Fluidized bed-downward flow bed pyrolysis-gasification integrated method and device

Abstract

The present application relates to fluidized bed-down bed pyrolysis-gasification integrated method and device, the present application is combined through fluidized bed pyrolysis furnace and down bed gasification furnace, and an oil shale pyrolysis gasification integrated method and related device are proposed, which includes the following steps: raw materials enter from the fluidized bed lower section feed inlet, gas and semi-coke are generated in the fluidized bed pyrolysis furnace; semi-coke is separated by gas-solid separator and freely falls to the down bed gasification furnace, and high-temperature gas after semi-coke gasification is used as hot carrier gas and is passed into the fluidized bed pyrolysis furnace; pyrolysis gas product is sent to condensing device for rapid cooling, wherein the condensable gas becomes tar after cooling, and the incondensable gas is partly used as product gas after further purification treatment, and the other part is used as hot carrier gas and is passed into the fluidized bed pyrolysis furnace after heating.The fluidized bed-down bed pyrolysis-gasification integrated method and device can effectively utilize small particle oil shale, and also effectively utilize the residual heat of fluidized bed pyrolysis semi-coke and gasification furnace gas product, so that the energy consumption of the whole circulating system is reduced.

Description

Technical Field

[0001] This invention belongs to the field of energy and chemical engineering, specifically relating to a method and apparatus for the co-production of shale oil and syngas using small-particle oil shale through fluidized bed-downward bed pyrolysis-gasification integration. Background Technology

[0002] Oil shale is a vast, unconventional fossil fuel, also known as "solid petroleum." Its main organic component, kerogen, is called the "mother of oil and gas." The product gas from oil shale pyrolysis and gasification can replace natural gas in some areas, and the shale oil produced by oil shale pyrolysis has a similar composition to crude oil. China has abundant oil shale resources, but most are continental oil shale. While large-scale mechanized mining can improve extraction efficiency, it leads to a significant increase in the proportion of small-particle oil shale, along with problems such as transportation difficulties and low utilization rates. Currently, my country's oil shale processing mainly uses fixed-bed pyrolysis technology, primarily using particles larger than 60 mm as raw materials. This results in the difficulty of utilizing small-particle oil shale, leading to its long-term accumulation in large quantities. Particle size has little impact on the properties of oil shale, but the price of large-particle oil shale raw materials on the market is often ten times that of small-particle oil shale, a situation also seen with other solid fossil fuels such as coal. Furthermore, the long-term open-air accumulation of small-particle oil shale can cause spontaneous combustion, water and soil pollution, resulting not only in substantial economic losses but also significant environmental damage.

[0003] To address the difficulty in utilizing small-particle oil shale, invention patent CN200810204396.6 discloses an oil shale fluidized bed retort system. This system can effectively utilize small-particle oil shale, but it suffers from low carbon conversion rate and difficulty in utilizing the waste heat from pyrolysis semi-coke. Invention patent CN201210189395.5 discloses a gas-solid combined heat-carrying oil shale fluidized bed retort system, and invention patent CN201210219096.1 discloses an oil shale fluidized bed steam low-temperature retort method and system. Existing oil shale fluidized bed retort systems can effectively utilize the organic components in semi-coke, but they still suffer from the problem of ineffective utilization of semi-coke waste heat and the need for a large amount of externally heated carrier gas for fluidized bed pyrolysis. Studies have shown that fluidized bed reactors are indeed suitable for the pyrolysis of small-particle oil shale. However, during fluidized bed pyrolysis, it is often difficult to directly control the residence time of the feedstock, leading to incomplete pyrolysis. In addition, due to the different fluidization properties of different particles, a large amount of small-particle dust will be emitted during fluidized bed pyrolysis. This dust mainly consists of small-particle semi-coke and powdered oil shale feedstock. This dust contains a large amount of organic matter residue and has a high temperature. Direct landfilling would not only waste energy but also cause pollution. Furthermore, fluidized bed pyrolysis requires a large amount of heat carrier gas, which greatly increases the pyrolysis cost.

[0004] Invention patent CN201410158250.8 discloses a system and process for the integrated utilization of oil shale dry distillation and semi-coke gasification. This process provides a high-temperature heat carrier for oil shale pyrolysis through semi-coke gasification, but the waste heat from the pyrolysis semi-coke is not effectively utilized. Invention patents CN202311512794.5 and others disclose coal pyrolysis-gasification coupling devices, which also suffer from the same problem. While existing integrated oil shale pyrolysis-gasification technologies have improved the shortcomings of traditional small-particle oil shale clean utilization to some extent, there is still room for improvement in energy utilization efficiency. The fluidized bed-downward bed pyrolysis-gasification integrated method and device proposed in this invention enables direct gasification of high-temperature pyrolysis semi-coke, effectively utilizing small-particle raw materials while offering advantages such as high carbon conversion rate and no need for an external heating carrier. Summary of the Invention

[0005] The purpose of this invention is to solve the problems of the difficulty in utilizing the principle of small-particle oil shale and the difficulty in utilizing the residual organic matter and residual heat in semi-coke in the existing technology. By combining a fluidized bed pyrolysis furnace and a downward bed gasification furnace, a new method and related equipment for integrated pyrolysis and gasification of oil shale are proposed.

[0006] To achieve the above objectives, the present invention provides an integrated method and apparatus for fluidized bed-downward bed pyrolysis-gasification, characterized in that: it includes a fluidized bed pyrolysis furnace (1), an air distribution plate (2), a gas-solid separator (3), a condenser (4), a downward bed gasifier (5), and an ash hopper (6); the fluidized bed pyrolysis furnace (1) has an inlet for raw material (A) at its lower end, and the downward bed gasifier (5) has an inlet for gasifying agent (B) at its upper part; the upper part of the fluidized bed is connected to the gas-solid separator; the top gas outlet of the gas-solid separator (3) is connected to the condenser (4); the bottom solid outlet of the gas-solid separator (3) is connected to the upper feed inlet of the downward bed gasifier (5); and the lower end of the downward bed gasifier (5) has a gasification product gas outlet (C). The bottom of the downward bed gasifier (5) is connected to the ash hopper (6); the gas outlet of the gas-solid separator (3) leads to the condenser (4). The condenser (4) can condense the high-temperature gas to obtain non-condensable gas and tar (E). Part of the non-condensable gas is further purified to become product gas (D), and the other part is heated to become heat carrier gas (F) and mixed with the gasification product gas before entering the fluidized bed pyrolysis furnace.

[0007] During fluidized bed pyrolysis, a large number of fine oil shale particles and semi-coke are blown out by the pyrolysis gas. These fine particles not only have a large amount of organic matter residue, but also have a high temperature. In order to make efficient use of this energy, this invention introduces a downward bed gasifier (5) to make secondary use of the organic matter in these fine particles, and adopts a free-fall connection method to effectively utilize the waste heat of the particles.

[0008] To prevent the gasifying agent (B) in the downflow bed gasifier (5) from flowing back into the cyclone separator and affecting the separation effect, the present invention adds an outlet valve to the gasification product gas outlet (C) of the downflow bed gasifier (5) to regulate the pressure inside the bed, ensuring that the downflow bed pressure is less than the internal pressure of the cyclone separator (3) and greater than the outlet pressure of the cyclone separator, so that the gasifying agent (B) flows downward and the pyrolysis gas generated in the fluidized bed pyrolysis furnace (1) flows upward.

[0009] To ensure the stability of the device operation, this invention utilizes the continuous feeding characteristics of a fluidized bed and maintains a constant flow rate of hot carrier gas by adjusting the flow rate of product gas (F), which will keep the total amount of solid particles separated by the gas-solid separator approximately constant.

[0010] This invention also provides an integrated fluidized bed-downward bed pyrolysis-gasification method, which uses the aforementioned integrated fluidized bed-downward bed pyrolysis-gasification device, as detailed below: a. The material is dried and sieved to obtain granular and powdered raw materials; b. The raw material is fed into the fluidized bed pyrolysis furnace (1) for pyrolysis reaction to produce semi-coke and pyrolysis gas; larger particles of raw material are discharged from the slag discharge port at the bottom of the bed after pyrolysis, and powdery raw material and small particles of semi-coke are carried out by the gas and enter the gas-solid separator (3) from the top of the bed. After gas-solid separation, the solid phase falls into the downward bed gasifier (5), and the gas phase enters the condenser (4). Among them, part of the non-condensable gas is further purified as product gas (D), and the other part is heated and used as heat carrier gas (F) to go into the fluidized bed pyrolysis furnace, while the condensable gas becomes tar (E) after cooling. c. Solid particles in the gas-solid separator (3) fall freely to the downflow bed gasifier (5), come into contact with the high-temperature gasifying agent gas (B) introduced from the upper end of the downflow bed, and undergo a violent gasification reaction to produce high-temperature gasification product gas (C) with reducing properties and fully utilized gasification residue. The gasification product gas (C) and product gas (F) are directly mixed and introduced into the fluidized bed pyrolysis furnace (1) as heat carrier gas. The gasification residue falls into the ash hopper (6) and is collected due to gravity. d. The gasification residue can be used to heat cold water to produce steam or to preheat the gasifying agent (B).

[0011] Furthermore, in step a, the raw materials are oil shale, low-rank coal, biomass, etc., with an ash content of less than 80% after drying, or mixtures of two or more of them.

[0012] Furthermore, in step a, the particle size of the oil shale feedstock (A) should be less than 30 mm.

[0013] Furthermore, in step b, the pyrolysis temperature in the fluidized bed pyrolysis furnace (1) is controlled between 300-600 ℃.

[0014] Furthermore, in step c, the gasification temperature in the downflow bed gasifier (5) is controlled between 700-1400 ℃.

[0015] The present invention can achieve the following technical effects: (1) The pyrolysis and gasification are coupled into one system. The product gas after gasification is used as the heat carrier for the pyrolysis reaction. The high-temperature pyrolysis semi-coke and powdered oil shale blown out by the pyrolysis gas are used as gasification feedstocks. The system has low energy consumption and high energy utilization rate. (2) The whole system has a simple structure, high oil and gas yield, and a wide range of applicable feedstocks. It effectively utilizes the organic components in the pyrolysis semi-coke and powdered oil shale, and avoids the pollution of the environment by the organic matter in the pyrolysis semi-coke and powdered oil shale. Attached Figure Description

[0016] Figure 1 This is a schematic diagram of the fluidized bed-downward bed pyrolysis-gasification integrated device involved in the present invention.

[0017] The system includes a fluidized bed pyrolysis furnace (1), an air distribution plate (2), a gas-solid separator (3), a condenser (4), a downflow gasifier (5), and an ash hopper (6). The fluidized bed pyrolysis furnace (1) has an inlet for raw material (A) at its lower end and an inlet for gasifying agent (B) at its upper part. The upper part of the fluidized bed is connected to the gas-solid separator. The gas outlet at the top of the gas-solid separator (3) is connected to the condenser (4), and the solid outlet at the bottom of the gas-solid separator (3) is connected to the feed inlet at the top of the downflow gasifier (5). The downflow gasifier (5) has a gasification product gas outlet (C) at its lower end and an ash hopper (6) at the bottom. The gas outlet at the top of the gas-solid separator (3) leads to the condenser (4). Part of the non-condensable gas is further purified to become product gas (D), and the other part is heated and mixed with the gasification product gas as heat carrier gas (F) before entering the fluidized bed pyrolysis furnace. The condensable gas becomes tar (E) after cooling. Detailed Implementation

[0018] To better illustrate the content and advantages of this invention, the invention will be described in detail below with reference to specific embodiments. However, the scope of protection of this invention is not limited to the following embodiments. Rather, these embodiments are provided to provide a more thorough and comprehensive understanding of the disclosure of this invention.

[0019] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention pertains. The terminology used herein in the description of the invention is for the purpose of describing particular embodiments only and is not intended to be limiting of the invention.

[0020] Example 1

[0021] Xinjiang oil shale is dried and screened to obtain oil shale raw material with a particle size <1 cm. The raw material is then transported from 1 / 8 above the air distribution plate to the fluidized bed pyrolysis furnace (1) for pyrolysis reaction, producing semi-coke and pyrolysis gas. The pyrolysis temperature is 480℃. Larger oil shale particles are discharged from the slag discharge port at the bottom of the bed after pyrolysis. Powdered raw material and small semi-coke particles are carried out by the gas and enter the gas-solid separator (3) from 1 / 5 above the furnace top of the bed. After gas-solid separation, the solid phase falls into the descending bed gasifier (5), and the gas phase enters the condenser (4). A portion of the non-condensable gas passes through the inlet. One part is purified into product gas (D), and another part is heated and used as heat carrier gas (F) to enter the fluidized bed pyrolysis furnace. The condensable gas is cooled to become tar (E). The solid particles in the gas-solid separator (3) fall freely into the downward bed gasifier (5) and come into contact with the high-temperature gasifying agent gas (B) that is vertically introduced from 1 / 10 of the top of the downward bed. A violent gasification reaction occurs, producing high-temperature gasified product gas (C) with reducing gas and fully utilized gasification residue. The temperature inside the gasifier is 1100 ℃. The gasified product gas (C) is discharged from the outlet at 9 / 10 of the distance from the top of the furnace and is directly mixed with the product gas (F) and introduced into the fluidized bed pyrolysis furnace (1) as heat carrier gas. The gasification residue falls into the ash hopper (6) and is collected due to gravity. The carbon conversion rate of the entire system is 97.93%.

[0022] Example 2

[0023] Xinjiang oil shale and cotton stalks were dried and sieved. Oil shale raw material with a particle size <1 cm and cotton stalk raw material with a particle size <3 cm were obtained and mixed in equal amounts. The raw material was conveyed from 1 / 8 above the air distribution plate to the fluidized bed pyrolysis furnace (1) for pyrolysis reaction to produce semi-coke and pyrolysis gas. The pyrolysis temperature was 500 °C. At ℃, larger oil shale particles and cotton stalks are discharged from the slag discharge port at the bottom of the bed after pyrolysis. Powdered raw materials and small particles of semi-coke are carried out by gas and enter the gas-solid separator (3) from 1 / 5 of the distance from the top of the furnace at the top of the bed. After gas-solid separation, the solid phase falls into the descending bed gasifier (5), and the gas phase enters the condenser (4). Part of the non-condensable gas is further purified and used as product gas (D), and the other part is heated and used as heat carrier gas (F) to go to the fluidized bed pyrolysis furnace. The condensable gas becomes tar (E) after cooling. The solid particles in the gas-solid separator (3) fall freely into the descending bed gasifier (5) and come into contact with the high-temperature gasifying agent gas (B) that is vertically introduced from 1 / 10 of the top of the descending bed. A violent gasification reaction occurs, producing high-temperature gasification product gas (C) with reducing gas and fully utilized gasification residue. The temperature inside the gasifier is 1000℃. At ℃, the gasification product gas (C) is discharged from the outlet at 9 / 10 of the distance from the top of the furnace and is directly mixed with the product gas (F) and fed into the fluidized bed pyrolysis furnace (1) as the heat carrier gas. The gasification residue falls into the ash hopper (6) due to gravity and is collected. The carbon conversion rate of the entire system is 98.65%.

[0024] Example 3

[0025] Xinjiang oil shale and cotton stalks were dried and sieved. Oil shale raw material with a particle size <1 cm and cotton stalk raw material with a particle size <3 cm were obtained and mixed in equal amounts. The raw material was conveyed from 1 / 8 above the air distribution plate to the fluidized bed pyrolysis furnace (1) for pyrolysis reaction to produce semi-coke and pyrolysis gas. The pyrolysis temperature was 500 °C. At ℃, larger oil shale particles are discharged from the slag outlet at the bottom of the bed after pyrolysis. Powdered raw materials and small particles of semi-coke are carried out by gas and enter the gas-solid separator (3) from 1 / 5 of the distance from the top of the furnace at the top of the bed. After gas-solid separation, the solid phase falls into the descending bed gasifier (5), and the gas phase enters the condenser (4). Part of the non-condensable gas is further purified and used as product gas (D), and the other part is heated and used as heat carrier gas (F) to go to the fluidized bed pyrolysis furnace. The condensable gas becomes tar (E) after cooling. The solid particles in the gas-solid separator (3) fall freely into the descending bed gasifier (5) and come into contact with the high-temperature gasifying agent gas (B) that is obliquely introduced from 1 / 10 of the top of the descending bed. A violent gasification reaction occurs, producing high-temperature gasification product gas (C) with reducing gas and fully utilized gasification residue. The temperature inside the gasifier is 1000℃. At ℃, the gasification product gas (C) is discharged from the outlet at 9 / 10 of the distance from the top of the furnace and is directly mixed with the product gas (F) and fed into the fluidized bed pyrolysis furnace (1) as the heat carrier gas. The gasification residue falls into the ash hopper (6) and is collected due to gravity. However, because the gasification agent gas inlet of the gasifier is inclined upward, some semi-coke is suspended at the gasifier inlet, which reduces the separation effect of the cyclone separator. The carbon conversion rate of the whole system is only about 89%, and the tar obtained contains a large amount of solid dust.

[0026] Example 4

[0027] The coal and cotton stalks were dried and sieved to obtain coal raw material with a particle size <1 cm and cotton stalk raw material with a particle size <3 cm, and they were mixed in equal amounts. The raw material was then conveyed from 1 / 8 above the air distribution plate to the fluidized bed pyrolysis furnace (1) for pyrolysis reaction to produce semi-coke and pyrolysis gas. The pyrolysis temperature was 450 °C. At ℃, larger oil shale particles are discharged from the slag outlet at the bottom of the bed after pyrolysis. Powdered raw materials and small particles of semi-coke are carried out by gas and enter the gas-solid separator (3) from 1 / 5 of the distance from the top of the furnace at the top of the bed. After gas-solid separation, the solid phase falls into the descending bed gasifier (5), and the gas phase enters the condenser (4). Part of the non-condensable gas is further purified and used as product gas (D), and the other part is heated and used as heat carrier gas (F) to go to the fluidized bed pyrolysis furnace. The condensable gas becomes tar (E) after cooling. The solid particles in the gas-solid separator (3) fall freely into the descending bed gasifier (5) and come into contact with the high-temperature gasifying agent gas (B) that is vertically introduced from 1 / 10 of the top of the descending bed. A violent gasification reaction occurs, producing high-temperature gasification product gas (C) with reducing gas and fully utilized gasification residue. The temperature inside the gasifier is 900℃. At ℃, the gasification product gas (C) is discharged from the outlet at 9 / 10 of the distance from the top of the furnace and is directly mixed with the product gas (F) and fed into the fluidized bed pyrolysis furnace (1) as the heat carrier gas. The gasification residue falls into the ash hopper (6) and is collected due to gravity. The carbon conversion rate of the entire system is 99.21%.

[0028] Comparative Example 1

[0029] Xinjiang oil shale is dried and screened to obtain oil shale raw material with a particle size of <1 cm. The raw material is transported from 1 / 8 above the air distribution plate to the fluidized bed pyrolysis furnace (1) for pyrolysis reaction to produce semi-coke and pyrolysis gas. The pyrolysis temperature is 500℃. Larger oil shale particles are discharged from the slag discharge port at the bottom of the bed after pyrolysis. Powdered raw material and small semi-coke particles are carried out by the gas and enter the gas-solid separator (3) from 1 / 5 above the furnace top of the bed. After gas-solid separation, the solid phase falls into the downward bed gasifier (5) and the gas phase enters the condenser (4). Part of the non-condensable gas is further purified and used as product gas (D), and the other part is heated and used as heat carrier gas (F) to go to the fluidized bed pyrolysis furnace. The condensable gas becomes tar (E) after cooling. The solid particles in the gas-solid separator (3) are discharged and cooled and then transported into the circulating fluidized bed for pyrolysis. The overall carbon conversion rate of the system is 83.25%, and it is necessary to add gas heating equipment to heat the external heating carrier.

Claims

1. An integrated fluidized bed-downward bed pyrolysis-gasification device, characterized in that: The system includes a fluidized bed pyrolysis furnace (1), an air distribution plate (2), a gas-solid separator (3), a condenser (4), a downflow gasifier (5), and an ash hopper (6). The air distribution plate (2) is located at the lower part of the fluidized bed pyrolysis furnace (1). The lower end of the fluidized bed pyrolysis furnace (1) has an inlet for raw material (A). The upper part of the downflow gasifier (5) has an inlet for gasifying agent (B). The upper part of the fluidized bed pyrolysis furnace (1) is connected to the gas-solid separator (3). The top gas outlet of the gas-solid separator (3) is connected to the condenser (4). The bottom solid outlet of the gas-solid separator (3) is connected to the upper feed inlet of the downflow gasifier (5), so that the semi-coke enters the downflow gasifier from the gas-solid separator (3) by free fall. (5); The gas-solid separator (3) adopts one or more sets of cyclone separators in series; The lower end of the downflow bed gasifier (5) is provided with the outlet of gasification product gas (C) so as to use the gas outlet valve at the outlet of gasification product gas (C) to regulate the pressure inside the bed, ensure that the pressure inside the downflow bed is less than the pressure inside the cyclone separator, and avoid gas backflow; The bottom of the downflow bed gasifier (5) is connected to the ash hopper (6); The gas outlet at the top of the gas-solid separator (3) leads to the condensing device (4), where part of the non-condensable gas is further purified and used as product gas (D), and the other part is heated and used as heat carrier gas (F) to mix with the gasification product gas and then enter the fluidized bed pyrolysis furnace (1), while the condensable gas becomes tar (E) after cooling.

2. The fluidized bed-downward bed pyrolysis-gasification integrated device according to claim 1, characterized in that: The raw material inlet is located at 1 / 50-1 / 5 of the distance from the air distribution plate (2) of the fluidized bed pyrolysis furnace (1).

3. The fluidized bed-downward bed pyrolysis-gasification integrated device according to claim 1, characterized in that: The fluidized bed pyrolysis furnace (1) has a connection port for connecting to the gas-solid separator (3) at a distance of 1 / 30-1 / 5 from the top of the furnace.

4. The fluidized bed-downward bed pyrolysis-gasification integrated device according to claim 1, characterized in that: The inlet of the gasifying agent (B) is set at a distance of 1 / 30-1 / 5 from the top of the gasifier (5).

5. The fluidized bed-downward bed pyrolysis-gasification integrated device according to claim 1, characterized in that: The outlet of gasification product gas (C) is set at a distance of 1 / 10-1 / 3 from the ash hopper of the downward bed gasifier (5).

6. The fluidized bed-downward bed pyrolysis-gasification integrated device according to claim 1, characterized in that: The inlet of the gasifying agent (B) is set perpendicularly or obliquely downward to the side of the downward bed gasifier (5), and the angle between the inlet and the side of the downward bed gasifier (5) is between 30° and 90°.

7. The fluidized bed-downward bed pyrolysis-gasification integrated device according to claim 1, characterized in that: The outlet of the gasification product gas (C) is set perpendicular to the side of the downward bed gasifier (5), and a dust collector is set at the front end of the outlet. The dust collector is any one or a combination of filter element or settling device.

8. A fluidized bed-downward bed pyrolysis-gasification integrated method, employing the fluidized bed-downward bed pyrolysis-gasification integrated device according to any one of claims 1-4, characterized in that, Includes the following steps: a. Reaction in fluidized bed pyrolysis furnace (1): Raw material (A) is added from above the air distribution plate (2) at the lower end of the fluidized bed and comes into contact with the high-temperature gasification product gas (C) rich in CO and H2 reducing gases from the downflow bed gasifier (5) and part of the supplemented heated carrier gas (F), resulting in a violent pyrolysis reaction and producing semi-coke and a large amount of pyrolysis gas; large particles of raw material are discharged from the slag discharge port at the lower end of the bed after pyrolysis; some small particles of raw material and small particles of semi-coke are carried out by the gas and enter the gas-solid separator (3) from the upper end of the bed. After gas-solid separation, the solid phase falls into the downflow bed gasifier (5) and the gas phase enters the condenser (4). Part of the non-condensable gas is further purified and used as product gas (D), and the other part is heated and used as carrier gas (F) to go into the fluidized bed pyrolysis furnace, while the condensable gas becomes tar (E) after cooling. b. Reaction in the downflow bed gasifier (5): Solid particles in the gas-solid separator (3) fall freely into the downflow bed gasifier (5) and come into contact with the high-temperature gasifying agent (B) introduced from the upper end of the downflow bed gasifier (5), resulting in a violent gasification reaction and producing high-temperature gasification product gas (C) rich in CO and H2 reducing gases, as well as fully utilized gasification residue; the gasification residue falls into the ash hopper (6) and is collected due to gravity.

9. The fluidized bed-downward bed pyrolysis-gasification integrated method according to claim 8, characterized in that: The raw materials are oil shale, low-rank coal, biomass, and mixtures of two or more of them, with an ash content of less than 80% after drying.

10. The fluidized bed-downward bed pyrolysis-gasification integrated method according to claim 8, characterized in that: The particle size of raw material (A) is less than 30 mm.

11. The fluidized bed-downward bed pyrolysis-gasification integrated method according to claim 8, characterized in that: The fluidized bed pyrolysis furnace (1) operates at a temperature of 300-600 ℃, and the downflow bed gasification furnace (5) operates at a temperature of 700-1400 ℃.

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