Apparatus and method for gasifying biomass to produce syngas

Abstract

The present application relates to the field of energy and chemical industry, and particularly relates to a device and method for preparing synthetic gas by biomass gasification. The device for preparing synthetic gas by biomass gasification comprises an ammonia gas combustion zone arranged at the bottom of a biomass reactor and a fluidization zone located above the ammonia gas combustion zone; the ammonia gas combustion zone is filled with ammonia gas combustion catalyst, and the fluidization zone contains granular SCR catalyst. The present application reduces the generation of tar and the emission of NOx by introducing ammonia gas and catalyst to assist the biomass gasification process, and provides clean and efficient raw materials for industrial production and energy utilization.

Description

Technical Field

[0001] This invention relates to the fields of energy and chemical technology, and in particular to an apparatus and method for producing syngas from biomass gasification. Background Technology

[0002] With the increasing severity of the global energy crisis and environmental problems, biomass energy, as a renewable and clean energy source, has received widespread attention and research. Biomass gasification to syngas technology is an important way to convert biomass feedstocks into high-quality gaseous fuels and has broad application prospects. However, in the biomass gasification process, the generation of tar and NOx produced by nitrogen-containing biomass gasification have always been difficult points restricting the technological development.

[0003] Tar is an unavoidable byproduct in biomass gasification. Tar production not only reduces gasification efficiency but can also lead to blockage and corrosion of gasification equipment, affecting its safe and stable operation. Currently, methods for treating tar mainly include physical purification and chemical conversion methods. Physical purification methods, such as filtration and condensation, are simple to operate but have limited effectiveness in treating tar. Chemical conversion methods, such as catalytic cracking and hydrocracking, can convert tar into more valuable chemicals, but they are complex and costly. Biomass feedstocks typically contain a certain amount of nitrogen, which is converted into harmful gases such as NOx during gasification. NOx not only pollutes the environment but may also harm human health. Currently, methods for reducing NOx emissions mainly include source control, technological upgrades, and end-of-pipe treatment. Source control primarily involves selecting low-nitrogen biomass feedstocks or using pretreatment technologies to reduce the nitrogen content in the feedstock; technological upgrades reduce NOx generation by improving gasification equipment or processes; and end-of-pipe treatment uses technologies such as flue gas denitrification to purify the generated NOx.

[0004] CN113684067A discloses an apparatus and method for producing syngas from biomass gasification, including components such as a feeder, preheater, reactor, multi-stage gas-solid separator, and syngas cooler. This apparatus effectively separates and collects tar through the multi-stage gas-solid separator, reducing tar accumulation in the system and providing the possibility of tar recovery and reuse. Furthermore, by optimizing gasification conditions, such as temperature, pressure, and the selection of gasifying agent, tar production can be further reduced. CN106398789A proposes a purification method for biomass gasification syngas, including steps such as tar removal, COS removal, crude desulfurization, decarbonization, and fine desulfurization of the crude syngas. Specifically, by employing activated carbon-based desulfurizing agents and MDEA lean liquor scrubbing technologies, sulfur and nitrogen compounds in the syngas can be removed, thereby reducing NOx emissions. Furthermore, it mentions further processing in a methanation reactor to produce low-NOx crude natural gas. CN110079364A discloses a method and system for treating biomass gasification tar. This patent application not only focuses on tar treatment but also addresses how to reduce NOx emissions through tar treatment. It proposes a tar treatment method including steps such as stratification, dilution, pressurization, spraying, waste heat utilization of tail gas, and tail gas detection. By fully cracking the tar and using it as boiler fuel, the resource utilization of tar is achieved, while reducing NOx emissions from tar combustion. Furthermore, the treatment system includes a tail gas detection device for monitoring and controlling NOx emissions. However, existing technologies for treating tar and NOx generally rely on enhanced process control and the addition of treatment units. The former increases the operational complexity of the equipment and makes it difficult to adjust in actual use, while the latter increases investment and operating costs. Summary of the Invention

[0005] To address the aforementioned technical problems, this invention provides a production apparatus and process for biomass gasification to produce syngas. By introducing ammonia and a catalyst to assist the biomass gasification process, this invention reduces tar production and NOx emissions, providing clean and efficient raw materials for industrial production and energy utilization.

[0006] In a first aspect, the present invention provides an apparatus for biomass gasification to produce syngas, comprising an ammonia combustion zone disposed at the bottom of a biomass reactor and a fluidization zone located above the ammonia combustion zone; the ammonia combustion zone is filled with an ammonia combustion catalyst, and the fluidization zone contains a particulate SCR catalyst.

[0007] Preferably, the top of the biomass reactor is provided with a syngas outlet; and / or, the fluidization zone is provided with a biomass particle inlet.

[0008] Further preferably, the ammonia combustion zone is provided with an ammonia inlet and an oxygen-containing gas inlet, and preferably multiple ammonia inlets and multiple oxygen-containing gas inlets are provided at the bottom of the ammonia combustion zone; and / or, the sulfidation zone is also provided with a fluidizing gas inlet, the fluidizing gas inlet being connected to a fluidizing gas source, and preferably multiple fluidizing gas inlets are provided around the reactor.

[0009] According to the present invention, the ammonia inlets and oxygen-containing gas inlets are dispersed in the bed, while the fluidizing gas inlets are multiple inlets surrounding the reactor, so that the gas is evenly distributed in the bed and the concentration is not too high in some areas.

[0010] Further preferably, it also includes a biomass feeding device connected to the biomass reactor; the biomass feeding device includes a biomass bin and a screw feeder, the biomass bin being connected to the screw feeder, and the screw feeder being connected to the biomass reactor at the biomass pellet inlet.

[0011] Secondly, the present invention provides a method for producing syngas from biomass gasification, comprising: adding biomass particles and SCR catalyst particles to the fluidization zone of a biomass reactor, introducing oxygen-containing gas and ammonia into the ammonia combustion zone of the biomass reactor, and then entering the fluidization zone after being ignited by the ammonia combustion catalyst, controlling the gas flow and reaction temperature, and carrying out ammonia combustion and biomass gasification reactions in the fluidization zone.

[0012] Further preferably, the oxygen content of the oxygen-containing gas is 10-50% by volume fraction, preferably air; and / or, the fluidizing gas is nitrogen.

[0013] Further preferred embodiments include an ammonia:air volume ratio of 0.05–0.2, a fluidizing gas velocity of 0.1–5 m / s, and a reaction zone temperature of 600–900 °C. For example, the ratio can be 0.05, 0.07, 0.08, 0.09, 0.1, 0.12, 0.14, 0.16, 0.18, 0.2, or any value between these values; the fluidizing gas velocity can be 0.2, 0.3, 0.5, 0.6, 0.8, 0.9, 1.1, 1.2, 1.5, 2.5, 3.5, 4.5 m / s, or any value between these values; and the temperature can be 600, 650, 700, 750, 800, 850, 900 °C, or any value between these values.

[0014] Further preferably, the ammonia combustion catalyst is selected from one or more of bimetallic oxide honeycomb ceramic catalysts, noble metal honeycomb ceramic catalysts, and Cu-based molecular sieve honeycomb catalysts; preferably, the active center of the bimetallic oxide honeycomb ceramic catalyst is selected from one or more of MnCo2O4, CoCr2O4, NiCo2O4, CuCr2O4, and CuMn2O4; the active center of the noble metal honeycomb ceramic catalyst is selected from one or more of Pt, Pd, Ru, and Au; the active center of the Cu-based molecular sieve honeycomb catalyst is selected from one of CuAg, CuCe, and Cu metal, and the molecular sieve support is selected from one of SSZ-13, S-1, Beta-25, and ZSM-5.

[0015] Further preferably, the granular SCR catalyst is a titanium vanadium oxide catalyst, a natural ore catalyst, or a Cu-based molecular sieve catalyst; preferably, the titanium vanadium oxide catalyst is selected from one or more of V2O5, TiO2, WO3, V2O5 / TiO2, and V2O5-WO3 / TiO2; the natural ore catalyst is selected from one or more of BaTiO3, LaMnO3, SrTiO3, and LaCoO3; the active center of the Cu-based molecular sieve catalyst is selected from one of CuAg, CuCe, and Cu metal, and the molecular sieve support is selected from one of SSZ-13, S-1, Beta-25, and ZSM-5; the particle size of the granular SCR catalyst is preferably 5 mm to 50 mm, more preferably 10 mm to 20 mm.

[0016] Further preferably, the biomass pellets are selected from one or more of wood pellets, straw pellets and seaweed pellets; preferably, the size of the biomass pellets is 5mm to 50mm, and more preferably 10mm to 20mm.

[0017] This invention introduces ammonia and uses a catalyst to assist the biomass gasification process. The tar precursors produced during biomass gasification are saturated and bond-broken under the action of hydrogen generated from ammonia decomposition, inhibiting tar formation during gasification. Simultaneously, the catalyst helps reduce NOx produced by ammonia. The addition of ammonia allows for front-end adjustment of the syngas ratio, reducing the need for gas ratio control. Besides the high-heat gases from the combustion of air and ammonia, nitrogen is introduced to maintain the fluidization state of the biomass. Initially, the SCR catalyst is added along with the biomass; after normal operation, only biomass is added. This reactor uses ammonia as a heat source to assist biomass gasification, providing all heat during the initial reaction phase. During stable operation, unused oxygen in the air reacts with some of the biomass to promote gasification. NOx produced during the process is eliminated by the introduced ammonia and the SCR catalyst. Attached Figure Description

[0018] To more clearly illustrate the technical solutions in this invention or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are some embodiments of this invention. For those skilled in the art, other drawings can be obtained from these drawings without creative effort.

[0019] Figure 1 This is a schematic diagram of a biomass gasification syngas production apparatus in an embodiment of the present invention.

[0020] Figure 2 This is a schematic diagram of the process of biomass gasification to syngas in an embodiment of the present invention. Detailed Implementation

[0021] To make the objectives, technical solutions, and advantages of this invention clearer, the technical solutions of this invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some, not all, of the embodiments of this invention. All other embodiments obtained by those skilled in the art based on the embodiments of this invention without creative effort are within the scope of protection of this invention.

[0022] Where specific techniques or conditions are not specified in the examples, they shall be performed in accordance with the techniques or conditions described in the literature in this field, or in accordance with the product instructions. Reagents or instruments whose manufacturers are not specified are all conventional products that can be purchased through legitimate channels.

[0023] In the description of the embodiments of the present invention, it should be noted that, unless otherwise explicitly specified and limited, the terms "first" and "second," etc., are used for the purpose of clearly identifying product components and do not represent any substantial difference. Terms such as "upper," "lower," and "inner" are only used to indicate relative positional relationships; when the absolute position of the described object changes, the relative positional relationship may also change accordingly. Those skilled in the art can understand the specific meaning of the above terms in the embodiments of the present invention according to the specific circumstances.

[0024] In the description of this specification, the references to terms such as "one embodiment," "some embodiments," "example," "specific example," or "some examples," etc., refer to specific features, structures, materials, or characteristics described in connection with that embodiment or example, which are included in at least one embodiment or example of the present invention. In this specification, the illustrative expressions of the above terms do not necessarily refer to the same embodiment or example. Furthermore, the specific features, structures, materials, or characteristics described may be combined in any suitable manner in one or more embodiments or examples. Moreover, without contradiction, those skilled in the art can combine and integrate the different embodiments or examples described in this specification, as well as the features of different embodiments or examples.

[0025] Example 1 The apparatus for biomass gasification to syngas provided in this embodiment ( Figure 1 The system includes: a biomass reactor 1 and a biomass feeding device 7; the biomass reactor 1 includes an ammonia combustion zone 2 and a fluidization zone 3, the ammonia combustion zone 2 is located at the bottom of the biomass reactor 1, and the fluidization zone 3 is located above the ammonia combustion zone 2.

[0026] The ammonia combustion zone 2 is used for the combustion reaction of ammonia and oxygen-containing gas. The ammonia combustion zone 2 is filled with an ammonia combustion catalyst. Multiple ammonia inlets 4 and multiple oxygen-containing gas inlets 5 are provided at the bottom of the ammonia combustion zone 2. These inlets are evenly distributed in the bed. The fluidization zone 3 is above the ammonia combustion zone 2.

[0027] The fluidized zone 3 is used for biomass pellet gasification reaction. The fluidized zone 3 is equipped with a biomass pellet inlet 6 and a syngas outlet 8. The biomass pellet inlet 6 is connected to the biomass feed device 7. The fluidized zone 3 contains granular SCR catalyst. It also includes a fluidizing gas inlet 9, connected to a fluidizing gas source. The fluidizing gas inlet 9 is located in the sulfidation zone 3, and multiple fluidizing gas inlets 9 are arranged around the reactor to maintain the fluidization state of the reactants within the fluidized zone 3 together with the gas from the ammonia combustion zone 2.

[0028] The biomass feeding device 7 includes a biomass bin and a screw feeder. Biomass pellets are fed from the biomass bin into the fluidization zone 3 of the biomass reactor 1 via the screw feeder.

[0029] This embodiment also provides a method for biomass gasification to produce syngas. Figure 2The steps are as follows: Air is preheated to 300℃, and ammonia is preheated to 250℃. The mixture passes through a disperser with an ammonia-to-air flow ratio of 0.1:1. Simultaneously, an ammonia combustion catalyst (MnCo2O4 honeycomb ceramic catalyst) bed is introduced. After passing through, the ammonia is ignited, serving as both a heating gas and a fluidizing gas. Straw pellets (average particle size 10mm) and SCR catalyst pellets (Cu / SSZ-13, average particle size 10mm) are premixed and fed into the reactor fluidization zone via a screw feeder. The feeder maintains the fluidization state of the materials within the fluidization zone with the introduced fluidizing gas. Ammonia combustion and biomass gasification reactions occur simultaneously within the fluidization zone. After normal operation, the amount of ammonia added is reduced, and the reaction temperature is controlled at 850±50℃, with a gas velocity controlled at 0.7±0.1m / s. The resulting biomass gas is then condensed to remove the tar (tar content 0.1g / m³). 3 The remaining gas is the product biosynthesis gas. The dry gas composition of the product biosynthesis gas is: H2: 41%; CO: 30%; CO2: 12%; CH4: 10%; C2H4: 3%.

[0030] Example 2 The apparatus for biomass gasification to syngas provided in this embodiment ( Figure 1 The system includes: a biomass reactor 1 and a biomass feeding device 7; the biomass reactor 1 includes an ammonia combustion zone 2 and a fluidization zone 3, the ammonia combustion zone 2 is located at the bottom of the biomass reactor 1, and the fluidization zone 3 is located above the ammonia combustion zone 2.

[0031] The ammonia combustion zone 2 is used for the combustion reaction of ammonia and oxygen-containing gas. The ammonia combustion zone 2 is filled with an ammonia combustion catalyst. Multiple ammonia inlets 4 and multiple oxygen-containing gas inlets 5 are provided at the bottom of the ammonia combustion zone 2. These inlets are evenly distributed in the bed. The fluidization zone 3 is above the ammonia combustion zone 2.

[0032] The fluidized zone 3 is used for biomass pellet gasification reaction. The fluidized zone 3 is equipped with a biomass pellet inlet 6 and a syngas outlet 8. The biomass pellet inlet 6 is connected to the biomass feed device 7. The fluidized zone 3 contains granular SCR catalyst. It also includes a fluidizing gas inlet 9, connected to a fluidizing gas source. The fluidizing gas inlet 9 is located in the fluidized zone 3 of the biomass reactor 1, and multiple fluidizing gas inlets 9 are arranged around the reactor, working together with the gas from the ammonia combustion zone 2 to maintain the fluidization state of the reactants within the fluidized zone 3.

[0033] The biomass feeding device 7 includes a biomass bin and a screw feeder. Biomass pellets are fed from the biomass bin into the fluidization zone 3 of the biomass reactor 1 via the screw feeder.

[0034] This embodiment also provides a method for biomass gasification to produce syngas. Figure 2 The steps are as follows: Air is preheated to 300℃, and ammonia is preheated to 250℃. After passing through a disperser, the ammonia to air flow ratio is 0.08:1. Simultaneously, an ammonia combustion catalyst bed (MnCo2O4 honeycomb ceramic catalyst) is introduced. After passing through, the ammonia is ignited, serving as both a heating gas and a fluidizing gas. Wood pellets (average particle size 15mm) and SCR catalyst particles (V2O5 / TiO2-based denitration catalyst, average particle size 15mm) are premixed and fed into the reactor fluidization zone via a screw feeder. The materials in the fluidization zone are kept fluidized by the introduced fluidizing gas. Ammonia combustion and biomass gasification reactions occur simultaneously in the fluidization zone. After normal operation, the amount of ammonia added is reduced, and the reaction temperature is controlled at 750±100℃, and the gas velocity is controlled at 0.7±0.1m / s. The obtained biomass gas is condensed to remove the tar (tar content 0.15g / m³). 3 The remaining gas is the product biosynthesis gas. The dry gas composition of the product biosynthesis gas is: H2: 43%; CO: 20%; CO2: 22%; CH4: 12%; C2+C3:1%.

[0035] Example 3 This embodiment uses the same apparatus and process as Embodiment 1, with the following differences in steps: Air is preheated to 300℃ and ammonia to 250℃. The mixture passes through a disperser with an ammonia-to-air flow ratio of 0.1:1. Simultaneously, an ammonia combustion catalyst (CoCr2O4 honeycomb ceramic catalyst) bed is introduced. After passing through, the ammonia is ignited, serving as both a heating gas and a fluidizing gas. Straw pellets (average particle size 10mm) and SCR catalyst pellets (LaMnO3, average particle size 15mm) are premixed and fed into the fluidization zone of the reactor via a screw feeder. The feeder maintains the fluidization state of the materials within the fluidization zone with the introduced fluidizing gas. Ammonia combustion and biomass gasification reactions occur simultaneously within the fluidization zone. After normal operation, the amount of ammonia added is reduced, and the reaction temperature is controlled at 850±50℃, with a gas velocity controlled at 0.7±0.1m / s. The resulting biomass gas is condensed to remove the tar (tar content 0.2g / m³). 3 The remaining gas is the product biosynthesis gas. The dry gas composition of the product biosynthesis gas is: H2: 41%; CO: 28%; CO2: 13%; CH4: 11%; C2H4: 3%.

[0036] Example 4 This embodiment uses the same apparatus and process as Embodiment 1, the difference being that: air is preheated to 300℃ and ammonia to 250℃. After passing through a disperser, the ammonia to air flow ratio is 0.08:1. Simultaneously, an ammonia combustion catalyst (NiCo2O4 honeycomb ceramic catalyst) bed is introduced. After passing through, the ammonia is ignited, serving as both a heating gas and a fluidizing gas. Straw pellets (average particle size 10mm) and SCR catalyst pellets (Cu / ZSM-5, average particle size 10mm) are premixed and fed into the fluidization zone of the reactor via a screw feeder. The feeder maintains the fluidization state of the materials within the fluidization zone with the introduced fluidizing gas. Ammonia combustion and biomass gasification reactions occur simultaneously within the fluidization zone. After normal operation, the amount of ammonia added is reduced, and the reaction temperature is controlled at 800±50℃, and the gas velocity is controlled at 0.7±0.1m / s. The obtained biomass gas is condensed to remove the tar (tar content 0.18g / m³). 3 The remaining gas is the product biosynthesis gas. The composition of the product biosynthesis gas is: H2: 40%; CO: 29%; CO2: 12%; CH4: 12%; C2H4: 5%.

[0037] Example 5 This embodiment uses the same apparatus and process as Embodiment 2, the difference being that: air is preheated to 300℃ and ammonia to 250℃. After passing through a disperser, the ammonia and air flow ratio is 0.1:1. Simultaneously, an ammonia combustion catalyst bed (CuMn2O4 honeycomb ceramic catalyst) is introduced. After passing through, the ammonia is ignited, serving as both a heating gas and a fluidizing gas. Wood pellets (average particle size 15mm) and SCR catalyst particles (Cu / SSZ-13, average particle size 15mm) are premixed and fed into the reactor fluidization zone via a screw feeder. The materials in the fluidization zone are kept fluidized by the introduced fluidizing gas. Ammonia combustion and biomass gasification reactions occur simultaneously in the fluidization zone. After normal operation, the amount of ammonia added is reduced, and the reaction temperature is controlled at 800±50℃, and the gas velocity is controlled at 0.7±0.1m / s. The obtained biomass gas is condensed to remove the tar (tar content 0.2g / m³). 3 The remaining gas is the product biosynthesis gas. The composition of the product biosynthesis gas is: H2: 43%; CO: 22%; CO2: 22%; CH4: 10%; C2+C3: 1.5%.

[0038] Example 6 This embodiment uses the same apparatus and process as Embodiment 2, the difference being that: air is preheated to 300℃ and ammonia to 250℃. After passing through a disperser, the ammonia and air flow ratio is 0.1:1. Simultaneously, an ammonia combustion catalyst bed (NiCo2O4 honeycomb ceramic catalyst) is introduced. After passing through, the ammonia is ignited, serving as both a heating gas and a fluidizing gas. Wood pellets (average particle size 15mm) and SCR catalyst particles (V2O5 / TiO2-based denitration catalyst, average particle size 15mm) are premixed and fed into the reactor fluidization zone via a screw feeder. The materials in the fluidization zone are kept fluidized by the introduced fluidizing gas. Ammonia combustion and biomass gasification reactions occur simultaneously in the fluidization zone. After normal operation, the amount of ammonia added is reduced, and the reaction temperature is controlled at 850±100℃, and the gas velocity is controlled at 0.7±0.1m / s. The obtained biomass gas is condensed to remove the tar (tar content 0.15g / m³). 3 The remaining gas is the product biosynthesis gas. The composition of the product biosynthesis gas is: H2: 43%; CO: 20%; CO2: 22%; CH4: 13%; C2+C3: 1.5%.

[0039] Comparative Example 1 Same as Example 1, except without the ammonia combustion zone. The resulting biomass gas is condensed to remove the tar (tar content 2 g / m³). 3 The remaining gas is the product biosynthesis gas. The composition of the product biosynthesis gas is: H2: 37%; CO: 25%; CO2: 18%; CH4: 10%; C2H4: 3%.

[0040] Comparative Example 2 Same as Example 2, except that no SCR catalyst was added. The resulting biomass gas was condensed to remove the tar (tar content 0.5 g / m³). 3 The remaining gas is the product biosynthesis gas. The composition of the product biosynthesis gas is: H2: 37%; CO: 15%; CO2: 33%; CH4: 13%; C2+C3: 1.5%.

[0041] NO X 2000ppm.

[0042] All the above gas compositions exclude nitrogen and water vapor present in the gas. The portion whose sum is less than 100% consists of organic compounds larger than C3.

[0043] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention, and not to limit them; although the present invention has been described in detail with reference to the foregoing embodiments, those skilled in the art should understand that modifications can still be made to the technical solutions described in the foregoing embodiments, or equivalent substitutions can be made to some of the technical features; and these modifications or substitutions do not cause the essence of the corresponding technical solutions to deviate from the spirit and scope of the technical solutions of the embodiments of the present invention.

Claims

1. An apparatus for biomass gasification to produce syngas, characterized in that, It includes an ammonia combustion zone located at the bottom of the biomass reactor and a fluidization zone located above the ammonia combustion zone; the ammonia combustion zone is filled with an ammonia combustion catalyst, and the fluidization zone contains a particulate SCR catalyst.

2. The apparatus according to claim 1, characterized in that, The top of the biomass reactor is equipped with a syngas outlet; And / or, the fluidization zone is provided with a biomass particle inlet.

3. The apparatus according to claim 1 or 2, characterized in that, The ammonia combustion zone is provided with an ammonia inlet and an oxygen-containing gas inlet, preferably with multiple ammonia inlets and multiple oxygen-containing gas inlets at the bottom of the ammonia combustion zone; and / or, the sulfidation zone is also provided with a fluidizing gas inlet, which is connected to a fluidizing gas source, preferably with multiple fluidizing gas inlets around the reactor.

4. The apparatus according to any one of claims 1-3, characterized in that, It also includes a biomass feeding device connected to the biomass reactor; the biomass feeding device includes a biomass bin and a screw feeder, the biomass bin being connected to the screw feeder, and the screw feeder being connected to the biomass reactor at the biomass pellet inlet.

5. A method for producing syngas from biomass gasification, characterized in that, include: Biomass pellets and SCR catalyst pellets are added to the fluidization zone of the biomass reactor. Oxygen-containing gas and ammonia are introduced into the ammonia combustion zone of the biomass reactor. After being ignited by the ammonia combustion catalyst, the gas enters the fluidization zone. The gas flow and reaction temperature are controlled. Ammonia combustion and biomass gasification reactions take place in the fluidization zone.

6. The method according to claim 5, characterized in that, The oxygen content of the oxygen-containing gas is 10-50% by volume fraction, preferably air; and / or, the fluidizing gas is nitrogen.

7. The method according to claim 5 or 6, characterized in that, The volume ratio of ammonia to air is 0.05–0.2:1, the fluidizing gas velocity is 0.1–5 m / s, and the temperature in the reaction zone is 600–900℃.

8. The method according to any one of claims 5-7, characterized in that, The ammonia combustion catalyst is selected from one or more of bimetallic oxide honeycomb ceramic catalysts, noble metal honeycomb ceramic catalysts, and Cu-based molecular sieve honeycomb catalysts; preferably, the active center of the bimetallic oxide honeycomb ceramic catalyst is selected from one or more of MnCo2O4, CoCr2O4, NiCo2O4, CuCr2O4, and CuMn2O4; the active center of the noble metal honeycomb ceramic catalyst is selected from one or more of Pt, Pd, Ru, and Au; the active center of the Cu-based molecular sieve honeycomb catalyst is selected from one of CuAg, CuCe, and Cu metal, and the molecular sieve support is selected from one of SSZ-13, S-1, Beta-25, and ZSM-5.

9. The method according to any one of claims 5-8, characterized in that, The granular SCR catalyst is a titanium vanadium oxide catalyst, a natural ore catalyst, or a Cu-based molecular sieve catalyst; preferably, the titanium vanadium oxide catalyst is selected from one or more of V2O5, TiO2, WO3, V2O5 / TiO2, and V2O5-WO3 / TiO2; the natural ore catalyst is selected from one or more of BaTiO3, LaMnO3, SrTiO3, and LaCoO3; the active center of the Cu-based molecular sieve catalyst is selected from one of CuAg, CuCe, and Cu metal, and the molecular sieve support is selected from one of SSZ-13, S-1, Beta-25, and ZSM-5; the particle size of the granular SCR catalyst is preferably 5 mm to 50 mm, more preferably 10 mm to 20 mm.

10. The method according to any one of claims 5-9, characterized in that, The biomass pellets are selected from one or more of wood pellets, straw pellets and seaweed pellets; preferably, the size of the biomass pellets is 5mm to 50mm, and more preferably 10mm to 20mm.

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