Biomass hydrogen production reduction reactor and chemical looping hydrogen production system

Abstract

The utility model relates to a biomass hydrogen production reduction reactor and a chemical looping hydrogen production system, the biomass hydrogen production reduction reactor comprises a reactor body, the interior of the reactor body comprises a top moving bed reaction layer, a middle material mixing layer and a bottom moving bed reaction layer; an oxygen carrier feed port and a produced hydrogen outlet are formed in the top of the reactor body, an oxygen carrier entering the reactor body forms an oxygen carrier material layer through supporting of a material distribution plate, and a blanking assembly is arranged between the material distribution plate and the middle material mixing layer; the reactor body is provided with a biomass feed inlet at the position of the middle material mixing layer, the middle material mixing layer is used for contacting and mixing the blanked oxygen carrier and the fed biomass, and the mixed material is blanked to the bottom moving bed reaction layer after passing through the mixing assembly. According to the utility model, the biomass and the oxygen carrier can be uniformly mixed, so that the biomass reaction is more thorough and complete.

Description

Technical Field

[0001] This application relates to the field of energy and chemical technology, and more specifically, to a biomass hydrogen production reduction reactor and a chemical looping hydrogen production system. Background Technology

[0002] Biomass is characterized by its wide distribution, low pollution, high reserves, and carbon neutrality. Biomass utilization pathways include bioconversion methods such as fermentation, and thermochemical conversion methods such as pyrolysis, gasification, and combustion. However, thermochemical conversion methods for biomass suffer from problems such as tar production, high energy consumption, low product calorific value, and low utilization rates, which hinder the further development of biomass resource utilization.

[0003] The mainstream approach to hydrogen production combining biomass gasification and chemical looping employs separate gasification reactors and hydrogen production reactors, or two chambers within the same reactor separated by a perforated partition. Biomass pretreatment is typically not performed. The gasification reactor is generally in a fluidized state with strong backmixing. The generated gas is primarily syngas. Large gas volumes result in significant consumption for gas separation and purification. High reaction temperatures easily lead to the formation of difficult-to-treat substances such as tar.

[0004] CN103672873A discloses a continuously operating solid fuel chemical looping reaction system. The chemical looping fuel reactor is internally divided by porous baffles. The upper part of the porous baffles is a moving bed fuel reactor for oxygen carrier reduction, and the lower part is a sputtered bed reactor for solid fuel gasification. The gas from the solid fuel gasification in the sputtered bed reactor passes through the porous baffles to reduce the oxygen carrier in the moving bed reactor. However, the system suffers from low reaction efficiency and low thermal utilization. Furthermore, the flow of oxygen carrier between reactors is achieved through a screw conveyor, which is difficult to withstand the high temperatures of the oxygen carrier.

[0005] In other existing hydrogen production systems that can withstand the high temperatures of oxygen carriers, the oxygen carriers are not directly mixed and in contact with biomass, making it difficult to guarantee the mass and heat transfer efficiency of the reaction and limiting the production of hydrogen. Utility Model Content

[0006] The purpose of this application is to provide a biomass hydrogen production reduction reactor and a chemical looping hydrogen production system, which can realize the contact mixing of biomass and oxygen carrier in the form of a moving bed reactor, ensuring uniform mixing of biomass and oxygen carrier. The reduction reactor can reduce the need for a separate biomass gasification reactor, simplify the process flow, and make the biomass reaction more thorough and complete.

[0007] To achieve the above objectives, in a first aspect, this utility model provides a biomass hydrogen production reduction reactor, comprising: a reactor body, wherein the interior of the reactor body includes a top moving bed reaction layer, a middle material mixing layer and a bottom moving bed reaction layer;

[0008] The top of the reactor body is provided with an oxygen carrier inlet and a hydrogen production outlet. The oxygen carrier entering the reactor body forms an oxygen carrier material layer supported by a material distribution plate. A material dropping component is provided between the material distribution plate and the middle material mixing layer.

[0009] The reactor body is provided with a biomass inlet in the middle material mixing layer. The middle material mixing layer is used to mix the oxygen carrier after it is fed with the biomass. The mixed material is fed to the bottom moving bed reaction layer after passing through the mixing component.

[0010] In an optional embodiment, the fabric plate is disposed on the radially inner side of the top moving bed reaction layer and located at the bottom of the oxygen carrier material layer, and the fabric plate is evenly distributed with air vents.

[0011] The material plate includes an integrally structured conical section and a straight section. The conical section is used to support the oxygen carrier material layer, and the annular gap between the straight section and the reactor body constitutes the material drop gap of the oxygen carrier material layer.

[0012] The conical section and the straight section are concentrically arranged with the reactor body, and the angle between the conical section and the horizontal plane is not less than the angle of repose of the oxygen carrier.

[0013] In an optional embodiment, the material feeding assembly includes a material feeding ring disposed below the straight section, the material feeding ring being connected to the inner wall of the reactor body and having at least a height difference with the bottom end of the straight section;

[0014] The inner edge of the material drop ring protrudes inward from the side wall of the straight section, and the oxygen carrier is dropped through the gap between the bottom end of the straight section and the inner edge of the material drop ring.

[0015] In an optional embodiment, a top steam inlet is provided at the bottom of the top moving bed reaction layer of the reactor body, and the connecting bottom edge of the top steam inlet on the reactor body is located below the bottom end of the straight section.

[0016] In an optional embodiment, the biomass inlet is located above the middle material mixing layer, and the mixing assembly is located in the middle material mixing layer, including mixing collision rollers that are stacked in the axial direction and diverge and intersect in the radial direction.

[0017] In an optional embodiment, the mixing collision rollers include multiple sets, which are arranged at intervals along the axial direction of the reactor body. A support column is vertically arranged at the center of the reactor body in the middle material mixing layer. Each set of mixing collision rollers includes an inner mixing roller connected to the support column and an outer mixing roller connected to the side wall of the reactor body.

[0018] In an optional implementation, the outer mixing rod in each group of mixing collision rods comprises two layers of different lengths, with each layer of the outer mixing rod having the same length.

[0019] In an optional embodiment, the reactor body includes a straight cylinder and a conical cylinder. The middle material mixing layer is located in the upper middle part of the straight cylinder, and the bottom moving bed reaction layer is located in the lower middle part of the straight cylinder and the conical cylinder. The reactor body is provided with a bottom steam inlet at the bottom of the straight cylinder, and the bottom of the conical cylinder is provided with a solid material outlet for supplying oxygen carrier and discharging biomass ash.

[0020] In an optional embodiment, the reactor body is provided with a material plate support and a support column support to support and fix the material plate and the support column respectively.

[0021] Secondly, this utility model provides a chemical chain hydrogen production system, including an air oxidation reactor, a hydrogen purification device, a biomass storage silo, an oxygen carrier lifting device, and a biomass hydrogen production reduction reactor as described in any of the foregoing embodiments.

[0022] The biomass hydrogen production reduction reactor and chemical looping hydrogen production system of this invention enable the oxygen carrier and biomass materials to undergo solid-solid co-current contact mixing, ensuring the mass and heat transfer efficiency of the contact mixing reaction. Simultaneously, the gas-solid counter-current moving bed configuration allows for sufficient reaction between the oxygen carrier and the gasified gas from biomass gasification, guaranteeing the reaction efficiency of the hydrogen production reduction reaction.

[0023] The placement of the feeding plate serves two purposes: firstly, it provides effective support for the oxygen carrier material layer; secondly, it allows the gas to be distributed more evenly in the top moving bed reaction layer, thereby enabling a more complete reduction reaction of the oxygen carrier.

[0024] The feeding assembly allows the oxygen carrier entering from the top to be fed in an orderly manner from the top moving vehicle reaction layer to the middle material mixing layer, avoiding the retention of the oxygen carrier in the oxygen carrier layer and facilitating better mixing of the oxygen carrier with the biomass pellets in the middle material mixing layer.

[0025] By incorporating the mixing components, the compressed state of biomass can be dispersed into fragmented materials, facilitating more uniform mixing with the oxygen carrier and thus enabling a more complete reaction.

[0026] Compared with existing reactor types, this invention has the technical characteristics of simple structure, low failure rate, uniform solid-solid mixing, and low investment.

[0027] Other features and advantages of this application will be described in detail in the following detailed description section. Attached Figure Description

[0028] To more clearly illustrate the technical solutions of the embodiments of this application, the accompanying drawings used in the embodiments will be briefly introduced below. It should be understood that the following drawings only show some embodiments of this application and should not be regarded as a limitation of the scope. For those skilled in the art, other related drawings can be obtained based on these drawings without creative effort.

[0029] Figure 1 This is a schematic diagram of the biomass hydrogen production reduction reactor in this application;

[0030] Figure 2 for Figure 1 Schematic diagram of the cross-sectional structure of the AA section;

[0031] Figure 3 for Figure 1 Schematic diagram of the cross-sectional structure of the middle BB section;

[0032] Figure 4 for Figure 1 A schematic diagram of the cross-sectional structure of the CC region;

[0033] Figure 5 for Figure 1 A schematic diagram of the cross-sectional structure of the DD region.

[0034] icon:

[0035] 1-Reactor body; 1a-Top moving bed reaction layer; 1b-Middle material mixing layer; 1c-Bottom moving bed reaction layer; 11-Oxygen carrier inlet; 12-Hydrogen production outlet; 13-Biomass inlet; 14-Top steam inlet; 15-Support column; 16-Bottom steam inlet; 17-Solid material outlet;

[0036] 2-Fabric plate; 21-Conical section; 22-Straight section;

[0037] 3-Feeding ring;

[0038] 4-Mixed impact rod; 41-Inner mixed impact rod; 42-Outer mixed impact rod;

[0039] 10-Straight body cylinder; 20-Conical body cylinder; 30-Fabric plate support; 40-Support column support. Detailed Implementation

[0040] To make the objectives, technical solutions, and advantages of the embodiments of this application clearer, the technical solutions of 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, and not all embodiments. The components of the embodiments of this application described and shown in the accompanying drawings can generally be arranged and designed in various different configurations.

[0041] In the description of this application, it should be noted that the terms "inner" and "outer," etc., indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings, or the orientation or positional relationship commonly used when the product is in use. They are used only for the convenience of describing this application and for simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on this application. Furthermore, the terms "first," "second," etc., are used only to distinguish descriptions and should not be construed as indicating or implying relative importance.

[0042] In the description of this application, it should also be noted that, unless otherwise expressly specified and limited, the terms "setup" and "connection" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral connection; they can refer to a direct connection or an indirect connection through an intermediate medium; and they can refer to the internal connection of two components. Those skilled in the art can understand the specific meaning of the above terms in this application based on the specific circumstances.

[0043] The biomass hydrogen production reduction reactor in this application is specifically a moving bed reactor, which mainly carries out chemical chain biomass hydrogen production by oxygen carrier and biomass. By setting up necessary material feeding structure and mixing structure, the solid-solid co-flow contact mixing of oxygen carrier and biomass particles is ensured, as well as the uniformity of contact mixing.

[0044] See Figure 1 The biomass hydrogen production reduction reactor provided in this utility model includes a reactor body 1. The reactor body 1 is the main structure of chemical chain biomass hydrogen production and mainly includes a top moving bed reaction layer 1a, a middle material mixing layer 1b and a bottom moving bed reaction layer 1c located inside it.

[0045] Specifically, the top moving bed reaction layer 1a is an axially flowing moving bed with gas-solid countercurrent flow, the bottom moving bed reaction layer 1c is an axially flowing moving bed with gas-solid countercurrent flow and solid-solid cocurrent flow, and the middle material mixing layer 1b is a spaced structure layer that provides mixing space for the reactants. The reaction spaces of the three parts are interconnected.

[0046] The top moving bed reaction layer 1a is specifically used for the reduction hydrogen production reaction of oxygen carrier and part of biomass gasification gas. The middle material mixing layer 1b is specifically used for solid-solid contact mixing of oxygen carrier and biomass. The mixing components of the middle material mixing layer 1b make the mixing of oxygen carrier and biomass more uniform. The bottom moving bed reaction layer 1c is specifically used for the main gasification reaction of biomass and the reduction hydrogen production reaction of oxygen carrier and biomass gasification gas.

[0047] The top of the reactor body is provided with an oxygen carrier inlet 11 and a hydrogen production outlet 12. The oxygen carrier inlet 11 is specifically used to introduce oxygen carrier into the reactor body, while the hydrogen production outlet 12 is mainly used to export the hydrogen produced inside the reactor body 1.

[0048] The oxygen carrier enters the reactor body 1 through the oxygen carrier inlet 11 and is supported by a distribution plate 2 located at the top of the reactor body. This distribution plate forms the oxygen carrier material layer of the top moving bed reaction layer 1a. The distribution plate 2 has evenly distributed perforations, allowing the biomass gas to pass through and react with the oxygen carrier in a reduction reaction. The even distribution of perforations on the distribution plate 2 ensures a more uniform gas distribution and a more complete reduction reaction.

[0049] From the perspective of facilitating the discharge of oxygen carrier and its contact and mixing with biomass pellets in the middle material mixing layer 1b, a discharge assembly is provided between the feeding plate 2 and the middle material mixing layer 1b. The discharge assembly enables the oxygen carrier on the upper part of the feeding plate 2 to flow down at a certain sliding speed, reducing the retention of oxygen carrier in the oxygen carrier material layer, and at the same time helping the biomass pellets and oxygen carrier to mix better.

[0050] From the perspective of introducing biomass materials, the reactor body 1 is provided with a biomass inlet 13 at the middle material mixing layer 1b. The biomass inlet 13 is mainly used to introduce biomass materials into the middle material mixing layer 1b, and after entering the reactor body, it will be mixed with oxygen carrier in solid-solid co-flow contact.

[0051] The middle material mixing layer 1b is used to contact and mix the oxygen carrier after it is dropped with the biomass after it is fed. After the mixed material is uniformly mixed by the mixing component, it is dropped into the bottom moving bed reaction layer 1c.

[0052] The mixing component can effectively break down and disperse the incoming biomass material, transforming it into dispersed fragments that are then uniformly mixed with the oxygen carrier, thereby enabling the biomass gasification reaction to proceed more fully and completely in the bottom moving bed reaction layer 1c.

[0053] In one specific embodiment, the material plate 2 is disposed radially inside the top moving bed reaction layer 1a and at the bottom of the oxygen carrier material layer, which can realize the bottom support of the oxygen carrier material layer and the dropping of the oxygen carrier.

[0054] Furthermore, the material distribution plate 2 includes an integrally structured conical section 21 and a straight section 22. The conical section 21 is used to support the oxygen carrier material layer, and the annular gap between the straight section 22 and the reactor body 1 constitutes the material drop gap of the oxygen carrier material layer. The oxygen carrier particles can slide down to the middle material mixing layer 1b through the material drop gap.

[0055] In order to ensure a stable oxygen carrier layer in the center of the reactor and to allow the oxygen carrier particles in the oxygen carrier layer to slide in the circumferential direction, the conical section 21 and the straight section 22 are concentrically arranged with the reactor body 1. Furthermore, in order to enable the oxygen carrier to slide dynamically at a certain speed, the angle between the conical section 21 and the horizontal plane is not less than the angle of repose of the oxygen carrier, so that the oxygen carrier particles can slide orderly into the above-mentioned falling gap, thereby controlling the falling speed of the oxygen carrier and mixing the oxygen carrier and biomass.

[0056] The material feeding assembly of this utility model includes a material feeding ring 3 disposed below the straight section 22. The material feeding ring 3 is connected to the inner wall of the reactor body 1 and has at least a height difference with the bottom of the straight section 22. With this arrangement, an annular material feeding gap can be formed between the bottom of the straight section 22 and the material feeding ring 3, ensuring that the oxygen carrier is fed into the middle material mixing layer 1b through the material feeding gap.

[0057] Specifically, the feeding ring 3 is an annular plate structure. The outer edge of the feeding ring 3 is connected to the inner wall of the reactor body 1, and the inner edge of the feeding ring 3 protrudes inward from the side wall of the straight section 22. The oxygen carrier is fed through the gap between the bottom end of the straight section 22 and the inner edge of the feeding ring 3. In the gap, because the inner edge of the feeding ring 3 protrudes inward from the side wall of the straight section 22, the oxygen carrier particles can be fed in a radially inward trend towards the reactor body 1, so as to fully contact the mixing components.

[0058] In order to ensure that the oxygen carrier particles can be stably fed, a top steam inlet 14 is provided at the bottom of the top moving bed reaction layer 1a of the reactor body 1. The top steam inlet 14 is mainly used to fill the upper part of the reactor body 1 with steam.

[0059] The introduction of water vapor can chemically inhibit the oxidation reaction that produces water during hydrogen production, thus ensuring the hydrogen conversion rate.

[0060] From a physical perspective, it can effectively spray oxygen carrier particles in the gap between the falling materials, ensuring the orderly falling of the oxygen carrier.

[0061] Based on this, the top steam inlet 14 is connected to the bottom edge of the reactor body 1 at the lower part of the bottom of the straight section 22. Combined with the evenly distributed air holes on the distribution plate 2, after the oxygen carrier particles are sprayed, the steam can pass through the distribution plate 2 and enter the radial inner side of the straight section 22 of the distribution plate 2. Then, it enters the top moving bed reaction layer 1a with the airflow, thus exerting the above-mentioned effect of inhibiting hydrogen oxidation reaction.

[0062] From the perspective of introducing biomass materials, the biomass inlet 13 is located above the middle material mixing layer 1b, and can be mixed with the oxygen carrier particles that slide down.

[0063] Mechanistically, the biomass material entering the reactor body is converted into gaseous gas, which is easily decomposed small molecules and flows upward to the oxygen carrier layer inside the reactor body to carry out a partial reduction hydrogen production reaction.

[0064] Large-molecule biomass that is not easily decomposed mixes with the oxygen carrier that falls with the sliding material, and finally falls to the bottom moving bed reaction layer 1c to carry out the main gasification reaction and reduction hydrogen production reaction.

[0065] It should also be noted that, along with the dynamic sliding descent of the oxygen carrier and its mixing with biomass materials in the middle material mixing layer 1b, the reduction hydrogen production reaction actually runs through the entire internal space of the reactor body.

[0066] Specifically, from the perspective of material mixing, in another specific embodiment, a mixing component is arranged in the middle material mixing layer 1b, mainly for mixing biomass materials and oxygen carrier. The mixing component includes mixing collision rollers 4 stacked in the axial direction of the reactor body and radially diverging and interlacing. The biomass materials can be broken down and dispersed into fragments by the mixing collision rollers 4, which facilitates more uniform mixing with the oxygen carrier and ensures the completeness of biomass gasification and reduction hydrogen production reactions.

[0067] The definition of the hybrid collision rod 4 is mainly based on its role in collision and mixing; see [link to relevant documentation]. Figures 2-5 The mixing collision rollers 4 in the middle material mixing layer 1b include multiple sets. The multiple sets of mixing collision rollers 4 are arranged at intervals along the axial direction of the reactor body 1. A support column 15 is vertically arranged at the center of the reactor body 1 located in the middle material mixing layer 1b. Each set of mixing collision rollers 4 includes an inner mixing roller 41 connected to the vertical support column 15 and an outer mixing roller 42 connected to the side wall of the reactor body 1.

[0068] This configuration allows for the formation of a tree-like structure of varying heights and lengths in the three-dimensional space of the central material mixing layer 1b. This static structure promotes the decomposition of biomass materials and the uniform mixing of oxygen carriers and biomass materials.

[0069] In this embodiment, the inner mixing rod 41 of each group of mixing collision rods 4 is located on the top layer, and the outer mixing rod 42 includes two layers of different lengths. The length of each outer mixing rod 42 is the same, and it is located below the inner mixing rod 41.

[0070] To enhance the collision mixing effect, the inner mixing rod 41 and the outer mixing rod 42, as well as the two layers of outer mixing rods 42, are arranged in a radially divergent and interwoven state.

[0071] It should be noted that this application does not limit the above-mentioned arrangement. In practical applications, the actual settings can be made according to the specific working conditions, and the requirements of collision and mixing of biomass materials and oxygen carriers need to be met.

[0072] The reactor body 1 includes a straight cylinder 10 and a conical cylinder 20. The middle material mixing layer 1b is located in the upper middle part of the straight cylinder 10, and the bottom moving bed reaction layer 1c is located in the lower middle part of the straight cylinder 10 and the conical cylinder 20. This ensures that sufficient reaction space is provided for the main gasification reaction and reduction hydrogen production reaction of biomass materials, ensuring that the biomass materials are fully and thoroughly reacted and ensuring the hydrogen production rate.

[0073] The reactor body 1 is located at the bottom of the main body cylinder 10 and is equipped with a bottom steam inlet 16, which can introduce steam into the bottom of the main body cylinder 10, so that the biomass material can be gasified under the catalytic effect of the reduced oxygen carrier and under water-rich conditions. As the oxygen carrier slowly moves downward, the biomass is gradually and completely gasified.

[0074] The bottom of the main cone 20 is provided with a solid material outlet 17 for supplying oxygen carrier and discharging biomass ash, which can guide the completely reacted biomass ash and oxygen carrier out of the reactor body.

[0075] In this embodiment, a material plate support 30 and a support column support 40 are provided inside the reactor body 1 to support and fix the material plate 2 and the support column 15 respectively, so as to ensure structural stability and reliability.

[0076] This invention also provides a chemical chain hydrogen production system, including an air oxidation reactor, a hydrogen purification device, a biomass storage silo, an oxygen carrier lifting device, and a biomass hydrogen production reduction reactor as described in any of the foregoing embodiments.

[0077] Chemical chain hydrogen production systems fall under the category of energy and chemical engineering, involving the utilization of biomass resources. Chemical chain gas-solid and solid-solid reaction hydrogen production can ensure mass and heat transfer in the reaction and produce high hydrogen yield.

[0078] The chemical chain hydrogen production system of this invention uses a moving bed axial flow reactor to achieve direct contact reaction between biomass and oxygen carrier to produce hydrogen. It employs a unique feeding component and mixing component to uniformly mix solid oxygen carrier and biomass.

[0079] The reduction of separate biomass gasification reactors simplifies the process of biomass-to-hydrogen production and makes the biomass reaction more complete.

[0080] In general, the biomass hydrogen production reduction reactor is equipped with an oxygen carrier inlet 11 and a hydrogen production outlet 12 at the top. The oxygen carrier inlet is connected to the oxygen carrier outlet of the air oxidation reactor in the chemical loop hydrogen production system, and the hydrogen production outlet 12 is connected to the hydrogen purification device.

[0081] The top moving bed reaction layer 1a and the middle material mixing layer 1b are separated by a material distribution plate 2 with ventilated holes. The oxygen carrier falls into the middle material mixing layer 1b of the reactor through the material dropping assembly.

[0082] The reactor is equipped with a top steam inlet 14, a biomass feed inlet 13 and a mixing component in the middle. The biomass feed inlet 13 is connected to a biomass storage bin, and the stored material in the biomass storage bin is pre-treated biomass pellets.

[0083] Steam carries oxygen carrier particles through the material drop gap into the middle of the reactor. Through the mixing component, the biomass disintegrates and mixes with the oxygen carrier. The lower part of the reduction reactor is equipped with a bottom steam inlet 16 and a solid material outlet 17. The solid material outlet 17 is connected to the oxygen carrier lifting device of the chemical loop hydrogen production system.

[0084] During the reaction, the oxygen carrier is blown into the middle of the reduction reactor by water vapor at about 100°C. The biomass particles inside the reactor are partially gasified, and the gasified gas enters the upper part of the reduction reactor through the vent to reduce the oxygen carrier.

[0085] Incompletely gasified biomass is broken up and dispersed by a mixing component, mixed with the oxygen carrier, and then falls to the bottom of the reactor. Under the catalytic action of the reduced oxygen carrier and in water-rich conditions, the biomass undergoes gasification. As the oxygen carrier slowly moves downwards, the biomass gradually becomes completely gasified. The reaction time in the reduction hydrogen production reactor is 40-60 minutes at 500-800℃.

[0086] It should be noted that, where there is no conflict, the features in the embodiments of this application can be combined with each other.

[0087] The above description is merely a preferred embodiment of this application and is not intended to limit this application. Various modifications and variations can be made to this application by those skilled in the art. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of this application should be included within the protection scope of this application.

Claims

1. A biomass hydrogen reduction reactor, characterized by, The application relates to a reactor body, which comprises a top moving bed reaction layer, a middle material mixing layer and a bottom moving bed reaction layer. The top of the reactor body is provided with an oxygen carrier feeding port and a hydrogen production outlet, the oxygen carrier entering the reactor body is supported by a distribution plate to form an oxygen carrier material layer, the distribution plate is uniformly provided with air permeable holes, and a material falling assembly is arranged between the distribution plate and the middle material mixing layer. The reactor body is provided with a biomass feeding port at the position of the middle material mixing layer, the middle material mixing layer is used for contacting and mixing the oxygen carrier after material falling and the biomass after feeding, and the mixed material falls to the bottom moving bed reaction layer through a mixing assembly. The distribution plate is arranged at the radial inner side of the top moving bed reaction layer and at the bottom of the oxygen carrier material layer.

2. The biomass hydrogen generation reduction reactor according to claim 1, wherein, The distribution plate comprises a conical cylinder section and a straight cylinder section in an integrated structure, the conical cylinder section is used for supporting the oxygen carrier material layer, and the annular gap between the straight cylinder section and the reactor body forms a material falling gap of the oxygen carrier material layer. The conical cylinder section and the straight cylinder section are concentrically arranged with the reactor body, and the included angle between the conical cylinder section and the horizontal plane is not less than the repose angle of the oxygen carrier. The material falling assembly comprises a material falling ring arranged below the straight cylinder section, the material falling ring is connected to the inner wall of the reactor body and has a height difference with the bottom end of the straight cylinder section.

3. The biomass hydrogen generation reduction reactor according to claim 2, wherein, The inner side edge of the material falling ring protrudes inwardly from the side wall of the straight cylinder section, and the oxygen carrier falls through the interval gap between the bottom end of the straight cylinder section and the inner side edge of the material falling ring. The reactor body is provided with a top steam inlet at the position of the bottom of the top moving bed reaction layer, and the connecting bottom edge of the top steam inlet on the reactor body is arranged below the bottom end of the straight cylinder section.

4. The biomass hydrogen generation reduction reactor according to claim 2, wherein, The biomass feeding port is arranged at the upper part of the middle material mixing layer, and the mixing assembly is arranged in the middle material mixing layer and comprises mixing collision rods which are arranged in axial stacking and radial divergence.

5. The biomass hydrogen production reduction reactor according to any one of claims 1-4, wherein, The mixing collision rods comprise multiple groups, the multiple groups of mixing collision rods are arranged at intervals along the axial direction of the reactor body, a support column is vertically arranged at the position of the center of the middle material mixing layer of the reactor body, each group of mixing collision rods comprises an inner mixing rod connected to the support column and an outer mixing rod connected to the side wall of the reactor body.

6. The biomass hydrogen generation reduction reactor according to claim 5, wherein, The outer mixing rod in each group of mixing collision rods comprises two layers with different lengths, and the lengths of the outer mixing rods in each layer are the same.

7. The biomass hydrogen generation reduction reactor according to claim 6, wherein, The reactor body comprises a body straight cylinder and a body conical cylinder, the middle material mixing layer is arranged at the middle upper position of the body straight cylinder, the bottom moving bed reaction layer is arranged at the middle lower position of the body straight cylinder and the body conical cylinder, the reactor body is provided with a bottom steam inlet at the bottom of the body straight cylinder, and the bottom of the body conical cylinder is provided with a solid material discharge outlet for discharging oxygen carrier and biomass ash.

8. The biomass hydrogen generation reduction reactor according to claim 5, wherein, The reactor body is provided with a distribution plate support and a support column support inside to support and fix the distribution plate and the support column respectively.

9. The biomass hydrogen generation reduction reactor according to claim 6, wherein, ​ 10. A chemical looping hydrogen generation system, characterized by, The biomass hydrogen production system comprises an air oxidation reactor, a hydrogen purification device, a biomass storage bin, an oxygen carrier lifting device and the biomass hydrogen production reduction reactor according to any one of claims 1-9.

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