Device for co-producing synthesis gas and hydrogen by integrating biomass chemical chain gasification and water decomposition

Abstract

The invention discloses a device for co-producing synthesis gas and hydrogen by integrating biomass chemical chain gasification and water decomposition, which comprises an oxidation reactor and a gasification reactor, one ends of the oxidation reactor and the gasification reactor are connected through a first cyclone separator, and the other ends of the oxidation reactor and the gasification reactor are connected through a second cyclone separator. The gasification reactor comprises an oxygen carrier reduction reaction zone, a biomass pyrolysis gasification catalytic reaction zone and a hydrogen production reaction zone, the oxygen carrier reduction reaction zone and the biomass pyrolysis gasification catalytic reaction zone are located in the same bubbling fluidized bed reactor, and the hydrogen production reaction zone is a rapid fluidized bed reactor; the biomass pyrolysis gasification catalytic reaction zone is connected with the hydrogen production reaction zone through an overflow structure, the oxygen carrier reduction reaction zone is connected with the first cyclone separator, and the hydrogen production reaction zone is connected with the second cyclone separator. And by optimizing reaction conditions in different regions, the co-production efficiency of the synthesis gas and the hydrogen is improved.

Description

Technical Field

[0001] The present invention relates to the technical field of biomass gasification, and particularly to a device for co-producing syngas and hydrogen by integrating biomass chemical-looping gasification and water splitting. Background Art

[0002] As one of the biomass thermochemical conversion technologies, biomass gasification can convert biomass into gaseous fuel, which is one of the most effective ways to realize the conversion of biomass energy. Traditional biomass gasification technologies use air, steam or oxygen as gasifying agents, and have problems such as high process energy consumption, high cost, low syngas yield and high tar content, which have become the bottleneck and main obstacles restricting the application of biomass gasification technology.

[0003] Biomass chemical-looping gasification is an application of chemical-looping technology in the field of biomass energy utilization. In the fuel reactor, an oxygen carrier is used to supply oxygen and heat for the gasification process to prepare syngas. It can avoid the dilution of syngas by nitrogen in the air, the high cost of pure oxygen preparation process and the high energy consumption of steam gasification, and the oxygen carrier can catalyze the cracking of tar to improve the syngas yield.

[0004] However, traditional biomass gasification technologies have problems such as large tar production, low syngas quality and insufficient hydrogen yield. Although existing chemical-looping gasification technologies can reduce tar through the oxygen carrier cycle, it is difficult to achieve efficient decoupling of gasification and hydrogen production. In addition, the coupling degree of the reduction and oxidation processes of the oxygen carrier in the traditional single-bed reactor is high, resulting in a rapid decline in catalyst activity and limited hydrogen purity. Therefore, there is an urgent need for an integrated device that can optimize reaction conditions in different regions and improve the co-production efficiency of syngas and hydrogen. Summary of the Invention

[0005] The purpose of the present invention is to provide a device for co-producing syngas and hydrogen by integrating biomass chemical-looping gasification and water splitting in order to solve the problems that existing biomass gasification is difficult to achieve efficient decoupling of gasification and hydrogen production, rapid decline in catalyst activity and limited hydrogen purity.

[0006] To achieve the above purpose, the present invention provides the following technical solutions: A device for co-producing syngas and hydrogen by integrating biomass chemical-looping gasification and water splitting, comprising: an oxidation reactor and a gasification reactor, one end of the oxidation reactor and the gasification reactor is connected by a first cyclone separator, and the other end is connected by a second cyclone separator.

[0007] Preferably, the gasification reactor includes an oxygen carrier reduction reaction zone, a biomass pyrolysis gasification catalytic reaction zone, and a hydrogen production reaction zone. The oxygen carrier reduction reaction zone and the biomass pyrolysis gasification catalytic reaction zone are located in the same bubbling fluidized bed reactor. The hydrogen production reaction zone is a fast fluidized bed reactor. The biomass pyrolysis gasification catalytic reaction zone and the hydrogen production reaction zone are connected by an overflow structure. The oxygen carrier reduction reaction zone is connected to a first cyclone separator, and the hydrogen production reaction zone is connected to a second cyclone separator.

[0008] Biomass pyrolysis gasification catalytic reaction zone: Designed with a bubbling fluidized bed, biomass pyrolyzes and gasifies here to generate syngas (CO / H2) and C1-C5 light hydrocarbons / tar (C n H m O z ), and under the catalysis of the oxygen carrier, part of the coke is oxidized to CO. The reaction equations are as follows:

[0009] Biomass → C + C n H m O z + CO + H2;

[0010] C + MeO → MeO 1-x + CO.

[0011] Oxygen carrier reduction reaction zone: Designed with a bubbling fluidized bed, the oxygen carrier in the oxidized state is selectively and deeply reduced by the light hydrocarbons / tar generated by biomass pyrolysis, exposing the metal catalytic surface. At the same time, the hydrocarbons are oxidized to CO2 / H2O or CO / H2O. The reaction equations are as follows:

[0012] MeO + C n H m O z → MeO 1-x + CO / CO2 + H2O.

[0013] Hydrogen production reaction zone: Designed with a fast fluidized bed, the oxygen carrier in the deeply reduced state reacts with H2O to generate high-purity H2 and is regenerated into the oxidized state for recycling. The reaction equation is as follows:

[0014] MeO 1-x + H2O → MeO 1-y + H2.

[0015] Overflow structure: The biomass pyrolysis gasification catalytic zone and the hydrogen production zone are connected by an overflow structure to achieve the directional flow of materials and the oxygen carrier, ensuring the independent optimization of reaction conditions in each zone. Here, differential pressure control is used. The pressure at the overflow port on the side of the gasification reactor is higher than that at the overflow port on the side of the hydrogen production reactor to achieve directional movement.

[0016] Oxygen carrier circulation: The oxygen carrier circulates between the reduction zone and the hydrogen production zone, and its catalytic activity and stability are enhanced through oxidation-reduction reactions.

[0017] The biomass pyrolysis gasification catalytic reaction zone and the oxygen carrier reduction reaction zone are of an integral structure; the lower part of the biomass pyrolysis gasification catalytic reaction zone communicates with the hydrogen production reaction zone through an overflow structure; the hydrogen production reaction zone is separated from the biomass pyrolysis gasification catalytic reaction zone and the oxygen carrier reduction reaction zone by a partition.

[0018] Preferably, the oxygen carrier reduction reaction zone is connected to the first cyclone separator through a first return riser, and the hydrogen production reaction zone is connected to the second cyclone separator through a second return riser.

[0019] Preferably, the oxidation reactor is a fast fluidized bed reactor with a constant diameter column.

[0020] Preferably, a first feed inlet is provided on the side of the lower part of the oxidation reactor, the first feed inlet forms an angle of 45-60° with the horizontal direction, and the first feed inlet is connected to the second return riser.

[0021] Preferably, a second feed inlet is provided at the top of the oxygen carrier reduction reaction zone of the gasification reactor, which forms an angle of 90° with the horizontal direction, and the second feed inlet is connected to the first return riser.

[0022] Preferably, a syngas outlet is provided on the side of the upper part of the oxygen carrier reduction reaction zone, a biomass feed inlet is provided on the side of the lower part of the biomass pyrolysis gasification catalytic reaction zone, a recycle gas inlet is provided at the bottom, and the outlet flue gas enters the gasification reactor through the recycle gas inlet for further conversion; a steam feed inlet is provided at the bottom of the hydrogen production reaction zone.

[0023] Preferably, the gasification reactor is of a constant diameter column structure or a cubic structure.

[0024] The present invention also discloses a method for co-producing syngas and hydrogen by integrating biomass chemical looping gasification and water splitting. Based on the above device, the method includes the following steps:

[0025] In the biomass pyrolysis gasification catalytic reaction zone, while biomass undergoes pyrolysis gasification, syngas (CO / H2) and low-carbon hydrocarbons / tar such as C1-C5 are generated. Under the catalytic action of the oxygen carrier, biomass char is partially oxidized into CO syngas.

[0026] The syngas, low-carbon hydrocarbons, and tar enter the oxygen carrier reduction reaction zone, and the fully oxidized oxygen carrier is selectively deeply reduced by the low-carbon hydrocarbons and tar, exposing the metal catalytic surface, enhancing the catalytic ability, while the low-carbon hydrocarbons / tar are oxidized into CO2 and H2O or CO and H2O.

[0027] Finally, the syngas enters the upper gas flow channel of the oxygen carrier reduction reactor, and part of the gas in the gas pipeline can return to the biomass gasification reaction zone through the recycle fan for recycling;

[0028] The air from the oxidation reactor fluidizes and oxidizes the oxygen carrier material. After that, the oxygen carrier flows through the first return standpipe to the oxygen carrier reduction reaction zone to oxidize part of the low-carbon hydrocarbons and tar generated by the pyrolysis of biomass;

[0029] The reduced oxygen carrier and part of the unreduced oxygen carrier enter the biomass pyrolysis gasification catalytic reaction zone to participate in the catalytic reaction of biomass pyrolysis gasification. Under the catalysis of the oxygen carrier, part of the biomass char can be oxidized into CO syngas;

[0030] The oxygen carrier in the deeply reduced state enters the hydrogen production reaction zone through the overflow structure. In the hydrogen production reaction zone, the oxygen carrier in the deeply reduced state reacts with H2O to produce high-purity H2. Subsequently, the oxygen carrier returns to the oxidation reactor through the second return valve.

[0031] Compared with the prior art, the beneficial effects of the present invention are as follows:

[0032] The design of the sub-region fluidized bed realizes the decoupling of the reaction process through physical isolation and the overflow structure, significantly improving the syngas and hydrogen production rates: In the traditional gasification reactor, the reaction system is complex, and various reactions are intertwined, making it difficult to achieve efficient decoupling of gasification and hydrogen production, resulting in low gasification efficiency. The present invention decouples the traditional single biomass chemical-looping gasification reactor into a biomass gasification reaction zone, an oxygen carrier reduction zone, and a hydrogen production reaction zone, and integrates them into a whole. It realizes the zonal control of oxygen carrier reduction and biomass gasification, and co-produces syngas and hydrogen, effectively avoiding the negative impact of the complex reaction system on the gasification efficiency, and ensuring the high purity of hydrogen through the overflow structure, achieving efficient decoupling of gasification and hydrogen production.

[0033] Through the deep reduction and regeneration mechanism of the oxygen carrier, the tar content is synchronously reduced and the high-efficiency activity of the catalyst is maintained: In the oxygen carrier reduction reaction zone, the fully oxidized oxygen carrier is reduced by the low-carbon hydrocarbons and tar generated by the pyrolysis of biomass, reducing the tar content in the syngas, and thus improving the quality of the outlet syngas; The partially reduced oxygen carrier enters the biomass pyrolysis gasification catalytic reaction zone, where it can not only catalyze the pyrolysis of biomass but also oxidize the biomass char into CO syngas, and the oxygen carrier is further reduced; The deeply reduced oxygen carrier enters the hydrogen production reactor and reacts with water to produce high-purity hydrogen, while the oxygen carrier is regenerated and oxidized. Through the multi-step reduction and regeneration mechanism of the oxygen carrier, the high-efficiency activity of the catalyst is maintained, the conversion rate of biomass is increased, and the catalytic effect can also reduce the content of impurities such as tar and low-carbon hydrocarbons in the syngas, improving the quality of the syngas and making the syngas more suitable for subsequent utilization.

[0034] The co - design of a bubbling fluidized bed and a fast fluidized bed respectively matches the kinetic requirements of pyrolysis gasification, reduction reaction and hydrogen production: By precisely controlling the gas flow rate, the zoning control of fluidization is achieved. The biomass pyrolysis gasification catalytic reaction zone and the oxygen - carrier reduction reaction zone adopt the form of a bubbling fluidized bed. The lower flow rate ensures that the biomass has sufficient residence time in the reactor for pyrolysis gasification reaction. At the same time, it is also beneficial for the full contact of the oxygen - carrier with biomass, tar and light hydrocarbons, strengthening the catalytic reaction effect and the purification effect of syngas impurities; while the hydrogen production reaction zone adopts the form of a fast fluidized bed. This higher flow rate enables the oxygen - carrier to flow rapidly in the reactor, which is conducive to the oxidation of the oxygen - carrier and the generation of hydrogen, while ensuring the high purity of the synthesized hydrogen. Different fluidization states act synergistically in different regions, promoting the efficient progress of the whole process of co - producing syngas and hydrogen. Brief Description of the Drawings

[0035] In order to more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the following will briefly introduce the drawings required for the description of the embodiments or the prior art. Obviously, the drawings in the following description are only some embodiments of the present invention. For those of ordinary skill in the art, without creative efforts, other drawings can be obtained based on these drawings.

[0036] Figure 1 It is a schematic diagram of the overall structure of the present invention.

[0037] The descriptions of the reference numerals are as follows: 1. Oxidation reactor; 21. First cyclone separator; 22. Second cyclone separator; 31. First return - material riser; 32. Second return - material riser; 4. First feed inlet; 5. Oxygen - carrier reduction reaction zone; 6. Biomass pyrolysis gasification catalytic reaction zone; 7. Overflow structure; 8. Hydrogen production reaction zone; 9. Gasification reactor. Detailed Embodiments

[0038] To make the objectives, technical solutions and advantages of the present invention clearer, the following will describe the technical solutions of the present invention in detail. Obviously, the described embodiments are only some embodiments of the present invention, rather than all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those of ordinary skill in the art without creative efforts fall within the scope of protection of the present invention.

[0039] As Figure 1 shown, the integrated device for co - producing syngas and hydrogen by biomass chemical - looping gasification and water splitting in this embodiment includes: an oxidation reactor 1 and a gasification reactor 9. One end of the oxidation reactor 1 and the gasification reactor 9 is connected through a first cyclone separator 21, and the other end is connected through a second cyclone separator 22.

[0040] The gasification reactor 9 includes an oxygen carrier reduction reaction zone 5, a biomass pyrolysis gasification catalytic reaction zone 6, and a hydrogen production reaction zone 8. The oxygen carrier reduction reaction zone 5 and the biomass pyrolysis gasification catalytic reaction zone 6 are located in the same bubbling fluidized bed reactor. The hydrogen production reaction zone 8 is a fast fluidized bed reactor. The biomass pyrolysis gasification catalytic reaction zone 6 and the hydrogen production reaction zone 8 are connected by an overflow structure 7. The oxygen carrier reduction reaction zone 5 is connected to the first cyclone separator 21, and the hydrogen production reaction zone 8 is connected to the second cyclone separator 22.

[0041] The oxygen carrier reduction reaction zone 5 and the first cyclone separator 21 are connected by a first return standpipe 31, and the hydrogen production reaction zone 8 and the second cyclone separator 22 are connected by a second return standpipe 32.

[0042] The oxidation reactor 1 is a fast fluidized bed reactor with a constant diameter cylindrical or cubic shape.

[0043] A first feed inlet 4 is provided on the lower side of the oxidation reactor 1. The first feed inlet 4 forms an angle of 45 - 60° with the horizontal direction and is connected to the second return standpipe 32. A second feed inlet is provided at the top of the oxygen carrier reduction reaction zone 5 of the gasification reactor 9. The second feed inlet forms an angle of 90° with the horizontal direction and is connected to the first return standpipe 31. Such a setting facilitates the flow of oxygen carrier particles.

[0044] A syngas outlet is provided on the upper side of the oxygen carrier reduction reaction zone 5. A biomass feed inlet is provided on the lower side of the biomass pyrolysis gasification catalytic reaction zone 6, and a recycle gas inlet is provided at the bottom. The outlet flue gas enters the gasification reactor 9 through the recycle gas inlet for further conversion. A steam feed inlet is provided at the bottom of the hydrogen production reaction zone 8.

[0045] The gasification reactor 9 has a constant diameter cylindrical structure or a cubic structure.

[0046] During use, a sufficient amount of oxygen carrier particles is added into the oxidation reactor 1; the air volume in the oxidation reactor 1 is adjusted to fully oxidize the oxygen carrier particles. After the oxygen carrier particles carry oxygen, they enter the oxygen carrier reduction reaction zone 5 through the side outlet of the oxidation reactor 1 and the first return riser 31. In the oxygen carrier reduction reaction zone 5, by adjusting the fluidization air volume, the oxygen carrier moves downward into the biomass pyrolysis gasification catalytic reaction zone 6. In the biomass pyrolysis gasification catalytic reaction zone 6, a turbulent flow state exists. The oxygen carrier particles can slowly flow through the overflow structure 7 on the side of the biomass gasification reaction zone 6 and enter the hydrogen production reaction zone 8. In the hydrogen production reaction zone 8, a fast flow state exists. The oxygen carrier returns to the oxidation reactor 1 again through the second return riser 32 and the first feed port 4 via the fluidized gas-solid separation outlet at the upper part of the hydrogen production reaction zone 8. After the operation is stable, the biomass pyrolysis gasification catalytic reactor 6 is fluidized by steam and recycled flue gas, and biomass is added into the biomass gasification reactor 6. Since the gas flow rate in the biomass gasification reactor 6 is low, the biomass will not be carried to a high place. At the bottom of the gasification reactor 6, the biomass undergoes a pyrolysis reaction to generate biomass char, syngas, tar, and light hydrocarbons; meanwhile, under the catalytic action of the oxygen carrier, the biomass char is partially oxidized to CO syngas; the generated syngas, tar, and light hydrocarbons move upward into the oxygen carrier reduction reaction zone 5. In the oxygen carrier reduction reaction zone 5, the fully oxidized oxygen carrier is selectively deeply reduced by light hydrocarbons such as C1-C5 and tar generated by biomass pyrolysis conversion, exposing the metal catalytic surface and enhancing the catalytic ability, while the light hydrocarbons and tar are partially oxidized to CO2 and H2O or CO and H2O; finally, the gas flows out from the syngas outlet pipe at the upper part of the oxygen carrier reduction reaction zone 5. Part of the gas in the gas flow pipe can be returned to the biomass gasification reaction zone through the recycle fan for recycling again; the oxygen carrier in the deep reduction state in the biomass pyrolysis gasification catalytic reaction zone enters the hydrogen production reaction zone 8 through the overflow structure 7. In the hydrogen production reaction zone 8, the oxygen carrier reacts with H2O to produce high-purity H2, and the oxygen carrier is oxidized.

[0047] The method for integrated biomass chemical-looping gasification and water splitting to co-produce syngas and hydrogen in this embodiment includes the following steps:

[0048] After the air from the oxidation reactor 1 fluidizes and oxidizes the oxygen carrier MeO material, the oxygen carrier flows to the oxygen carrier reduction reaction zone 5 through the first return riser 31. In the oxygen carrier reduction reaction zone 5, the fully oxidized oxygen carrier is reduced by light hydrocarbons / tar generated by biomass pyrolysis conversion, exposing the metal catalytic surface and enhancing the catalytic ability, while the light hydrocarbons / tar are oxidized to CO2 and H2O or CO and H2O; the reaction formula is as follows:

[0049] MeO + C n H m O z → MeO 1-x + CO / CO2 + H2O.

[0050] The reduced oxygen carrier enters the biomass pyrolysis gasification catalytic reaction zone 6. In the biomass pyrolysis gasification catalytic reaction zone, while the biomass undergoes pyrolysis gasification, syngas (CO / H2) and low-carbon hydrocarbons / tar are produced. Under the catalytic action of the oxygen carrier, the biomass is partially oxidized to produce CO syngas. The reaction formula is as follows:

[0051] Biomass → C + C n H m O z + CO + H2;

[0052] C + MeO → MeO 1-x + CO.

[0053] The reduced oxygen carrier enters the hydrogen production reaction zone 8 through the overflow structure 7. In the hydrogen production reaction zone 8, the reduced oxygen carrier reacts with H2O to produce high-purity H2. Subsequently, the oxygen carrier returns to the oxidation reactor 1 again through the second cyclone separator 22. The reaction formula is as follows:

[0054] MeO 1-x + H2O → MeO 1-y + H2.

[0055] Part of the gas from the outlet of the oxygen carrier reduction reaction zone 5 is introduced into the biomass pyrolysis gasification catalytic reaction zone 6 again for recycling.

[0056] The present invention realizes the decoupling of the reaction process through physical isolation and the overflow structure, significantly improving the syngas and hydrogen production rates. The collaborative design of the bubbling fluidized bed and the fast fluidized bed respectively matches the kinetic requirements of pyrolysis gasification, reduction reaction and hydrogen production. Different fluidization states act synergistically in different regions, promoting the efficient progress of the entire co-production process of syngas and hydrogen.

[0057] Within the technical scope disclosed by the present invention, changes or substitutions that can be easily conceived should be covered within the protection scope of the present invention. Therefore, the protection scope of the present invention should be subject to the protection scope of the said claims.

Claims

1. An apparatus for co-producing syngas and hydrogen by integrating biomass chemical-looping gasification and water splitting, characterized in that, Comprising: An oxidation reactor (1) and a gasification reactor (9), one end of the oxidation reactor (1) and the gasification reactor (9) is connected by a first cyclone separator (21), and the other end is connected by a second cyclone separator (22).

2. The device for co-producing syngas and hydrogen by integrating biomass chemical-looping gasification and water splitting according to claim 1, wherein: The gasification reactor (9) includes an oxygen carrier reduction reaction zone (5), a biomass pyrolysis gasification catalytic reaction zone (6) and a hydrogen production reaction zone (8). The oxygen carrier reduction reaction zone (5) and the biomass pyrolysis gasification catalytic reaction zone (6) are located in the same bubbling fluidized bed reactor. The hydrogen production reaction zone (8) is a fast fluidized bed reactor. The biomass pyrolysis gasification catalytic reaction zone (6) and the hydrogen production reaction zone (8) are connected by an overflow structure (7). The oxygen carrier reduction reaction zone (5) is connected to the first cyclone separator (21), and the hydrogen production reaction zone (8) is connected to the second cyclone separator (22).

3. The device for co-producing syngas and hydrogen by integrating biomass chemical looping gasification and water splitting according to claim 2, characterized in that: The oxygen carrier reduction reaction zone (5) is connected to the first cyclone separator (21) through a first return riser (31), and the hydrogen production reaction zone (8) is connected to the second cyclone separator (22) through a second return riser (32).

4. The device for co-producing syngas and hydrogen by integrating biomass chemical-looping gasification and water splitting according to claim 3, wherein: The oxidation reactor (1) is a fast fluidized bed reactor with a constant diameter column structure.

5. The device for co-producing syngas and hydrogen by integrating biomass chemical-looping gasification and water splitting according to claim 4, characterized in that: A first feed inlet (4) is provided on the lower side of the oxidation reactor (1). The first feed inlet (4) forms an angle of 45 - 60° with the horizontal direction, and the first feed inlet (4) is connected to the second return riser (32).

6. The device for co-producing syngas and hydrogen by integrating biomass chemical-looping gasification and water splitting according to claim 5, wherein: A second feed inlet is provided at the top of the oxygen carrier reduction reaction zone (5) of the gasification reactor (9), and the second feed inlet is connected to the first return riser (31).

7. The device for co-producing syngas and hydrogen by integrating biomass chemical-looping gasification and water splitting according to claim 6, characterized in that: A syngas outlet is provided on the upper side of the oxygen carrier reduction reaction zone (5). A biomass feed inlet is provided on the lower side of the biomass pyrolysis gasification catalytic reaction zone (6), and a recycle gas inlet is provided at the bottom. The outlet flue gas enters the gasification reactor (9) through the recycle gas inlet for further conversion. A steam feed inlet is provided at the bottom of the hydrogen production reaction zone (8).

8. The device for co-producing syngas and hydrogen by integrating biomass chemical-looping gasification and water splitting according to claim 7, wherein: The gasification reactor (9) has a constant diameter column structure or a cubic structure.

9. A method for co-producing syngas and hydrogen by integrating biomass chemical looping gasification and water splitting, based on the device for co-producing syngas and hydrogen by integrating biomass chemical looping gasification and water splitting according to claim 8, characterized in that, Including the following steps: After the air from the oxidation reactor (1) fluidizes and oxidizes the oxygen carrier material, the oxygen carrier flows through the first return riser (31) to the oxygen carrier reduction reaction zone (5). In the oxygen carrier reduction reaction zone (5), the fully oxidized oxygen carrier is reduced by the low-carbon hydrocarbons / tar produced by the biomass pyrolysis conversion, exposing the metal catalytic surface and enhancing the catalytic ability, while the low-carbon hydrocarbons / tar are oxidized into CO2 and H2O or CO and H2O. The reduced oxygen carrier enters the biomass pyrolysis gasification catalytic reaction zone (6). In the biomass pyrolysis gasification catalytic reaction zone, while the biomass undergoes pyrolysis gasification, syngas and low-carbon hydrocarbons / tar are produced. Under the catalytic action of the oxygen carrier, the biomass is partially oxidized into CO syngas. The reduced oxygen carrier enters the hydrogen production reaction zone (8) through the overflow structure (7). In the hydrogen production reaction zone (8), the reduced oxygen carrier reacts with H2O to produce high-purity H2. Subsequently, the oxygen carrier returns to the oxidation reactor (1) through the second cyclone separator (22). Part of the gas exiting from the outlet of the oxygen carrier reduction reaction zone (5) is introduced into the biomass pyrolysis gasification catalytic reaction zone (6) again for recycling.

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