Entrained flow, reaction, heat transfer coupled gasifier

Abstract

The utility model provides a flow, reaction, heat transfer coupling's gas flow bed gasification furnace. The gas flow bed gasification furnace includes furnace body, and furnace body includes the radiation heat transfer area, gasification reaction area and solid collection area who intercommunicate in turn from top to bottom, is equipped with the first necking at the junction of radiation heat transfer area and gasification reaction area, the first necking is located on the central axis of furnace body, and the diameter of first necking is less than the diameter of radiation heat transfer area, gasification reaction area. The gasification furnace of the utility model not only can improve carbon conversion rate, realizes more efficient energy recovery, can also promote the smooth discharge of molten slag, thereby in improving the biomass gasification efficiency and flexibility, reduce environmental pollution, realize the sustainable development utilization of biomass energy.

Description

Technical Field

[0001] This utility model relates to a fluidized bed gasifier that couples flow, reaction, and heat transfer. Background Technology

[0002] In the current development of sustainable energy, the effective utilization of biomass resources has become a research hotspot. Biomass gasification is a technology that converts solid biomass into usable gaseous fuel. Its basic process involves the decomposition of biomass under high-temperature conditions in an oxygen-deficient or oxygen-limited environment to produce syngas. The advantage of this technology is that it can convert waste biomass resources into high-value gaseous fuels, reducing the environmental burden of biological waste and providing a new pathway for clean energy production.

[0003] Fluidized bed gasification technology improves the contact efficiency between gas and solids, which is beneficial for increasing the gasification reaction rate, while effectively reducing harmful waste such as tar. Therefore, this technology is widely used. Multi-nozzle gasification technology has many advantages, including high load capacity, strong adaptability, and high conversion rate. By setting multiple nozzles on the gasifier, multi-nozzle gasification technology not only allows for flexible adjustment of the system load through nozzle operation but also enables the synergistic processing of multiple raw materials through the diversion operation of different nozzles.

[0004] Although biomass multi-nozzle fluidized bed gasification technology has shown promising application prospects in theory and experiments, it still faces some technical challenges in commercial applications. Existing gasifiers focus more on reaction in terms of function, with relatively less consideration for flow and heat transfer. Utility Model Content

[0005] To overcome the shortcomings of existing gasifiers, such as limited load control range, high fly ash content in the produced syngas, and difficulty in achieving ideal carbon conversion rates, this invention provides a fluidized bed gasifier that couples flow, reaction, and heat transfer. This fluidized bed gasifier couples flow, reaction, and heat transfer, which not only enhances the reaction and improves carbon conversion, but also recovers the high-grade steam, a byproduct of the high-temperature syngas, achieving more efficient energy recovery. Furthermore, it reduces the ash content of the syngas, thereby improving biomass gasification efficiency and flexibility while reducing the risk of equipment ash accumulation, thus realizing the sustainable development and utilization of biomass energy.

[0006] The present invention solves the above-mentioned technical problems through the following technical solution:

[0007] This utility model provides a fluidized bed gasifier with coupled flow, reaction, and heat transfer, which includes a furnace body. The furnace body includes, from top to bottom, interconnected radiative heat transfer zone, gasification reaction zone, and solid collection zone. A first constriction is provided at the connection between the radiative heat transfer zone and the gasification reaction zone. The first constriction is located on the central axis of the furnace body, and the minimum diameter of the first constriction is smaller than the diameter of the radiative heat transfer zone and the diameter of the gasification reaction zone.

[0008] The top of the radiative heat transfer zone is provided with an outlet for discharging syngas;

[0009] The sidewall of the gasification reaction zone is provided with n pairs of nozzle chambers, where n is a positive integer greater than or equal to 1; each pair of nozzle chambers is symmetrically arranged along the central axis of the furnace body; each nozzle chamber contains one nozzle; the deflection angle of each nozzle in the radial direction of the gasification reaction zone is 2°-12°; the nozzles in each pair of nozzle chambers are parallel to each other in the radial direction of the gasification reaction zone; each nozzle is inclined upward along the height direction of the fluidized bed gasifier.

[0010] In this utility model, "each pair of nozzle chambers is symmetrically arranged along the central axis of the furnace body" means that the two nozzle chambers are arranged opposite each other, which is beneficial for equipment connection and installation.

[0011] In this invention, the deflection angle of the nozzle refers to the angle between the nozzle and the line connecting two opposing nozzle chambers on the plane of the gasification reaction zone with nozzle chambers.

[0012] In this invention, the deflection setting of the nozzle helps to generate strong centrifugal force and form a strong swirling field inside the gasification reaction zone during the gasification process, which helps to prolong the residence time of the material and improve the carbon conversion rate. Furthermore, the solid particles are thrown onto the wall of the gasification reaction zone under the action of centrifugal force, flow downward along the wall, and form coarse slag that is discharged into the solid collection zone, thereby reducing the ash content in the syngas.

[0013] In this invention, by tilting the nozzle upwards along the height direction of the fluidized bed gasifier, a spiral upward swirling flow field is formed. This not only enhances the centrifugal effect, allowing for more thorough mixing of the gasification feedstock and gasifying agent, but also avoids the vertical impact of the airflow on the furnace wall and nozzle, reducing the risk of wear. Furthermore, it avoids high temperatures in the area near the burner, thus protecting the burner.

[0014] In this invention, the structure of the first constriction can guide the syngas to flow upward while hindering the upward movement of solid particles (fly ash), which can significantly reduce the content of solid particles in the gas phase, thereby reducing the fly ash content in the syngas. Furthermore, when the syngas containing a small amount of solid particles passes upward through the first constriction, the first constriction has a rectification effect, guiding the solid particles to move towards the center of the radiative heat transfer zone. The syngas is discharged from the outlet at the top of the radiative heat transfer zone, thereby weakening the movement of solid particles towards the wall of the radiative heat transfer zone and thus reducing adhesion and heat transfer performance.

[0015] In this invention, each of the nozzle chambers can be arranged on the same plane in the horizontal direction.

[0016] In this invention, each of the nozzle chambers can be arranged on different planes in the horizontal direction, but each pair of opposite nozzle chambers must be arranged on the same plane.

[0017] In some embodiments, the outlet of each of the nozzles is located on the same plane in the horizontal direction.

[0018] In some embodiments, the deflection angle of each nozzle in the radial direction of the gasification reaction zone is 5°-10°, for example, 5°.

[0019] In some embodiments, in the height direction of the fluidized bed gasifier, each nozzle makes an angle of 0°-15° with the horizontal plane, but not 0°.

[0020] In some implementations, the number of nozzle chambers is 1-4 pairs, for example, 1 pair or 2 pairs.

[0021] In this invention, the nozzle chambers are symmetrically arranged to facilitate the installation of the nozzles.

[0022] In some embodiments, the number of nozzles is 2 to 8, for example, 2 or 4.

[0023] In a specific implementation, when the number of nozzles is four, each nozzle deflects clockwise in the radial direction of the gasification reaction zone, or each nozzle deflects counterclockwise in the radial direction of the gasification reaction zone, in order to enhance the load control capability and material handling flexibility during the gasification process.

[0024] In a specific implementation, each pair of nozzles is used to supply the same material to the gasification reaction zone; the material may be in powder, slurry, or gaseous form.

[0025] In a specific embodiment, the nozzle is a multi-channel nozzle; those skilled in the art should know that the structure of a multi-channel nozzle, from the center outwards, includes a gasification raw material channel and a gasifying agent channel.

[0026] In a preferred embodiment, the multi-channel nozzle can be a three-channel burner, consisting of a gasification feedstock channel, an oxygen channel, and a steam channel from the center outwards. When the three-channel burner is operating normally without steam, CO2 can be introduced as a protective gas. The three streams of biomass powder are ejected from the burner, with a high-speed oxygen stream flowing outside the biomass powder at a certain angle. The oxygen stream disperses the biomass powder through vibration and other means.

[0027] In one embodiment, one pair of nozzles supplies biomass to the gasification reaction zone, while another pair of nozzles supplies waste to the same zone, enabling co-processing of waste. This split-flow design not only increases the functional versatility of the fluidized bed gasifier but also enhances the overall energy recovery and utilization rate through the utilization of the calorific value of the waste.

[0028] In this invention, the height and inner diameter of the gasification reaction zone can be determined based on the reaction time and residence time of the gasification raw materials.

[0029] In this invention, the height and inner diameter of the radiative heat transfer zone can be determined based on the amount of heat transferred.

[0030] In some embodiments, each of the nozzle chambers is located in the middle of the gasification reaction zone; preferably, each of the nozzle chambers is located at 1 / 3 to 2 / 3 of the height of the gasification reaction zone.

[0031] In this invention, the first constriction has a structure that is narrow in the middle and wide at the top and bottom; the minimum diameter of the first constriction refers to the diameter of the middle section of the first constriction.

[0032] In some embodiments, the ratio of the minimum diameter of the first constriction to the inner diameter of the gasification reaction zone is (0.2-0.8):1.

[0033] In some embodiments, a second constriction is provided at the connection between the gasification reaction zone and the solid collection zone; compared with the downcomer in the prior art, the structural design of the second constriction allows the molten slag to gather towards the center under the action of gravity and fall into the solid collection zone for quenching.

[0034] The second constriction has a structure that is narrow in the middle and wide at the top and bottom; the minimum diameter of the second constriction refers to the diameter of the middle section of the second constriction.

[0035] The solid collection area may be referred to as a slag pool.

[0036] In a specific embodiment, the second constriction is located on the central axis of the furnace body.

[0037] In a specific implementation, the minimum diameter of the second constriction is smaller than the diameter of the gasification reaction zone and the diameter of the solid collection zone.

[0038] In a specific implementation, the ratio of the minimum diameter of the second constriction to the inner diameter of the gasification reaction zone is (0.2-0.8):1.

[0039] In some embodiments, the fluidized bed gasifier further includes a shell, which is disposed outside the furnace body to form a sleeve structure.

[0040] In some embodiments, the fluidized bed gasifier further includes a water-cooled wall disposed on the wall surface of the radiative heat transfer zone and the gasification reaction zone. The water-cooled wall is used to recover heat dissipation from the gasifier, and the radiative heat transfer zone is also used to absorb and transfer heat to maximize the absorption and utilization of thermal energy. By combining the radiative heat transfer zone and the water-cooled wall, the overall energy efficiency of the gasifier can be improved.

[0041] In this invention, the air outlet at the top of the radiative heat transfer zone can be connected to a syngas pipeline.

[0042] The positive and progressive effects of this utility model are as follows:

[0043] (1) The gasifier of this utility model adopts a multi-nozzle circumferential opposing deflection structure. On the one hand, it can achieve a larger load control range than a single nozzle by switching multiple nozzles, and can also gasify multi-phase raw materials in a coordinated manner. On the other hand, through the deflection structure design of the nozzles, a swirling flow field can be formed in the furnace, which can improve the reaction efficiency and optimize the flow and separation of gas and solid phases, thereby improving the overall conversion efficiency.

[0044] (2) The gasifier of this utility model adopts a narrow-mouth connection between the radiation heat transfer zone and the gasification reaction zone to rectify the particle-syngas two-phase flow and realize the control of the gas-solid flow path.

[0045] (3) This utility model achieves integrated flow-reaction-heat transfer in the gasifier through structural optimization design, thereby improving gasification efficiency and energy recovery rate. It can efficiently convert biomass and waste, achieve high carbon conversion rate and energy recovery rate, and reduce environmental pollution, providing a new solution for the sustainable use of biomass energy.

[0046] (4) In the preferred embodiment of this utility model, the dual heat recovery design of water-cooled wall and radiant heat transfer zone can generate steam as a by-product while recovering heat, which effectively improves the energy utilization rate of the gasifier. Specifically, the radiant waste boiler directly absorbs the heat energy of high-temperature gas through radiant heat exchange (instead of traditional convective heat exchange), which can quickly reduce the syngas temperature of up to 1200-1600℃ to 700-900℃, while generating high-pressure steam of 9-14 MPa (steam temperature of 450-550℃), which is industrial high-grade steam.

[0047] In addition, the higher temperature at the bottom of the gasifier can promote the flow of molten slag. Attached Figure Description

[0048] Figure 1 This is a schematic diagram of the structure of the fluidized bed gasifier in Example 1;

[0049] Figure 2 This is a schematic diagram of the cross-section of the gasification reaction zone in the fluidized bed gasifier of Example 1;

[0050] Figure 3 This is a schematic diagram of the material flow direction in the fluidized bed gasifier of Example 1.

[0051] Explanation of reference numerals in the attached figures:

[0052] Fluidized bed gasifier 1

[0053] Radiative heat transfer zone 101

[0054] First narrowing 102

[0055] Gasification reaction zone 103

[0056] Second narrowing 104

[0057] Solid collection area 105

[0058] Water-cooled wall 106

[0059] Air outlet 107

[0060] Nozzle chamber 108

[0061] Nozzle 109

[0062] Casing 110. Detailed Implementation

[0063] The preferred embodiments are listed below, and the present invention will be described more clearly and completely in conjunction with the accompanying drawings.

[0064] Example 1

[0065] This embodiment discloses a fluidized bed gasifier with coupled flow, reaction, and heat transfer. Figure 1 This is a schematic diagram of the structure of the fluidized bed gasifier in this embodiment. Figure 2 This is a schematic cross-sectional view of the gasification reaction zone in the fluidized bed gasifier of this embodiment.

[0066] The fluidized bed gasifier 1 includes a furnace body, which includes, from top to bottom, interconnected radiative heat transfer zone 101, gasification reaction zone 103, and solid collection zone 105. A first constriction 102 is provided at the connection between the radiative heat transfer zone 101 and the gasification reaction zone 103. The first constriction 102 is located on the central axis of the furnace body, and the minimum diameter of the first constriction 102 is smaller than the diameter of the radiative heat transfer zone 101 and the diameter of the gasification reaction zone 103.

[0067] The top of the radiant heat transfer zone 101 is provided with an outlet 107 for discharging syngas;

[0068] Two pairs of nozzle chambers 108 are provided on the side wall of the gasification reaction zone 103; each pair of nozzle chambers 108 is symmetrically arranged along the central axis of the furnace body; each nozzle chamber 108 is provided with a nozzle 109; the deflection angle of each nozzle 109 in the radial direction of the gasification reaction zone 103 is 5°; the nozzles 109 in each pair of nozzle chambers 108 are parallel to each other in the radial direction of the gasification reaction zone 103.

[0069] Each nozzle 109 is inclined upward along the height direction of the fluidized bed gasifier 1; in the height direction of the fluidized bed gasifier 1, the angle between each nozzle 109 and the horizontal plane is 5°.

[0070] Each pair of nozzle chambers 108 is located on the same plane in the horizontal direction; the outlet of each nozzle 109 is located on the same plane in the horizontal direction; each nozzle 109 is deflected counterclockwise in the radial direction of the gasification reaction zone 103; each pair of nozzles 109 is used to supply the same material to the gasification reaction zone 103; each nozzle 109 adopts a three-channel burner, with the gasification raw material channel, oxygen channel and steam channel arranged sequentially from the center outwards; each nozzle chamber 108 is located at 1 / 2 the height of the gasification zone 103.

[0071] The ratio of the minimum diameter of the first constriction 102 to the inner diameter of the gasification reaction zone 103 is 0.5:1;

[0072] A second constriction 104 is provided at the connection between the gasification reaction zone 103 and the solid collection zone 105; the second constriction 104 is located on the central axis of the furnace body; the minimum diameter of the second constriction 104 is smaller than the diameter of the gasification reaction zone 103 and the diameter of the solid collection zone 105; the ratio of the minimum diameter of the second constriction 104 to the inner diameter of the gasification reaction zone 103 is 0.5:1.

[0073] The fluidized bed gasifier 1 also includes a shell 110, which is located outside the furnace body to form a sleeve structure; the fluidized bed gasifier 1 also includes a water-cooled wall 106, which is located on the wall surface of the radiant heat transfer zone 101 and the gasification reaction zone 103.

[0074] Application Example 1

[0075] This application embodiment discloses the operation method of the fluidized bed gasifier of Embodiment 1, which includes the following steps:

[0076] Gasification feedstock and gasifying agent are supplied to the gasifier 101 through each nozzle 109, and a gasification reaction is carried out, resulting in syngas and solid slag in the radiation zone 101 and solid collection zone 105, respectively. That is, this embodiment can achieve gas-slag separation, that is, syngas can be collected from the gas outlet 107, and solid slag can be discharged from the solid collection zone 105.

[0077] The temperature of the gasification reaction zone 103 is set to 1300℃ and the pressure to 2.8MPa; the temperature of the radiative heat transfer zone 101 is set to 1000℃; the temperature of the solid collection zone 105 is basically the same as that of the gasification reaction zone 103; the slag pool at the bottom of the solid collection zone 105 is used to cool the molten slag.

[0078] Figure 3 This is a schematic diagram of the material flow direction in the fluidized bed gasifier of this embodiment. Due to the structural design of the fluidized bed gasifier in this embodiment, a swirling flow field is generated during the feeding and gasification process, causing solid particles to be thrown to the wall by centrifugal force in the gasification chamber. Syngas rises into the radiation zone, and molten slag falls into the solid collection zone.

[0079] The gasification feedstock is biomass, which is supplied to gasifier 1 via a carrier gas feed rate of 25 t / h. The gasifying agents are oxygen and steam, with a feed flow rate of 6000 Nm³. 3 / h.

[0080] Effective gas output (load) of gasifier: ~20000 Nm 3 / h.

[0081] Ash and slag production: Ash dry basis flow rate is 297 kg / h, slag dry basis flow rate is 1188 kg / h; ash-to-slag ratio is 2:8. (The ash contains a high residual carbon content, while the slag contains a low residual carbon content. A lower ash-to-slag ratio indicates a lower residual carbon content in the product and a more complete reaction.)

[0082] Using the above-mentioned fluidized bed gasifier for gasification reaction, the carbon conversion rate of the gasification feedstock can reach 99.5%.

[0083] Comparative Example 1

[0084] This comparative example discloses an OMB gasifier in the art; its core difference from the fluidized bed gasifier of Example 1 is that the nozzles are arranged opposite each other in the gasifier; and, the gasifier does not have a radiant heat transfer section, an outlet at the top of the radiant heat transfer zone, and a first constriction as in Example 1 above the gasification chamber; this comparative example does not have an outlet at the top of the radiant heat transfer zone, so the gas and slag flow is parallel and gas and slag separation cannot be achieved.

[0085] The other structures are basically the same as those of the fluidized bed gasifier in Example 1.

[0086] Comparative Example 2

[0087] This comparative example discloses an SE gasifier in the art; its core difference from the fluidized bed gasifier of Example 1 is that only one nozzle is provided at the top of the gasifier; and, the gasifier does not have a radiant heat transfer section, an outlet at the top of the radiant heat transfer zone, and a first constriction as in Example 1 above the gasification chamber; this comparative example does not have an outlet at the top of the radiant heat transfer zone, so it is a gas-slag co-flow and cannot achieve gas-slag separation.

[0088] The other structures are basically the same as those of the fluidized bed gasifier in Example 1.

[0089] Comparative Example 3

[0090] This comparative example discloses a GE gasifier in the art; its core difference from the fluidized bed gasifier of Example 1 is that only one nozzle is provided at the top of the gasifier; and, the gasifier does not have a radiant heat transfer section, an outlet at the top of the radiant heat transfer zone, and a first constriction as in Example 1 above the gasification chamber; this comparative example does not have an outlet at the top of the radiant heat transfer zone, so it is a gas-slag co-flow and cannot achieve gas-slag separation.

[0091] The other structures are basically the same as those of the fluidized bed gasifier in Example 1.

[0092] Comparative Example 4

[0093] This comparative example discloses an aerospace furnace in the art; its core difference from the fluidized bed gasifier of Example 1 is that only one nozzle is provided at the top of the gasifier; and, the gasifier does not have a radiant heat transfer section, an outlet at the top of the radiant heat transfer zone, and a first constriction as in Example 1 above the gasification chamber; this comparative example does not have an outlet at the top of the radiant heat transfer zone, so it is a gas-slag co-flow and cannot achieve gas-slag separation.

[0094] The other structures are basically the same as those of the fluidized bed gasifier in Example 1.

[0095] Example 1

[0096] This effective embodiment verifies the load regulation capability of the fluidized bed gasifier in Embodiment 1.

[0097] When adjusting the load of the gasifier, the pressure and temperature of the gasifier should be precisely controlled within the aforementioned target values ​​to ensure gasification efficiency and safety. Setting the load range ensures that the pressure and temperature inside the gasifier remain within a safe and effective operating range under different working pressures.

[0098] When using SE gasifiers, GE gasifiers, or aerospace gasifiers, the oxygen flow rate at the nozzle needs to be limited within a certain range to ensure the safety and efficiency of the gasifier. For example, the design requirements for gasifiers stipulate that the oxygen flow rate should not exceed 135 m / s and should not be lower than 103 m / s. This helps maintain stable combustion and gasification processes inside the gasifier. Considering that biomass feedstock and oxygen enter the gasifier through the same nozzle, the oxygen flow rate at the burner outlet needs to be monitored when adjusting the load. In this case, the load range for the aforementioned SE gasifiers, GE gasifiers, or aerospace gasifiers is generally 60% to 110%.

[0099] When using the fluidized bed gasifier of Example 1, during low-load adjustment, a pair of nozzles can be closed first, thereby reducing the load to 50%. Based on this, the nozzle's adjustment capacity of 60% to 110% can be further utilized. The overall load range of the fluidized bed gasifier of Example 1 is 30% to 110%.

[0100] Example 2

[0101] This embodiment studies the ash-to-slag ratio produced by the fluidized bed gasifier of Example 1 and existing gasifiers by controlling the swirling flow field and the gas-slag separation at the constriction. Table 1 shows the ash-to-slag ratio produced by different gasifiers.

[0102] Table 1

[0103]

[0104] As shown in the table above, the fluidized bed gasifier of this application, through the combination of "multi-nozzle swirl + upward-curving nozzles + constricted nozzle structure," generates a swirling flow field during feeding and gasification. The material spirals upward, causing solid particles to be thrown against the wall by centrifugal force in the gasification chamber, reducing the amount of particles escaping with the syngas. Furthermore, the constricted nozzle structure hinders the upward movement of particles, further reducing the amount of particles escaping with the syngas. These measures significantly reduce the amount of fly ash particles carried out by the syngas (product gas), resulting in an ash-to-slag ratio of approximately 2:8.

[0105] Example 3

[0106] This effective embodiment verifies the combined heat transfer effect of the water-cooled wall and the radiant zone of the gasifier in Example 1.

[0107] In the gasifier combining a water-cooled wall and a radiant zone in Example 1, besides the water-cooled wall transferring approximately 3.6 GJ / h of heat, the radiant zone can cool the syngas from 1300°C to 1000°C, with a heat transfer rate as high as 15.5 GJ / h. High-grade heat can be collected in the radiant zone, such as generating high-pressure saturated steam at 11.8 MPaG. The cooled syngas at 1000°C is then further subjected to heat recovery processing.

[0108] The fluidized bed gasifier using the combined heat transfer technology described in this application can effectively recover the sensible heat of high-temperature syngas, significantly improving the thermal efficiency of the gasifier.

Claims

1. A fluidized bed gasifier with coupled flow, reaction, and heat transfer, characterized in that, It includes a furnace body, which comprises, from top to bottom, interconnected radiative heat transfer zone, gasification reaction zone, and solid collection zone. A first constriction is provided at the connection between the radiative heat transfer zone and the gasification reaction zone. The first constriction is located on the central axis of the furnace body, and the minimum diameter of the first constriction is smaller than the diameter of the radiative heat transfer zone and the diameter of the gasification reaction zone. The top of the radiative heat transfer zone is provided with an outlet for discharging syngas; The sidewall of the gasification reaction zone is provided with n pairs of nozzle chambers, where n is a positive integer greater than or equal to 1; each pair of nozzle chambers is symmetrically arranged along the central axis of the furnace body; each nozzle chamber contains one nozzle; the deflection angle of each nozzle in the radial direction of the gasification reaction zone is 2°-12°; the nozzles in each pair of nozzle chambers are parallel to each other in the radial direction of the gasification reaction zone; each nozzle is inclined upward along the height direction of the fluidized bed gasifier.

2. The fluidized bed gasifier with coupled flow, reaction, and heat transfer as described in claim 1, characterized in that, All of the nozzle chambers are disposed on the same plane in the horizontal direction; The outlet of each nozzle is located on the same plane in the horizontal direction.

3. The fluidized bed gasifier with coupled flow, reaction, and heat transfer as described in claim 1, characterized in that, The deflection angle of each nozzle in the radial direction of the gasification reaction zone is 5°-10°; In the height direction of the fluidized bed gasifier, the angle between each nozzle and the horizontal plane is 0°-15°, but not 0°.

4. The fluidized bed gasifier with coupled flow, reaction, and heat transfer as described in claim 1, characterized in that, The number of nozzle chambers is 1-4 pairs; the number of nozzles is 2-8.

5. The fluidized bed gasifier with coupled flow, reaction, and heat transfer as described in claim 4, characterized in that, When the number of nozzles is 4, each nozzle satisfies one or more of the following conditions: ① Each of the nozzles is deflected clockwise in the radial direction of the gasification reaction zone, or each of the nozzles is deflected counterclockwise in the radial direction of the gasification reaction zone; ② Each pair of nozzles is used to supply the same material to the gasification reaction zone; ③The nozzle is a multi-channel nozzle.

6. The fluidized bed gasifier with coupled flow, reaction, and heat transfer as described in claim 1, characterized in that, Each of the nozzle chambers is located in the middle of the gasification reaction zone; The ratio of the minimum diameter of the first constriction to the inner diameter of the gasification reaction zone is (0.2-0.8):

1.

7. The fluidized bed gasifier with coupled flow, reaction, and heat transfer as described in claim 6, characterized in that, Each of the nozzle chambers is located at a height of 1 / 3 to 2 / 3 of the gasification reaction zone.

8. The fluidized bed gasifier with coupled flow, reaction, and heat transfer as described in claim 1, characterized in that, A second constriction is provided at the connection between the gasification reaction zone and the solid collection zone.

9. The fluidized bed gasifier with coupled flow, reaction, and heat transfer as described in claim 8, characterized in that, The second narrowing meets one or more of the following conditions: ①The second constriction is located on the central axis of the furnace body; ② The minimum diameter of the second constriction is smaller than the diameter of the gasification reaction zone and the diameter of the solid collection zone; ③ The ratio of the minimum diameter of the second constriction to the inner diameter of the gasification reaction zone is (0.2-0.8):

1.

10. The fluidized bed gasifier with coupled flow, reaction, and heat transfer as described in claim 1, characterized in that, The fluidized bed gasifier also includes a shell, which is located outside the furnace body to form a sleeve structure; The fluidized bed gasifier also includes a water-cooled wall, which is disposed on the wall surface of the radiative heat transfer zone and the gasification reaction zone.

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