Device integrating biomass chemical chain gasification and water splitting to produce synthesis gas and hydrogen

Abstract

The present invention discloses a device for co-producing synthesis gas and hydrogen by integrating biomass chemical chain gasification and water decomposition, comprising: an oxidation reactor and a gasification reactor, wherein the oxidation reactor and the gasification reactor are connected at one end by a first cyclone separator and at the other end by 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, wherein 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 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 the first cyclone separator, and the hydrogen production reaction zone is connected to the second cyclone separator. By optimizing the reaction conditions by region, the efficiency of co-production of synthesis gas and hydrogen is improved.

Description

Technical Field

[0001] The present invention relates to the technical field of biomass gasification, and in particular to a device integrating biomass chemical chain gasification and water decomposition for co-producing synthesis gas and hydrogen. Background Art

[0002] Biomass gasification, as a biomass thermochemical conversion technology, converts biomass into gaseous fuel and is one of the most effective ways to achieve biomass energy conversion. Traditional biomass gasification technologies use air, steam, or oxygen as gasifying agents. These technologies suffer from high process energy consumption, high costs, low syngas yields, and high tar content, which have become bottlenecks and major obstacles to their application.

[0003] Biomass chemical chaining gasification is an application of chemical chaining technology in the field of biomass energy utilization. In the fuel reactor, oxygen carriers are used to supply oxygen and heat for the gasification process to produce synthesis gas. This can avoid the dilution of synthesis gas by nitrogen in the air, the high cost of pure oxygen preparation process and the high energy consumption of water vapor gasification. In addition, the oxygen carrier can catalyze the cracking of tar and improve the synthesis gas yield.

[0004] However, traditional biomass gasification technology suffers from problems such as high tar production, low-quality syngas, and insufficient hydrogen yield. While existing chemical-looping gasification technology can reduce tar production through oxygen carrier circulation, it struggles to efficiently decouple gasification from hydrogen production. Furthermore, the high degree of coupling between the oxygen carrier reduction and oxidation processes in traditional single-bed reactors leads to a rapid decrease 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 efficiency of co-production of syngas and hydrogen. Summary of the Invention

[0005] The purpose of the present invention is to provide a device that integrates biomass chemical chain gasification and water decomposition to jointly produce synthesis gas and hydrogen in order to solve the above problems, so as to solve the problems of existing biomass gasification that are difficult to achieve efficient decoupling of gasification and hydrogen production, rapid decline in catalyst activity, and limited hydrogen purity.

[0006] To achieve the above objectives, the present invention provides the following technical solution: a device for integrating biomass chemical chain gasification and water decomposition to co-produce synthesis gas and hydrogen, comprising: an oxidation reactor and a gasification reactor, wherein one end of the oxidation reactor and the gasification reactor are 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 and gasification catalytic reaction zone and a hydrogen production reaction zone, the oxygen carrier reduction reaction zone and the biomass pyrolysis and 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 and 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 the first cyclone separator, and the hydrogen production reaction zone is connected to the second cyclone separator.

[0008] Biomass pyrolysis and gasification catalytic reaction zone: adopts bubbling fluidized bed design, biomass is pyrolyzed and gasified to produce synthesis gas (CO / H2) and C1-C5 low carbon hydrocarbons / tar (C n H m O z ), and partially oxidize the coke to CO under the catalysis of the oxygen carrier. The reaction formula is 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: Using a bubbling fluidized bed design, the low-carbon hydrocarbons / tar produced by biomass pyrolysis selectively and deeply reduce the oxidized oxygen carriers, exposing the metal catalytic surface and simultaneously oxidizing the hydrocarbons to CO2 / H2O or CO / H2O. The reaction formula is as follows:

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

[0013] Hydrogen production reaction zone: Using a fast fluidized bed design, the deeply reduced oxygen carrier reacts with H2O to generate high-purity H2, which is then regenerated into an oxidized oxygen carrier for recycling. The reaction formula is as follows:

[0014] MeO 1-x +H2O→MeO 1-y +H2.

[0015] Overflow structure: The biomass pyrolysis and gasification catalytic zone and the hydrogen production zone are connected by an overflow structure, enabling directional flow of materials and oxygen carriers, ensuring independent optimization of reaction conditions in each zone. Pressure differential control is used here, with the overflow pressure on the gasification reactor side higher than the overflow pressure on the hydrogen production reactor side, achieving directional movement.

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

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

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

[0019] Preferably, the oxidation reactor is a fast fluidized bed reactor of equal diameter cylinder.

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

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

[0023] Preferably, the gasification reactor is an iso-diameter cylindrical structure or a cubic structure.

[0024] The present invention also discloses a method for integrating biomass chemical chain gasification and water decomposition to co-produce synthesis gas and hydrogen, based on the above-mentioned device, comprising the following steps:

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

[0026] Synthesis gas, light hydrocarbons and tar enter the oxygen carrier reduction reaction zone. The fully oxidized oxygen carrier is selectively and deeply reduced by the light hydrocarbons and tar, exposing the metal catalytic surface and improving the catalytic ability. The light hydrocarbons / tar are oxidized into CO2 and H2O or CO and H2O.

[0027] The synthesis gas finally enters the upper air flow channel of the oxygen carrier reduction reactor. Part of the gas in the air flow channel can be returned to the biomass gasification reaction zone through the recirculation fan for recirculation;

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

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

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

[0031] Compared with the prior art, the present invention has the following beneficial effects:

[0032] The regional fluidized bed design achieves decoupling of the reaction process through physical isolation and overflow structure, significantly improving the yield of synthesis gas and hydrogen: the reaction system in the traditional gasification reactor is complex, and multiple 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 chain 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 zoning control of oxygen carrier reduction and biomass gasification, and produces synthesis gas and hydrogen in parallel, effectively avoiding the negative impact of the complex reaction system on the gasification efficiency, and ensures the high purity of hydrogen through the overflow structure to achieve efficient decoupling of gasification and hydrogen production.

[0033] Through the deep reduction and regeneration mechanism of the oxygen carrier, the tar content is simultaneously reduced and the high 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 produced by the pyrolysis of biomass, reducing the tar content in the synthesis gas and thereby improving the quality of the exported synthesis gas; the partially reduced oxygen carrier enters the biomass pyrolysis and gasification catalytic reaction zone, where it not only catalyzes the pyrolysis of biomass but also oxidizes the biomass char into CO synthesis gas, further reducing the oxygen carrier; the deeply reduced oxygen carrier enters the hydrogen production reactor, where it reacts with water to produce high-purity hydrogen, while the oxygen carrier is simultaneously regenerated and oxidized. Through the multi-step reduction and regeneration mechanism of the oxygen carrier, the high activity of the catalyst is maintained, the conversion rate of biomass is improved, and the catalytic effect can also reduce the content of impurities such as tar and low-carbon hydrocarbons in the synthesis gas, improving the quality of the synthesis gas and making the synthesis gas more suitable for subsequent utilization.

[0034] The collaborative design of a bubbling fluidized bed and a fast fluidized bed respectively matches the kinetic requirements of pyrolysis and gasification, reduction reaction, and hydrogen production: precise control of gas flow rates enables zoned control of liquefaction. The biomass pyrolysis and gasification catalytic reaction zone and the oxygen carrier reduction reaction zone utilize a bubbling fluidized bed. The low flow rate ensures that the biomass has sufficient residence time in the reactor for the pyrolysis and gasification reaction. It also facilitates full contact between the oxygen carrier and the biomass, tar, and low-carbon hydrocarbons, enhancing the catalytic reaction and the purification of syngas impurities. The hydrogen production reaction zone utilizes a fast fluidized bed. This high flow rate enables the oxygen carrier to flow rapidly within the reactor, facilitating its oxidation and hydrogen generation, while ensuring the high purity of the synthesized hydrogen. Different fluidization states act synergistically in different zones, promoting the efficient co-production of syngas and hydrogen. BRIEF DESCRIPTION OF THE DRAWINGS

[0035] In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the following briefly introduces the drawings required for use in the embodiments or the description of the prior art. Obviously, the drawings described below are only some embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying any creative work.

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

[0037] The description of the accompanying drawings is 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 and gasification catalytic reaction zone; 7. Overflow structure; 8. Hydrogen production reaction zone; 9. Gasification reactor. DETAILED DESCRIPTION

[0038] To make the objectives, technical solutions, and advantages of the present invention more clear, the technical solutions of the present invention will be described in detail below. Obviously, the embodiments described are only some embodiments of the present invention, not all embodiments. Based on the embodiments of the present invention, all other implementations obtained by ordinary technicians in this field without making any creative work are within the scope of protection of the present invention.

[0039] like Figure 1 As shown, the device of this embodiment for integrating biomass chemical chain gasification and water decomposition to produce synthesis gas and hydrogen includes: an oxidation reactor 1 and a gasification reactor 9, wherein the oxidation reactor 1 and the gasification reactor 9 are connected at one end through a first cyclone separator 21 and at the other end through a second cyclone separator 22.

[0040] The gasification reactor 9 includes an oxygen carrier reduction reaction zone 5, a biomass pyrolysis and gasification catalytic reaction zone 6 and a hydrogen production reaction zone 8. The oxygen carrier reduction reaction zone 5 and the biomass pyrolysis and 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 and 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 is connected to the first cyclone separator 21 through a first material return riser 31 , and the hydrogen production reaction zone 8 is connected to the second cyclone separator 22 through a second material return riser 32 .

[0042] The oxidation reactor 1 is a fast fluidized bed reactor of equal diameter cylinder or cube.

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

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

[0045] The gasification reactor 9 is an iso-diameter cylindrical structure or a cubic structure.

[0046] During use, a sufficient amount of oxygen carrier particles is added to the oxidation reactor 1; the air volume in the oxidation reactor 1 is adjusted to fully oxidize the oxygen carrier particles. After carrying oxygen, the oxygen carrier particles enter the oxygen carrier reduction reaction zone 5 from the side outlet of the oxidation reactor 1 through the first return riser 31. In the oxygen carrier reduction reaction zone 5, by adjusting the fluidized air volume, the oxygen carrier downwardly enters the biomass pyrolysis and gasification catalytic reaction zone 6. The biomass pyrolysis and gasification catalytic reaction zone 6 is in a turbulent flow state. The oxygen carrier particles can slowly flow through the overflow structure 7 on the side of the biomass gasification reaction zone 6 into the hydrogen production reaction zone 8. The hydrogen production reaction zone 8 is in a fast flow state. The oxygen carrier passes through the fluidized gas-solid separation outlet at the top of the hydrogen production reaction zone 8 and returns to the oxidation reactor 1 from the first feed port 4 through the second return riser 32. After the operation is stable, the biomass pyrolysis gasification catalytic reactor 6 is fluidized by water vapor and circulating flue gas, and biomass is added to the biomass gasification reactor 6. Due to the low gas flow rate in the biomass gasification reactor 6, the biomass will not be carried to a high place. At the bottom of the gasification reactor 6, the biomass undergoes pyrolysis reaction to generate biomass coke, synthesis gas, tar and low-carbon hydrocarbons; at the same time, under the catalytic action of the oxygen carrier, the biomass coke is partially oxidized to CO synthesis gas; the generated synthesis gas, tar and low-carbon hydrocarbons enter the oxygen carrier reduction reaction zone 5 upward, and in the oxygen carrier reduction reaction zone 5, the fully oxidized oxygen carrier is selectively oxidized by the biomass The low-carbon hydrocarbons such as C1-C5 and tar produced by pyrolysis conversion are deeply reduced, exposing the metal catalytic surface and improving the catalytic ability, while the low-carbon hydrocarbons and tar are partially oxidized into CO2 and H2O or CO and H2O; finally, the gas flows out from the synthesis gas outlet pipe at the top of the oxygen carrier reduction reaction zone 5, and part of the gas in the air flow pipe can be returned to the biomass gasification reaction zone for recirculation through the recirculation fan; the deeply reduced oxygen carrier in the biomass pyrolysis gasification catalytic reaction zone enters the hydrogen production reaction zone 8 through the overflow structure 7, and the oxygen carrier reacts with H2O in the hydrogen production reaction zone 8 to produce high-purity H2, and the oxygen carrier is oxidized.

[0047] The method of integrating biomass chemical chaining gasification and water splitting to produce synthesis gas 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 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 light hydrocarbons / tar produced by biomass pyrolysis, exposing the metal catalytic surface and improving the catalytic ability. The light hydrocarbons / tar are oxidized into 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 and gasification catalytic reaction zone 6. In the biomass pyrolysis and gasification catalytic reaction zone, the biomass undergoes pyrolysis and gasification, producing synthesis gas (CO / H2) and light hydrocarbons / tar. Under the catalytic action of the oxygen carrier, the biomass is partially oxidized into CO synthesis gas; 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, where it reacts with H2O to produce high-purity H2. The oxygen carrier then returns to the oxidation reactor 1 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 exiting the oxygen carrier reduction reaction zone 5 is introduced again into the biomass pyrolysis and gasification catalytic reaction zone 6 and circulated again.

[0056] This invention decouples the reaction processes through physical isolation and overflow structures, significantly improving the yields of syngas and hydrogen. The coordinated design of the bubbling fluidized bed and the fast fluidized bed respectively matches the kinetic requirements of pyrolysis and gasification, reduction reactions, and hydrogen production. Different fluidization states act synergistically in different areas, promoting the efficient co-production of syngas and hydrogen.

[0057] Within the technical scope disclosed by the present invention, any changes or substitutions that can be easily imagined should be included in the protection scope of the present invention. Therefore, the protection scope of the present invention should be based on the protection scope of the claims.

Claims

1. A device integrating biomass chemical chain gasification and water decomposition to produce synthesis gas and hydrogen, characterized in that: include: An oxidation reactor (1) and a gasification reactor (9), wherein one end of the oxidation reactor (1) and the gasification reactor (9) are connected via a first cyclone separator (21), and the other end is connected via a second cyclone separator (22); the gasification reactor (9) comprises 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 via 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).

2. The device for integrated biomass chemical chaining gasification and water splitting for co-production of synthesis gas and hydrogen according to claim 1, characterized in that: The oxygen carrier reduction reaction zone (5) is connected to the first cyclone separator (21) via a first return material riser (31), and the hydrogen production reaction zone (8) is connected to the second cyclone separator (22) via a second return material riser (32).

3. The device for integrated biomass chemical chaining gasification and water splitting for co-production of synthesis gas and hydrogen according to claim 1, characterized in that: The oxidation reactor (1) is a fast fluidized bed reactor with a constant diameter column.

4. The device for integrated biomass chemical chaining gasification and water splitting for co-production of synthesis gas and hydrogen according to claim 3, characterized in that: A first feed port (4) is provided on the lower side of the oxidation reactor (1), the first feed port (4) forms an angle of 45-60° with the horizontal direction, and the first feed port (4) is connected to a second return material riser (32).

5. The device for integrated biomass chemical chaining gasification and water splitting for co-production of synthesis gas and hydrogen according to claim 4, characterized in that: 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 material riser (31).

6. The device for integrated biomass chemical chaining gasification and water splitting for co-production of synthesis gas and hydrogen according to claim 5, characterized in that: The oxygen carrier reduction reaction zone (5) is provided with a synthesis gas outlet on the upper side, the biomass pyrolysis and gasification catalytic reaction zone (6) is provided with a biomass feeding port on the lower side, and a recirculating gas inlet is provided at the bottom. The outlet flue gas enters the gasification reactor (9) through the recirculating gas inlet for further conversion; and the hydrogen production reaction zone (8) is provided with a water vapor feeding port at the bottom.

7. The device for integrated biomass chemical chaining gasification and water splitting for co-production of synthesis gas and hydrogen according to claim 6, characterized in that: The gasification reactor (9) is an isodiameter cylindrical structure or a cubic structure.

8. A method for co-producing synthesis gas and hydrogen by integrating biomass chemical chaining gasification and water splitting, based on the device for co-producing synthesis gas and hydrogen by integrating biomass chemical chaining gasification and water splitting according to claim 7, characterized in that: The following steps are involved: 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 pyrolysis conversion of the biomass, exposing the metal catalytic surface and improving 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 and gasification catalytic reaction zone (6). In the biomass pyrolysis and gasification catalytic reaction zone, the biomass undergoes pyrolysis and gasification, while producing synthesis gas and low-carbon hydrocarbons / tar. Under the catalytic action of the oxygen carrier, the biomass is partially oxidized into CO synthesis gas. The reduced oxygen carrier enters the hydrogen production reaction zone (8) through the overflow structure (7), and reacts with H2O in the hydrogen production reaction zone (8) to produce high-purity H2. The oxygen carrier then returns to the oxidation reactor (1) through the second cyclone separator (22); Part of the gas exiting the oxygen carrier reduction reaction zone (5) is introduced again into the biomass pyrolysis and gasification catalytic reaction zone (6) and circulated again.

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