Gas-solid reactor capable of online enhancement of reaction activity of solid

Abstract

A gas-solid reactor capable of online enhancement of the reaction activity of solid. The gas-solid reactor comprises an inner reactor cylinder (10), which is divided into an activation section (11) an

Description

Gas-solid reaction is a widely used type of reaction in reality, such as flue gas purification, reactions between catalysts and gases, gasification of solid powders, combustion reactions, reforming reactions, and so on. The reactors currently used for gas-solid reactions include fixed beds, fluidized beds, moving beds, etc. For solid particle combustion, the task of the reactor is to ensure good gas-solid contact and complete target reaction, without considering changing the performance of the solid particles. However, there is a type of gas-solid reaction that produces combustible gases, such as the reforming reaction between volatile matter and catalyst, and the gasification reaction of char powder. The high calorific value and suitable composition of the combustible gas produced are required. In addition, the reactor needs to be sealed and not leak, otherwise it may cause a fire. Importantly, gas-solid reactors also need to maintain the reactivity of solids, and deactivated solid particles need to be replaced in a timely manner. The existing fixed bed reactors are suitable for non industrial gasification reactions, combustion reactions, and catalyst reactions, but they cannot guarantee the activity of solid catalysts, and replacement is particularly troublesome. For example, in Fischer Tropsch synthesis, the fixed bed for catalyst formation needs to be cooled carefully and must be completely replaced after a certain period of use, which cannot maintain the activity of the catalyst. For example, fluidized beds are suitable for gasification reactions, combustion reactions, and catalyst reactions, but they suffer from severe abrasion and erosion and cannot maintain the activity of the catalyst. A moving bed reactor is expected to maintain catalytic activity during the reaction process, but traditional moving bed reactors are difficult to achieve organized direct gas-solid contact, and the activity and consumption of solid particles cannot be precisely controlled. In addition, the existing fixed bed reactors also have the problems of complex heat exchanger heating and high equipment maintenance requirements. SUMMARY The present invention is made to solve the above-mentioned problems, with the aim of providing a gas-solid reactor capable of online enhancement of the reaction activity of solid particles. The present invention provides a gas-solid reactor capable of online enhancement of the reaction activity of solid particles, the gas-solid reactor comprising: an inner reactor cylinder, divided into an activation section and a reaction section;a solid particle feeding device, connected to a head end of the activation section, for feeding solid particles used as reaction materials or catalysts; a reaction gas feeding device,connected to a head or tail end of the activation section, for feeding reaction gas; a high-temperature gas flow feeding device, for feeding high-temperature gas flow to activate the solid particles in the activation section; a gas product output device, connected to a tail end of the reaction section, for outputting the gas product after the reaction between the solid particles and the reaction gas; a heat supply system, located outside the reaction section, for supplying the heat source required by the reaction section, and for heating and maintaining the solid particles and the reaction gas inside the reaction section 12 from the outside through the heat source;and a solid particle discharging device, connected to a tail end of the reaction section, for cooling and discharging solid particles after the reaction, the length of the activation section 11 is LI, the length of the reaction section 12 is L2, and the length ratio of the activation section 11 and the reaction section 12 is Ll / L2=0.35 to 0.5, the outer side of the activation section 11 and the outer side of the reaction section 12 are separated by a thermal insulation layer made of insulation material. In the gas-solid reactor, the reactor inner cylinder is horizontally divided into the activation section and the reaction section, and the high-temperature gas flow feeding device is set at the bottom of the activation section, for feeding high-temperature gas flow from the bottom to activate the solid particles inside the activation section. In the gas-solid reactor, the reactor inner cylinder is a rotary kiln, the solid particles are driven forward by the rotation of the reactor inner cylinder inside the reactor inner cylinder. In the gas-solid reactor, the reactor is equipped with a solid particle pushing device, including spiral blades set in the reactor inner cylinder and a motor driving the rotation of the spiral blades; and the solid particles are pushed forward by the solid particle pushing device inside the reactor inner cylinder. In the gas-solid reactor, a cylinder wall of the activation section is uniformly perforated with pores, the size of the pores is 0.35 to 0.7 times the average size of the solid particles, and the porosity is 15% to 25%. In the gas-solid reactor, an angle between the pavement of the solid particles and an axis in the activation section 11 is a, a>90°. In the gas-solid reactor, an angle between an entering cambered surface of the high-temperature gas flow and an axis in the activation section is P, P=30° to 45°, and pores on the outer circumference of the entering cambered surface of the high-temperature gas flow are covered by an insulation layer. In the gas-solid reactor, the solid particle feeding device is a spiral feeder, a chute feeder, or a star feeder with a discharge hopper. In the gas-solid reactor, the heat supply system is a heating jacket, and has a heating gas flow inlet and a heating gas flow outlet, and the heating gas flow circulates inside. In the gas-solid reactor, the top of the tail end of reaction section is equipped with a gas product discharge outlet connected to gas product outlet device, and a particle blocking device is installed at the gas product discharge outlet to prevent solid particles from being carried into the product gas flow. In the gas-solid reactor, the solid particle discharge device is a spiral discharge machine equipped with a water-cooled jacket, or a rotary cooling cylinder equipped with a water-cooled or air-cooled jacket. Technical effects of the invention The present invention provides a gas-solid reactor capable of online enhancement of the reaction activity of solid particles. The gas-solid reactor comprises an inner reactor cylinder, which is divided into an activation section and a reaction section, wherein a solid particle feeding device, a reaction gas feeding device and a high-temperature gas flow feeding device are connected to the activation section; and a gas product output device, a heat supply system and a solid particle discharging device are connected to the reaction section. Solid particles fed into the activation section come into contact with a high-temperature gas flow fed from the bottom first and are activated, thus improving the reaction activity; then, the solid particles come into contact with a reaction gas to start a reaction. This gas-solid reactor is capable of online activation treatment of solid particles, utilizing the role of solid particles to promote chemical reactions between gas and solid, resulting in high-quality gas product and effectively improving the value of the final product, thereby enhancing the efficiency of the reactor. Greatly saves external energy while effectively solving some problems encountered in gas-solid reactions in practice. Organized contact between solid particles and reaction gases has been achieved, with controllable activity and consumption of solid particles, reducing equipment maintenance requirements and further lowering comprehensive processing costs. BRIEF DESCRIPTION OF THE DRAWINGS Fig. 1 is a schematic diagram of the structure of a gas-solid reactor capable of online enhancement of the reaction activity of solid particles in Example 1 of the present invention. Fig. 2 is a sectional view of Figure 1 at the activation section of the inner reactor cylinder. Fig. 3 is a schematic diagram of the distribution of pores and internal solid particles in the activation section of Example 1 of the present invention, as well as the angle of entry of high-temperature gas flow. Fig. 4 is a schematic diagram of the structure of a gas-solid reactor capable of online enhancement of the reaction activity of solid particles in Example 2 of the present invention. Fig. 5 is a schematic diagram of the structure of a gas-solid reactor capable of online enhancement of the reaction activity of solid particles in Example 6 of the present invention. Symbol description in the diagrams: 1 solid particle, 2 conveyor belt, 3 silo, 10 inner reactor cylinder, 11 activation section, 111 pore, 12 reaction section, 20 solid particle feeding device, 30 reaction gas feeding device, 40 high-temperature gas flow feeding device, 50 gas product output device, 60 heat supply system, 61 heating gas flow inlet, 62 heating gas flow outlet, 70 solid particle discharging device, 80 insulation layer, 90 solid particle pushing device, 91 spiral blades, 92 motor. DETAILED DESCRIPTION In order to make the technical means, creative features, objectives, and effects of the present invention easy to understand and comprehend, the following examples, combined with the drawings, provide a specific explanation of the present invention. Example 1 Fig. 1 is a schematic diagram of the structure of a gas-solid reactor capable of online enhancement of the reaction activity. As shown in Fig. 1, this example provides a gas-solid reactor capable of online enhancement of the reaction activity of solid particles, comprising:an inner reactor cylinder 10, a solid particle feeding device 20, a reaction gas feeding device 30, a high-temperature gas flow feeding device 40, a gas product output device 50, a heat supply system 60, and a solid particle discharging device 70. The inner reactor cylinder 10 is horizontally arranged and divided into an activation section 11 and a reaction section 12 along the head to tail direction. The length of activation section 11 is LI, and the length of reaction section 12 is L2. The length ratio of activation section 11 to reaction section 12 is Ll / L2=0.35 to 0.5. The activation section 11 is connected to the solid particle feeding device 20, the reaction gas feeding device 30, and the high-temperature gas flow feeding device 40. The reaction section 12 is connected to the product gas output device 50, the heat supply system 60, and heat supply system 60. The outer side of the activation section 11 and the outer side of the reaction section 12 are separated by a insulation layer 80 made of insulation material. Pores on the outer circumference of the entering cambered surface of the high-temperature gas flow inside the activation section 11 are covered by an insulation layer 80. Fig. 2 is a sectional view of Figure 1 at the activation section 11 of the inner reactor cylinder 10. As shown in Fig. 1 and Fig. 2, the solid particle feeding device 20 is connected to the solid particle feeding inlet at the head end of the activation section 11, for feeding solid particles 1 used as reaction materials or catalysts. The solid particle feeding device 20 is a spiral feeder or a chute feeder. The reaction gas feeding device 30 is connected to the reaction gas feeding inlet at the head or tail end of the activation section 11, for feeding reaction gas, and the gas is a physical state that can be a mixture of permanent gases and condensates. The reaction gas feeding device 30 is set at the bottom of the activation section 11, for feeding high-temperature gas flow from the bottom to activate the solid particles inside the activation section 11. Due to the presence of an insulation layer 80, the high-temperature gas flow supplied to activation section 11 will not enter the outside of reaction section 12. A cylinder wall of the activation section 11 is uniformly perforated with poresill (see Fig. 3) for high-temperature gas to enter. The size of the pores 111 is 0.35 to 0.7 times the average size of the solid particles 1, and the shape is designed to prevent solid particles 1 from leaking out of the pores. The porosity (i.e. pore area / total area of the cylinder wall of the activation section) is 15% to 25%. The gas product output device 50 is connected to a gas product discharge outlet at the tail end of the reaction section 12, for outputting the gas product after the reaction between the solid particles 1 and the reaction gas. A particle blocking device is installed at the gas product discharge outlet to prevent the solid particles 1 from being carried into the product gas flow. The gas product output device 50 can be an exhaust fan. The heat supply system 60 is located outside the reaction section 12, for supplying the heat source required by the reaction section 12, and for heating and maintaining the solid particles 1 and the reaction gas inside the reaction section 12 from the outside through the heat source. The heat supply system 60 can be a heating jacket with a heating gas flow inlet 61 and a heating gas flow outlet 62, and the heating gas flow circulates inside the heating jacket. The solid particle discharging device70 is connected to a solid particle discharge outlet at the tail end of the reaction section 12, for cooling and discharging the solid particles 1 after the reaction. The solid particle discharge device 70 can be a spiral discharge machine equipped with a water-cooled jacket, or a rotary cooling cylinder equipped with a water-cooled or air-cooled jacket. By adjusting the discharge position of the solid particle discharge device 70, the thickness of the layer of the solid particles 1 in the reaction section 12 can be adjusted to make the gas-solid contact in the reaction section 12 more complete and the reaction more thorough. For the inner reactor cylinder 10, the diameter of the activation section 11 can be equal to or greater than the diameter of the reaction section 12. The diameter of reaction section 12 can decrease along the direction from the head to the tail, resulting in a greater accumulation of the solid particles 1 in this section, thereby enhancing the contact between the solid particles 1 and the reaction gas. A plate can also be installed in reaction section 12, which can make the mixing of the solid particles 1 and reaction gas more uniform and the contact more thorough. In this example, the solid particles 1 are driven forward by the rotation of the inner reactor cylinder 10 inside the inner reactor cylinder 10. The movement rate of the solid particles 1 in the activation section 11 and the reaction section 12 can be consistent or inconsistent. Fig. 3 is a schematic diagram of the distribution of pores 111 and internal solid particles 1 in the activation section 11, as well as the angle of entry of high-temperature gas flow. As shown in Fig. 3, in the activation section 11, the angle between the pavement of the solid particles 1 and the axis is a, a>90°. The angle is adjusted by the relative flow velocity of the solid particles 1 between the activation section 11 and the reaction section 12, as well as the diameter ratio between the activation section 11 and the reaction section 12. If the activity time of the solid particle 1 is long, the ratio of the diameter of the activation section 11 to the diameter of the reaction section 12 is set to be greater than 1 and the flow rate of the solid particle 1 in the activation section 11 is slow. If the flow rate of gas product is greater than 150% of the flow rate of the reaction gas, the diameters of the activation section 11 and the reaction section 12 are set to be consistent. The angle between the entering cambered surface of the high-temperature gas flow and the axis is 0, 0=30 0 to 45 °. The working principle of this gas-solid reactor is that the solid particles 1 supplied by the solid particle feeding device 20 enter the activation section 11 of the inner reactor cylinder 10, and are activated by contact with the high-temperature gas flow from the high-temperature gas flow feeding device 40, which increases the reaction activity. Then, they come into contact with the reaction gas from the reaction gas feeding device 30 to start the reaction. Due to the fact that the high-temperature gas flow supplied by the high-temperature gas flow feeding device 40 only enters the activation section 11 from the bottom, the high-temperature gas flow does not directly come into contact with the reaction gas, but passes through the solid particles 1 and then comes into contact with the reaction gas. Therefore, the solid particles 1 in contact with the reaction gas are activated particles by the high-temperature gas flow. Although there are uniformly distributed pores 111 on the wall of the activation section 11, as shown in Fig. 2, there is a thermal insulation layer 80 on the outer side of the activation section 11 except for the bottom, so high-temperature gas flow will not enter the activation section 11 from other positions outside the bottom. Next, the reaction gas and the solid particles 1 enter the reaction section 12 of the inner reactor cylinder 10, and the heat supply system 60 heats and maintains the reaction section 12. The reaction gas and the solid particles 1 fully contact and react in the reaction section 12. Finally, the gas product after the reaction is outputted through the gas product output device 50, and the solid particles 1 after the reaction are discharged through the solid particle discharging device 70 and transported to the silo 3 via the conveyor belt 2. More specifically, in this example, the inner reactor cylinder 10 is a rotary kiln. The length ratio L1 / L2 of the activation section 11 and the reaction section 12 is 0.35, and the diameter ratio of the activation section 11 and the reaction section 12 is 1.2. Solid particle feeding device 20 uses a spiral feeder. The solid particles 1 are 600°C pyrolytic char, and the reaction gas feeding device 30 feeds 600°C volatile matter. The mass ratio of the solid particles 1 to reaction gas is 0.8. The high-temperature gas flow feeding device 40 feeds 1200°C high-temperature flue gas, and the feeding amount is 1 / 6 of the volume of volatile matter. The heat supply system 60 uses a heating jacket, and the solid particle discharging device 70 uses a spiral discharge machine with a water-cooled jacket. When starting, Adjust the rotational speed of the inner reactor cylinder 10 so that the angle between the pavement of the solid particles and the axis in the activation section 11 is a, a=120 °, and the angle between the entering cambered surface of the high-temperature gas flow and the axis is 0, 0=42 ° . Pores on the outer circumference of the entering cambered surface of the high-temperature gas flow are covered by the insulation layer 80. When reacting in the reaction section 12, the thickness of the layer of the solid particles 1 in the reaction section 12 is adjusted by adjusting the discharge position of the solid particle discharging device 70, so that the angle between the pavement of the solid particles 1 in the reaction section 12 and the axis is a, a=220 °. After entering the activation section 11, the pyrolysis char comes into contact with the 1200°C high-temperature flue gas from the high-temperature gas flow feeding device 40, and the temperature is raised to 730°C, which increases the reaction activity. At the same time, a part of the char is also gasified by the high-temperature flue gas, and the specific surface area is increased from 21.39 m2 / g to 34 m2 / g. Then, it comes into contact with the 600°C volatile matter from the reaction gas feeding device 30 and begins to react. Next, driven by the rotation of the inner cylinder 10 in the reactor, it enters the reaction section 12 and further fully contacts and reacts under the heating and insulation effect of the 750°C to 800°C flue gas in the reaction gas feeding device 60. After the reaction is completed, the tar in the volatile matter has turned into combustible gas, and the gas production is 200% of the original volatile matter flow rate, which is outputted through the gas product output device 50. The tar content in the gas product is very low. After testing and analysis, the main components of the gas product are CO, CH4, H2, CO2, N2, with a calorific value of 10.5 MJ / Nm3. After simple purification, the gas product can meet the requirements for subsequent use. Compared with traditional fixed beds, this gas-solid reactor achieves online activation of the solid particles 1. Compared with fluidized beds, this gas-solid reactor avoids the high pressure of the high-temperature gas flow and the reaction gas. Example 2 Fig. 4 is a schematic diagram of the structure of a gas-solid reactor capable of online enhancement of the reaction activity. As shown in Fig. 4, this example provides a gas-solid reactor capable of online enhancement of the reaction activity of solid particles. The difference between this example and example 1 is that the solid particles 1 in this example are pushed forward inside the inner reactor cylinder 10 by the solid particle pushing device 90. The solid particle pushing device 90 comprises a spiral blade 91 and a motor 92 driving the rotation of the spiral blade 91. The spiral blade 91 can be a helical blade with an axis or a non axis shaped helical blade. The shape and density of the spiral blades 91 in the activation section 11 and the reaction section 12 can be consistent or inconsistent. Correspondingly, the movement rate of the solid particles 1 in the activation section 11 and the reaction section 12 can be consistent or inconsistent. In this example, the length ratio L1 / L2 of the activation section 11 and the reaction section 12 of the inner reactor cylinder 10 is 0.5, and the diameter ratio of the activation section 11 and the reaction section 12 is 1. The interior of the inner reactor cylinder 10 is equipped with spiral blades 91, which are driven by a motor 92 to rotate inside the inner reactor cylinder 10. The solid particle feeding device 20 adopts a star shaped feeder with a feeding hopper, and the solid particles 1 are a Ni based catalyst loaded on pyrolysis char. The reaction gas feeding device 30 feeds syngas (3H2+CO+CO2), and the mass ratio of solid particles 1 to the reaction gas is 0.8. The high-temperature gas flow feeding device 40 feeds syngas (2H2+CO) at 680°C, with a feed amount of 1 / 3 of the amount of gas flow fed by the reaction gas feeding device 30. The heat supply system 60 uses a heating jacket, and the solid particle discharging device 70 uses a rotary cooling cylinder with a water-cooled jacket. When starting, adjust the speed of the solid particle pushing device 90 so that the angle between the pavement of the solid particles and the axis in the activation section 11 is a, a=128°, and the angle between the entering cambered surface of the high-temperature gas flow and the axis is p, p=40° . Pores on the outer circumference of the entering cambered surface of the high-temperature gas flow are covered by the insulation layer 80. When reacting in the reaction section 12, the thickness of the layer of the solid particles 1 in the reaction section 12 is adjusted by adjusting the discharge position of the solid particle discharging device 70, so that the angle between the pavement of the solid particles 1 in the reaction section 12 and the axis is a, a=240°. After entering the activation section 11, the Ni based catalyst comes into contact with the 680°C syngas (2H2+CO) from the high-temperature gas flow feeding device 40, and the temperature is raised to 300-350°C. It is reduced by the high-temperature syngas, which increases the reaction activity. Then, it comes into contact with the syngas (3H2+CO+CO2) from the reaction gas feeding device 30 and begins to react. Next, after being pushed into the reaction section 12 by the solid particle pushing device 90, it further fully contacts and reacts under the heating and insulation effect of the 380 to 400 °C flue gas in the reaction gas feeding device 60. After the reaction is completed, the main components of the syngas have turned into methane (CH4) gas, which is outputted through the gas product output device 50. The gas product has been tested and analyzed, and its main components are CH4 (55%), H2 (15%), CO2+CO (30%), with a calorific value of 22.1 MJ / Nm3. After dust removal and purification, the gas product can meet the requirements of power generation, replacing natural gas as industrial gas, and serving as a clean fuel for boilers. In this example, the spiral blades 91 in the activation section 11 adopt a large spacing, which can make the Ni based catalyst stay in the activation section 11 for a longer time and be more fully reduced by the syngas at 680°C. The spiral blades 91 in the reaction section 12 adopt a small spacing, which can make the gas-solid contact more complete and the reaction more thorough. Compared with traditional fixed beds, this gas-solid reactor achieves online activation of Ni based catalyst particles. Compared with fluidized beds, this gas-solid reactor avoids the high pressure of the reaction gas and a large amount of catalyst carried and worn by the gas flow. The advantage of this gas-solid reactor is that it facilitates the adjustment of gas composition at the atmospheric pressure. Example 3 This example provides a gas-solid reactor capable of online enhancement of the reaction activity of solid particles, as shown in Fig. 2, using the same structure as in example 2. The solid particles 1 in this example are pushed forward inside the inner reactor cylinder 10 by the solid particle pushing device 90. In this example, the length ratio L1 / L2 of the activation section 11 and the reaction section 12 of the inner reactor cylinder 10 is 0.45, and the diameter ratio of the activation section 11 and the reaction section 12 is 1.16. The interior of the inner reactor cylinder 10 is equipped with spiral blades 91, which are driven by a motor 92 to rotate inside the inner reactor cylinder 10. The solid particle feeding device 20 adopts a star shaped feeder with a feeding hopper, and the solid particles 1 are a Ni-Zn based catalyst loaded on pyrolysis char. The diameter ratio of the activation section 11 and the reaction section 12 mentioned above is set to ensure that the Ni-Zn based catalyst loaded on the pyrolysis char has sufficient reduction activation time in the activation section 11. The reaction gas feeding device 30 feeds a mixture of volatile matter (containing tar) and water vapor, with water vapor fed from the outside to meet the gasification requirements of volatile matter (containing tar). The mass ratio of solid particles 1 to the reaction gas is 0.7. The high-temperature gas flow feeding device 40 feeds gas product (H2) at 600°C, with a feed amount of 1 / 2 of the amount of gas flow fed by the reaction gas feeding device 30. The heat supply system 60 uses a heating jacket, and the solid particle discharging device 70 uses a rotary cooling cylinder with a water-cooled jacket. When starting, adjust the speed of the solid particle pushing device 90 so that the angle between the pavement of the solid particles and the axis in the activation section 11 is a, a=158°, and the angle between the entering cambered surface of the high-temperature gas flow and the axis is P, P=41°. Pores on the outer circumference of the entering cambered surface of the high-temperature gas flow are covered by the insulation layer 80. When reacting in the reaction section 12, the thickness of the layer of the solid particles 1 in the reaction section 12 is adjusted by adjusting the discharge position of the solid particle discharging device 70, so that the angle between the pavement of the solid particles 1 in the reaction section 12 and the axis is a, a=240°. After entering the activation stage 11, the Ni-Zn based catalyst comes into contact with the 600°C gas product (H2) from the high-temperature gas flow feeding device 40, and the temperature is raised to around 380°C. It is reduced by the gas product (H2), which increases the reaction activity. Then, it comes into contact with a mixture of volatile components (containing tar) and water vapor from the reaction gas feeding device 30 and begins the reaction. Next, after being pushed into the reaction section 12 by the solid particle pushing device 90, it further fully contacts and reacts under the heating and insulation effect of the 600°C flue gas in the reaction gas feeding device 60. After the reaction is completed, the main components of the mixture of volatile matter (containing tar) and water vapor have turned into hydrogen (H2) gas, which is outputted through the product gas product output device 50. The gas product has been tested and analyzed, and its main components are H2 (>60%), H2O+CO2+CO (30%), with a calorific value of 15.1 MJ / Nm3. After dust removal and purification, the gas product can meet the requirements for hydrogen production gas. In this example, the spacing between the spiral blades in the activation section 11 is about twice that in the reaction section 12, which which can makethe Ni-Zn based catalyst stay in the activation section 11 for a long time, and be more fully reduced by the gas (H2) product at 600 °C, and have sufficient gas-solid contact and complete reaction in the reaction section 12. Compared with traditional fixed beds, this gas-solid reactor achieves online activation of Ni-Zn based catalyst particles. Compared with fluidized beds, this gas-solid reactor avoids the high pressure of the reaction gas and a large amount of catalyst carried and worn by the gas flow. The advantage of this gas-solid reactor is that it facilitates the preparation of volatile matter into H2 at the atmospheric pressure. Example 4 This example provides a gas-solid reactor capable of online enhancement of the reaction activity of solid particles, as shown in Fig. 1, using the same structure as in example 1. The solid particles 1 in this example are pushed forward inside the inner reactor cylinder 10 by the rotation of the inner reactor cylinder 10. In this example, the inner reactor cylinder 10 is a rotary kiln, the length ratio L1 / L2 of the activation section 11 and the reaction section 12 is 0.35, and the diameter ratio of the activation section 11 and the reaction section 12 is 1.25. The solid particle feeding device 20 adopts a chute feeder, and the solid particles 1 are CaCOs. The reaction gas feeding device 30 feeds flue gas from a small garbage incinerator, containing acidic gases such as HC1 and SO2. The flue gas is fed from the tail end of the activation section 11, and the mass ratio of solid particles 1 to reaction gas is 0.2. The high-temperature gas flow feeding device 40 feeds 1280 °C high-temperature flue gas, with a feed amount of 1 / 5 of the volume of the volatile matter. The heat supply system 60 uses a heating jacket, and the solid particle discharging device 70 uses a rotary cooling cylinder with a water-cooled jacket. When starting, adjust the speed of the inner reactor cylinder 10 so that the angle between the pavement of the solid particles and the axis in the activation section 11 is a, a=180°, and the angle between the entering cambered surface of the high-temperature gas flow and the axis is p=45°. Pores on the outer circumference of the entering cambered surface of the high-temperature gas flow are covered by the insulation layer. When reacting in the reaction section 12, the thickness of the layer of the solid particles 1 in the reaction section 12 is adjusted by adjusting the discharge position of the solid particle discharging device 70, so that the angle between the pavement of the solid particles 1 in the reaction section 12 and the axis is a, a=310°. After entering the activation section 11, CaCO? comes into contact with the high-temperature gas flow at 1280°C supplied by the high-temperature gas flow feeding device 40, and its temperature is raised to around 850°C. It is reduced by the hot flue gas, enhancing its reaction activity. Then, it comes into contact with the flue gas supplied by the reaction gas feeding device 30 and begins the reaction. Then, driven by the rotation of the inner reactor cylinder 10 of the reactor, it enters the reaction section 12 and fully contacts and reacts under the flue gas insulation effect of the reaction gas feeding device 60. After the reaction is completed, the HC1 and SO: gases in the flue gas are absorbed and discharged through the gas product output device 50. The gas product has been tested and analyzed, and the main pollutant components were 80:(55 mg / Nm3) and HC1 (10 mg / Nm3). After dust removal and purification, the gas product can meet the requirements for standard discharge. Compared with the traditional fixed bed, this gas-solid reactor achieves the online activation of CaCOs particles. Compared with the fluidized bed, this gas-solid reactor avoids the need for high-pressure fans for the reaction gas and the large-scale carrying and wear of CaCOs by the gas flow. Examples This example provides a gas-solid reactor capable of online enhancement of the reaction activity of solid particles, as shown in Fig. 2, using the same structure as in example 2. The solid particles 1 in this example are pushed forward inside the inner reactor cylinder 10 by the solid particle pushing device 90. In this example, the length ratio L1 / L2 of the activation section 11 and the reaction section 12 of the inner reactor cylinder 10 is 0.5, and the diameter ratio of the activation section 11 and the reaction section 12 is 1. The interior of the inner reactor cylinder 10 is equipped with spiral blades 91, which are driven by a motor 92 to rotate inside the inner reactor cylinder 10. The solid particle feeding device 20 adopts a star shaped feeder with a feeding hopper, and the solid particles 1 are 560°C pyrolytic char that have just been outputted from the pyrolysis furnace. The reaction gas feeding device 30 feeds pyrolysis gas with tar and water vapor, which is fed from the tail end of the activation section 11. The mass ratio of the solid particles 1 to the reaction gas is 0.67. The high-temperature gas flow feeding device 40 feeds 1280°C flue gas (containing CO2 / H2O / O2), with a feed amount of 1 / 9 of the amount of gas flow fed by the reaction gas feeding device 30. The heat supply system 60 uses a heating jacket, and the solid particle discharging device 70 uses a rotary cooling cylinder with a water-cooled jacket. When starting, adjust the speed of the solid particle pushing device 90 so that the angle between the pavement of the solid particles and the axis in the activation section 11 is a, a=148°, and the angle between the entering cambered surface of the high-temperature gas flow and the axis is P=45°. Pores on the outer circumference of the entering cambered surface of the high-temperature gas flow are covered by the insulation layer. When reacting in the reaction section 12, the thickness of the layer of the solid particles 1 in the reaction section 12 is adjusted by adjusting the discharge position of the solid particle discharging device 70, so that the angle between the pavement of the solid particles 1 in the reaction section 12 and the axis is a, a=270°. After entering the activation section 11, the pyrolysis char at 560°C comes into contact with the flue gas at 1280°Cfrom the high-temperature gas flow feeding device 40, and the temperature is raised to around 850°C. It is vaporized by the hot flue gas, which increases the reaction activity. Afterwards, it comes into contact with the pyrolysis gas from the high-temperature gas flow feeding device30 and begins the reaction. Next, after being pushed into the reaction section 12 by the solid particle pushing device 90, it further fully contacts and reacts under the heating and insulation effect of the 380°C to 400°C flue gas in the reaction gas feeding device 60. After the reaction is completed, the tar in the pyrolysis gas has turned into H2, CH4, and CO gases, which are outputted together with the original gases through the gas product output device 50. The gas product has been tested and analyzed, and its main components are CH4(8%), H2(36%), CO(21%), C2He(1.4%), C2H4(2.6%), CO2(29%), N2(2%), with tar content less than lg / Nm3. After dust removal and purification, the gas product can meet the requirements as a raw material for synthesis gas. In this example, the spacing between the spiral blades in the activation section 11 is about 1.5 times that in the reaction section 12. Compared with traditional fixed beds, this gas-solid reactor achieves online activation of the char particles. Compared with fluidized beds, this gas-solid reactor avoids high pressure of the reaction gases and the char wear on the reactor. The advantage of this gas-solid reactor is that it facilitates the conversion of volatile matter into raw materials for synthesis gas at the atmospheric pressure. Example 6 This example provides a gas-solid reactor capable of online enhancement of the reaction activity of solid particles, as shown in Fig. 5, using a similar structure as in example 1 (see Fig. 1), but the entire device is placed vertically. The solid particles 1 inside the inner reactor cylinder 10 naturally descends by gravity. In this example, the inner reactor cylinder 10 is a fixed cylinder wall, the length ratio L1 / L2 of the activation section 11 and the reaction section 12 is 0.45, and the diameter ratio of the activation section 11 and the reaction section 12 is 1.16. The solid particle feeding device 20 adopts a spiral feeder. The solid particles 1 are a mixture of the garbage pyrolysis char powder and CaO, with a mass ratio of 5:1 between the char powder and CaO. The reaction gas feeding device 30 feeds the volatile matter and water vapor generated from the garbage pyrolysis, which are fed from the lower periphery of the activation section 11. The mass ratio of the solid particles 1 to the reaction gas is 0.88:1, and the high-temperature gasflow feeding device 40 feeds high-temperature flue gas with a temperature higher than 1200°C, with a feed amount of 1 / 5 of the volume of the volatile matter. The heat supply system 60 uses a heating jacket, and the solid particle discharging device 70 uses a rotary cooling cylinder with a water-cooled jacket. When starting, adjust the height of the solid particles 1 in the reactor, so that the height of the pavement of the solid particles 1 in the activation section 11 meets the angle P, P=45 °, between the entering cambered surface of the high-temperature gas flow and the axis of the material layer. Pores on the outer circumference of the entering cambered surface of the high-temperature gas flow are covered by the insulation layer. When reacting in reaction section 12, the residence time of the solid particles 1 in reaction section 12 is adjusted by adjusting the discharge position of solid particle discharging device 70. After entering the activation section 11, the mixture of the char powder and CaO comes into contact with high-temperature flue gas above 1200°C from the high-temperature gas flow feeding device 40, and the temperature is raised to around 850 to 900°C. It is reduced by the hot flue gas, which increases the reaction activity. After being activated, it falls into the reaction section 12 and comes into contact with the reaction gas (volatile matter and water vapor) supplied from the reaction gas feeding device 30, and begins to react. Next, after entering the reaction section 12 with the inner reactor cylinder 10 fixed, it fully contacts and reacts under the heating and insulation effect of the flue gas in the reaction gas feeding device 60. After the reaction is completed, the volatile matter of the garbage is converted into hydrogen-rich synthesis gas, which is outputted through the gas product output device 50. The gas product has been tested and analyzed, H2(55%), CO( 12%), CO2(24%), N2(7.2%), 02(1.8%). After dust removal and purification, the gas product can meet the requirements for extracting hydrogen gas and preparing synthesis gas. The outputted residue char-containing ash can be used for making foam bricks, sintered bricks and burning cement. Compared with traditional fixed beds, this gas-solid reactor achieves online hydrogen production from the waste pyrolysis volatiles. Compared with fluidized beds, this gas-solid reactor avoids the need for high-pressure fans for reaction gases and the large amount of particles carried and worn by the gas flow. Effects of the examples According to the example 1 to the example 6, it can be seen that when high-temperature flue gas is introduced into the activation section and the amount and temperature of the high-temperature flue gas are controlled, the solid particles can be activated. Furthermore, the catalytic cracking of volatile components containing tar is achieved by heating the solid particles, effectively utilizing the reactivity of the charcoal. Both the rotary kiln reactors and the spiral tube reactors are applicable. According to the example 2 and the example 3, it can be seen that when the solid particles are used as catalysts, this gas-solid reactor can be used to produce high concentrations of methane gas or hydrogen gas, which can become the raw material for supplying methane or hydrogen gas. According to the example 4, it can be seen that when the solid particles are desulfurizers or deacidification agents, this gas-solid reactor can achieve desulfurization and dechlorination through inexpensive limestone CaCOs, meeting the flue gas purification requirements of small incinerators. According to the example 1 to the example 6, it can be seen that through this gas-solid reactor, high-quality gas can be obtained and low-priced char or residue solid (the solid particles) can be effectively utilized, effectively reducing operating costs. In conclusion, the gas-solid reactor capable of online enhancement of the reaction activity of solid particles according to the present invention divides the inner reactor cylinder into an activation section and a reaction section, with the two parts connected internally and separated externally by an insulation layer. The opening of the activation section allows high-temperature gas flow to come into contact with the solid particles, enabling online activation treatment of the solid particles so as to function, and promoting chemical reactions between gas and solid, resulting in high product gas quality, effectively improving the value of the final product, enhancing the efficiency of the reactor, maximizing external energy savings, avoiding waste water generation, and avoiding problems such as coking and char deposition in traditional reactors. The organized contact between the solid particles and reaction gas is achieved, and the activity and consumption of the solid particles are controllable. Reduced equipment maintenance requirements and further lowered comprehensive processing costs. The above examples are preferred examples of the present invention and are not intended to limit the scope of protection of the present invention.

Claims

1 .A gas-solid reactor capable of online enhancement of the reaction activity of solid particles, the gas-solid reactor comprising:an inner reactor cylinder, divided into an activation section and a reaction section;a solid particle feeding device, connected to a head end of the activation section, for feeding solid particles used as reaction materials or catalysts;a reaction gas feeding device,connected to a head or tail end of the activation section, for feeding reaction gas;a high-temperature gas flow feeding device, for feeding high-temperature gas flow to activate the solid particles in the activation section;a gas product output device, connected to a tail end of the reaction section, for outputting the gas product after the reaction between the solid particles and the reaction gas;a heat supply system, located outside the reaction section, for supplying the heat source required by the reaction section, and for heating and maintaining the solid particles and the reaction gas inside the reaction section from the outside through the heat source;anda solid particle discharging device, connected to a tail end of the reaction section, for cooling and discharging solid particles after the reaction,the length of the activation section 11 is LI, the length of the reaction section 12 is L2, and the length ratio of the activation section 11 and the reaction section 12 is Ll / L2=0.35 to 0.5,the outer side of the activation section 11 and the outer side of the reaction section 12 are separated by a thermal insulation layer made of insulation material.2.The gas-solid reactor capable of online enhancement of the reaction activity of solid particles claim 1, the reactor inner cylinder is horizontally divided into the activation section and the reaction section, and the high-temperature gas flow feeding device is set at the bottom of the activation section, for feeding high-temperature gas flow from the bottom to activate the solid particles inside the activation section.3.The gas-solid reactor capable of online enhancement of the reaction activity of solid particles claim 1, the reactor inner cylinder is a rotary kiln, the solid particles are driven forward by the rotation of the reactor inner cylinder inside the reactor inner cylinder.4.The gas-solid reactor capable of online enhancement of the reaction activity of solid particles claim 1, the reactor is equipped with a solid particle pushing device, including spiral blades set in the reactor inner cylinder and a motor driving the rotation of the spiral blades; and the solid particles are pushed forward by the solid particle pushing device inside the reactor inner cylinder.5.The gas-solid reactor capable of online enhancement of the reaction activity of solid particlesclaim 1, a cylinder wall of the activation section is uniformly perforated with pores, the size of the pores is 0.35 to 0.7 times the average size of the solid particles, and the porosity is 15% to 25%.6.The gas-solid reactor capable of online enhancement of the reaction activity of solid particles claim 1, an angle between the pavement of the solid particles and an axis in the activation section 11 is a, a>90° .7.The gas-solid reactor capable of online enhancement of the reaction activity of solid particles claim 1, an angle between an entering cambered surface of the high-temperature gas flow and an axis in the activation section is P, P=30 ° to 45 0 , and pores on the outer circumference of the entering cambered surface of the high-temperature gas flow are covered by an insulation layer.8.The gas-solid reactor capable of online enhancement of the reaction activity of solid particles claim 1, the solid particle feeding device is a spiral feeder, a chute feeder, or a star feeder with a discharge hopper.9.The gas-solid reactor capable of online enhancement of the reaction activity of solid particles claim 1, the heat supply system is a heating jacket, and has a heating gas flow inlet and a heating gas flow outlet, and the heating gas flow circulates inside.10.The gas-solid reactor capable of online enhancement of the reaction activity of solid particles claim 1, the top of the tail end of reaction section is equipped with a gas product discharge outlet connected to gas product outlet device, and a particle blocking device is installed at the gas product discharge outle to prevent solid particles from being carried into the product gas flow.11.The gas-solid reactor capable of online enhancement of the reaction activity of solid particles claim 1, the solid particle discharge device is a spiral discharge machine equipped with a water-cooled jacket, or a rotary cooling cylinder equipped with a water-cooled or air-cooled jacket.

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