A downdraft gasifier

Abstract

The application provides a downdraft gasifier, which comprises at least two gasification chambers, the gasification chamber comprises a cylinder, the top of the cylinder is a feeding port, the bottom of the cylinder is a gas and slag discharging port, a buffer speed reduction disperser is arranged in the cylinder, and a plurality of layers of flame burners are arranged on the cylinder, each layer of the flame burners comprises a plurality of flame burners; the gas and slag discharging ports of the two gasification chambers are connected with a separation chamber through inclined pipelines; in the application, one separation chamber is matched with a plurality of gasification chambers, flexible production capacity increase and decrease are realized, flexible maintenance is realized, the plurality of layers of flame burners are arranged, heating uniformity is good, and uniform heating and complete gasification of materials are ensured.

Description

Technical Field

[0001] This application relates to the field of gasifier technology, specifically to a settling gasifier. Background Technology

[0002] Settling gasifiers are key equipment in chemical reaction processes, and the choice of furnace type in gasification processes affects the economics of the entire process and plays an important role in the overall plant operating efficiency. A settling gasifier is a gasification device that uses solid fuels such as coal, municipal solid waste, and biomass as raw materials to generate syngas through gasification reaction, and the ash and slag in the furnace are discharged naturally by gravity.

[0003] The existing gasifiers are of the following types: entrained flow, fluidized bed, and fixed bed. They have a relatively high capacity, but all of them require pre-processing of raw materials. For example, entrained flow requires grinding, biomass raw materials need to be pre-carbonized or baked, and coal-water slurry gasification requires grinding coal into slurry. Moreover, the cost of grinding coal is relatively high, resulting in high processing costs. Furthermore, when a gasifier malfunctions, the entire gasifier needs to be shut down for maintenance, which further affects the capacity.

[0004] To address the aforementioned issues, this application proposes to develop a settling gasifier capable of rapid pyrolysis gasification, and capable of partial shutdown and maintenance of a single furnace when a problem occurs. After a detailed search, the applicant has not found any relevant technical solutions.

[0005] Therefore, a new technical solution is needed to solve the above-mentioned technical problems. Utility Model Content

[0006] This application provides a settling gasifier, comprising at least two gasification chambers, wherein the gasification chambers include:

[0007] The cylinder has a feed inlet at the top and an exhaust and slag discharge outlet at the bottom. At least two layers of buffer speed-reducing dispersers are installed inside the cylinder, and multiple layers of flame burners are installed on the cylinder, with each layer of flame burners including multiple burners. The exhaust and slag discharge outlets of the two gasification chambers are connected to the separation chamber through inclined pipes.

[0008] As a preferred embodiment, the inclined pipe is equipped with a high-temperature resistant valve.

[0009] As a preferred embodiment, the number of high-temperature resistant valves is two.

[0010] As a preferred embodiment, during 100% intensity gasification, the wall temperature T2 of the gasification chamber is 800℃-1200℃, and the temperature T3 of the core reaction zone where the material reacts within the gasification chamber increases sequentially from top to bottom, with a temperature difference of 100℃-200℃ between adjacent temperatures.

[0011] As a preferred embodiment, the temperature T1 at 10mm to 50mm outside the cylinder wall of the gasification chamber 1 is 600℃-1000℃.

[0012] As a preferred embodiment, the outer side of the separation chamber is provided with multiple layers of flame burners, each layer comprising multiple flame burners.

[0013] As a preferred option, the multi-layer flame burner is positioned within a range of 1500 mm to 2500 mm above the centerline of the feed inlet of the separation chamber.

[0014] As a preferred embodiment, the buffer deceleration diffuser includes a hollow central disc, with an edge ring correspondingly disposed at the lower part of the central disc. There is a gap between the central disc and the edge ring, and multiple flame burners are disposed on the cylinder corresponding to the gap. The central disc and the edge ring are connected by a connector. The central disc is inclined downwards and gradually increases in size. The top of the central disc is closed, and the lower part of the central disc is open. Multiple sets of central disc circular holes are formed on the side wall of the central disc. The edge ring is inclined downwards and gradually decreases in size. Both the top and the lower part of the edge ring are open. Multiple sets of edge ring circular holes are formed on the side wall of the edge ring.

[0015] As a preferred embodiment, the diameter of the inner circle of the intermediate disk is 2 / 3 to 4 / 5 of the diameter of the cylinder.

[0016] As a preferred embodiment, the circular holes in the intermediate disk are distributed in a gradient, increasing in size from top to bottom.

[0017] As a preferred option, the diameter of the circular hole in the intermediate disk is 5mm-30mm.

[0018] As a preferred embodiment, the edge ring has a transition arc on the side of its edge sidewall near the top.

[0019] As a preferred embodiment, the angle between the edge sidewall and the central axis of the gasification chamber is 15°-75°.

[0020] As a preferred embodiment, the angle between the tangent of the transition arc on the side near the top and the central axis of the gasification chamber is 60°-85°.

[0021] As a preferred embodiment, the edge annular holes are distributed in a gradient, increasing in size from top to bottom.

[0022] As a preferred embodiment, the diameter of the top of the edge ring is equal to the inner diameter of the gasifier, and the diameter of the bottom of the edge ring is equal to 0.6-0.7 times the inner diameter of the intermediate disk.

[0023] As a preferred embodiment, the shape of the circular hole in the intermediate disk is at least one of the following: circular, elliptical, or plum blossom-shaped.

[0024] As a preferred embodiment, the shape of the edge ring hole is at least one of a circle, an ellipse, or a plum blossom shape.

[0025] This application has the following advantages:

[0026] 1. Multiple gasification chambers are equipped with one separation chamber, enabling flexible increases or decreases in production and flexible maintenance;

[0027] 2. The multi-layered and multiple arrangement of flame burners ensures good heating uniformity, guaranteeing uniform heating and complete vaporization of the material;

[0028] 3. The buffer deceleration disperser can break up lumpy, granular, or even irregularly shaped raw materials, preventing large pieces of raw materials from agglomerating or small pieces from piling up. No matter how large the initial size difference of the raw materials is, after buffering, they can be more evenly distributed in the gasification reaction zone, reducing uneven processing caused by large pieces getting stuck or small pieces gathering. Therefore, it has less restriction on the shape and size of the raw materials and is more adaptable.

[0029] 4. The buffer and deceleration disperser is set up to slow down the falling speed of raw materials by blocking and guiding the flow, so that raw materials of different sizes and shapes can stay in the optimal reaction temperature range for a sufficient time, ensuring that volatiles are fully released and fixed carbon is fully reacted, and reducing the waste of unreacted raw materials;

[0030] 5. The buffer speed-reducing disperser can disperse the raw materials, making the high-temperature carbon layer evenly distributed. At the same time, it guides the gasifying agent and tar vapor to form a stable countercurrent or cross-flow contact, increasing the contact area between the two. In addition, the buffer speed-reducing disperser can also reduce the obstruction of the airflow by the raw material particles, allowing the tar vapor to mix more smoothly with the high-temperature medium, ensuring the full decomposition of tar. Attached Figure Description

[0031] Figure 1 This is a schematic diagram of the structure of this application; Figure 2 A schematic diagram of the structure of the buffer deceleration disperser of this application; Figure 3 This is a cross-sectional view of the buffer deceleration diffuser of this application; Figure 4 This is a schematic diagram of the intermediate disk of this application; Figure 5 This is a cross-sectional view of the intermediate disk of this application; Figure 6 This is a schematic diagram of the edge ring of this application; Figure 7 This is a cross-sectional view of the edge ring of this application; Figure 8 yes Figure 5 A magnified view of part A in the middle; Figure 9 yes Figure 7A magnified view of part B in the middle section; Figure 10 This is a schematic diagram of the vaporization chamber temperature during 100% intensity vaporization; Figure 11 This is a schematic diagram of the vaporization chamber temperature when vaporization is performed at 70% intensity. Figure 12 This is a schematic diagram of the vaporization chamber temperature during 120% intensity vaporization; 1. Gasification chamber; 2. Shell; 3. Feed inlet; 4. Exhaust and slag discharge outlet; 5. Edge ring; 6. Intermediate disc; 7. Connecting parts; 8. Spacing; 9. Flame burner; 10. Inclined pipe; 11. Separation chamber; 12. High-temperature resistant valve; 13. Rib plate; 14. Side wall; 15. Circular hole in intermediate disc; 16. Edge side wall; 17. Circular hole in edge ring; 18. Transition arc; 19. Central axis of gasification chamber. Detailed Implementation

[0032] The following is in conjunction with the appendix Figure 1 — Figure 12 The specific embodiments of this utility model will be described in detail below. It should be noted that the specific embodiments described herein are for illustration and explanation only and are not intended to limit the scope of this utility model. Example 1

[0033] like Figure 1 As shown, this embodiment provides a gasifier, including at least two gasification chambers 1. Each gasification chamber 1 includes a cylinder 2. The top of the cylinder 2 is a feed inlet 3, through which materials requiring pyrolysis, such as pulverized coal and biomass fragments, enter and fall freely. The bottom of the cylinder 2 is an exhaust and slag discharge outlet 4. At least two layers of buffer deceleration dispersers are installed inside the cylinder 2. These buffer deceleration dispersers reduce the free fall velocity of the materials and disperse the particulate materials. Each layer of buffer deceleration disperser consists of an edge ring 5 and an intermediate disc 6. The intermediate disc 6 and the edge ring 5 are connected by a connector 7, preferably by welding for support. The diameter of the upper end of the edge ring 5 is equal to the inner diameter of the cylinder 2. Equally, the edge ring 5 is welded to the inside of the cylinder 2; multiple layers of flame burners 9 are provided on the cylinder 2, each layer of flame burners 9 includes multiple flame burners, and the number of flame burners 9 in each layer is preferably 2-8; more specifically: the cylinder 2 of the gasification chamber 1 corresponding to the distance 8 between the edge ring 5 and the intermediate disk 6 is provided with several flame burners 9 to ensure the uniformity of the heating flame, which can be double burners, four burners, six burners, eight burners, etc., evenly distributed, the flame burners 9 can be hydrogen-oxygen flame burners, or other types of flame burners, and the technician can choose according to the specific needs, and this application does not make specific limitations; when setting the flame burners 9, it is necessary to avoid the connecting parts 7 to avoid problems caused by high temperature.

[0034] The exhaust and slag discharge ports 4 of the two gasification chambers 1 are connected to the separation chamber 11 through inclined pipes 10. Two high-temperature resistant valves 12 are installed on the inclined pipes 10. The installation of high-temperature resistant valves 12 can isolate the gasification chambers 1. The installation of two high-temperature resistant valves 12 facilitates the control of production capacity and local shutdown maintenance. The separation chamber 11 adopts the separation chamber of the prior art, which can achieve efficient gas purification and ensure the high quality of syngas. A slag pool is set at the bottom of the separation chamber 11 to ensure carbon conversion rate. The solids first pass through cyclone separation, and some fly ash and / or gasification slag settle down. Then they enter the baffle separation zone of the three-dimensional mass transfer tower. Fly ash and / or slag settle into the slag pool of the ash silo. The gas passes through two stages of coarse purification separation and comes out from the top of the separation chamber 11.

[0035] Preferably, the sidewall of the separation chamber 11 can be arranged with multiple layers and multiple flame burners 9 to heat the synthesis gas and minimize the tar content; specifically, they are arranged in the lower middle part of the separation chamber 11, in the range of 1500 mm to 2500 mm above the center line of the feed inlet. Example 2

[0036] This embodiment provides a specific description of the temperature of the gasification chamber 1. During 100% intensity gasification, the side wall temperature T2 of the cylinder 2 of the gasification chamber 1 is 800℃-1200℃. The temperature T3 of the core reaction zone in the gasification chamber 1 where the material reacts increases from top to bottom, and the temperature difference between adjacent temperatures is 100℃-200℃. The temperature is controlled by the flame burner 9, such as controlling the hydrogen-oxygen ratio and the amount of hydrogen and oxygen used.

[0037] The gasification chamber 1 typically has three key temperatures that need to be controlled: the temperature T1 located 10mm to 50mm from the outer side of the cylinder 2's sidewall, the cylinder 2's sidewall temperature T2, and the core reaction zone temperature T3. In this embodiment, five layers of flame burners 9 are used, each layer of flame burners 9 corresponding to a core reaction zone temperature T3 that reacts with the material. Figure 10 As shown, during 100% intensity gasification, the temperature T1 near the side wall of cylinder 2 is 1000℃, the temperature T2 of the side wall of cylinder 2 is 1100℃-1200℃, and the temperature T3 of the core reaction zone that reacts with the material is 1100℃, 1200℃, 1400℃, 1500℃ and 1600℃ from top to bottom. This is because the material added to the top of gasification chamber 1 is in its original state at room temperature and without pyrolysis, resulting in a lower core reaction temperature. Figure 11 The values ​​in the diagram represent the temperatures near the second sidewall of the cylinder (T1) and the core reaction zones (T3) at 70% intensity gasification. The temperature of the second sidewall (T2) is 770℃-840℃. Figure 12 The temperatures T1 near the side wall of cylinder 2 and T3 in each core reaction zone are at 120% intensity gasification. The temperature T2 of the side wall of cylinder 2 is 1320℃-1400℃. Example 3

[0038] This embodiment provides a detailed description of the buffer deceleration disperser: The buffer deceleration disperser includes a hollow intermediate disk 6, with an edge ring 5 correspondingly arranged at the lower part of the intermediate disk 6. The upper intermediate disk 6 guides the material to the surrounding area, while the lower edge ring 5 gathers the material towards the center, thereby extending the time for the material to participate in the reaction from the feed inlet 3 to the exhaust and slag discharge outlet 4. There is a gap 8 between the intermediate disk 6 and the edge ring 5, and the intermediate disk 6 and the edge ring 5 are connected by a connector 7, preferably by welding for support connection. More preferably, a reinforcing device such as a stiffener 13 can be installed between the edge ring 5 installed at the bottom of the gasification chamber 1 and the inner wall of the cylinder 2 of the gasification chamber 1. The stiffener 13 is connected to the inner wall of the cylinder 2 and the edge ring 5 by welding or other means. The setting of the stiffener 13 further improves the stability of the buffer deceleration disperser.

[0039] The intermediate disk 6 is inclined downwards and gradually increases in size. The top of the intermediate disk 6 is closed, and the bottom of the intermediate disk 6 is open. Multiple sets of intermediate disk circular holes 15 are formed on the side wall 14 of the intermediate disk 6; preferably, as shown... Figure 4 As shown, in this embodiment, the cross-sectional shape of the intermediate disk 6 is an isosceles right triangle, with a maximum diameter of 754mm at the bottom, a height of 379mm from the bottom to the top, and a hypotenuse length of 533mm, meaning the inclined length of the sidewall 14 is 533mm, and the thickness of the sidewall 14 is 3mm. The diameter of the inner circle of the intermediate disk 6 is 2 / 3 to 4 / 5 of the diameter of the cylinder 2. Multiple sets of intermediate disk circular holes 15 are distributed in a gradient, increasing in size from top to bottom. The diameter of the intermediate disk circular holes 15 is 5mm-30mm, and the shape of the intermediate disk circular holes 15 is at least one of circular, elliptical, and plum blossom shapes. In this embodiment, as shown... Figure 5 As shown, holes are made at 25mm intervals from top to bottom along the circumference. There are 4 groups of holes with a diameter of 5mm, 4 groups of holes with a diameter of 10mm, 4 groups of holes with a diameter of 15mm, and 4 groups of holes with a diameter of 20mm. The edge ring 5 slopes downwards and gradually decreases in size. Both the top and bottom of the edge ring 5 are open. The diameter of the top of the edge ring 5 is equal to the inner diameter of the cylinder 2, and the diameter of the bottom of the edge ring 5 is 0.6-0.7 times the inner diameter of the intermediate disk 6. Multiple sets of edge ring circular holes 17 are formed on the edge sidewall 16 of the edge ring 5. Preferably, a transition arc 18 is provided on the side of the edge sidewall 16 near the top. Figure 6In this embodiment, the diameter of the top of the edge ring 5 is 1000mm, the diameter of the bottom is 500mm, the height from the bottom to the top is 272mm, the radius of the transition arc 18 is 50mm, the wall thickness of the edge sidewall 16 is 3mm, the angle between the edge sidewall 16 and the central axis 19 of the gasification chamber is 30 degrees, and the angle between the tangent of the transition arc 18 near the top and the central axis 19 of the gasification chamber is 85 degrees; the edge ring circular holes 17 are gradient-distributed, increasing in size from top to bottom, with a diameter of 5mm-30mm, and the shape of the edge ring circular holes 17 is at least one of circular, elliptical, and plum blossom-shaped. In this embodiment, as shown... Figure 7 As shown, holes are made at 25mm intervals along the circumference from top to bottom. There are 4 groups of holes with a diameter of 5mm, 4 groups of holes with a diameter of 10mm, 4 groups of holes with a diameter of 15mm, and 4 groups of holes with a diameter of 20mm.

[0040] In this embodiment, the distance between the bottom of the edge ring 5 and the top of the middle disk 6 is 800mm. When two sets of buffer deceleration dispersers are set, the distance between the tops of the two edge rings 5 ​​is 1000mm.

[0041] The aforementioned connector 7 may interfere with some of the edge ring holes 17 and the middle disc holes 15. However, since there are many edge ring holes 17 and middle disc holes 15, the interference will not affect the performance. Example 4

[0042] This embodiment provides a specific application of using the above-mentioned sedimentation gasifier to treat wheat straw, specifically: Wheat straw is crushed into lengths of 10mm-50mm and has a moisture content of ≤15%. The wheat straw is fed into the cylinder 2 through the feed inlet 3. It first impacts the top of the intermediate disc 6 on the upper layer of the buffer deceleration disperser, reducing its speed. Fine particles and pyrolyzed materials fall through the circular holes 15 of the intermediate disc. The diameter of the circular holes 15 increases from top to bottom. For larger particles, incompletely gasified materials, and materials with no significant volume reduction, the falling path is relatively long. Larger straw materials are guided by the inclined sidewall 14 to slide towards the edge, falling into the gap 8 formed with the edge ring 5. In this area, they are directly heated by the flame burner 9 and continue to fall along the edge sidewall 16 of the edge ring 5. Continuing downstream, the residence time is extended to 8-12 seconds to ensure the full release of volatiles and secondary cracking of tar. The resulting crude syngas and fly ash enter the separation chamber 11 from the exhaust slag outlet 4 through the inclined pipe 10. The fly ash first undergoes cyclone separation, with some fly ash settling, and then enters the three-dimensional mass transfer tray baffle separation zone. The fly ash settles into the primary slag pool of the ash silo. The gas undergoes two stages of coarse purification separation and exits from the top of the separation chamber 11. The setting of two gasification chambers 1 allows for easy adjustment according to production output. When one of the gasification chambers 1 malfunctions, it can be shut down for maintenance without affecting the operation of the overall equipment, achieving partial non-stop maintenance of the entire equipment. Example 5

[0043] This embodiment provides another specific application, using the above-mentioned settling gasifier to process high-density, regularly shaped shaped biomass pellets, taking the gasification of pellets with a diameter of 8mm and a length of 20mm-40mm as an example: Because the particles have good flowability but high initial density and high falling kinetic energy, and require a longer internal heat and mass transfer time to achieve complete gasification, a three-layer buffer deceleration disperser is set in the gasification chamber 1 in this embodiment to further increase the reaction path and residence time. The edge ring 5 of the bottom buffer deceleration disperser is welded to the inner wall of the cylinder 2 with a stiffening plate 13 to withstand the continuous impact of the particles.

[0044] When the biomass pellets impact the multi-layer buffer deceleration disperser, they are effectively decelerated and redistributed. The pellets roll and slide on each layer of the structure, constantly exposing new reaction surfaces. They also exchange heat efficiently with the high-temperature gas flow through the central disc circular holes 15 and the edge ring circular holes 17. This Z-shaped downward path ensures that the total residence time in the gasification chamber reaches 15-20 seconds, far exceeding the free fall time, thus ensuring complete reaction in the core part. For high-density shaped biomass pellets, this system achieves extremely high gasification efficiency, with a carbon conversion rate ≥95%. The outlet syngas has high cleanliness, and the tar content can be stably kept below 30mg / Nm³, which can be directly used to drive gas-fired internal combustion engines or synthesize chemicals. After gasification, the pellets enter the separation chamber 11 for separation, which will not be described in detail here.

[0045] In summary, due to the adoption of the above technical solution, this application has the following advantages: 1. Multiple gasification chambers can be matched with one separation chamber, enabling flexible increases or decreases in production and flexible maintenance; 2. The multi-layered arrangement of flame burners ensures good heating uniformity, guaranteeing uniform heating and complete vaporization of the material; 3. The buffer deceleration disperser can break up lumpy, granular, or even irregularly shaped raw materials, preventing large pieces of raw materials from agglomerating or small pieces from piling up. No matter how large the initial size difference of the raw materials is, after buffering, they can be more evenly distributed in the gasification reaction zone, reducing uneven processing caused by large pieces getting stuck or small pieces gathering. Therefore, it has less restriction on the shape and size of the raw materials and is more adaptable. 4. The buffer deceleration disperser is set up to slow down the falling speed of raw materials by blocking and guiding the flow, so that raw materials of different sizes and shapes can stay in the optimal reaction temperature range for a sufficient time. This ensures the residence time of the gasified raw materials, ensures the full release of volatiles and the full reaction of fixed carbon, and reduces the waste of unreacted raw materials. 5. The buffer speed-reducing disperser can disperse the raw materials, making the high-temperature carbon layer evenly distributed. At the same time, it guides the gasifying agent and tar vapor to form a stable countercurrent or cross-flow contact, increasing the contact area between the two. In addition, the buffer speed-reducing disperser can also reduce the obstruction of the airflow by the raw material particles, allowing the tar vapor to mix more smoothly with the high-temperature medium, ensuring the full decomposition of tar.

[0046] The devices and connections not specifically described above are all existing technologies, and will not be described in detail here.

[0047] The preferred embodiments of this application have been described in detail above with reference to the accompanying drawings. However, this application is not limited to the specific details of the above embodiments. Within the scope of the technical concept of this application, various simple modifications can be made to the technical solution of this application, and these simple modifications all fall within the protection scope of this application.

[0048] It should also be noted that the various specific technical features described in the above specific embodiments can be combined in any suitable way without contradiction. In order to avoid unnecessary repetition, the various possible combinations in this application will not be described separately.

[0049] Furthermore, various different implementations of this application can be combined in any way, as long as they do not violate the spirit of this application, and such combinations should also be regarded as the content disclosed in this application.

Claims

1. A settling gasifier, characterized in that, It includes at least two gasification chambers (1), each gasification chamber (1) includes a cylinder (2), the top of the cylinder (2) is a feed inlet (3), the bottom of the cylinder (2) is an exhaust and slag discharge port (4), a buffer speed reduction disperser is provided inside the cylinder (2), and multiple layers of flame burners (9) are provided on the cylinder (2), each layer of flame burners (9) includes multiple; the exhaust and slag discharge ports (4) of the two gasification chambers (1) are connected to the separation chamber (11) through an inclined pipe (10).

2. The settling gasifier according to claim 1, characterized in that, A high-temperature resistant valve (12) is installed on the inclined pipe (10).

3. A settling gasifier according to claim 1, characterized in that, When the gasification chamber (1) is gasified at 100% intensity, the cylinder wall temperature T2 is 800℃-1200℃. The core reaction zone temperature T3 in the gasification chamber (1) that reacts with the material increases from top to bottom, and the temperature difference between adjacent temperatures is 100℃-200℃.

4. A settling gasifier according to claim 3, characterized in that, The temperature T1 at 10mm to 50mm outside the cylinder wall of the gasification chamber (1) is 600℃-1000℃.

5. A settling gasifier according to claim 1, characterized in that, The separation chamber (11) has multiple layers of flame burners (9) arranged on its side wall, with each layer of flame burners (9) comprising multiple burners.

6. A settling gasifier according to claim 1, characterized in that, The buffer deceleration diffuser includes a hollow intermediate disk (6), with an edge ring (5) correspondingly arranged at the lower part of the intermediate disk (6). There is a gap (8) between the intermediate disk (6) and the edge ring (5). Multiple flame burners (9) are arranged on the cylinder (2) corresponding to the gap (8). The intermediate disk (6) and the edge ring (5) are connected by a connector (7). The intermediate disk (6) is inclined downward and gradually increases in size. The top of the intermediate disk (6) is closed and the lower part of the intermediate disk (6) is open. Multiple sets of intermediate disk circular holes (15) are opened on the side wall (14) of the intermediate disk (6). The edge ring (5) is inclined downward and gradually decreases in size. The top and bottom of the edge ring (5) are open. Multiple sets of edge ring circular holes (17) are opened on the edge side wall (16) of the edge ring (5).

7. A settling gasifier according to claim 6, characterized in that, The diameter of the inner circle of the intermediate disk (6) is 2 / 3 to 4 / 5 of the diameter of the cylinder (2).

8. A settling gasifier according to claim 6, characterized in that, The circular holes (15) in the intermediate disk are distributed in a gradient, increasing in size from top to bottom.

9. A settling gasifier according to claim 6, characterized in that, The edge annular holes (17) are distributed in a gradient, increasing in size from top to bottom.

10. A settling gasifier according to claim 6, characterized in that, The diameter of the top of the edge ring (5) is equal to the inner diameter of the cylinder (2), and the diameter of the top of the edge ring (5) is 1.2-1.5 times the inner diameter of the intermediate disk (6).

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