A method and apparatus for high temperature thermal reforming of biomass to syngas

Abstract

This invention discloses a method and apparatus for producing syngas from biomass gasification via high-temperature thermal reforming, belonging to the technical field of biomass gasification. The apparatus includes a high-temperature thermal reforming reactor, a heat exchanger, a waste liquid collector, a crude syngas scrubbing tower, and a gas-liquid separator. The interior of the high-temperature thermal reforming reactor is divided into a stepwise combustion zone, a high-temperature reduction zone, and an ash collection zone from top to bottom. Crude gas is added from the top of the high-temperature thermal reforming reactor and subsequently undergoes combustion and reforming reactions in the stepwise combustion zone and the high-temperature reforming zone, converting CH4 and tar into CO and H2. The lower part of the high-temperature thermal reforming reactor is the ash collection zone, which is connected to the heat exchanger via a gas outlet. The heat exchanger is connected to the crude syngas scrubbing tower, and the crude syngas scrubbing tower is connected to the gas-liquid separator. Waste liquid from both the crude syngas scrubbing tower and the gas-liquid separator is discharged into the waste liquid collector. This invention solves the problems of high methane content and difficult tar treatment in biomass gasification products.

Description

Technical Field

[0001] This invention belongs to the field of biomass gasification technology, specifically relating to a method and apparatus for producing syngas through high-temperature thermal reforming of biomass gasification. Background Technology

[0002] Biomass gasification is a renewable and clean energy production technology that uses waste biomass to convert into gaseous fuels. It helps reduce greenhouse gas emissions, improve energy security, promote sustainable development, and plays an important role in future energy and environmental development.

[0003] Because the syngas produced by biomass gasification has a high tar content, it requires further conversion and purification. Currently, the mainstream methods for purifying crude gasified gas include physical removal and catalytic conversion. A search revealed that patent CN113684067A discloses a biomass gasification syngas production device, which mainly includes a preheater, reactor, primary gas-solid separator, secondary gas-solid separator, and syngas cooler. Although this device can flexibly adjust the operating load, the entire process is complex, and the investment and operating costs are high. Patent CN214193142U discloses a biomass gasification system based on heat recovery. This system uses physical methods to remove tar and then converts the methane in the syngas. However, this method has a low carbon conversion rate, and the resulting tar-containing wastewater causes secondary pollution and is difficult to treat, resulting in high overall production costs. Meanwhile, patent CN216404311U discloses a low-tar biomass gasification system. Although this device can reduce the tar content of the gasified material, the large amount of dust and sulfur-containing substances generated during biomass gasification can easily lead to catalyst poisoning. Furthermore, tar cracking can easily produce a large amount of carbon deposits on the catalyst surface, leading to catalyst deactivation. It is evident that traditional crude gasification gas purification methods mainly face problems such as complex process routes, low carbon conversion rates, severe secondary pollution, and easy catalyst deactivation.

[0004] Therefore, in the field of biomass gasification, there is an urgent need to develop a production device with high thermal efficiency, good operational stability, low investment cost, and simple process flow to solve the technical problem of producing high-quality syngas from biomass gasification. Summary of the Invention

[0005] To address the problems of complex process routes, low carbon conversion rates, and severe secondary pollution in existing biomass crude gasification gas purification technologies, this invention provides a method and apparatus for high-temperature thermal reforming to produce syngas from biomass gasification. The invention improves the method for purifying crude syngas from biomass gasification and optimizes the purification device, enabling it to stably and efficiently purify crude gasification gas, improve the purity of the syngas, further enhance the overall carbon conversion rate of the gasification system, and reduce environmental pollution during the production process.

[0006] To achieve the above objectives, the present invention employs the following technical solutions:

[0007] An apparatus for producing syngas from biomass gasification by high-temperature thermal reforming includes a high-temperature thermal reforming reactor, a heat exchanger, a waste liquid collector, a crude syngas scrubbing tower, and a gas-liquid separator.

[0008] The high-temperature thermal reforming reactor is provided with several first air inlets and crude gasification gas inlets at the top, second air inlets and third air inlets at the upper part of the side wall; cooling water inlets and air outlets at the lower part of the side wall; and ash outlets at the bottom.

[0009] The outlet of the high-temperature thermal reforming reactor is connected to the inlet of the heat exchanger, the outlet of the heat exchanger is connected to the inlet of the crude syngas scrubbing tower, and the gas outlet of the crude syngas scrubbing tower is connected to the inlet of the gas-liquid separator. The liquid outlets of the crude syngas scrubbing tower and the gas-liquid separator are both connected to the liquid inlet of the waste liquid collector via pipelines. The outlet of the waste liquid collector is connected to the cooling water inlet of the high-temperature thermal reforming reactor.

[0010] Furthermore, the interior of the high-temperature thermal reforming reactor is divided into a stepwise combustion zone, a high-temperature reduction zone, and an ash collection zone from top to bottom.

[0011] Furthermore, the height difference between the second air inlet and the first air inlet accounts for 1 / 5 to 1 / 3 of the height of the high-temperature thermal reforming reactor; the height difference between the second air inlet and the third air inlet accounts for 1 / 5 to 1 / 3 of the height of the high-temperature thermal reforming reactor.

[0012] Furthermore, the first air inlet is arranged radially on the top of the high-temperature thermal reforming reactor, with a specific angle of 10~45° with the axis of the high-temperature thermal reforming reactor.

[0013] Furthermore, the high-temperature thermal reforming reactor is constructed from a pressure-resistant steel shell and refractory materials, with a height-to-diameter ratio of 5 to 50.

[0014] A method for producing syngas from biomass gasification using the above-mentioned apparatus via high-temperature thermal reforming includes the following steps:

[0015] Step 1: The crude gasification gas from the gasifier is stably fed into the high-temperature thermal reforming reactor through the crude gasification gas inlet; O2 is introduced into the reactor through the first, second, and third inlets.

[0016] Step 2: The crude gasification gas and O2 undergo a high-temperature thermal reforming reaction at 1000℃~1300℃, and the generated product gas is discharged from the outlet.

[0017] Step 3: The product gas enters the heat exchanger for waste heat recovery, which raises the temperature of the heat carrier in the heat exchanger from 80℃~106℃ at the inlet to 350℃~700℃, and lowers the temperature of the product gas from 400℃~800℃ at the inlet to 200℃~500℃ at the outlet.

[0018] Step 4: The cooled product gas is passed into a crude syngas washing tower to further remove impurities;

[0019] Step 5: The purified product gas is passed into a gas-liquid separator to remove the moisture it contains, and syngas for chemical production is obtained.

[0020] Step 6: The waste liquid from the crude syngas washing tower and gas-liquid separator is discharged into the waste liquid collector, and then transported by the waste liquid collector through pipeline to the cooling water inlet of the high-temperature thermal reforming reactor to cool the ash residue.

[0021] Furthermore, the tar content of the crude gasification gas is greater than 1 g / Nm³. 3 The product gas contains more than 98% syngas.

[0022] Furthermore, the operating pressure of the high-temperature thermal reforming reactor is 0.1 MPa to 3 MPa.

[0023] Furthermore, the molar ratio of O2 supplied through the first air inlet to the O2 required for complete combustion of the crude gasified gas is 0.05~0.09, the molar ratio of O2 supplied through the second air inlet to the O2 required for complete combustion of the crude gasified gas is 0.02~0.07, and the molar ratio of O2 supplied through the third air inlet to the O2 required for complete combustion of the crude gasified gas is 0.06~0.10.

[0024] Furthermore, the ash slag discharged from the high-temperature thermal reforming reactor is cooled from 1000℃~1300℃ to below 200℃.

[0025] Compared with the prior art, the present invention has the following advantages:

[0026] 1. The present invention relates to a high-temperature thermal reforming reactor, which has the advantages of high energy efficiency, reliable operation and low pollutant emissions.

[0027] 2. The biomass gasification high-temperature thermal reforming process developed in this invention uses a high-temperature thermal reforming reactor to efficiently convert tar and other organic matter in the crude gasification gas into syngas mainly composed of CO and H2, eliminating the tar treatment section and improving the overall economic efficiency of the biomass gasification system.

[0028] 3. The reaction device of this invention is simple, does not use a catalyst, has high carbon utilization, and the product synthesis gas can be used for Fischer-Tropsch synthesis, methanol synthesis, etc. after conventional purification treatment.

[0029] 4. The use of segmented oxygen intake to convert carbonaceous organic matter in the crude gasification gas effectively avoids reactor ablation caused by excessively high local temperatures.

[0030] 5. The introduction of O2 using an impinging flow method increases the turbulence of the flow field within the reforming reactor, thereby promoting the conversion of carbonaceous organic matter.

[0031] 6. The height difference between the first and third air inlets accounts for about 50% of the height of the high-temperature thermal reforming reactor, which improves the control of the oxidation reaction and reduces the investment cost of the reactor. Attached Figure Description

[0032] Figure 1 This is a flowchart of the biomass gasification high-temperature thermal reforming process in this invention;

[0033] Figure 2 This is a structural diagram of the high-temperature thermal reforming reactor in an embodiment of the present invention;

[0034] Reference numerals in the attached diagram: 1. High-temperature thermal reforming reactor; 2. Heat exchanger; 3. Waste liquid collector; 4. Crude syngas scrubbing tower; 5. Gas-liquid separator; 6. Ash collection zone; 7. High-temperature reduction zone; 8. Stepwise combustion zone; 9. Ash outlet; 10. Cooling water inlet; 11. Gas outlet; 12. Third gas inlet; 13. Second gas inlet; 14. First gas inlet; 15. Crude gasification gas inlet. Detailed Implementation

[0035] To gain a deeper understanding of this invention, we will provide a comprehensive and detailed description. However, this invention has various implementations and is not limited to the specific examples listed herein. These examples are presented to enhance a full understanding of the disclosure of this invention.

[0036] An apparatus for high-temperature thermal reforming of biomass to produce syngas, such as... Figure 1 and Figure 2 As shown, it includes a high-temperature thermal reforming reactor 1, a heater 2, a waste liquid collector 3, a crude syngas washing tower 4, and a gas-liquid separator 5;

[0037] The high-temperature thermal reforming reactor 1 is provided with several first air inlets 14 and crude gasification gas inlets 15 at the top, and second air inlets 13 and third air inlets 12 at the upper part of the side wall; cooling water inlets 10 and air outlets 11 at the lower part of the side wall; and ash outlets 9 at the bottom.

[0038] The outlet 11 of the high-temperature thermal reforming reactor 1 is connected to the inlet of the heat exchanger 2. The outlet of the heat exchanger 2 is connected to the inlet of the crude syngas washing tower 4. The gas outlet of the crude syngas washing tower 4 is connected to the inlet of the gas-liquid separator 5. The liquid outlets of the crude syngas washing tower 4 and the gas-liquid separator 5 are both connected to the liquid inlet of the waste liquid collector 3 through pipelines. The outlet of the waste liquid collector 3 is connected to the cooling water inlet 10 of the high-temperature thermal reforming reactor 1.

[0039] Furthermore, the interior of the high-temperature thermal reforming reactor 1 is divided into a stepwise combustion zone 8, a high-temperature reduction zone 7, and an ash collection zone 6 from top to bottom.

[0040] Furthermore, the height difference between the second air inlet 13 and the first air inlet 14 accounts for 1 / 5 to 1 / 3 of the height of the high-temperature thermal reforming reactor 1; the height difference between the second air inlet 13 and the third air inlet 12 accounts for 1 / 5 to 1 / 3 of the height of the high-temperature thermal reforming reactor 1.

[0041] Furthermore, the first air inlet 14 is arranged radially on the top of the high-temperature thermal reforming reactor 1, with a specific angle of 10~45° with the axis of the high-temperature thermal reforming reactor 1.

[0042] Furthermore, the high-temperature thermal reforming reactor 1 is constructed from a pressure-resistant steel shell and refractory materials, with a height-to-diameter ratio of 5 to 50.

[0043] A method for producing syngas from biomass gasification using the above-mentioned apparatus via high-temperature thermal reforming includes the following steps:

[0044] Step 1: The crude gasification gas from the gasifier is stably fed into the high-temperature thermal reforming reactor 1 through the crude gasification gas inlet 15; O2 is introduced into the reactor through the first inlet 14, the second inlet 13, and the third inlet 12.

[0045] Step 2: The crude gasification gas and O2 are subjected to a high-temperature thermal reforming reaction at 1000℃~1300℃, and the generated product gas is discharged from the gas outlet 11.

[0046] Step 3: The product gas enters heat exchanger 2 for waste heat recovery, which raises the temperature of the heat carrier in heat exchanger 2 from 80℃~106℃ at the inlet to 350℃~700℃, and lowers the temperature of the product gas from 400℃~800℃ at the inlet of heat exchanger 2 to 200℃~500℃ at the outlet of heat exchanger 2.

[0047] Step 4: The cooled product gas is passed into the crude syngas washing tower 4 to further remove impurities;

[0048] Step 5: The purified product gas is passed into a gas-liquid separator 5 to remove the moisture it contains, and syngas for chemical production is obtained.

[0049] Step 6: The waste liquid from the crude syngas washing tower 4 and the gas-liquid separator 5 is discharged into the waste liquid collector 3, and then transported by the waste liquid collector 3 through pipeline to the cooling water inlet of the high-temperature thermal reforming reactor 1 to cool the ash residue.

[0050] Furthermore, the tar content of the crude gasification gas is greater than 1 g / Nm³. 3 The product gas contains more than 98% syngas.

[0051] Furthermore, the operating pressure of the high-temperature thermal reforming reactor 1 is 0.1 MPa to 3 MPa.

[0052] Furthermore, the molar ratio of O2 delivered by the first air inlet 14 to the O2 required for complete combustion of the crude gasified gas is 0.05~0.09, the molar ratio of O2 delivered by the second air inlet 13 to the O2 required for complete combustion of the crude gasified gas is 0.02~0.07, and the molar ratio of O2 delivered by the third air inlet 12 to the O2 required for complete combustion of the crude gasified gas is 0.06~0.10.

[0053] Furthermore, the ash slag discharged from the high-temperature thermal reforming reactor 1 is cooled from 1000℃~1300℃ to below 200℃.

[0054] Example 1

[0055] A method and apparatus for producing syngas from biomass gasification by high-temperature thermal reforming, the specific implementation details of which are as follows:

[0056] 1) The height-to-diameter ratio of the high-temperature thermal reforming reactor 1 is 10, the angle between the first air inlet 14 and the axis of the high-temperature thermal reforming reactor 1 is 33°, the ratio of the distance between the first air inlet 14 and the second air inlet 13 in the furnace cavity to the height of the high-temperature thermal reforming reactor 1 is 0.23, and the ratio of the distance between the second air inlet 13 and the third air inlet 12 in the furnace cavity to the height of the high-temperature thermal reforming reactor 1 is 0.22.

[0057] 2) The first air inlet 14 feeds O2 with an ER of 0.05 into the step-by-step combustion zone 8, the second air inlet 13 feeds material with an ER of 0.03 into the step-by-step combustion zone 8, and the third air inlet 12 feeds O2 with an ER of 0.10 into the step-by-step combustion zone 8.

[0058] Using maple wood as the biomass source, the composition of the crude gasification gas is shown in Table 1, and the final composition of the syngas is shown in Table 2.

[0059] Table 1. Composition of crude gasification gas in Example 1

[0060] Components <![CDATA[H2]]> CO <![CDATA[CO2]]> <![CDATA[CH4]]> <![CDATA[C2H4]]> <![CDATA[C2H6]]> <![CDATA[C3H8]]> <![CDATA[C6H6]]> <![CDATA[tar (g / Nm 3 )]]> Content, mol% 21.75 14.73 41.09 17.49 0.24 1.32 0.33 3.05 9.30

[0061] Table 2. Composition of Syngas in Example 1

[0062] Components <![CDATA[H2]]> CO <![CDATA[CO2]]> Content, mol% 39.90 59.43 0.67

[0063] Example 2

[0064] use Figure 1 The process flow shown is as follows, and the specific implementation details are as follows:

[0065] 1) The height-to-diameter ratio of the high-temperature thermal reforming reactor 1 is 18, the angle between the first air inlet 14 and the axis of the high-temperature thermal reforming reactor 1 is 25°, the ratio of the distance between the first air inlet 14 and the second air inlet 13 in the furnace cavity to the height of the high-temperature thermal reforming reactor 1 is 0.31, and the ratio of the distance between the second air inlet 13 and the third air inlet 12 in the furnace cavity to the height of the high-temperature thermal reforming reactor 1 is 0.22.

[0066] 2) The first air inlet 14 sends O2 with an ER of 0.07 into the step combustion zone 8, the second air inlet 13 sends O2 with an ER of 0.05 into the step combustion zone 8, and the third air inlet 12 sends O2 with an ER of 0.12 into the step combustion zone 8.

[0067] Using corn stalks as the biomass source, the composition of the crude gasification gas is shown in Table 3, and the final composition of the syngas is shown in Table 4.

[0068] Table 3 Composition of crude gasification gas in Example 2

[0069] Components <![CDATA[H2]]> CO <![CDATA[CO2]]> <![CDATA[CH4]]> <![CDATA[C2H4]]> <![CDATA[C2H6]]> <![CDATA[C3H8]]> <![CDATA[C6H6]]> <![CDATA[tar (g / Nm 3 )]]> Content, mol% 25.36 15.17 36.72 18.41 0.25 0.67 0.22 3.20 10.40

[0070] Table 4. Composition of Syngas in Example 2

[0071] Components <![CDATA[H2]]> CO <![CDATA[CO2]]> Content, mol% 43.12 56.31 0.57

[0072] Example 3

[0073] use Figure 1 The process flow shown is as described in Example 1. Specific implementation details are as follows:

[0074] 1) The height-to-diameter ratio of the high-temperature thermal reforming reactor 1 is 32, the angle between the first air inlet 14 and the axis of the high-temperature thermal reforming reactor 1 is 40°, the ratio of the distance between the first air inlet 14 and the second air inlet 13 in the furnace cavity to the height of the high-temperature thermal reforming reactor 1 is 0.28, and the ratio of the distance between the second air inlet 13 and the third air inlet 12 in the furnace cavity to the height of the high-temperature thermal reforming reactor 1 is 0.16.

[0075] 2) The first air inlet 14 inputs O2 with an ER of 0.06 into the step combustion zone 8, the second air inlet 13 inputs O2 with an ER of 0.03 into the step combustion zone 8, and the third air inlet 12 inputs O2 with an ER of 0.11 into the step combustion zone 8.

[0076] Using waste plastics as a biomass source, the composition of the crude gasification gas is shown in Table 5, and the final composition of the syngas is shown in Table 6.

[0077] Table 5 Composition of crude gasification gas in Example 3

[0078] Components <![CDATA[H2]]> CO <![CDATA[CO2]]> <![CDATA[CH4]]> <![CDATA[C2H4]]> <![CDATA[C2H6]]> <![CDATA[C3H8]]> <![CDATA[C6H6]]> <![CDATA[tar (g / Nm 3 )]]> Content, mol% 25.48 16.94 35.32 16.33 1.49 1.79 0.12 2.54 8.28

[0079] Table 6. Syngas composition in Example 3

[0080] Components <![CDATA[H2]]> CO <![CDATA[CO2]]> Content, mol% 40.65 59.27 0.08

[0081] Example 4

[0082] use Figure 1 The process flow shown is as described in Example 1. Specific implementation details are as follows:

[0083] 1) The height-to-diameter ratio of the high-temperature thermal reforming reactor 1 is 20, the angle between the first air inlet 14 and the axis of the high-temperature thermal reforming reactor 1 is 17°, the ratio of the distance between the first air inlet 14 and the second air inlet 13 in the furnace cavity to the height of the high-temperature thermal reforming reactor 1 is 0.35, and the ratio of the distance between the second air inlet 13 and the third air inlet 12 in the furnace cavity to the height of the high-temperature thermal reforming reactor 1 is 0.19.

[0084] 2) The first air inlet 14 sends O2 with an ER of 0.08 into the step combustion zone 8, the second air inlet 13 sends O2 with an ER of 0.05 into the step combustion zone 8, and the third air inlet 12 inputs O2 with an ER of 0.15 into the step combustion zone 8.

[0085] Using cotton stalks as a biomass source, the composition of the crude gasification gas is shown in Table 7, and the final composition of the syngas is shown in Table 8.

[0086] Table 7 Composition of crude gasification gas in Example 4

[0087] Components <![CDATA[H2]]> CO <![CDATA[CO2]]> <![CDATA[CH4]]> <![CDATA[C2H4]]> <![CDATA[C2H6]]> <![CDATA[C3H8]]> <![CDATA[C6H6]]> <![CDATA[tar (g / Nm 3 )]]> Content, mol% 22.43 16.12 37.24 17.09 1.62 2.28 0.29 3.01 9.67

[0088] Table 8. Composition of Syngas in Example 4

[0089] Components <![CDATA[H2]]> CO <![CDATA[CO2]]> Content, mol% 38.56 61.32 0.12

[0090] Example 5

[0091] use Figure 1The process flow shown is as described in Example 1. Specific implementation details are as follows:

[0092] 1) The height-to-diameter ratio of the high-temperature thermal reforming reactor 1 is 23, the angle between the first air inlet 14 and the axis of the high-temperature thermal reforming reactor 1 is 25°, the ratio of the distance between the first air inlet 14 and the second air inlet 13 in the furnace cavity to the height of the high-temperature thermal reforming reactor 1 is 0.23, and the ratio of the distance between the second air inlet 13 and the third air inlet 12 in the furnace cavity to the height of the high-temperature thermal reforming reactor 1 is 0.21.

[0093] 2) The first air inlet 14 inputs O2 with an ER of 0.06 into the step combustion zone 8, the second air inlet 13 inputs O2 with an ER of 0.03 into the step combustion zone 8, and the third air inlet 12 inputs O2 with an ER of 0.10 into the step combustion zone 8.

[0094] Using coconut shells as the biomass source, the composition of the crude gasification gas is shown in Table 9, and the final composition of the syngas is shown in Table 10.

[0095] Table 9 Composition of crude gasification gas in Example 5

[0096] Components <![CDATA[H2]]> CO <![CDATA[CO2]]> <![CDATA[CH4]]> <![CDATA[C2H4]]> <![CDATA[C2H6]]> <![CDATA[C3H8]]> <![CDATA[C6H6]]> <![CDATA[tar (g / Nm 3 )]]> Content, mol% 25.47 15.32 36.72 14.33 1.30 2.53 0.26 3.86 7.26

[0097] Table 10 Composition of Syngas in Example 5

[0098] Components <![CDATA[H2]]> CO <![CDATA[CO2]]> Content, mol% 41.02 57.69 0.29

[0099] As can be seen from the examples, the purity of the syngas reached over 99%, and the gasification efficiency was high. The above experiments verified the feasibility of the biomass high-temperature thermal reforming gasification process designed based on a high-temperature thermal reforming reactor, which reduces tar content and increases syngas yield through high-temperature thermal reforming.

[0100] Contents not described in detail in this specification are prior art known to those skilled in the art. Although illustrative specific embodiments of the invention have been described above to facilitate understanding by those skilled in the art, it should be understood that the invention is not limited to the scope of the specific embodiments. Various modifications are readily apparent to those skilled in the art as long as they fall within the spirit and scope of the invention as defined and determined by the appended claims, and all inventions utilizing the concept of this invention are protected.

Claims

1. An apparatus for high-temperature thermal reforming of biomass to produce syngas, characterized in that: It includes a high-temperature thermal reforming reactor (1), a heat exchanger (2), a waste liquid collector (3), a crude syngas scrubbing tower (4), and a gas-liquid separator (5). The high-temperature thermal reforming reactor (1) is provided with several first air inlets (14) and crude gasification gas inlets (15) at the top, and second air inlets (13) and third air inlets (12) at the upper part of the side wall; cooling water inlets (10) and air outlets (11) are provided at the lower part of the side wall; and ash outlets (9) are provided at the bottom. The outlet (11) of the high-temperature thermal reforming reactor (1) is connected to the inlet of the heat exchanger (2), the outlet of the heat exchanger (2) is connected to the inlet of the crude syngas scrubbing tower (4), the gas outlet of the crude syngas scrubbing tower (4) is connected to the inlet of the gas-liquid separator (5); the liquid outlets of the crude syngas scrubbing tower (4) and the gas-liquid separator (5) are both connected to the liquid inlet of the waste liquid collector (3) through pipelines; the outlet of the waste liquid collector (3) is connected to the cooling water inlet (10) of the high-temperature thermal reforming reactor (1).

2. The apparatus for high-temperature thermal reforming to produce syngas from biomass gasification according to claim 1, characterized in that: The interior of the high-temperature thermal reforming reactor (1) is divided into a step-by-step combustion zone (8), a high-temperature reduction zone (7), and an ash collection zone (6) from top to bottom.

3. The apparatus for high-temperature thermal reforming to produce syngas from biomass gasification according to claim 1, characterized in that: The height difference between the second air inlet (13) and the first air inlet (14) is 1 / 5 to 1 / 3 of the height of the high-temperature thermal reforming reactor (1); the height difference between the second air inlet (13) and the third air inlet (12) is 1 / 5 to 1 / 3 of the height of the high-temperature thermal reforming reactor (1).

4. The apparatus for high-temperature thermal reforming to produce syngas from biomass gasification according to claim 1, characterized in that: The first air inlet (14) is arranged radially on the top of the high-temperature thermal reforming reactor (1), and the angle between it and the axis of the high-temperature thermal reforming reactor (1) is 10~45°.

5. The apparatus for high-temperature thermal reforming to produce syngas from biomass gasification according to claim 1, characterized in that: The high-temperature thermal reforming reactor (1) is constructed of a pressure-resistant steel shell and refractory materials, with a height-to-diameter ratio of 5 to 50.

6. A method for producing syngas from biomass gasification using the apparatus according to any one of claims 1 to 5, characterized in that, Includes the following steps: Step 1: The crude gasification gas from the gasifier is stably fed into the high-temperature thermal reforming reactor (1) through the crude gasification gas inlet (15); from the first inlet (14), the second inlet (13) and the third inlet (12). Introduce O2; Step 2: The crude gasification gas and O2 are subjected to a high-temperature thermal reforming reaction at 1000℃~1300℃, and the generated product gas is discharged from the outlet (11). Step 3: The product gas enters the heat exchanger (2) for waste heat recovery, so that the heat carrier in the heat exchanger (2) is heated from 80℃~106℃ at the inlet to 350℃~700℃, and the temperature of the product gas is reduced from 400℃~800℃ at the inlet of the heat exchanger (2) to 200℃~500℃ at the outlet of the heat exchanger (2). Step 4: The cooled product gas is passed into the crude syngas washing tower (4) to further remove impurities; Step 5: The purified product gas is passed into a gas-liquid separator (5) to remove the water contained therein, and syngas for chemical production is obtained. Step 6: The waste liquid from the crude syngas washing tower (4) and the gas-liquid separator (5) is discharged into the waste liquid collector (3), and then transported by the waste liquid collector (3) through the pipeline to the cooling water inlet of the high-temperature thermal reforming reactor (1) to cool the ash residue.

7. The method for producing syngas from biomass gasification by high-temperature thermal reforming according to claim 6, characterized in that: The tar content of the crude gasification gas is greater than 1 g / Nm³. 3 The product gas contains more than 98% syngas.

8. The method for producing syngas from biomass gasification by high-temperature thermal reforming according to claim 6, characterized in that: The working pressure of the high-temperature thermal reforming reactor (1) is 0.1-3 MPa.

9. The method for producing syngas from biomass gasification by high-temperature thermal reforming according to claim 6, characterized in that: The molar ratio of O2 delivered by the first air inlet (14) to the O2 required for complete combustion of the crude gasified gas is 0.05~0.09, the molar ratio of O2 delivered by the second air inlet (13) to the O2 required for complete combustion of the crude gasified gas is 0.02~0.07, and the molar ratio of O2 delivered by the third air inlet (12) to the O2 required for complete combustion of the crude gasified gas is 0.06~0.

10.

10. The method for producing syngas from biomass gasification by high-temperature thermal reforming according to claim 6, characterized in that: The ash slag discharged from the high-temperature thermal reforming reactor (1) is cooled from 1000℃~1300℃ to below 200℃.

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