle in the direction of the central axis of the gasification reactor; the particle flow distance refers to the distance generated by the reactants moving along the central axis of the gasification reactor for a limited time.

[0007] In one possible implementation, the plurality of vaporizing agents includes at least: oxygen, water vapor, and carbon dioxide; The plurality of vaporizing agent nozzles include at least one or more oxygen vaporizing agent nozzles, one or more water vapor vaporizing agent nozzles, and one or more carbon dioxide vaporizing agent nozzles.

[0008] In one possible implementation, the oxygen vaporizing agent nozzle is located below the feed inlet at the bottom of the vaporization reactor; The water vapor vaporizing agent nozzle is positioned at a higher height than the oxygen vaporizing agent nozzle in the gasification reactor, and the carbon dioxide vaporizing agent nozzle is positioned at a higher height than the water vapor vaporizing agent nozzle in the gasification reactor, so that the oxygen vaporizing agent nozzle, the water vapor vaporizing agent nozzle, and the carbon dioxide vaporizing agent nozzle constitute a three-stage gasification nozzle structure axially arranged along the central axis of the gasification reactor.

[0009] In one possible implementation, the gasification reactor further includes a plurality of temperature sensors located below each of the gasifying agent nozzles and at the outlet of the gasification reactor. The oxygen vaporizing agent nozzle is equipped with an oxygen flow regulating valve group, which is linked to an oxygen flow meter to adjust the gas flow rate of the oxygen vaporizing agent nozzle according to the temperature feedback from the temperature sensor.

[0010] In one possible implementation, the steam vaporizer nozzle is equipped with a steam generator and a flow control unit, through which the gas flow rate of the steam vaporizer nozzle is regulated.

[0011] In one possible implementation, the gasification reactor is also equipped with a gas chromatograph and an infrared sensor at the outlet pipe for real-time detection of the actual molar ratio of H2 and CO in the generated target synthesis gas. The carbon dioxide vaporizer nozzle is equipped with a proportional-integral valve to adjust the gas flow rate of the carbon dioxide vaporizer nozzle according to the actual molar ratio.

[0012] In one possible implementation, the central axis of the gasifying agent nozzle for gasifying agent injection forms a 30° angle with the tangential direction of the inner wall of the reactor.

[0013] In one possible implementation, the apparatus further includes: a cyclone separator, wherein the inlet pipe on the side wall of the cyclone separator is connected to the outlet pipe at the top of the pyrolysis reactor, and the outlet pipe at the top of the cyclone separator is connected to the inlet pipe of the gasification reactor. The cyclone separator is used to separate the bio-oil and the initial syngas produced in the pyrolysis reactor and transport them to the gasification reactor.

[0014] In one possible implementation, a spiral feeder is provided at the bottom of the pyrolysis reactor. The bottom pipe of the cyclone separator is connected to the bottom of the pyrolysis reactor, and is used to transport the separated biochar to the screw conveyor and discharge it through the screw conveyor.

[0015] The beneficial effects of this application are as follows: The control device proposed in the embodiments of this application adopts an axial multi-stage gasifying agent nozzle module, which coordinates the axial arrangement spacing of each stage of gasifying agent nozzles with the biomass residence time (reaction time of each stage), and realizes directional control of syngas by injecting oxygen, water vapor and carbon dioxide in an axial stage.

[0016] The above description is only an overview of the technical solution of this application. In order to better understand the technical means of this application and to implement it in accordance with the contents of the specification, and to make the above and other objects, features and advantages of this application more obvious and understandable, the following are specific embodiments of this application. Attached Figure Description

[0017] To more clearly illustrate the technical solutions in the embodiments or related technologies of this application, the accompanying drawings used in the description of the embodiments or related technologies will be briefly introduced below. Obviously, the accompanying drawings described below are some embodiments of this application. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort. It should be noted that the scale in the drawings is for illustration only and does not represent the actual scale.

[0018] Figure 1 This is a schematic diagram of the structure of a biomass gasification control device according to an embodiment of this application; Figure 2 This is a schematic diagram of an axial arrangement spacing in an embodiment of this application; Explanation of reference numerals in the attached diagram: 1. Pyrolysis reactor; 2. Gasification reactor; 3. Oxygen vaporizer nozzle; 4. Water vaporizer nozzle; 5. Carbon dioxide vaporizer nozzle; and 6. Cyclone separator. Detailed Implementation

[0019] To make the above-mentioned objectives, features, and advantages of this application more apparent and understandable, the technical solutions in the embodiments of this application will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of this application, not all embodiments. Based on the embodiments in this application, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of this application.

[0020] The terms "first," "second," etc., used in the specification and claims of this application are used to distinguish similar objects and not to describe a specific order or sequence. It should be understood that such terms can be used interchangeably where appropriate so that embodiments of this application can be implemented in orders other than those illustrated or described herein, and the objects distinguished by "first" and "second" are generally of the same class, not limited in number; for example, the first object can be one or at least two. Furthermore, in the specification and claims, "and / or" indicates at least one of the connected objects, and the character " / " generally indicates that the preceding and following objects are in an "or" relationship.

[0021] Biomass gasification refers to the process where biomass feedstock is fed into a high-temperature gasification reactor, where, under the action of gasification media such as CO2, oxygen, and steam, the biomass undergoes drying, pyrolysis, partial oxidation, and reduction to produce a mixture of gases including CO, H2, and CH4. The gasifying agent refers to the gaseous medium participating in the pyrolysis and gasification reaction; common types include air, oxygen, steam, and carbon dioxide. Its type and proportion directly affect product distribution and reaction efficiency. Multi-gasifying agent synergistic control refers to the precise control of the gasification process by dynamically adjusting the proportions, injection locations, and flow rates of various gasifying agents (such as oxygen, steam, and carbon dioxide) to optimize gas composition, improve gasification efficiency, and reduce byproducts (such as tar). Syngas is the main gaseous product of gasification, primarily composed of CO, H2, and CH4, and can be used as fuel or chemical feedstock.

[0022] Biomass gasification is an important way to achieve efficient utilization of renewable energy. However, existing gasification technologies lack a synergistic feedback mechanism for multiple variables (temperature, gas composition, and gasifying agent ratio) and do not fully utilize the coupling effect between catalyst and gasifying agent, resulting in insufficient control precision and efficiency.

[0023] In traditional gasification processes, gasifying agents are typically injected in fixed proportions or in stages, lacking a dynamic synergistic mechanism. This results in large fluctuations in the composition of the produced gas and low gasification efficiency (e.g., CO+H2 content less than 70%). Quantitative control of the syngas production ratio is also difficult. Traditional single-agent systems exhibit inherent contradictions in H2 / CO regulation. For example, water vapor as a single gasifying agent generates more H2 and CH4, and less CO; CO2 as a single gasifying agent generates more CO and less H2. The H2 / CO ratio can reach 3.2±0.5 with water vapor gasification, but drops to 0.8±0.3 with CO2 gasification, indicating that the H2 / CO ratio in the syngas is significantly affected by the gasifying agent. The use of a single gasifying agent cannot precisely meet the stoichiometric ratio requirements for methanol synthesis (H2 / CO = 2.0±0.1). Therefore, introducing multiple gasifying agents is necessary to solve the problem of quantitatively controlling H2 / CO production during gasification to meet the requirements for direct methanol synthesis. Introducing CO2 can further reduce the tar content produced in the gasification reaction and help control the ratio of H2 to CO in the syngas, but there are still problems with large fluctuations in the syngas ratio and difficulty in accurately controlling the syngas ratio.

[0024] In view of the above problems, the first aspect of this application proposes a biomass gasification control device, referring to... Figure 1 , Figure 1 A schematic diagram of a biomass gasification control device is shown, such as... Figure 1 As shown, the device includes: A pyrolysis reactor is used to pyrolyze biomass feedstock to obtain pyrolysis products, said pyrolysis products including: bio-oil and initial syngas; A gasification reactor is used to perform a gasification reaction on the pyrolysis reactants using a variety of gasifying agents to obtain a target syngas, wherein the target syngas includes H2 and CO; wherein the gasification reactor includes a multi-stage gasifying agent nozzle module; The multi-stage gasification nozzle module includes: multiple gasifying agent nozzles, each of which is used to inject a gasifying agent into the gasification reactor; The plurality of gasifying agent nozzles are axially arranged along the central axis of the gasification reactor; and the gasifying agent nozzles that inject the same type of gasifying agent are located at the same height of the gasification reactor.

[0025] In this embodiment, as Figure 1 As shown, Figure 1 The dashed arrows in the diagram indicate the direction along the central axis of the gasification reactor 2, which is the length direction of the gasification reactor 2, or the direction of gas flow. Multiple gasifying agent nozzles are axially arranged along the central axis at different heights (relative to the bottom of the gasification reactor). This utilizes a multi-stage gasifying agent nozzle module (such as...) Figure 1 As shown in steps 3, 4, and 5), the flow of the gasifying agent input to the reactor is controlled so that the molar ratio of H2 to CO in the generated target syngas is within a first threshold range. The first threshold range can be 1.9-2.1.

[0026] This application proposes an integrated system for simultaneously synthesizing H2 / CO syngas. It directly pyrolyzes and gasifies biomass to generate H2 / CO-rich gas, employing multi-stage dynamic control of the gasifying agent to directly produce H2 / CO syngas with a ratio sufficient for methanol synthesis. Combined with waste heat recovery and tar cracking technology, this system significantly improves energy efficiency and environmental performance, and is suitable for the large-scale processing of various biomass raw materials such as straw and sawdust.

[0027] like Figure 1 As shown, the pulverized and dried biomass feedstock is transported to pyrolysis reactor 1. Pyrolysis reactor 1 then feeds the biomass feedstock into a fluidized bed, where a preliminary pyrolysis reaction takes place at 400-500℃, yielding pyrolysis reactants, namely ash, biochar, bio-oil, and a small amount of syngas (i.e., initial syngas). During the low-temperature pyrolysis stage, biomass generates tar (such as benzene, phenols, polycyclic aromatic hydrocarbons, etc.), which enters gasification reactor 2 along with the bio-oil and syngas. The biomass feedstock can be one or more types of biomass, such as straw (C / H≈0.6), sawdust (C / H≈0.8), etc. The bio-oil (containing tar), being gaseous at 400-500℃, enters the secondary reactor along with the syngas. The bio-oil can include oxygenated compounds such as acetic acid, methanol, acetone, aldehydes (such as formaldehyde), and phenols (such as phenol), and tar (Tar) including polycyclic aromatic hydrocarbons (such as naphthalene and anthracene), benzene compounds (such as toluene and xylene), and long-chain hydrocarbons. The initial synthesis gas includes H2, CO, CH4, etc.

[0028] In one possible implementation, the apparatus further includes: a cyclone separator 6, wherein the inlet pipe on the side wall of the cyclone separator 6 is connected to the outlet pipe at the top of the pyrolysis reactor, and the outlet pipe at the top of the cyclone separator is connected to the inlet pipe of the gasification reactor. The cyclone separator is used to separate the bio-oil and the initial syngas produced in the pyrolysis reactor and transport them to the gasification reactor.

[0029] In one possible implementation, a spiral feeder is provided at the bottom of the pyrolysis reactor. The bottom pipe of the cyclone separator is connected to the bottom of the pyrolysis reactor, and is used to transport the separated biochar to the screw conveyor and discharge it through the screw conveyor.

[0030] The biochar generated in reactor 1 is mainly collected (ash content <5%) by the bottom spiral feeder and discharged. The remaining products (bio-oil and initial syngas) are separated by cyclone separator 6 and transported to gasification reactor 2. Cyclone separator 6 is connected to the outlet pipe of reactor 1. The core function of the cyclone separator is to separate solid particles and gaseous products in the gas-solid two-phase flow. The solid particles include: biochar generated in reactor 1 (unreacted carbonaceous solids) and ash (inorganic impurities in biomass), preventing solids from entering the secondary reactor and causing blockage, while simultaneously recovering the biochar (which can be used as a soil conditioner or fuel). The gaseous products include: bio-oil vapor (containing tar), initial syngas (H2, CO, CH4, etc.), and the fluidizing medium (N2). The gas-solid mixture enters the cyclone separator at high tangential speed, forming a rotating vortex inside. Due to its lower density, the gas flows downwards from the cyclone. Figure 1 As shown, the solid particles, due to their high density, are thrown against the container wall and fall along the wall to the bottom collection port, where they are discharged.

[0031] The cyclone separator transports the separated gaseous products to gasification reactor 2. Gasification reactor 2 utilizes various gasifying agents to gasify the pyrolysis reactants at an ambient temperature of 700-800℃ and a slight positive pressure of 0.1-0.3MPa, yielding the target syngas, namely high-purity H2 / CO syngas. Specifically, reactor 2 decomposes large-molecule tar into smaller-molecule gases (such as H2 and CO) through high-temperature pyrolysis. The gasifying agent reactions include: using steam to promote the water-gas reaction, using oxygen to partially burn the tar to provide heat, and CO2 participating in the reforming reaction.

[0032] In one possible implementation, each gasifying agent nozzle corresponds to a gasifying agent, and each gasifying agent participates in one stage of the gasification reaction. The axial spacing of each stage of gasifying agent nozzles is matched with the particle flow distance under the time required for the corresponding reaction stage; Wherein, the axial arrangement spacing represents the distance between the gasifying agent nozzle and the adjacent next-stage gasifying agent nozzle along the central axis of the gasification reactor; the particle flow distance refers to the distance the reactants travel along the central axis of the gasification reactor over a limited time. Matching the axial arrangement spacing and the particle flow distance means that they are sufficiently close, with the difference within a first threshold range. For example, the absolute value of the difference between the two is less than 3 cm.

[0033] Specifically, biomass pellets move along the axial direction and react step by step within the fluidized bed. Multi-stage nozzles inject different gasifying agents according to the needs of each reaction stage; different gasifying agents correspond to different reaction stages, such as... Figure 1As shown, the reaction in the gasification reactor is mainly divided into three stages: the oxygen gasifying agent nozzle 3 at the bottom provides initial combustion heat by injecting oxygen, which is the first reaction stage (oxidation); the water vapor gasifying agent nozzle 4 in the middle provides water vapor to promote the water-gas reaction (C + H2O → CO + H2), which is the second reaction stage (reduction); and the carbon dioxide gasifying agent nozzle 5 at the top provides carbon dioxide to adjust the final H2 / CO molar ratio (CO2 + C → 2CO), which is the third reaction stage (reforming).

[0034] In this embodiment, the axial spacing of the nozzles is matched with the residence time of the biomass particles; that is, the nozzle positions from bottom to top are distributed according to the design and matched with the residence time of the biomass particles (2-5 seconds). Here, biomass particle residence time is a common concept in fluidized bed reactors, referring to the average time required for solid particles (or droplets) to move from feed to discharge within the reactor.

[0035] Specifically, matching the axial spacing of the nozzles with the residence time of biomass pellets means that the axial spacing of the nozzles in each stage of the gasifying agent is matched with the particle flow distance required for the corresponding reaction stage. In other words, the nozzle position matches the time consumed in each reaction stage (oxidation, reduction, reforming). The axial height of the gasifying agent nozzles matches the spatial gradient of the reaction process (the gasifying agent nozzles are arranged in layers according to the reaction stages, and their height matches the reaction requirements of each stage), where the bottom nozzles correspond to the oxidation stage, the middle nozzles to the reduction stage, and the upper nozzles to the reforming stage. Physical travel time (t) 流动 = Time taken for particles to flow from nozzle A to nozzle B; Chemical reaction time (t) 反应 = The time required to complete this stage (such as oxidation or reduction) is determined by designing the nozzle position so that the physical movement time is close to the chemical reaction time.

[0036] Reference Figure 2 , Figure 2 A schematic diagram of an axial arrangement spacing is shown, such as... Figure 2As shown, the axial arrangement spacing of the oxygen gasifying agent represents the distance d1 between the oxygen gasifying agent nozzle and the steam gasifying agent nozzle along the central axis of the gasification reactor; distance d1 needs to be sufficiently close to the particle flow distance under the required time t1 of the first reaction stage. The axial arrangement spacing of the steam gasifying agent nozzle represents the distance d2 between the steam gasifying agent nozzle and the carbon dioxide gasifying agent nozzle along the central axis of the gasification reactor; distance d2 needs to be sufficiently close to the particle flow distance under the required time t2 of the second reaction stage. The axial arrangement spacing of the carbon dioxide gasifying agent represents the distance d3 between the carbon dioxide gasifying agent nozzle and the gasification reactor outlet along the central axis of the gasification reactor. Distance d3 needs to be sufficiently close to the particle flow distance under the required time t3 of the third reaction stage. The axial arrangement spacing of the multi-stage gasifying agent nozzles can be determined according to the following rule: the time required for biomass particles to flow from the nth stage nozzle to the (n+1)th stage nozzle is equal to the chemical transformation characteristic time (t) of the reaction stage (oxidation / reduction / reforming) corresponding to the gasifying agent of the nth stage nozzle. 反应 ).

[0037] Computational fluid dynamics (CFD) is used to determine the particle flow trajectory and time distribution, optimizing the nozzle spacing. For example, assuming the total residence time of biomass particles in the gasification reactor is 5 seconds: the gasifying agent needs to be injected at the 1st second (oxidation), 3rd second (reduction), and 4.5th second (reforming) after the particles enter. If the particle velocity is 0.2 m / s, then: the spacing between oxygen gasifying agent nozzle A1 and steam gasifying agent nozzle A2 = (3s - 1s) × 0.2m / s = 0.4m (40cm); the spacing between steam gasifying agent nozzle A2 and carbon dioxide gasifying agent nozzle A3 = (4.5s - 3s) × 0.2m / s = 0.3m (30cm). Matching nozzle position with residence time essentially reflects the time dimension (reaction process) through spatial layout (axial spacing), ensuring that the gasifying agent is precisely introduced when biomass particles undergo key stages such as pyrolysis, oxidation, reduction, and reforming. This synchronizes the timing of gasifying agent injection with the reaction process, thereby optimizing the composition of syngas (e.g., H2 / CO≈2) and improving energy efficiency.

[0038] In one possible implementation, the plurality of vaporizing agents includes at least: oxygen, water vapor, and carbon dioxide; The plurality of vaporizing agent nozzles include at least one or more oxygen vaporizing agent nozzles, one or more water vapor vaporizing agent nozzles, and one or more carbon dioxide vaporizing agent nozzles.

[0039] Specifically, each nozzle is equipped with an independent oxygen storage tank, steam generator, or carbon dioxide storage tank.

[0040] In one possible implementation, the oxygen vaporizing agent nozzle is located below the feed inlet at the bottom of the vaporization reactor; The water vapor gasifying agent nozzle is positioned at a higher height than the oxygen gasifying agent nozzle in the gasification reactor, and the carbon dioxide gasifying agent nozzle is positioned at a higher height than the water vapor gasifying agent nozzle in the gasification reactor. This forms a three-stage gasification nozzle structure with the oxygen gasifying agent nozzle, the water vapor gasifying agent nozzle, and the carbon dioxide gasifying agent nozzle arranged axially along the central axis of the gasification reactor. This allows for directional control of syngas through a multi-stage axial gasifying agent injection system designed in conjunction with the biomass residence time (by injecting oxygen, water vapor, and carbon dioxide in stages axially).

[0041] like Figure 1 As shown, after entering the gasification section, multiple stages of gasifying agent nozzles are arranged axially: different gasifying agents (oxygen, water vapor, and carbon dioxide) are injected respectively. The oxygen gasifying agent nozzle is located at the bottom of the gasification reactor, the water vapor gasifying agent nozzle is located in the middle of the gasification reactor, and the carbon dioxide gasifying agent nozzle is located at the top of the gasification reactor. Thus, by arranging multiple stages of nozzles along the central axis of the gasification reactor (the main direction of material flow), the gasification reaction is optimized step by step through spatial gradation, achieving precise control of H2 / CO.

[0042] In one possible implementation, the gasification reactor further includes a plurality of temperature sensors located below each of the gasifying agent nozzles and at the outlet of the gasification reactor. The oxygen vaporizing agent nozzle is equipped with an oxygen flow regulating valve group, which is linked to an oxygen flow meter to adjust the gas flow rate of the oxygen vaporizing agent nozzle according to the temperature feedback from the temperature sensor.

[0043] Specifically, the temperature sensor can be composed of K-type thermocouples (accuracy ±1℃), which can collect real-time temperature data every 30 seconds. Each vaporizing agent nozzle is equipped with a corresponding temperature measuring device to monitor the initial temperature of each vaporizing agent. Oxygen is injected through the bottom nozzle (oxygen vaporizing agent nozzle 3), and an oxygen flow regulating valve assembly is configured to initiate partial combustion to provide heat. The control method is: an electric regulating valve linked to an oxygen flow meter (0-50 L / min), dynamically adjusted based on temperature feedback. The bottom nozzle is located at the initial position (0 seconds) when the particles enter the gasification reactor, injecting oxygen to match the immediate heat demand of the oxidation stage. For example, the oxygen vaporizing agent nozzle 3 can be located above the lowest gas distribution plate of reactor 2, with a vertical distance of 50-100 mm from the gas distribution plate (ensuring uniform oxygen diffusion to the fluidized bed), and an injection velocity of 20-30 m / s (ensuring penetration of the fluidized bed and avoiding localized oxygen deficiency).

[0044] In one possible implementation, the steam vaporizer nozzle is equipped with a steam generator and a flow control unit, through which the gas flow rate of the steam vaporizer nozzle is regulated.

[0045] Specifically, steam (180-200℃) is injected into the middle nozzle (steam vaporizer nozzle 4), connected to the steam generator and flow control unit, to promote the water-gas reaction (C+H2O→CO+H2), i.e., the second reaction stage. The control method is: the steam generator pressure (0.5-1.0MPa) and flow rate (0-30 L / min) are matched with the gasification demand in real time. For example, the middle nozzle is 10-20cm away from the bottom nozzle (corresponding to 1-2 seconds after particle flow) when steam is injected to match the peak period of the reduction reaction.

[0046] In one possible implementation, the gasification reactor is further equipped with a gas chromatograph and an infrared sensor at the outlet pipe for real-time detection of the actual molar ratio of H2 and CO in the generated target synthesis gas; for example, the sampling frequency of the gas chromatograph and the infrared sensor can be to collect the concentrations of H2, CO, and CO2 and the H2 / CO ratio once every 30 seconds.

[0047] The carbon dioxide vaporizer nozzle is equipped with a proportional-integral valve to adjust the gas flow rate of the carbon dioxide vaporizer nozzle according to the actual molar ratio.

[0048] Specifically, carbon dioxide is injected through the upper nozzle (carbon dioxide vaporizing agent nozzle 5), and an external carbon dioxide storage tank and flow regulation device are provided to adjust the H2 / CO ratio. The control method is as follows: a proportional-integral valve regulates the CO2 flow rate (0-20 L / min), combined with online gas analysis for dynamic optimization. For example, CO2 is injected 10-20 cm away from the middle nozzle (after 3-4 seconds of particle flow) to match the final state ratio adjustment requirements.

[0049] In one possible implementation, the central axis of the gasifying agent nozzle for gasifying agent injection forms a 30° angle with the tangential direction of the inner wall of the reactor.

[0050] Specifically, designing the gasifying agent nozzle with a 30° angled spray can enhance the mixing efficiency between the gasifying agent and the material.

[0051] The control system proposed in this application boasts high energy utilization efficiency. Through a two-stage reaction unit thermal coupling design, energy efficiency is enhanced. The reaction path is optimized via a temperature gradient: the primary fluidized bed, i.e., the pyrolysis reactor (400-500℃), focuses on biomass pyrolysis, achieving efficient separation of biochar, bio-oil, and syngas through low-temperature pyrolysis (biochar ash content <5%, fixed carbon >60%); the secondary fluidized bed, i.e., the gasification reactor (700-800℃), focuses on gasification. The high-temperature environment promotes the water-gas reaction (C+H2O→CO+H2) and CO2 reforming (CO2+C→2CO), improving the biomass pyrolysis gasification effect and resulting in high calorific value syngas. Methanol synthesis requires H2 / CO≈2; by injecting different gasifying agents, dynamic matching and precise H2 / CO control eliminate the need for additional conversion reaction units in traditional processes, saving on additional equipment investment. Furthermore, its versatility in raw material application is enhanced. For different biomass materials such as straw (C / H≈0.6) and sawdust (C / H≈0.8), by adjusting the gasifying agent flow rate (e.g., increasing the steam flow rate by 10%-15% for sawdust), the H2 / CO ratio can be stably controlled at 2.0±0.1. This solves the problem of large ratio fluctuations (±15%) during traditional single-agent gasification (such as steam), making it particularly suitable for large-scale treatment of various agricultural and forestry wastes. A portion of the captured CO2 is used for gasifying agent recycling, reducing carbon emissions by 30%.

[0052] The various embodiments in this specification are described in a progressive manner, with each embodiment focusing on the differences from other embodiments. The same or similar parts between the various embodiments can be referred to each other.

[0053] Finally, it should be noted that in this document, relational terms such as "first" and "second" are used only to distinguish one entity or operation from another, and do not necessarily require or imply any such actual relationship or order between these entities or operations. Furthermore, the terms "comprising," "including," or any other variations thereof are intended to cover non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements includes not only those elements but also other elements not expressly listed, or elements inherent to such a process, method, article, or apparatus. Without further limitations, an element defined by the phrase "comprising one..." does not exclude the presence of other identical elements in the process, method, article, or apparatus that includes said element.

[0054] The above provides a detailed description of a biomass gasification reactor provided in this application. Specific examples have been used to illustrate the principles and implementation methods of this application. The descriptions of the above embodiments are only for the purpose of helping to understand the method and core ideas of this application. At the same time, for those skilled in the art, there will be changes in the specific implementation methods and application scope based on the ideas of this application. Therefore, the content of this specification should not be construed as a limitation of this application.

[0055] Other embodiments of this application will readily occur to those skilled in the art upon consideration of the specification and practice of the invention disclosed herein. This application is intended to cover any variations, uses, or adaptations of this application that follow the general principles of this application and include common knowledge or customary techniques in the art not disclosed herein. The specification and examples are to be considered exemplary only, and the true scope and spirit of this application are indicated by the following claims.

[0056] It should be understood that this application is not limited to the precise structure described above and shown in the accompanying drawings, and various modifications and changes can be made without departing from its scope. The scope of this application is limited only by the appended claims.

[0057] The terms "an embodiment," "embodiment," or "one or more embodiments" as used herein mean that a particular feature, structure, or characteristic described in connection with an embodiment is included in at least one embodiment of this application. Furthermore, please note that the examples of the phrase "in one embodiment" do not necessarily all refer to the same embodiment.

[0058] Numerous specific details are set forth in the specification provided herein. However, it will be understood that embodiments of this application may be practiced without these specific details. In some instances, well-known methods, structures, and techniques have not been shown in detail so as not to obscure the understanding of this specification.

[0059] In the claims, any reference signs placed between parentheses should not be construed as limiting the claims. The word "comprising" does not exclude the presence of elements or steps not listed in the claims. The word "a" or "an" preceding an element does not exclude the presence of a plurality of such elements. This application can be implemented by means of hardware comprising several different elements and by means of a suitably programmed computer. In a unit claim enumerating several means, several of these means may be embodied by the same item of hardware. The use of the words first, second, and third, etc., does not indicate any order. These words can be interpreted as names.

[0060] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of this application, and are not intended to limit them. Although this application has been described in detail with reference to the foregoing embodiments, those skilled in the art should understand that modifications can still be made to the technical solutions described in the foregoing embodiments, or equivalent substitutions can be made to some of the technical features. Such modifications or substitutions do not cause the essence of the corresponding technical solutions to deviate from the spirit and scope of the technical solutions of the embodiments of this application.

Claims

1. A biomass gasification reaction apparatus, characterized by comprising: The reaction device comprises: a pyrolysis reactor for pyrolyzing a biomass raw material to obtain a pyrolysis product, the pyrolysis product comprising bio-oil and initial synthesis gas; a gasification reactor for gasifying the pyrolysis product by using a plurality of gasification agents to obtain target synthesis gas, the target synthesis gas comprising H2 and CO; wherein the gasification reactor comprises a multi-stage gasification agent nozzle module; the multi-stage gasification nozzle module comprises a plurality of gasification agent nozzles, each of which is used to inject a gasification agent into the gasification reactor; the plurality of gasification agent nozzles are arranged axially along the central axis of the gasification reactor; and the gasification agent nozzles injecting the same kind of gasification agent are located at the same height of the gasification reactor.

2. The biomass gasification reaction apparatus according to claim 1, wherein Each stage of the gasification agent nozzle corresponds to a gasification agent, and each gasification agent participates in a reaction stage in the gasification reaction; the axial arrangement spacing of each stage of the gasification agent nozzle matches the particle flow distance under the required time of the corresponding reaction stage; wherein the axial arrangement spacing represents the spacing of the gasification agent nozzle and the adjacent next stage of the gasification agent nozzle along the central axis of the gasification reactor; and the particle flow distance refers to the distance generated by the movement of the reactant along the central axis of the gasification reactor within a limited time.

3. The biomass gasification reaction apparatus according to claim 1, wherein The plurality of gasification agents at least comprises oxygen, steam and carbon dioxide; The plurality of gasification agent nozzles at least comprises one or more oxygen gasification agent nozzles, one or more steam gasification agent nozzles, and one or more carbon dioxide gasification agent nozzles.

4. The biomass gasification reaction apparatus according to claim 3, wherein The oxygen gasification agent nozzle is located below the feed inlet at the bottom of the gasification reactor; The position height of the steam gasification agent nozzle in the gasification reactor is higher than the position height of the oxygen gasification agent nozzle, and the position height of the carbon dioxide gasification agent nozzle in the gasification reactor is higher than the position height of the steam gasification agent nozzle, so that the oxygen gasification agent nozzle, the steam gasification agent nozzle and the carbon dioxide gasification agent nozzle form a three-stage gasification nozzle structure arranged axially along the central axis of the gasification reactor.

5. The biomass gasification reaction apparatus according to claim 3, wherein The gasification reactor further comprises a plurality of temperature sensors, which are located at a position below each of the gasification agent nozzles and at an outlet position of the gasification reactor; The oxygen gasification agent nozzle is configured with an oxygen flow adjusting valve group, which is linked with an oxygen flow meter, for adjusting the gas flow of the oxygen gasification agent nozzle according to the temperature feedback of the temperature sensor.

6. The biomass gasification reaction apparatus according to claim 3, wherein The steam gasification agent nozzle is configured with a steam generator and a flow control unit, and the gas flow of the steam gasification agent nozzle is regulated by the steam generator and the flow control unit.

7. The biomass gasification reaction apparatus according to claim 3, wherein The gasification reactor is further configured with a gas chromatograph and an infrared sensor at the outlet pipe, for real-time detection of the actual molar ratio of H2 and CO in the generated target synthesis gas; The carbon dioxide gasification agent nozzle is configured with a proportional integral valve, for adjusting the gas flow of the carbon dioxide gasification agent nozzle through the proportional integral valve according to the actual molar ratio.

8. The biomass gasification reaction apparatus according to claim 1, wherein The center axis of the gasification agent nozzle for gasification agent injection forms a 30° angle with the tangential direction of the inner wall of the reactor.

9. The biomass gasification reaction apparatus according to claim 1, wherein The device further comprises a cyclone separator, an inlet pipe on the sidewall of the cyclone separator being in communication with an outlet pipe at the top of the pyrolysis reactor, and an outlet pipe at the top of the cyclone separator being in communication with an inlet pipe of the gasification reactor; The cyclone separator is used to separate the bio-oil generated in the pyrolysis reactor and the initial synthesis gas, and deliver them to the gasification reactor.

10. The biomass gasification reaction apparatus according to claim 9, wherein A spiral discharger is arranged at the bottom of the pyrolysis reactor, and a bottom pipe of the cyclone separator is in communication with the bottom of the pyrolysis reactor, so as to deliver the separated biochar to the spiral discharger and discharge the biochar through the spiral discharger.

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