Nozzle for gasification of biomass powder and gasification furnace

Abstract

The application provides a nozzle for biomass powder gasification and a gasification furnace, and relates to the technical field of biomass combustion equipment. The nozzle comprises coaxially nested outer ring nozzles, middle ring nozzles, inner ring nozzles and center nozzles. Outer ring, middle ring and inner ring channels are sequentially formed between the outer side walls and the inner side walls of each adjacent nozzle. The inner wall of the center nozzle encloses a center channel. The side wall of the inner ring channel is provided with an inlet and an outlet. The inlet transports a biomass powder and conveying gas mixture. The outlet is located upstream of the inlet. A separator is arranged between the inlet and the outlet for separating part of the conveying gas from the mixture and discharging the part of the conveying gas to the outlet. A cyclone and a filter are arranged in the separator, and the cyclone is arranged below the filter. In the application, when the biomass powder is transported to the inner ring channel along with the conveying gas, the separator separates part of the conveying gas from the mixture and discharges the part of the conveying gas to the outlet, thereby reducing the conveying gas discharged from the nozzle and further reducing the inert gas entering the gasification furnace.

Description

Technical Field

[0001] This utility model relates to the field of biomass combustion equipment technology, and in particular to a nozzle and gasifier for biomass powder gasification. Background Technology

[0002] Entrained flow biomass powder gasification typically uses high-pressure carbon dioxide or nitrogen as the carrier gas. The biomass powder is transported to the gasifier via a pneumatic conveying system, where an oxidant (air, oxygen-enriched gas, oxygen, steam, etc.) is used to gasify the raw material to produce syngas (CO, H2), which can be used as a feedstock for various green chemicals and oil products. This technology has advantages such as high carbon conversion rate, high effective gas composition, low fly ash content, low ash-to-slag ratio, and no secondary pollution.

[0003] Existing gasification nozzles are mostly designed based on pulverized coal (which has relatively regular particles and a high bulk density). Compared with pulverized coal gasification, especially in high-pressure gasification processes, biomass powder has a low bulk density and irregular particles. When using gasification nozzles designed based on pulverized coal to process biomass powder, they cannot be adapted to the irregular particle shape, low bulk density, and wide particle size distribution of biomass powder. This results in low mixing efficiency, weak two-phase flow control capability, large pressure loss, and poor particle size adaptability. Ultimately, this manifests as excessive carrier gas consumption and insufficient conveying efficiency, making it difficult to meet the high-efficiency process requirements of biomass gasification. Utility Model Content

[0004] The technical problem to be solved by this application is to overcome the defects in the prior art where the gasification nozzle cannot be adapted to the irregular particle shape, low bulk density, and wide particle size distribution of biomass powder, resulting in excessively high nozzle carrier gas consumption and insufficient conveying efficiency during gasification, which makes it difficult to meet the high-efficiency process requirements of biomass fluidized bed gasification. The application provides a nozzle and gasifier for biomass powder gasification.

[0005] This application solves the above-mentioned technical problems through the following technical solution:

[0006] This application provides a nozzle for biomass powder gasification, the nozzle comprising an outer ring nozzle, a middle ring nozzle, an inner ring nozzle and a center nozzle arranged coaxially from the outside to the inside;

[0007] An outer ring channel is formed between the inner wall of the outer ring nozzle and the outer wall of the middle ring nozzle, which are coaxially arranged from the outside to the inside; a middle ring channel is formed between the inner wall of the middle ring nozzle and the outer wall of the inner ring nozzle; an inner ring channel is formed between the inner wall of the inner ring nozzle and the outer wall of the center nozzle; and a center channel is formed by the inner wall of the center nozzle.

[0008] An inlet and an outlet are respectively provided on the side wall of the inner ring channel away from the inner ring nozzle, and the outlet is located upstream of the inlet; the inlet is used to transport a mixture of biomass powder and gas.

[0009] The nozzle further includes a separator disposed in the inner annular channel and located between the outlet and the inlet, the separator being used to separate and lead a portion of the delivery gas from the mixture to the outlet for discharge;

[0010] The separator is equipped with a hydrocyclone and a filter, with the hydrocyclone positioned below the filter.

[0011] In this scheme, a separator is installed in the inner ring channel of the nozzle, and an outlet is opened on the side wall of the inner ring channel. The separator is located between the outlet and the inlet of the material (a mixture of biomass powder and conveying gas). When the biomass powder is conveyed to the inner ring channel along with the conveying gas, the separator separates part of the conveying gas from the mixture and discharges the separated conveying gas from the outlet, thereby reducing the total amount of conveying gas sprayed out by the nozzle head and thus reducing the total amount of inert gas entering the gasifier.

[0012] Optionally, the hydrocyclone is used to separate the biomass powder and the conveying gas in the mixture;

[0013] The filter is used to intercept the biomass powder in the mixture and to allow the conveying gas to pass through.

[0014] In this design, the separator integrates a hydrocyclone and a filter in a staged separation structure. The hydrocyclone uses centrifugal force to coarsely separate the biomass powder from the conveying gas, trapping large powder particles. The gas then enters the upper filter for further filtration of fine particulate impurities, and finally, clean gas is output from the outlet. This design, through the synergistic effect of "cyclone + filtration," not only improves powder separation efficiency and prevents fine powder escape, but also simplifies piping through a compact structure, reducing the need for bends or valves. Furthermore, the separated conveying gas can be used as protective gas and interlayer gas.

[0015] Optionally, the number of swirls in the hydrocyclone is S, where 0 < S ≤ 5; S is preferably 3-5.

[0016] In this scheme, the swirl number S of the hydrocyclone is limited to 0 < S ≤ 5. This range achieves a balance between efficient separation and low energy consumption by controlling the fluid rotation intensity: a moderate swirl intensity (S ≤ 5) can drive the biomass powder and the conveying gas to produce effective centrifugal separation (the powder gathers towards the wall and is trapped), while avoiding airflow turbulence or secondary entrainment of fine powder caused by excessive swirl (S > 5); at the same time, a low swirl number reduces the flow resistance of the fluid in the hydrocyclone.

[0017] Optionally, the filter includes a filter screen with pores having a size greater than or equal to 10 micrometers and less than or equal to 50 micrometers.

[0018] Optionally, the nozzle further includes an inclined tube, one end of which is connected to the inlet, and the other end of which is used to dispense the mixture of biomass powder and conveying gas;

[0019] The axial distance from the center of the separator to the outlet is L1, and the axial distance from the connection point of the inclined tube and the inlet near the separator to the outlet is L2. The ratio between L1 and L2 is 0.1 < L1 / L2 < 0.3; preferably 0.2.

[0020] In this scheme, by limiting the ratio of L1 to L2, the flow path of the mixture in the channel is optimized: the material fed into the inclined tube enters the separation area quickly over a short distance, and the separator can perform preliminary separation of the mixture in advance, reducing the residence time of the material in the channel and avoiding powder deposition or blockage caused by uneven flow rate; at the same time, the reasonable axial spacing ensures the separation efficiency of the separator for the conveying gas (the separated gas is discharged from the outlet), reduces the total amount of inert gas entering the gasifier, and improves the gasification reaction efficiency.

[0021] Optionally, the contraction angle α of the central channel is 0°-20°, the contraction angle b of the inner ring nozzle is 20°-30°, the contraction angle c of the middle ring nozzle is 30°-45°, and the contraction angle d of the outer ring nozzle is 40°-60°; preferably, the contraction angle α of the central channel is 20°, the contraction angle b of the inner ring nozzle is 25°, the contraction angle c of the middle ring nozzle is 30°, and the contraction angle d of the outer ring nozzle is 40°.

[0022] The contraction angle of each nozzle refers to the angle formed by the sidewall of the nozzle in the axial section view.

[0023] This application provides a gasifier, which includes a nozzle for gasifying biomass powder as described above.

[0024] This application provides a method for gasifying biomass powder, wherein the biomass powder gasification method uses a gasifier as described above, and the biomass powder gasification method includes:

[0025] Combustible gas is introduced into the central channel and the outer ring channel, inert gas is introduced into the inner ring channel, and oxygen is introduced into the middle ring channel. The ignition device is then turned on to ignite the central channel.

[0026] After ignition, the separator is turned on, and oxygen or protective gas is introduced into the central channel, the mixture of biomass powder and conveying gas is introduced into the inner ring channel, oxygen is introduced into the middle ring channel, and water vapor is introduced into the outer ring channel to generate products.

[0027] Optionally, the outlet velocity of the ejected material from the central channel is 10-80 m / s;

[0028] And / or, the outlet velocity of the inner ring channel when ejected is 1-30 m / s;

[0029] And / or, the outlet velocity of the ejected material from the central ring channel is 50-100 m / s;

[0030] And / or, the outlet velocity of the outer ring channel when ejected is 0.5-10 m / s;

[0031] Preferably, the outlet velocity of the ejected material from the central channel is 15 m / s, the outlet velocity of the ejected material from the inner ring channel is 10 m / s, the outlet velocity of the ejected material from the middle ring channel is 65 m / s, and the outlet velocity of the ejected material from the outer ring channel is 8 m / s.

[0032] Optionally, the pressure of the gasifier is less than or equal to 8 MPaG, and preferably, the pressure of the gasifier is 4.5 MPaG.

[0033] The positive and progressive effects of this application are as follows:

[0034] This application incorporates a separator within the inner ring channel of the nozzle, with an outlet on the side wall of the inner ring channel. The separator is positioned between the outlet and the material inlet (a mixture of biomass powder and conveying gas). When the biomass powder is conveyed into the inner ring channel along with the conveying gas, the separator separates a portion of the conveying gas from the mixture and discharges the separated conveying gas from the outlet, thereby reducing the total amount of conveying gas ejected from the nozzle head and consequently reducing the total amount of inert gas entering the gasifier.

[0035] After a portion of the transport gas, i.e., inert gas, is separated by a separator, the remaining inert gas enters the gasifier. The biomass powder is then gasified in the gasifier to obtain usable gas. The gasifier pressure is 4.5 MPaG, the biomass processing capacity is 100 t / h, and the bulk density of the biomass powder is 180 kg / m³. 3 The conveying gas is CO2. Using this method, the inert gas recovery rate is 10%, and the effective gas purity can be improved by 1.5%. Attached Figure Description

[0036] Figure 1 This is a schematic diagram of the overall structure of a nozzle for biomass powder gasification provided in an embodiment of this application;

[0037] Figure 2 This is a schematic diagram of the specific structure of a nozzle for biomass powder gasification provided in the embodiments of this application;

[0038] Figure 3 This is a schematic diagram of the specific structure of the separator in a nozzle for biomass powder gasification provided in an embodiment of this application.

[0039] Figure 4 This is a schematic diagram showing the specific location of the separator in a nozzle for biomass powder gasification provided in an embodiment of this application;

[0040] Figure 5 This is a schematic diagram of material transport in a nozzle for biomass powder gasification provided in an embodiment of this application.

[0041] Explanation of reference numerals in the attached figures:

[0042] Outer ring nozzle 1

[0043] Central ring nozzle 2

[0044] Inner ring nozzle 3

[0045] Center nozzle 4

[0046] Outer Ring Road 5

[0047] Central Link 6

[0048] Imported 61

[0049] Exports 62

[0050] Inner Ring Road 7

[0051] Central passage 8

[0052] Separator 9

[0053] Hydrocyclone 10

[0054] Filter 11

[0055] Inclined tube 12

[0056] First positioning block 13

[0057] Second positioning block 14

[0058] Third positioning block 15 Detailed Implementation

[0059] The technical solutions of the embodiments of this application will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of this application, and not all embodiments. Based on the embodiments of this application, all other embodiments obtained by those of ordinary skill in the art without creative effort are within the scope of protection of this application.

[0060] It should be noted that if this embodiment involves directional indicators (such as up, down, left, right, front, back, etc.), the directional indicators are only used to explain the relative positional relationship and movement of the components in a specific posture. If the specific posture changes, the directional indicators will also change accordingly.

[0061] Furthermore, if this embodiment involves descriptions such as "first" or "second," these descriptions are for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of technical features indicated. Therefore, features defined with "first" or "second" may explicitly or implicitly include at least one of those features. Additionally, the technical solutions of the various embodiments can be combined with each other, but this must be based on the ability of those skilled in the art to implement them. If the combination of technical solutions is contradictory or impossible to implement, it should be considered that such a combination of technical solutions does not exist and is not within the scope of protection claimed in this application.

[0062] Please see Figure 1-4 This embodiment provides a nozzle for biomass powder gasification. Figure 1 This is a schematic diagram of the overall structure of a nozzle for biomass powder gasification provided in an embodiment of this application. Figure 2 This is a schematic diagram of the specific structure of a nozzle for biomass powder gasification provided in the embodiments of this application, such as... Figure 1 and Figure 2 As shown, the nozzle includes an outer ring nozzle 1, a middle ring nozzle 2, an inner ring nozzle 3, and a center nozzle 4 arranged coaxially from the outside to the inside. An outer ring channel 5 is formed between the inner wall of the outer ring nozzle 1 and the outer wall of the middle ring nozzle 2. A middle ring channel 6 is formed between the inner wall of the middle ring nozzle 2 and the outer wall of the inner ring nozzle 3. An inner ring channel 7 is formed between the inner wall of the inner ring nozzle 3 and the outer wall of the center nozzle 4. The inner wall of the center nozzle 4 encloses a center channel 8. An inlet 61 and an outlet 62 are respectively opened on the side wall of the inner ring channel 7 away from the inner ring nozzle 3, with the outlet 62 located upstream of the inlet 61. The inlet 61 is used to convey a mixture of biomass powder and conveying gas. The nozzle also includes a separator 9, which is disposed in the inner ring channel 7 and located between the outlet 62 and the inlet 61. The separator 9 is used to separate and lead out a portion of the conveying gas from the mixture to the outlet 62 for discharge. Figure 3This is a schematic diagram illustrating the specific structure of the separator in a nozzle for biomass powder gasification provided in this application embodiment, as shown below. Figure 3 As shown, the separator 9 is equipped with a hydrocyclone 10 and a filter 11, with the hydrocyclone 10 positioned below the filter 11.

[0063] Biomass powder has a low bulk density (usually lower than pulverized coal, about 0.1-0.3 g / cm³), resulting in a larger volume for the same mass. If traditional carrier gases (such as nitrogen (N2) or carbon dioxide (CO2)) are used for transportation, the amount of carrier gas (i.e., the amount of inert gas) required per unit time will increase significantly. After entering the gasifier, these carrier gases become non-reactive inert components, diluting the effective gas concentration. The effective components of the syngas (carbon monoxide (CO) and hydrogen (H2)) are diluted by the inert gas, reducing the calorific value and chemical utilization value per unit volume of gas (processes such as methanol synthesis and ammonia synthesis have strict requirements on gas concentration). By installing a separator 9 in the inner ring channel 7 of the nozzle, and opening an outlet 62 on the side wall of the inner ring channel 7, the separator 9 is located between the outlet 62 and the material (a mixture of biomass powder and conveying gas) inlet 61. When the biomass powder is conveyed to the inner ring channel 7 along with the conveying gas, the separator 9 separates part of the conveying gas from the mixture and discharges the separated conveying gas from the outlet 62, thereby reducing the total amount of conveying gas ejected from the nozzle head and thus reducing the total amount of inert gas entering the gasifier.

[0064] In this embodiment, the hydrocyclone 10 is used to separate the biomass powder and the conveying gas in the mixture, and the filter 11 is used to intercept the biomass powder in the mixture and allow the conveying gas to pass through. The separator 9 integrates the hydrocyclone 10 and the filter 11 into a staged separation structure. The hydrocyclone 10 uses centrifugal force to coarsely separate the biomass powder from the conveying gas, trapping large particles. The gas then enters the upper filter 11 for further filtration of fine particulate impurities, and finally, clean gas is output from the outlet 62. This design, through the synergistic effect of "cyclone + filtration," not only improves powder separation efficiency and prevents fine powder escape, but also simplifies the pipeline through a compact structure, reducing the need for bends or valves. Furthermore, the separated conveying gas can be used as protective gas and interlayer gas.

[0065] Specifically, the swirling number of the hydrocyclone 10 is S, where 0 < S ≤ 5, and S is preferably 3-5. The swirling number reflects the ratio of the tangential velocity to the axial velocity of the fluid at the nozzle outlet 62. The filter 11 includes a filter screen or filter element, wherein the size of the pores on the filter screen is greater than or equal to 10 micrometers and less than or equal to 50 micrometers.

[0066] By limiting the swirl number S of the hydrocyclone 10 to 0 < S ≤ 5, this range achieves a balance between efficient separation and low energy consumption by controlling the fluid rotation intensity: a moderate swirl intensity (S ≤ 5) can drive the biomass powder and the conveying gas to produce effective centrifugal separation (the powder gathers towards the wall and is trapped), while avoiding airflow turbulence or secondary entrainment of fine powder caused by excessive swirl (S > 5); at the same time, a low swirl number reduces the flow resistance of the fluid in the hydrocyclone 10.

[0067] In this embodiment, Figure 4 This is a schematic diagram showing the specific location of the separator in a nozzle for biomass powder gasification provided in an embodiment of this application, as shown below. Figure 4 As shown, the nozzle also includes inclined tubes 12, typically numbered 1-4, with the number increasing as the raw material throughput increases. One end of each inclined tube 12 is connected to the inlet 61, and the other end is used to feed a mixture of biomass powder and conveying gas. The axial distance from the center of the separator 9 to the outlet 62 is L1. If the separator 9 includes a filter 11 and a hydrocyclone 10, then L1 represents the axial distance from the bottom of the filter screen of the filter 11 to the outlet 62. The axial distance from the connection point of the inclined tube 12 with the inlet 61 near the separator 9 to the outlet 62 is L2. The ratio of L1 to L2 is 0.1 < L1 / L2 < 0.3; preferably 0.2.

[0068] This application optimizes the flow path of the mixture in the channel by limiting the ratio of L1 to L2: the material fed into the inclined tube 12 enters the separation area quickly over a short distance, and the separator 9 can perform preliminary separation of the mixture in advance, reducing the residence time of the material in the channel and avoiding powder deposition or blockage caused by uneven flow rate; at the same time, the reasonable axial spacing ensures the separation efficiency of the separator 9 for the conveying gas (the separated gas is discharged from the outlet 62), reduces the total amount of inert gas entering the gasifier, and improves the gasification reaction efficiency.

[0069] Combination Figure 2 Continuing the explanation, in this embodiment, the contraction angle α of the central channel 8 is 0°-20°, the contraction angle b of the inner ring nozzle 3 is 20°-30°, the contraction angle c of the middle ring nozzle 2 is 30°-45°, and the contraction angle d of the outer ring nozzle 1 is 40°-60°. The contraction angle of each nozzle refers to the angle formed by the sidewalls of the nozzle in the axial section view. Specifically, the contraction angle α of the central channel 8 is 20°, the contraction angle b of the inner ring nozzle 3 is 25°, the contraction angle c of the middle ring nozzle 2 is 30°, and the contraction angle d of the outer ring nozzle 1 is 40°.

[0070] In this embodiment, a first positioning block 13 is arranged in the inner ring channel 7 of the nozzle, a second positioning block 14 is arranged in the middle ring channel 6, and a third positioning block 15 is arranged in the outer ring channel 5. The first positioning block 13, the second positioning block 14, and the third positioning block 15 are all arranged at one end of the nozzle near the nozzle head, and the third positioning block 15 is located upstream of the second positioning block 14, and the second positioning block 14 is located upstream of the first positioning block 13. As Figure 2 shown, the vertical distance from the first positioning block 13 to the nozzle head of the nozzle is L5, the vertical distance from the second positioning block 14 to the nozzle head of the nozzle is L4, and the vertical distance from the third positioning block 15 to the nozzle head of the nozzle is L3. Among them, L5 < L4 < L3. Specifically, the positioning block in this solution is a flexible structure, and the positioning block utilizes the synergistic effect of gas controllability and mechanical elastic deformation to achieve high-precision and high-flexibility positioning. Among them, the core part of the positioning block mainly includes: a sealing component, a positioning component, a pneumatic component, a spring, high-pressure gas, etc.

[0071] This embodiment also provides a gasifier, and the gasifier includes the nozzle for biomass powder gasification as described above.

[0072] This embodiment also provides a method for biomass powder gasification. The method for biomass powder gasification uses the gasifier as described above, and the method for biomass powder gasification includes:

[0073] S1: Introduce combustible gas into the central channel 8 and the outer ring channel 5, introduce inert gas into the inner ring channel 7, introduce oxygen into the middle ring channel 6, and turn on the ignition device to ignite the central channel 8;

[0074] S2: After ignition is completed, start the separator 9, and introduce oxygen or protective gas into the central channel 8, introduce the mixture of biomass powder and conveying gas into the inner ring channel 7, introduce oxygen into the middle ring channel 6, and introduce water vapor into the outer ring channel 5 to generate products.

[0075] Among them, the combustible gas can be liquefied petroleum gas, natural gas, etc., and the inert gas can be nitrogen, carbon dioxide, etc.

[0076] Specifically, Figure 5 is a schematic diagram of material transportation in the nozzle for biomass powder gasification provided in the embodiment of the present application. As Figure 5 shown, at startup, the ignition device is located in the central channel 8, liquefied petroleum gas is introduced into the central channel 8, carbon dioxide is introduced into the inner ring channel 7, oxygen is introduced into the middle ring channel 6, and liquefied petroleum gas is introduced into the outer ring channel 5.

[0077] When transporting biomass powder with a small bulk density, start the separator 9 above the inner ring channel 7, introduce oxygen into the central channel 8, introduce the mixture of biomass powder and conveying gas into the inner ring channel 7, introduce oxygen into the middle ring channel 6, and introduce water vapor into the outer ring channel 5.

[0078] In this scheme, the outlet velocity 62 of the central channel 8 is 10-80 m / s, the outlet velocity 62 of the inner ring channel 7 is 1-30 m / s, the outlet velocity 62 of the middle ring channel 6 is 50-100 m / s, and the outlet velocity 62 of the outer ring channel 5 is 0.5-10 m / s; preferably, the outlet velocity of the central channel is 15 m / s, the outlet velocity of the inner ring channel is 10 m / s, the outlet velocity of the middle ring channel is 65 m / s, and the outlet velocity of the outer ring channel is 8 m / s.

[0079] The pressure of the gasifier is less than or equal to 8 MPaG, preferably 4.5 MPaG.

[0080] The following is a specific example, 1, in which the biomass powder is wheat straw powder, the biomass processing scale is 100 t / h, and the bulk density is 180 kg / m³. 3 The conveying gas is carbon dioxide (CO2), and the gasifier pressure is 4.5 MPaG. The contraction angle α of the central channel 8 is 20°; the contraction angle b of the inner ring nozzle 3 is 25°, the contraction angle c of the middle ring nozzle 2 is 30°, and the contraction angle d of the outer ring nozzle 1 is 40°, with L1 / L2 being 0.2. When the cyclone number S of the hydrocyclone 10 is 5 and the filter screen size is 50 μm, 10% of the conveying gas can be recovered and reused as protective gas or interlayer gas. The remaining inert gas enters the gasifier, where the biomass powder is gasified (gasification pressure 4.5 MPaG) to obtain effective gas, which can improve the purity by 1.5%, and the inert gas recovery rate is 10%.

[0081] In Example 2, the swirl number S of the hydrocyclone 10 is 5, the filter size is 10 μm, and the other conditions remain unchanged.

[0082] In Example 3, the swirl number S of the hydrocyclone 10 is 3, the filter size is 50 μm, and the other conditions remain unchanged.

[0083] In Example 4, the swirl number S of the hydrocyclone 10 is 3, the filter size is 10 μm, and the other conditions remain unchanged.

[0084] This application also provides two comparative examples, 1 and 2. In comparative example 1, the swirl number S of the hydrocyclone 10 is 0, the filter screen size is 50 μm, and other conditions remain unchanged. In comparative example 2, the swirl number S of the hydrocyclone 10 is 0, the filter screen size is 10 μm, and other conditions remain unchanged. In this scheme, the amount of gas that the separator 9 can extract depends on the swirl number of the hydrocyclone 10 and the size of the filter screen of the filter 11. At the same time, the extraction of some inert gas through the separator can effectively improve the purity of the effective gas generated in the subsequent gasifier. Please refer to the effect comparison table 1 below.

[0085] Table 1

[0086]

[0087] Table 1 shows that the cyclone number and filter size jointly affect the gas recovery rate and the improvement of effective gas purity: the cyclone number is the core driving factor. Its increase (e.g., from 0 to 5) enhances the initial impurity separation through centrifugal force, significantly improving the gas recovery rate (e.g., from 5% to 10% for a 50μm filter) and purity (from 0.7% to 1.5%). The filter size needs to be matched with the cyclone. At the same cyclone number, the 50μm filter, due to its lower resistance, can more efficiently intercept residual particles and reduce flow limitation after most impurities have been removed by the cyclone. Therefore, the gas recovery rate (e.g., 10% for a cyclone number of 5 vs. 8% for a 10μm filter) and the improvement in purity (1.5% vs. 1.2%) are both better than those of the 10μm filter. The process without cyclone (comparative example) relies solely on filter filtration. Due to its high resistance and low separation efficiency, the effect is significantly lower than that of the process with cyclone. In summary, for practical applications, a high cyclone number (such as 5) should be prioritized, paired with a large filter size (such as 50μm) to balance efficiency and purification effect.

[0088] While specific embodiments of this application have been described above, those skilled in the art should understand that these are merely illustrative examples, and the scope of protection of this application is defined by the appended claims. Those skilled in the art can make various changes or modifications to these embodiments without departing from the principles and essence of this application, but all such changes and modifications fall within the scope of protection of this application.

Claims

1. A nozzle for biomass powder gasification, characterized in that, The nozzle includes an outer ring nozzle, a middle ring nozzle, an inner ring nozzle, and a center nozzle arranged coaxially from the outside to the inside; An outer ring channel is formed between the inner wall of the outer ring nozzle and the outer wall of the middle ring nozzle, which are coaxially arranged from the outside to the inside; a middle ring channel is formed between the inner wall of the middle ring nozzle and the outer wall of the inner ring nozzle; an inner ring channel is formed between the inner wall of the inner ring nozzle and the outer wall of the center nozzle; and a center channel is formed by the inner wall of the center nozzle. An inlet and an outlet are respectively provided on the side wall of the inner ring channel away from the inner ring nozzle, and the outlet is located upstream of the inlet; the inlet is used to transport a mixture of biomass powder and gas. The nozzle further includes a separator disposed in the inner annular channel and located between the outlet and the inlet, the separator being used to separate and lead a portion of the delivery gas from the mixture to the outlet for discharge; The separator is equipped with a hydrocyclone and a filter, with the hydrocyclone positioned below the filter.

2. The nozzle for biomass powder gasification as described in claim 1, characterized in that, The hydrocyclone is used to separate the biomass powder and the conveying gas in the mixture; The filter is used to intercept the biomass powder in the mixture and to allow the conveying gas to pass through.

3. The nozzle for biomass powder gasification as described in claim 2, characterized in that, The number of swirls in the hydrocyclone is S, where 0 < S ≤ 5.

4. The nozzle for biomass powder gasification as described in claim 3, characterized in that, The number of swirls S in the hydrocyclone is 3-5.

5. The nozzle for biomass powder gasification as described in claim 4, characterized in that, The filter includes a filter screen with pores having a size greater than or equal to 10 micrometers and less than or equal to 50 micrometers.

6. The nozzle for biomass powder gasification as described in claim 5, characterized in that, The nozzle also includes an inclined tube, one end of which is connected to the inlet, and the other end of which is used to dispense the mixture of biomass powder and conveying gas. The axial distance from the bottom of the filter screen of the separator to the outlet is L1, and the axial distance from the connection point of the inclined tube and the inlet near the separator to the outlet is L2. The ratio between L1 and L2 is 0.1 < L1 / L2 < 0.

3.

7. The nozzle for biomass powder gasification as described in claim 6, characterized in that, The ratio between L1 and L2 is 0.

2.

8. The nozzle for biomass powder gasification as described in claim 1, characterized in that, The contraction angle α of the central channel is 0°-20°, the contraction angle b of the inner ring nozzle is 20°-30°, the contraction angle c of the middle ring nozzle is 30°-45°, and the contraction angle d of the outer ring nozzle is 40°-60°. The contraction angle of each nozzle refers to the angle formed by the sidewall of the nozzle in the axial section view.

9. The nozzle for biomass powder gasification as described in claim 8, characterized in that, The contraction angle α of the central channel is 20°, the contraction angle b of the inner ring nozzle is 25°, the contraction angle c of the middle ring nozzle is 30°, and the contraction angle d of the outer ring nozzle is 40°.

10. A gasifier, characterized in that, The gasifier includes a nozzle for gasifying biomass powder as described in any one of claims 1-9.

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