A solid carbonaceous fuel multifunctional thermal conversion apparatus and method

Abstract

The application provides a solid carbon-containing fuel multifunctional thermal conversion device and method, which comprises a multifunctional reactor, a lifting reactor and a particle classifier; the multifunctional reactor comprises first, second, third, fourth and fifth reaction cavities arranged coaxially; the first, second and third reaction cavities are arranged in sequence from top to bottom; the fourth reaction cavity is arranged outside the joint of the first and second reaction cavities and connects the first and second reaction cavities into one; the fifth reaction cavity is arranged outside the joint of the second and third reaction cavities and connects the second and third reaction cavities into one; the outlet of the lifting reactor is connected with the inlet of the particle classifier; the two particle material outlets of the particle classifier are respectively connected with the first solid bed material feeding port and the second solid bed material feeding port of the multifunctional reactor through valves; and the inlet of the lifting reactor is connected with the first solid discharging port and the third solid upper discharging port of the multifunctional reactor through valves. The application has rich functions, high integration and can adopt multiple operation modes.

Description

Technical Field

[0001] This invention belongs to the field of energy and chemical technology, and relates to a solid carbon-containing fuel thermal conversion device and method. More specifically, it relates to a multifunctional solid carbon-containing fuel thermal conversion device and method, which is a multi-operation mode pyrolysis gasification device and method combining moving bed and fluidized bed. Background Technology

[0002] Solid carbon fuels are a major component of the world's energy supply today, but their utilization also contributes to the global greenhouse effect. Therefore, the efficient and clean utilization of solid carbon fuels is a significant issue involving both energy and the environment. Solid carbon fuels can be pyrolyzed and gasified to produce oil, syngas, and semi-coke, which can be refined and further processed to obtain fuels and chemical products.

[0003] Both pyrolysis and gasification are strongly endothermic reactions. Traditional processes maintain the reaction by introducing oxygen or air into the same reactor to burn a portion of the fuel. Within the reactor, combustion, pyrolysis, and gasification reactions occur, forming a complex reaction network. Each sub-reaction cannot be independently controlled to achieve optimal reaction conditions; simultaneously, the products of each sub-reaction influence each other, hindering the target reaction. The most significant problem is that using oxygen or air dilutes the generated CO2 and N2 from the air itself, resulting in low effective component content and low calorific value in the pyrolysis or syngas. Decoupling the reactions is a novel approach to address these issues. This involves setting up separate fuel reactors and combustion reactors, using a solid circulating bed to transfer heat from the combustion reactor to the fuel reactor, providing the energy required for pyrolysis / gasification. For example, the dual fluidized bed pyrolysis gasification process of the Institute of Process Engineering, Chinese Academy of Sciences (patent CN101781583B: method and apparatus for high-value utilization of coal pyrolysis gasification); and the dual fluidized bed gasification process of the Guangzhou Institute of Energy Research, Chinese Academy of Sciences (patent CN101880552B: a gasification apparatus and method for preparing hydrogen-rich syngas from biomass).

[0004] This method effectively avoids the aforementioned problems. However, it also has the following drawbacks: the products carry dust, causing a decline in the quality of syngas and tar, requiring additional dust removal and purification processes; at the same time, most existing decoupling processes have specific requirements for particle size, and the raw materials and circulating bed materials need to be ground and screened, and some particle sizes are not well utilized; in addition, when using chemical looping gasification, the need for excessive oxygen carrier heating can lead to over-oxidation of syngas; in the CaO adsorption enhanced gasification process, it is impossible to simultaneously handle the high-temperature tar reforming and low-temperature chemical adsorption CO2 processes, requiring further decoupling to achieve this. Summary of the Invention

[0005] This invention proposes a multifunctional thermal conversion device and method for solid carbon-containing fuels, aiming to enable the reaction to occur in different spaces and times, thereby achieving decoupling and individual control of key sub-reactions and improving feedstock utilization. Different target products can be obtained by changing the gas-solid feedstock, circulating bed material, and operating mode.

[0006] Technical solution of the present invention:

[0007] A multifunctional thermal conversion device for solid carbon fuel includes a multifunctional reactor, a lifting reactor, and a particle classifier. The multifunctional reactor includes a first, second, third, fourth, and fifth reaction chambers arranged coaxially. The first, second, and third reaction chambers are arranged sequentially from top to bottom. The lower port of the first reaction chamber is not higher than the upper port of the second reaction chamber. The lower port of the second reaction chamber is not higher than the upper port of the third reaction chamber. The fourth reaction chamber is located outside the junction of the first and second reaction chambers and connects the first and second reaction chambers into one unit. The fifth reaction chamber is located outside the junction of the second and third reaction chambers and connects the second and third reaction chambers into one unit.

[0008] The first reaction chamber is provided with an adjacent first solid bed material inlet and a first solid fuel inlet, located at the top of the first reaction chamber; the fourth reaction chamber is provided with an adjacent second solid bed material inlet and a second solid fuel inlet, located on the upper side of the fourth reaction chamber; the fifth reaction chamber is provided with a third solid fuel inlet, located on the upper side of the fifth reaction chamber.

[0009] The first reaction chamber is further provided with a first air inlet located in the middle of the side of the first reaction chamber; the second reaction chamber is provided with a second air inlet located in the middle of the side of the second reaction chamber; the third reaction chamber is provided with a third air inlet located in the middle of the side of the third reaction chamber; the bottom of the fourth reaction chamber is further provided with a fourth air inlet and a gas distribution plate, the fourth air inlet being located below the gas distribution plate; the bottom of the fifth reaction chamber is further provided with a fifth air inlet and a gas distribution plate, the fifth air inlet being located below the gas distribution plate.

[0010] The bottom of the third reaction chamber is also provided with a first solid discharge port; the middle side of the fourth reaction chamber is also provided with a second upper solid discharge port and a second lower solid discharge port, wherein the second upper solid discharge port is located above the top of the upper section of the second reaction chamber, and the second lower solid discharge port is located below the top of the upper section of the second reaction chamber. The middle side of the fifth reaction chamber is also provided with a third upper solid discharge port and a third lower solid discharge port, wherein the third upper solid discharge port is located above the top of the upper section of the third reaction chamber, and the third lower solid discharge port is located below the top of the upper section of the third reaction chamber.

[0011] The first reaction chamber is also provided with a first air outlet, located on the upper side of the first reaction chamber; the fourth reaction chamber is also provided with a second air outlet, located at the top of the fourth reaction chamber; the fifth reaction chamber is also provided with a third air outlet, located at the top of the fifth reaction chamber.

[0012] The upper section of the first reaction chamber is also equipped with a solid mixing internal component for rapid mixing of solid bed material and solid fuel.

[0013] The first reaction chamber is also equipped with a solid material level control internal component, located between the first air inlet and the first air outlet, for detecting the material level and controlling the discharge rate of solid materials.

[0014] Preferably, the second solid fuel inlet is tangentially arranged along the wall of the fourth reaction chamber; the third solid fuel inlet is tangentially arranged along the wall of the fifth reaction chamber.

[0015] Preferably, the first reaction chamber includes an upper section and a lower section, wherein the diameter of the upper section is larger than the diameter of the lower section; the second reaction chamber includes an upper section and a lower section, wherein the diameter of the upper section is larger than the diameter of the lower section; and the third reaction chamber includes an upper section and a lower section, wherein the diameter of the upper section is larger than the diameter of the lower section.

[0016] Preferably, the diameter of the fourth reaction chamber is larger than the diameter of the upper section of the second reaction chamber, and the height of the fourth reaction chamber is larger than the height of the upper section of the second reaction chamber.

[0017] Preferably, the diameter of the fifth reaction chamber is larger than the diameter of the upper section of the third reaction chamber, and the height of the fifth reaction chamber is larger than the height of the upper section of the third reaction chamber.

[0018] Preferably, a vertical baffle is provided between the fourth reaction chamber and the upper section of the second reaction chamber, dividing the fourth reaction chamber into two parts, an inner and an outer part, which are isolated at the top and have a gap at the bottom. The height of the gap is less than the height of the upper section of the second reaction chamber.

[0019] The thermal conversion device is connected as follows: the outlet of the lifting reactor is connected to the inlet of the particle classifier; the two particle material outlets of the particle classifier are respectively connected to the first solid bed material inlet and the second solid bed material inlet of the multifunctional reactor through valves; the inlet of the lifting reactor is respectively connected to the first solid discharge outlet and the third solid discharge outlet of the multifunctional reactor through valves.

[0020] A multifunctional thermal conversion method for solid carbon-containing fuels, employing the aforementioned apparatus, wherein the first, second, and third reaction chambers utilize a moving bed mode, while the fourth and fifth reaction chambers utilize a fluidized bed or entrained bed mode. Five different modes are achieved through the coordination of these different reaction chambers:

[0021] (I) Mode 1: The first solid fuel and the first solid bed material enter from the first solid fuel inlet and the first solid bed material inlet, respectively. After mixing at the solid mixing internal component, they enter the lower section of the first reaction chamber. The first gaseous feedstock enters the lower section of the first reaction chamber from the first air inlet, and the gas and solid flow counter-currently upwards to contact and react with the first solid fuel. The first gaseous product generated by the reaction is collected from the first air outlet, and the first solid product generated by the reaction enters the second reaction chamber together with the first solid bed material. The second gaseous feedstock, carrying the second solid fuel, enters the fourth reaction chamber from the second solid fuel inlet, where a pyrolysis-gasification reaction occurs to generate gas and the second solid product. The gas generated by the reaction merges with the third gaseous feedstock entering from the second air inlet, and together they flow co-currently through the second reaction chamber and react to generate the second gaseous product, which is discharged from the third air outlet. The second solid product enters the second reaction chamber and combines with the first solid product to form a solid product. The solid product and the first solid bed material are collected together from the first solid discharge outlet. The first solid bed material is recycled back to the first reaction chamber after being lifted and particle classified.

[0022] Mode 1 can be used to prepare hydrogen-rich syngas. Specifically, the return valve connecting the first solid bed feed inlet and the particle classifier is opened, and the return valve connecting the second solid bed feed inlet and the particle classifier is closed. The first solid bed feed consists of high-temperature active bed particles from the particle classifier, including but not limited to CO2 adsorbent. The high-temperature active bed particles and the first solid fuel particles enter the first reaction chamber, where they are rapidly mixed and heat-exchanged at the solid mixing internal component, and then sequentially exit from the first solid outlet through the second and third reaction chambers. The discharge rate of the first solid outlet is controlled by the solid material level control internal component, ensuring that the material fills the lower section of the first reaction chamber and that the material level is not higher than the first gas outlet; and two accumulation surfaces are formed in the upper sections of the second and third reaction chambers, respectively. In the first reaction chamber, the solid fuel particles react with the oxidant entering from the first gas inlet, burning at 800-1000°C, generating high temperatures that activate the CO2 adsorbent and improve its CO2 adsorption capacity. The second solid fuel is solid fuel powder. Solid fuel powder enters the fourth reaction chamber, where it undergoes a gasification reaction with the gasification medium at 650-950℃, producing syngas, semi-coke, and a small amount of tar. Closing the second outlet makes the internal pressure of the fourth reaction chamber greater than that of the fifth reaction chamber, allowing the syngas to pass through the upper section of the second reaction chamber in a gas-solid co-current flow. In the second reaction chamber, the syngas undergoes a water-gas shift reaction with water vapor at 400-600℃, while CO2 reacts with the adsorbent to produce hydrogen-rich syngas. The tar and semi-coke carried by the syngas are further gasified and reformed under the action of water vapor, thus increasing the gas yield. The generated hydrogen-rich syngas enters the fifth reaction chamber from the upper section of the third reaction chamber and exits through the third outlet. After the reaction, the adsorbent is heated, lifted, and separated by a booster reactor and a particle classifier before entering the first reaction chamber to begin a new cycle.

[0023] (II) Mode 2: The first solid bed material enters the first, second, and third reaction chambers sequentially from the first solid bed material inlet, forming a moving bed with a certain porosity. The first solid fuel enters the fourth reaction chamber from the second solid fuel inlet, and the first gaseous feedstock enters the fourth reaction chamber from the fourth inlet via a gas distribution plate as fluidizing gas and reaction gas. In the fourth reaction chamber, the first solid fuel undergoes a fluidized bed pyrolysis-gasification reaction with the gaseous feedstock, generating gas and the first solid product; the gas and solid react counter-currently through the first reaction chamber with the first solid bed material, generating the first gaseous product which is discharged from the first outlet, and the reacted first solid bed material enters the third reaction chamber; the first solid product is discharged from the second solid bottom outlet. In the third reaction chamber, the first solid bed material comes into counter-current contact with the second gaseous feedstock entering from the third inlet and reacts further, generating the second gaseous product which is collected from the third outlet; the further reacted first solid bed material is collected from the first solid outlet, and after being lifted and particle classified, it is recycled back to the first reaction chamber.

[0024] Mode 2 can also be used for chemical chain hydrogen production. Specifically, the return valve connecting the first solid bed feed inlet and the particle classifier is opened, while the return valve connecting the second solid bed feed inlet and the particle classifier is closed. The first solid bed material is active bed material particles, including but not limited to metal oxides and composite metal oxides. Active bed material at 700-950°C from the particle classifier is added to the first reaction chamber from the first solid feed inlet, and then sequentially exits from the first solid discharge outlet through the second and third reaction chambers. The discharge rate of the first solid discharge outlet is controlled by the solid material level control internal components, ensuring that the material does not completely fill the lower section of the first reaction chamber but the material level is higher than the first gas inlet; and two accumulation surfaces are formed respectively in the upper sections of the second and third reaction chambers. The first solid fuel particles enter the fourth reaction chamber and undergo pyrolysis under the action of 500-600°C hot fluidized gas, generating volatiles and semi-coke. Semi-coke is collected from the second solid discharge port, while volatiles pass through the upper section of the second reaction chamber's packing surface in a gas-solid countercurrent flow through the first reaction chamber. At 800-950℃, they undergo a redox reaction with the active bed material, reducing it to a lower valence state. The lower valence state active bed material particles enter the third reaction chamber, contacting water vapor entering from the third inlet. At 550-660℃, they undergo a water splitting reaction to generate hydrogen. The hydrogen passes through the upper section of the third reaction chamber's packing surface into the fifth reaction chamber and is collected from the third outlet. After the reaction, the active bed material is heated, lifted, and separated by the lifting reactor and particle classifier before entering the first reaction chamber to begin a new cycle.

[0025] (III) Mode 3: The first solid fuel enters the first, second, and third reaction chambers through the first solid fuel inlet, forming a moving bed with a certain porosity. The first gaseous feedstock carries the second solid fuel into the fifth reaction chamber through the third solid fuel inlet, where a pyrolysis-gasification reaction occurs, generating gaseous and second solid products. The gas passes through the second reaction chamber, contacts the first solid fuel, and reacts to generate a first gaseous product and a first solid product. The first gaseous product is discharged from the second gas outlet; the first and second solid products merge into a solid product, which enters the third reaction chamber together and is collected from the first solid outlet.

[0026] Mode 3 can be used to couple gasification and pyrolysis to produce high-quality syngas and tar. Specifically, the return valve connecting the first solid bed feed inlet and the particle classifier, as well as the return valve connecting the second solid bed feed inlet and the particle classifier, are closed. First solid fuel particles are added from the first solid fuel feed inlet and then sequentially exit from the first solid discharge outlet through the second and third reaction chambers. The discharge rate of the first solid discharge outlet is controlled by the solid material level control internal components, ensuring that the material fills the lower section of the first reaction chamber and the material level does not exceed the first gas outlet; and two accumulation surfaces are formed in the upper sections of the second and third reaction chambers, respectively. The second solid fuel is solid fuel powder. High-temperature gaseous feedstock carrying the solid fuel powder enters the fifth reaction chamber from the third solid fuel feed inlet, where it reacts at 750-950℃ to generate syngas and semi-coke. The syngas carrying the semi-coke passes through the second reaction chamber via the accumulation surface in the upper section of the third reaction chamber in a gas-solid countercurrent manner. During this process, the semi-coke is trapped by the solid fuel particle bed and moves downwards together; simultaneously, the solid fuel particles, under the influence of the heat carried by the syngas, have their temperature increased to 400-600℃ and undergo pyrolysis to generate pyrolysis gas and pyrolysis oil; since the syngas contains active components, it promotes the lightening of the tar, thereby improving the tar quality. The syngas, pyrolysis gas, and high-quality pyrolysis oil enter the fourth reaction chamber through the upper section of the second reaction chamber and are extracted from the second outlet.

[0027] (iv) Mode 4: The first solid bed material enters the first, second, and third reaction chambers from the first solid bed material inlet, forming a moving bed with a certain porosity; the first solid fuel enters the fifth reaction chamber from the third solid fuel inlet; the first gaseous feedstock enters the fifth reaction chamber from the fifth inlet via a gas distribution plate as fluidizing gas and reaction gas. The first solid fuel undergoes fluidized bed pyrolysis-gasification reaction with the gaseous feedstock in the fifth reaction chamber, generating gas and the first solid product; the gas and solid flow countercurrently through the second reaction chamber, contacting and reacting with the first solid bed material to generate the first gaseous product, which is discharged from the second outlet; the first solid product is discharged from the third solid bottom outlet. The reacted first solid bed material is collected from the first solid outlet and enters the lifting reactor and particle classifier. After heating, lifting, and separation, it re-enters the first reaction chamber to begin a new cycle.

[0028] Mode 4 can be used for catalytic upgrading of tar. Specifically, the return valve connecting the first solid bed feed inlet and the particle classifier is opened, and the return valve connecting the second solid bed feed inlet and the particle classifier is closed. The first solid bed is an active bed, including but not limited to catalysts and oxygen carriers. Active bed particles are added from the first solid bed feed inlet and then sequentially exited from the first solid outlet through the second and third reaction chambers. The discharge rate of the first solid outlet is controlled by the solid material level control internal components, so that the material fills the first reaction chamber and the material level is not higher than the first gas outlet; and two accumulation surfaces are formed in the upper sections of the second and third reaction chambers respectively. The first solid fuel is solid fuel particles. The solid fuel particles enter the fifth reaction chamber from the third solid feed inlet and undergo pyrolysis under the action of 500-600℃ hot fluidized gas to generate volatiles and semi-coke. The semi-coke is discharged through the third solid outlet, and the volatiles pass through the accumulation surface of the upper section of the third reaction chamber in a gas-solid countercurrent manner through the second reaction chamber. In the second reaction chamber, volatiles undergo tar deoxygenation and secondary reactions of heavy tar on the surface of the catalyst or oxygen carrier at 300-500℃. Simultaneously, the granular bed formed by the activated bed material captures and purifies the dust carried by the volatiles. The cleaned volatiles, after catalytic reforming, enter the fourth reaction chamber through the stacking surface of the second reaction chamber and are extracted from the second outlet. The reacted activated bed material passes through a lift reactor and a particle classifier, undergoing heating, lifting, and separation before re-entering the first reaction chamber to begin a new cycle.

[0029] (V) Mode 5: The first solid bed material and the first solid fuel enter the fourth reaction chamber from the second solid bed material inlet and the second solid fuel inlet, respectively. The first gaseous feedstock enters the fourth reaction chamber from the fourth inlet via a gas distribution plate as fluidizing gas and reaction gas. The first solid fuel undergoes a fluidized bed pyrolysis-gasification reaction with the gaseous feedstock in the fourth reaction chamber, generating a first gaseous product and a first solid product. The first gaseous product passes through the first reaction chamber and is discharged from the first outlet. The first solid product and the first solid bed material overflow into the upper section of the second reaction chamber, forming a material layer of a certain height in the second reaction chamber, which serves as a gas seal. The second gaseous feedstock enters the third reaction chamber from the third inlet, serving as a loosening gas and return gas, allowing the first solid product and the first solid bed material in the second reaction chamber to enter the fifth reaction chamber. The third gaseous feedstock enters the fifth reaction chamber from the fifth inlet via a gas distribution plate, where it further reacts with the first solid product and the first solid bed material in the fifth reaction chamber, generating a second gaseous product which is collected from the third outlet. The reacted first solid bed material and the first solid product are collected from the third solid upper outlet. The first solid bed material is lifted, heated, and separated before entering the fourth reaction chamber to begin a new cycle.

[0030] Mode 5 can be used to decouple chemical looping gasification to prepare different H2 / CO syngas. Specifically, the return valve connecting the first solid bed feed inlet and the particle classifier is closed, while the return valve connecting the second solid bed feed inlet and the particle classifier is opened. The first solid bed feed is a high-temperature active bed feed from the particle classifier, including but not limited to metal oxides and composite metal oxides. The first solid fuel is solid fuel particles. The high-temperature active bed feed and solid fuel particles enter the fourth reaction chamber from the first solid bed feed inlet and the first solid fuel feed inlet, respectively, and are fluidized under the action of fluidizing gas entering from the fourth inlet. Simultaneously, the solid fuel particles undergo rapid pyrolysis at 800-900℃, generating volatiles and semi-coke. Due to the action of the baffles, the volatiles pass downward through the active bed feed layer. During this process, the volatiles undergo a redox reaction with the active bed material particles at 800-950℃, reducing them to a lower valence state and converting them into a first syngas with a low H2 / CO ratio. The first syngas is collected from the first outlet. The semi-coke and the low-valence active bed material particles overflow into the upper part of the second reaction chamber, forming a material layer of a certain height in the lower section of the second reaction chamber, which serves as a seal. The third inlet introduces circulating gas as loosening gas and return gas, allowing the low-valence active bed material and semi-coke to enter the fifth reaction chamber. The gasification medium enters the fifth reaction chamber from the fifth inlet through the gas distribution plate, where the semi-coke undergoes deoxidation at 650-800℃, generating a second syngas with a high H2 / CO ratio. The second syngas is collected from the third outlet. The reacted semi-coke and active bed material are collected from the third solids outlet and enter the lifting reactor and particle classifier. After heating, lifting, and separation, the active bed material enters the fourth reaction chamber to begin a new cycle.

[0031] Preferably, when the particle size of the solid bed material and solid fuel is ≤0.5mm, the second solid bed material inlet, the second solid fuel inlet, or the third solid bed material inlet and the third solid fuel inlet are selected for feeding; when the particle size of the solid bed material and solid fuel is ≥4mm and ≤13mm, the first solid bed material inlet and the first solid fuel inlet are selected for feeding.

[0032] Preferably, the first solid fuel and the second solid fuel are one or more of low-rank coal, biomass, petroleum coke, coke, charcoal, plastics, rubber, and asphalt.

[0033] Preferably, the first solid bed material and the second solid bed material are one or more mixtures of inert bed materials and active bed materials. The inert bed material includes, but is not limited to, quartz sand, river sand, and ceramic particles; the active bed material includes, but is not limited to, metal oxygen carriers, composite metal oxygen carriers, CO2 adsorbents, catalysts, and natural ores.

[0034] The beneficial effects of this invention are:

[0035] 1. The multifunctional thermal conversion device for solid carbon-containing fuels of the present invention, through the series connection of multiple chambers, separates the sub-reactions in the pyrolysis-gasification process of solid fuels to occur in different spaces and at different times, thereby achieving decoupling and individual control of key sub-reactions. It is equipped with three solid fuel inlets and two solid bed feed inlets, enabling simultaneous feeding of multiple streams of solid bed material and solid fuel. It can realize the pyrolysis, gasification, or coupling of gasification and pyrolysis of various fuels, making the device versatile in function.

[0036] 2. In this invention, the first, second and third reaction chambers adopt a moving bed mode, and the fourth and fifth reaction chambers adopt a fluidized bed or entrained bed mode. By coordinating different reaction chambers, three different modes can be achieved, which is suitable for the thermal conversion process of fuel and bed material with a large particle size range. The device has high integration and is flexible and convenient to operate.

[0037] 3. The moving particle bed formed in the first and second reaction chambers of this invention can capture the dust carried in the gas products, realize the thermal dust removal of high-temperature gas products, which is conducive to the continuous and stable operation of the thermal conversion process and can produce high-quality gas products and tar. Attached Figure Description

[0038] Figure 1 This is a schematic diagram of a multifunctional reactor for solid carbon-containing fuels.

[0039] Figure 2 This is a schematic diagram of a multi-functional reactor with a moving bed and an upper entrainment bed.

[0040] Figure 3 This is a schematic diagram of a multifunctional reactor with a moving bed and upper fluidized bed configuration.

[0041] Figure 4 This is a schematic diagram of a multi-functional reactor with a moving bed and lower entrainment bed configuration.

[0042] Figure 5 This is a schematic diagram of a multifunctional reactor with a moving bed and a lower fluidized bed configuration.

[0043] Figure 6 This is a schematic diagram of a dual fluidized bed mode for a multifunctional reactor.

[0044] Figure 7 This is a schematic diagram of a multifunctional thermal conversion device for solid carbon-containing fuels.

[0045] In the diagram: 1. First reaction chamber: 1-1 Upper section of the first reaction chamber, 1-2 Lower section of the first reaction chamber, 1-3 First solid bed feed inlet, 1-4 First solid fuel feed inlet, 1-5 First air inlet, 1-6 First air outlet, 1-7 Solid mixing internal component, 1-8 Solid material level control internal component; 2. Second reaction chamber: 2-1 Upper section of the second reaction chamber, 2-2 Lower section of the second reaction chamber, 2-3 Second air inlet; 3. Third reaction chamber: 3-1 Upper section of the third reaction chamber, 3-2 Lower section of the third reaction chamber, 3-3 Third air inlet, 3-4 First solid discharge outlet; 4. Fourth reaction chamber: 4-1 Second solid bed feed inlet... 4-2 Second solid fuel inlet, 4-3 First gas outlet, 4-4 Second upper solid discharge outlet, 4-5 Second lower solid discharge outlet, 4-6 Fourth gas inlet, 4-7 Gas distribution plate A, 4-8 Baffle; 5 Fifth reaction chamber, 5-1 Third solid fuel inlet, 5-2 Third gas outlet, 5-3 Third upper solid discharge outlet, 5-4 Third lower solid discharge outlet, 5-5 Fifth gas inlet, 5-6 Gas distribution plate B; 6 Lifting reactor; 7 Particle classifier; 8-1 Return valve A, 8-2 Third upper solid discharge outlet valve; 9-1 Return valve B, 9-2 First solid discharge outlet valve. Detailed Implementation

[0046] The specific embodiments of the present invention will be further described below with reference to the accompanying drawings and technical solutions.

[0047] The solid carbon-containing fuel multifunctional thermal conversion device of the present invention, such as Figure 1 and 7 As shown, the reactor includes a multifunctional reactor 1-5, a lifting reactor 6, and a particle classifier 7. The multifunctional reactor 1-5 includes a first reaction chamber 1, a second reaction chamber 2, a third reaction chamber 3, a fourth reaction chamber 4, and a fifth reaction chamber 5 arranged coaxially. The first reaction chamber 1, the second reaction chamber 2, and the third reaction chamber 3 are arranged sequentially from top to bottom. The lower port of the first reaction chamber is not higher than the upper port of the second reaction chamber. The lower port of the second reaction chamber is not higher than the upper port of the third reaction chamber. The fourth reaction chamber 4 is located outside the junction of the first reaction chamber 1 and the second reaction chamber 2, and connects the first reaction chamber 1 and the second reaction chamber 2 into one unit. The fifth reaction chamber 5 is located outside the junction of the second reaction chamber 2 and the third reaction chamber 3, and connects the second reaction chamber 2 and the third reaction chamber 3 into one unit.

[0048] The first reaction chamber 1 is provided with a first solid bed material inlet 1-3 and a first solid fuel inlet 1-4; the fourth reaction chamber 4 is provided with a second solid bed material inlet 4-1 and a second solid fuel inlet 4-2; and the fifth reaction chamber is provided with a third solid fuel inlet 5-1.

[0049] The first reaction chamber 1 is further provided with a first air inlet 1-5, located in the middle of the side of the first reaction chamber 1; the second reaction chamber 2 is provided with a second air inlet 2-3, located in the middle of the side of the second reaction chamber 2; the third reaction chamber 3 is provided with a third air inlet 3-3, located in the middle of the side of the third reaction chamber 3; the bottom of the fourth reaction chamber 4 is further provided with a fourth air inlet 4-6 and a gas distribution plate A4-7, with the fourth air inlet 4-6 located below the gas distribution plate A4-7; the bottom of the fifth reaction chamber 5 is further provided with a fifth air inlet 5-5 and a gas distribution plate B5-6, with the fifth air inlet 5-5 located below the gas distribution plate B5-6.

[0050] The bottom of the third reaction chamber 3 is also provided with a first solid discharge port 3-4; the middle of the fourth reaction chamber 4 is also provided with a second upper solid discharge port 4-4 and a second lower solid discharge port 4-5, wherein the second upper solid discharge port 4-4 is located above the top of the upper section 2-1 of the second reaction chamber, and the second lower solid discharge port 4-5 is located below the top of the upper section 2-1 of the second reaction chamber. The middle of the fifth reaction chamber 5 is also provided with a third upper solid discharge port 5-3 and a third lower solid discharge port 5-4, wherein the third upper solid discharge port 5-3 is located above the upper port of the upper section 3-1 of the third reaction chamber, and the third lower solid discharge port 5-4 is located below the upper port of the upper section 3-1 of the third reaction chamber.

[0051] The first reaction chamber 1 is also provided with a first air outlet 1-6, located on the upper side of the first reaction chamber; the fourth reaction chamber 4 is also provided with a second air outlet 4-3, located at the top of the fourth reaction chamber; the fifth reaction chamber 5 is also provided with a third air outlet 5-2, located at the top of the fifth reaction chamber.

[0052] The upper section 1-1 of the first reaction chamber is also provided with a solid mixing internal component 1-7.

[0053] The first reaction chamber is also equipped with a solid material level control internal component 1-8, located between the first air inlet 1-5 and the first air outlet 1-6.

[0054] A vertical baffle 4-8 is provided between the fourth reaction chamber 4 and the upper section 2-1 of the second reaction chamber, dividing the fourth reaction chamber 4 into two parts, an inner and an outer part, which are isolated at the top and have a gap at the bottom.

[0055] The thermal conversion device is connected as follows: the outlet of the lifting reactor 6 is connected to the inlet of the particle classifier 7; the two particle material outlets of the particle classifier 7 are respectively connected to the first solid bed material inlet 1-3 and the second solid bed material inlet 4-1 of the multifunctional reactor through valves; the inlet of the lifting reactor 6 is respectively connected to the first solid discharge outlet 3-4 and the third solid upper discharge outlet 5-3 of the multifunctional reactor through valves.

[0056] The raw material analysis of the solid carbon-containing fuels in the following five embodiments is shown in Table 1.

[0057] Table 1. Raw material analysis of solid carbon fuels

[0058]

[0059]

[0060] Example 1 (e.g.) Figure 2 As shown, Mode 1):

[0061] Open return valve B9-1 and close return valve A8-1. The first, second, and third reaction chambers employ a moving bed mode, while the fourth reaction chamber employs a sandwich bed mode, achieving hydrogen production through a combination of biomass sandwich bed gasification and moving bed decoupled adsorption-enhanced gasification.

[0062] The first solid bed material is calcium carbonate at 750℃, and the first solid fuel is semi-coke from pine sawdust at room temperature. Both have a particle size of 0.4mm to 0.8mm, and their feed rates are 4kg / h and 0.5kg / h, respectively. Calcium carbonate and semi-coke enter the first reaction chamber 1 through the first solid bed material inlet 1-3 and the first solid fuel inlet 1-4, respectively, and are rapidly mixed and heat-exchanged after passing through the solid mixing internal component 1-7. The first gaseous feedstock is hot air at 600℃, which enters through the first air inlet 1-5 at a rate of 6kg / h and flows counter-currently through the lower section 1-2 of the first reaction chamber. The discharge rate of the first solid discharge outlet 3-4 is controlled by the solid material level control internal component 1-8 to ensure that the lower section 1-2 of the first reaction chamber is filled with material, and the material level is not higher than the first air outlet 1-6. In the first reaction chamber 1, the semi-coke undergoes a combustion reaction, raising the temperature to 850℃. At this temperature, calcium carbonate decomposes into calcium oxide and CO2. Calcium oxide enters the second reaction chamber 2, while CO2 and combustion flue gas are discharged from the first outlet 1-6 as the first gas products.

[0063] The second solid fuel is pine wood chips with a particle size of less than 0.4 mm, fed at a rate of 0.1 kg / h to 0.2 kg / h.

[0064] Carried by the second gaseous feedstock, water vapor, it enters the fourth reaction chamber 4 through the second solid fuel inlet 4-2, where it undergoes gasification at 800℃, generating syngas, semi-coke, and a small amount of tar. The syngas passes through the upper section of the second reaction chamber's stacked surface and then flows through the second reaction chamber 2 in a gas-solid co-current manner. In the upper section 2-1 of the second reaction chamber, the tar carried by the syngas decomposes under the action of high-temperature calcium oxide, while the entrained semi-coke is further gasified under the action of water vapor, increasing the syngas yield.

[0065] The third gaseous feedstock, 300°C steam, enters from the second inlet 2-3 at a rate of 0.3 kg / h, flowing along with the syngas in a gas-solid co-current stream through the lower section 2-2 of the second reaction chamber. In the lower section 2-2, at 500°C, a water-gas shift reaction and the carbonation of calcium oxide occur, producing the second gaseous product hydrogen, as well as calcium carbonate and calcium hydroxide. The hydrogen enters the fifth reaction chamber from the upper surface of the third reaction chamber and exits from the third outlet 5-2; its composition analysis is shown in Table 2. Calcium carbonate and calcium hydroxide exit from the first solid discharge outlet 3-4, and after passing through the lifting reactor 6 and the particle classifier 7, return to the first reaction chamber 1.

[0066] Table 2 Data on CaO adsorption-enhanced gasification hydrogen production

[0067]

[0068] Example 2 (e.g.) Figure 3 As shown, Mode 2):

[0069] Open return valve B9-1 and close return valve A8-1. The first, second, and third reaction chambers adopt a moving bed mode, and the fourth reaction chamber adopts a fluidized bed mode to achieve chemical loop hydrogen production.

[0070] The first solid bed material is high-temperature hematite with a particle size of 0.4mm to 0.8mm, which is added from the first solid bed material inlet 1-3 at a feeding rate of 4kg / h. The discharge rate of the first solid discharge outlet 3-4 is controlled by the solid material level control internal component 1-7 so that the lower section 1-2 of the first reaction chamber is not filled with material but the material level is higher than the first air inlet 1-5.

[0071] The first solid fuel is pine sawdust with a particle size of 5-10 mm, which enters the fourth reaction chamber 4 from the second solid fuel inlet 4-2 at a feed rate of 0.5 kg / h. The first gaseous feedstock recirculation tail gas (600℃) enters the fourth reaction chamber 4 from the fourth inlet 4-6 via the gas distribution plate A4-7 as fluidizing gas. Pine sawdust pyrolysis occurs, generating volatiles and semi-coke. The semi-coke after reaction is discharged through the second solid lower outlet 4-5, and the volatiles pass through the upper accumulation surface of the third reaction chamber in a gas-solid countercurrent manner through the first reaction chamber 1. In the first reaction chamber 1, the volatiles react with high-temperature hematite at 800℃ to generate tail gas and reduced hematite. Part of the heat in the tail gas is recovered and extracted as the first gaseous product, and part is recycled back to the fourth reaction chamber 4 as fluidizing gas and gaseous heat carrier. The reduced hematite enters the third reaction chamber 3 via the second reaction chamber 2.

[0072] The second gaseous feedstock, water vapor, enters from the third inlet 3-3 at a rate of 0.5 kg / h and flows counter-currently through the third reaction chamber 3. At 600℃, it undergoes a water cracking reaction, producing hydrogen and Fe3O4. Hydrogen, as the second gaseous product, passes through the upper section of the third reaction chamber's stacked surface into the fifth reaction chamber and is extracted from the third outlet 5-2. The analysis results are shown in Table 3. Fe3O4 is extracted from the first solid discharge outlet 3-4, passes through the lifting reactor 6 and the particle classifier 7, and then returns to the first reaction chamber 1.

[0073] Table 3 Data on hydrogen production via chemical chaining

[0074]

[0075] Example 3 (e.g.) Figure 4 As shown, Mode 3):

[0076] Close return valves A8-1 and B9-1. The first, second, and third reaction chambers adopt a moving bed mode, while the fifth reaction chamber adopts a conveyor bed mode, realizing the production of high-quality oil and syngas through biomass fluidized bed gasification coupled with coal moving bed pyrolysis.

[0077] The first solid fuel is Yuyang coal with a particle size of 6-13mm, which is added from the first solid fuel inlet 1-4 at a feeding rate of 1.0kg / h and extracted from the first solid discharge outlet 3-4. A moving bed with a certain porosity is formed in the first, second and third reaction chambers. The discharge rate of the first solid discharge outlet 3-4 is controlled by the solid material level control internal component 1-8, so that the material fills the lower section 1-2 of the first reaction chamber and the material level is not higher than the first gas outlet 1-6; and two accumulation surfaces are formed at the upper section 2-1 of the second reaction chamber and the upper section 3-1 of the third reaction chamber, respectively.

[0078] The second solid fuel, pine sawdust with a particle size of less than 0.4 mm, is fed at a rate of 1.5 kg / h and carried by the first gaseous feedstock, water vapor, at a rate of 0.25 kg / h into the fifth reaction chamber through the third solid fuel inlet 5-1. In the fifth reaction chamber, the pine sawdust gasifies, producing syngas and semi-coke at 800℃. The syngas, carrying the semi-coke, passes through the stack surface in a counter-current flow through the second reaction chamber 2, where the semi-coke is retained by the Yuyang coal bed. In the second reaction chamber 2, the Yuyang coal, under the influence of the syngas atmosphere and its heat, reaches a temperature of 400-500℃ and undergoes pyrolysis. The gaseous products enter the fourth reaction chamber through the upper stack surface of the second reaction chamber and are then extracted from the second outlet 4-2. After condensation and separation, high-calorific-value syngas and high-yield tar are obtained. The pine sawdust gasified semi-coke and the Yuyang coal pyrolysis semi-coke are extracted together from the first outlet 3-4. The analysis of the light tar is shown in Table 4.

[0079] Table 4 Data on the production of high-quality oil and gas through gasification coupled pyrolysis

[0080]

[0081] Example 4 (e.g.) Figure 5 As shown, Mode 4):

[0082] Open return valve B9-1 and close return valve A8-1. The first, second, and third reaction chambers adopt a moving bed mode, and the fifth reaction chamber adopts a fluidized bed mode, realizing the production of high-quality oil and syngas through biomass fluidized bed pyrolysis and moving bed catalytic upgrading.

[0083] The first solid bed material is hematite with a particle size of 6-10 mm, which is added from the first solid bed material inlet 1-3 at a feeding rate of 3.0 kg / h and extracted from the first solid discharge outlet 3-4. A moving bed layer with a certain porosity is formed in the first, second and third reaction chambers. The discharge rate of the first solid discharge outlet 3-4 is controlled by the solid material level control internal component 1-8, so that the material fills the lower section 1-2 of the first reaction chamber and the material level is not higher than the first gas outlet 1-6; and two accumulation surfaces are formed at the upper section 2-1 of the second reaction chamber and the upper section 3-1 of the third reaction chamber, respectively.

[0084] The first solid fuel is pine sawdust with a particle size of less than 6 mm, which enters the fifth reaction chamber 5 from the third solid fuel inlet 5-1 at a feeding rate of 2.0 kg / h. The first gaseous feedstock recirculation gas enters the fifth reaction chamber 5 from the fifth gas inlet 5-5 via the gas distribution plate B5-6 as fluidizing gas and reaction gas, and is fed at a feeding rate of 0.65 kg / h. Pyrolysis of the pine sawdust occurs in the fifth reaction chamber 5, generating volatiles and semi-coke at 550℃. The semi-coke is discharged through the third solid fuel lower outlet 5-4, while the volatiles pass through the upper accumulation surface of the third reaction chamber and pass through the second reaction chamber 2 in a gas-solid countercurrent manner. In the second reaction chamber 2, at 400℃, a deoxygenation reaction of volatile tar and a secondary reaction of heavy tar occur. A granular bed formed by solid bed material captures dust carried by the volatiles. The clean volatiles, after catalytic reforming, enter the fourth reaction chamber through the upper section of the second reaction chamber and are then extracted from the second outlet 4-3. After condensation and separation, high-calorific-value pyrolysis gas and upgraded tar are obtained. The analysis of the light tar is shown in Table 5. The catalyst after the reaction returns to the first reaction chamber 1 after passing through the lifting reactor 6 and the particle classifier 7.

[0085] Table 5 Data on pyrolysis + catalytic upgrading

[0086]

[0087] Example 5 (e.g.) Figure 6 As shown, mode 5):

[0088] Open return valve A8-1 and close return valve B9-1. Both the fourth and fifth reaction chambers are in fluidized bed mode, enabling two-step chemical looping gasification to produce syngas with different H2 / CO ratios.

[0089] The first solid bed material is high-temperature calcium ferrite with a particle size of 0.4 mm to 0.8 mm, and the first solid fuel is pine sawdust with a particle size of 5 to 10 mm. Their feed rates are 4 kg / h and 0.1 kg / h, respectively. The high-temperature calcium ferrite and pine sawdust enter the fourth reaction chamber 4 through the second solid bed material inlet 4-1 and the second solid fuel inlet 4-2, respectively. The first gaseous feedstock circulating gas enters the fourth reaction chamber 4 through the fourth air inlet 4-6 and the gas distribution plate A4-7 at a feed rate of 0.6 kg / h. The calcium ferrite, at a temperature of 900℃, mixes with the pine sawdust, causing the pine sawdust to undergo a pyrolysis reaction, producing volatiles and semi-coke.

[0090] Due to the action of baffles 4-8, volatiles pass downward through the calcium ferrite bed. During this process, the volatiles react with the high-temperature calcium ferrite, reducing it to deoxygenated calcium ferrite, which itself is converted into the first syngas with a low H2 / CO ratio. The first syngas separates from the deoxygenated calcium ferrite in the upper section of the second reaction chamber and is extracted upward along the first reaction chamber from the first outlet 1-6 as the first gas product. The deoxygenated calcium ferrite and semi-coke overflow into the upper section 2-1 of the second reaction chamber, forming a material layer of a certain height in the lower section 2-2 of the second reaction chamber.

[0091] The third inlet 3-3 introduces circulating gas as loosening gas and return gas, allowing deoxidized calcium ferrite and semi-coke to enter the fifth reaction chamber 5. The second reaction feedstock, water vapor, is fed into the fifth reaction chamber 5 from the fifth inlet 5-5 via the gas distribution plate B5-6 at a feed rate of 0.1 kg / h. At 750℃, deoxidation of the semi-coke occurs, generating second syngas, calcium ferrite, and ash. The second syngas is collected as the second gaseous product from the third outlet 5-2, while calcium ferrite and ash are collected from the third solids outlet 5-3. Calcium ferrite is returned to the first reaction chamber 1 after passing through the lifting reactor 6 and the particle classifier 7. The analysis results of the first and second syngas are shown in Table 6.

[0092] Table 6 Results of decoupled chemical looping gasification

[0093]

Claims

1. A multifunctional thermal conversion device for solid carbon-containing fuels, characterized in that, The aforementioned multifunctional thermal conversion device for solid carbon fuel includes a multifunctional reactor, a lifting reactor, and a particle classifier. The multifunctional reactor includes a first, second, third, fourth, and fifth reaction chambers arranged coaxially. The first, second, and third reaction chambers are arranged sequentially from top to bottom. The lower port of the first reaction chamber is not higher than the upper port of the second reaction chamber. The lower port of the second reaction chamber is not higher than the upper port of the third reaction chamber. The fourth reaction chamber is located outside the junction of the first and second reaction chambers, connecting them as a single unit. The fifth reaction chamber is located outside the junction of the second and third reaction chambers, connecting them as a single unit. The first reaction chamber is provided with an adjacent first solid bed material inlet and a first solid fuel inlet, located at the top of the first reaction chamber; the fourth reaction chamber is provided with an adjacent second solid bed material inlet and a second solid fuel inlet, located on the upper side of the fourth reaction chamber; the fifth reaction chamber is provided with a third solid fuel inlet, located on the upper side of the fifth reaction chamber. The first reaction chamber is further provided with a first air inlet, located in the middle of the side of the first reaction chamber; the second reaction chamber is provided with a second air inlet, located in the middle of the side of the second reaction chamber; the third reaction chamber is provided with a third air inlet, located in the middle of the side of the third reaction chamber; the bottom of the fourth reaction chamber is further provided with a fourth air inlet and a gas distribution plate, the fourth air inlet being located below the gas distribution plate; the bottom of the fifth reaction chamber is further provided with a fifth air inlet and a gas distribution plate, the fifth air inlet being located below the gas distribution plate. The bottom of the third reaction chamber is also provided with a first solid discharge port; the middle side of the fourth reaction chamber is also provided with a second upper solid discharge port and a second lower solid discharge port, wherein the position of the second upper solid discharge port is higher than the top of the upper section of the second reaction chamber, and the position of the second lower solid discharge port is lower than the top of the upper section of the second reaction chamber; the middle side of the fifth reaction chamber is also provided with a third upper solid discharge port and a third lower solid discharge port, wherein the position of the third upper solid discharge port is higher than the top of the upper section of the third reaction chamber, and the position of the third lower solid discharge port is lower than the top of the upper section of the third reaction chamber. The first reaction chamber is also provided with a first air outlet, located on the upper side of the first reaction chamber; the fourth reaction chamber is also provided with a second air outlet, located at the top of the fourth reaction chamber; the fifth reaction chamber is also provided with a third air outlet, located at the top of the fifth reaction chamber. The upper section of the first reaction chamber is also equipped with a solid mixing internal component for rapid mixing of solid bed material and solid fuel; The first reaction chamber is also equipped with a solid material level control internal component, located between the first air inlet and the first air outlet, for detecting the material level and controlling the discharge rate of solid materials; The thermal conversion device is connected as follows: the outlet of the lifting reactor is connected to the inlet of the particle classifier; the two particle material outlets of the particle classifier are respectively connected to the first solid bed material inlet and the second solid bed material inlet of the multifunctional reactor through valves; the inlet of the lifting reactor is respectively connected to the first solid discharge outlet and the third solid discharge outlet of the multifunctional reactor through valves.

2. The multifunctional thermal conversion device for solid carbon-containing fuels according to claim 1, characterized in that, The second solid fuel inlet is tangentially arranged along the wall of the fourth reaction chamber; the third solid fuel inlet is tangentially arranged along the wall of the fifth reaction chamber.

3. A multifunctional thermal conversion device for solid carbon-containing fuels according to claim 1 or 2, characterized in that, The first reaction chamber includes an upper section and a lower section, wherein the diameter of the upper section is larger than the diameter of the lower section; the second reaction chamber includes an upper section and a lower section, wherein the diameter of the upper section is larger than the diameter of the lower section; the third reaction chamber includes an upper section and a lower section, wherein the diameter of the upper section is larger than the diameter of the lower section.

4. A multifunctional thermal conversion device for solid carbon-containing fuels according to claim 1 or 2, characterized in that, The diameter of the fourth reaction chamber is greater than the diameter of the upper section of the second reaction chamber, and the height of the fourth reaction chamber is greater than the height of the upper section of the second reaction chamber.

5. A multifunctional thermal conversion device for solid carbon-containing fuels according to claim 1 or 2, characterized in that, The diameter of the fifth reaction chamber is greater than the diameter of the upper section of the third reaction chamber, and the height of the fifth reaction chamber is greater than the height of the upper section of the third reaction chamber.

6. A multifunctional thermal conversion device for solid carbon-containing fuels according to claim 1 or 2, characterized in that, A vertical baffle is provided between the fourth reaction chamber and the upper section of the second reaction chamber, dividing the fourth reaction chamber into two parts, an inner and an outer part, which are isolated at the top and have a gap at the bottom; the height of the gap is less than the height of the upper section of the second reaction chamber.

7. A multifunctional thermal conversion method for solid carbon-containing fuels, using the apparatus described in any one of claims 1-6, characterized in that, The first, second, and third reaction chambers adopt a moving bed mode, while the fourth and fifth reaction chambers adopt a fluidized bed or entrained bed mode. Five different modes are achieved through the combination of different reaction chambers: (I) Mode 1: The first solid fuel and the first solid bed material enter from the first solid fuel inlet and the first solid bed material inlet, respectively. After being mixed at the solid mixing internal component, they enter the lower section of the first reaction chamber. The first gaseous raw material enters the lower section of the first reaction chamber from the first air inlet. The gas and solid flow counter-currently upwards and contacts the first solid fuel, and a reaction occurs. The first gaseous product generated by the reaction is collected from the first air outlet. The first solid product generated by the reaction enters the second reaction chamber together with the first solid bed material. The second gaseous raw material carries the second solid fuel from the second solid fuel inlet into the fourth reaction chamber, where a bed pyrolysis-gasification reaction occurs to generate gas and second solid products. The gas generated by the reaction merges with the third gaseous raw material entering from the second air inlet. Together, the gas and solid flow co-currently through the second reaction chamber and react to generate the second gaseous product, which is discharged from the third air outlet. The second solid product enters the second reaction chamber and combines with the first solid product to form a solid product. The solid product and the first solid bed material are collected together from the first solid outlet. The first solid bed material is recycled back to the first reaction chamber after being lifted and classified into particles. (II) Mode 2: The first solid bed material enters the first, second, and third reaction chambers sequentially from the first solid bed material inlet to form a moving bed with a certain porosity; the first solid fuel enters the fourth reaction chamber from the second solid fuel inlet, and the first gaseous feedstock enters the fourth reaction chamber from the fourth inlet via a gas distribution plate as fluidizing gas and reaction gas; the first solid fuel undergoes fluidized bed pyrolysis-gasification reaction with the gaseous feedstock in the fourth reaction chamber to generate gas and the first solid product; the gas and solid react countercurrently through the first reaction chamber to react with the first solid bed material, generating the first gaseous product which is discharged from the first outlet, and the reacted first solid bed material enters the third reaction chamber; the first solid product is discharged from the second solid bottom outlet; in the third reaction chamber, the first solid bed material comes into countercurrent contact with the second gaseous feedstock entering from the third inlet and reacts further to generate the second gaseous product which is collected from the third outlet; the further reacted first solid bed material is collected from the first solid outlet, and after being lifted and particle classified, it is recycled back to the first reaction chamber; (III) Mode 3: The first solid fuel enters the first, second and third reaction chambers from the first solid fuel inlet to form a moving bed with a certain porosity; the first gaseous feedstock carries the second solid fuel from the third solid fuel inlet to the fifth reaction chamber, where a pyrolysis-gasification reaction occurs to generate gaseous and second solid products; the gas passes through the second reaction chamber and comes into contact with the first solid fuel and reacts to generate a first gaseous product and a first solid product; the first gaseous product is discharged from the second gas outlet; the first solid product and the second solid product are combined into a solid product, which enters the third reaction chamber together and is collected from the first solid outlet. (iv) Mode 4: The first solid bed material enters the first, second and third reaction chambers from the first solid bed material inlet to form a moving bed with a certain porosity; the first solid fuel enters the fifth reaction chamber from the third solid fuel inlet; the first gaseous raw material enters the fifth reaction chamber from the fifth gas inlet through the gas distribution plate as fluidizing gas and reaction gas; the first solid fuel undergoes fluidized bed pyrolysis-gasification reaction with the gaseous raw material in the fifth reaction chamber to generate gas and the first solid product; the gas and solid flow countercurrently through the second reaction chamber to contact and react with the first solid bed material to generate the first gaseous product and discharge from the second gas outlet; the first solid product is discharged from the third solid lower outlet; the reacted first solid bed material is collected from the first solid outlet and enters the lifting reactor and particle classifier, and after heating, lifting and separation, it re-enters the first reaction chamber to start a new cycle; (V) Mode 5: The first solid bed material and the first solid fuel enter the fourth reaction chamber from the second solid bed material inlet and the second solid fuel inlet, respectively. The first gaseous raw material enters the fourth reaction chamber from the fourth inlet through the gas distribution plate as fluidizing gas and reaction gas. The first solid fuel undergoes fluidized bed pyrolysis-gasification reaction with the gaseous raw material in the fourth reaction chamber to generate the first gaseous product and the first solid product. The first gaseous product passes through the first reaction chamber and is discharged from the first outlet. The first solid product and the first solid bed material overflow into the upper section of the second reaction chamber, forming a material layer of a certain height in the second reaction chamber, which serves as a gas seal. Function: The second gaseous feedstock enters the third reaction chamber through the third inlet, serving as a loosening gas and return gas, allowing the first solid product and the first solid bed material in the second reaction chamber to enter the fifth reaction chamber; the third gaseous feedstock enters the fifth reaction chamber through the fifth inlet via the gas distribution plate, where it further reacts with the first solid product and the first solid bed material in the fifth reaction chamber, generating a second gaseous product which is then collected from the third outlet; the reacted first solid bed material and the first solid product are collected from the third solid top outlet; the first solid bed material, after being lifted, heated, and separated, then enters the fourth reaction chamber to begin a new cycle.

8. The multifunctional thermal conversion method for solid carbon-containing fuels according to claim 7, characterized in that, When the particle size of the solid bed material and solid fuel is ≤0.5mm, the second solid bed material inlet, the second solid fuel inlet, or the third solid bed material inlet and the third solid fuel inlet shall be selected for feeding; when the particle size of the solid bed material and solid fuel is ≥4 mm and ≤13 mm, the first solid bed material inlet and the first solid fuel inlet shall be selected for feeding.

9. A multifunctional thermal conversion method for solid carbon-containing fuels according to claim 7 or 8, characterized in that, The first solid fuel and the second solid fuel are both one or more of the following: low-rank coal, biomass, petroleum coke, coke, charcoal, plastics, rubber, and asphalt.

10. A multifunctional thermal conversion method for solid carbon-containing fuels according to claim 7 or 8, characterized in that, The first solid bed material and the second solid bed material are both one or more of inert bed materials and active bed materials; the inert bed material is one or more of quartz sand, river sand, and ceramic particles.

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