An apparatus and method for co-production of biomass gas, charcoal, and oil based on microwave rapid pyrolysis.

Abstract

The invention discloses a device and method for biomass gas, charcoal and oil co-production based on microwave rapid pyrolysis, which relates to the technical field of biomass microwave pyrolysis and efficient conversion, and includes: a microwave generator and a fluidized bed furnace, a cyclone separator, a catalytic cracking device, a condensing device, an adsorption device, a pressure swing adsorption device, a SOFC power generation device and an adsorbent regeneration device which are sequentially connected through pipelines; the fluidized bed furnace, the cyclone separator and the catalytic cracking device are all provided with a microwave generator; a charcoal powder collecting device 1 is provided at the bottom of the fluidized bed furnace; a charcoal powder collecting device 2 is provided at the bottom of the cyclone separator; a catalyst bed is provided in the catalytic cracking device; an adsorbent bed is provided in the adsorption device; the carbon slag in the charcoal powder collecting device 1 is used as a reducing agent, and the used catalyst bed and adsorbent bed are reduced in the adsorbent regeneration device; the SOFC power generation device is electrically connected to the microwave generator and the adsorbent regeneration device. The invention can realize the high-value utilization of biomass gas, charcoal and oil.

Description

Technical Field

[0001] The invention relates to the technical field of biomass microwave pyrolysis and efficient conversion, and in particular to a device and method for biomass gas, charcoal and oil co-production based on microwave rapid pyrolysis. Background Art

[0002] In recent years, the overexploitation of fossil fuels has led to serious environmental problems and energy crises. Biomass, as a typical renewable energy source, has the advantages of large reserves, wide distribution and low pollution. The comprehensive utilization value of biomass can be realized by converting biomass into high-value materials such as syngas, bio-oil and porous carbon through thermochemical means. Microwave fast pyrolysis technology is an efficient biomass conversion technology and an emerging pyrolysis technology for preparing high-value bio-oil.

[0003] Due to the complexity of biomass pyrolysis, traditional pyrolysis technology converts biomass into bio-oil by thermal cracking, and produces a small amount of pyrolysis gas and coke. In addition, due to the slow heating rate and uneven heating, the traditional pyrolysis technology leads to the production of tar during the pyrolysis process. Tar seriously affects the quality of bio-oil. In addition, pyrolysis coke and pyrolysis gas mainly release energy through incineration and other methods, and their high-value utilization has not been achieved.

[0004] There is currently a method for pyrolysis-coupled chemical chain gasification dual-cycle oil and gas co-production. This method uses a pyrolysis multi-stage chemical chain gasification method to achieve oil and gas co-production. Although this method increases the yield of synthesis gas, the pyrolysis carbon is not effectively utilized, which to a certain extent affects the high-value utilization of biomass.

[0005] Therefore, how to design a device and method for the co-production of biomass gas, charcoal and oil based on microwave rapid pyrolysis, which can achieve the high-value synthesis of biomass gas, charcoal and oil, and obtain carbon electrode materials that can be used for supercapacitors through the cascade utilization of biomass, and collect the light bio-oil obtained by pyrolysis; in addition, through the subsequent gas separation and purification process, the combustible gas rich in H2 and CO is obtained in a cascade manner, and the conversion of the chemical energy of the combustible gas into electrical energy is realized through the SOFC power generation device. These are problems that technical personnel in this field urgently need to solve. Summary of the invention

[0006] In view of this, the present invention proposes a device and method for co-production of biomass gas, charcoal and oil based on microwave rapid pyrolysis, aiming to solve the technical problems that the utilization rate of pyrolysis gas and pyrolysis carbon in the above-mentioned traditional biomass gas, charcoal and oil co-production device is low and the high-value utilization of biomass cannot be effectively achieved.

[0007] In order to achieve the above object, the present invention adopts the following technical solution:

[0008] On one hand, the present invention provides a device for co-production of biomass gas, charcoal and oil based on microwave rapid pyrolysis, comprising: a microwave generator and a fluidized bed furnace, a cyclone separator, a catalytic cracking device, a condensing device, an adsorption device, a pressure swing adsorption device, a SOFC power generation device and an adsorbent regeneration device which are sequentially connected through pipelines;

[0009] There are multiple microwave generators, and the fluidized bed furnace, the cyclone separator and the catalytic cracking device are all provided with microwave generators for controlling the reaction temperature;

[0010] A first carbon powder collecting device is provided at the bottom slag discharge port of the fluidized bed furnace; a second carbon powder collecting device is provided at the bottom slag discharge port of the cyclone separator;

[0011] The catalytic cracking device is provided with a detachable catalyst bed; the adsorption device is provided with a detachable adsorbent bed; the carbon slag in the carbon powder collecting device is added to the adsorbent regeneration device as a reducing agent, and the used catalyst bed and the adsorbent bed are transferred to the adsorbent regeneration device for decomposition and reduction; the gas outlet of the adsorbent regeneration device transports the combustible gas to the SOFC power generation device through a pipeline to generate electricity;

[0012] The SOFC power generation device is electrically connected to the microwave generator and the adsorbent regeneration device to supply power.

[0013] When the device for co-production of biomass gas and charcoal oil based on microwave rapid pyrolysis provided by the present invention is used, the fluidized bed furnace, cyclone separator and catalytic cracking device all control the internal reaction temperature through a microwave generator; biomass is added to the fluidized bed furnace for rapid pyrolysis, and the high-temperature pyrolysis gas generated in the furnace carries light charcoal powder into the cyclone separator, and the heavy charcoal powder in the furnace is transported to the charcoal powder collecting device 1 through the slag discharge port at the bottom of the furnace for storage and as a reducing agent. The light charcoal powder is separated in the cyclone separator, and the charcoal powder is secondary heated by a microwave generator to obtain usable charcoal powder material, and collected in the charcoal powder collecting device 2. The high-temperature pyrolysis gas discharged from the cyclone separator is transported to the catalytic cracking device through a pipeline, and the pyrolysis gas is catalytically reformed through the catalyst bed and then passed into the condensing device to obtain light bio-oil. The non-condensable pyrolysis gas (mainly combustible H2 and CO) discharged from the condensing device is transported to the adsorption device through a pipeline, and after being purified by the adsorbent bed, it is introduced into the pressure swing adsorption device through a pipeline. The pressure swing adsorption device separates and purifies the combustible H2 and CO to obtain high-purity synthesis gas, and the high-purity synthesis gas is sent to the SOFC power generation device through a pipeline for power generation. The generated electricity is used as an auxiliary energy source for the microwave generator and the adsorbent regeneration device. The used catalyst bed and adsorbent bed can be taken out and placed in the adsorbent regeneration device for decomposition and reduction, and the heavy carbon powder in the carbon powder collection device is used as a reducing agent. The CO gas generated in the reduction process in the adsorbent regeneration device is sent to the SOFC power generation device through a pipeline for power generation for utilization.

[0014] As a further improvement of the above technical solution, it also includes an activator feeding mechanism, which is connected to and communicates with the pipeline communicating between the fluidized bed furnace and the cyclone separator to transport the activator to the cyclone separator.

[0015] The beneficial effect of the above technical solution is that the activator is fed into the cyclone separator through the activator feeding mechanism, which can realize the separation and activation of light carbon powder inside the cyclone separator simultaneously, and the separated carbon powder and activator are secondary activated at the bottom of the cyclone separator, and finally a porous carbon electrode material that can be used for supercapacitors can be obtained, thereby realizing the high-value utilization of pyrolytic carbon.

[0016] As a further improvement of the above technical solution, the carbon powder collecting device 1 includes a screw conveying mechanism 1 and a collecting container 1; the inlet of the screw conveying mechanism 1 is connected to the slag discharge port at the bottom of the fluidized bed furnace, and the outlet of the screw conveying mechanism 1 is connected to the collecting container 1, so as to convey the heavy carbon powder in the fluidized bed furnace to the collecting container 1;

[0017] The second carbon powder collecting device includes a second screw conveying mechanism and a second collecting container; the inlet of the second screw conveying mechanism is connected to the bottom slag discharge port of the cyclone separator, and the outlet of the second screw conveying mechanism is connected to the second collecting container to convey the light carbon powder in the cyclone separator to the second collecting container.

[0018] The beneficial effects of the above technical solution are: the spiral conveying mechanism 1 is used to control the heavy carbon slag or carbon powder in the fluidized bed furnace to be input from the bottom slag discharge port thereof to the collecting container 1 for centralized storage, so as to facilitate centralized retrieval and addition to the adsorbent regeneration device as a reducing agent for utilization, thereby realizing the high-value utilization of pyrolytic carbon; the spiral conveying mechanism 2 is used to control the light carbon powder in the cyclone separator to be transported from the bottom slag discharge port thereof to the collecting container 2 for centralized storage, so as to facilitate centralized retrieval and use as a porous carbon electrode material for supercapacitors.

[0019] As a further improvement of the above technical solution, a hood is provided in the fluidized bed furnace.

[0020] The beneficial effect of the above technical solution is that N2 can be introduced into the fluidized bed furnace through a hood arranged in the furnace to maintain an inert atmosphere in the furnace.

[0021] As a further improvement of the above technical solution, the condensing device includes a condenser and an oil storage tank; the inlet of the condenser is connected to the outlet of the catalytic cracking device through a pipeline, and the outlet of the condenser is connected to the inlet of the adsorption device through a pipeline; the oil storage tank is connected to the condenser through a pipeline to collect oil.

[0022] The beneficial effects of the above technical solution are: the condenser can liquefy the condensable pyrolysis gas to obtain light bio-oil and store it in an oil storage tank for centralized recycling; the non-condensable pyrolysis gas is transported from the outlet of the condenser to the adsorption device for purification treatment for easy utilization.

[0023] As a further improvement of the above technical solution, the catalyst bed comprises a mounting frame and a mesh tube mounted on the mounting frame; the mounting frame is detachably connected to the catalytic cracking device; the inner cavity of the mesh tube is filled with catalyst, and the pipe opening of the mesh tube is a catalyst access opening;

[0024] The catalyst bed and the adsorbent bed have the same structure.

[0025] The beneficial effects of the above technical solution are: the inner cavity of the mesh tube of the catalyst bed and the adsorbent bed is used to fill the catalyst or adsorbent; the use of the mesh tube can achieve full contact between the catalyst, adsorbent and pyrolysis gas; by designing the installation frame as a detachable structure, it can be easily taken out and placed in the adsorbent regeneration device to reduce the catalyst and adsorbent, so as to facilitate reuse.

[0026] It should be noted that the mounting frame is a plate-frame structure, and there are multiple mesh tubes, which are arranged in parallel in sequence and on the mounting frame. The detachable connection structure between the mounting frame of the catalyst bed and the catalytic cracking device can be designed with reference to the prior art, and will not be described in detail here.

[0027] As a further improvement of the above technical solution, the catalyst in the catalyst bed and the adsorbent in the adsorbent bed are both carbide slag.

[0028] The beneficial effects of the above technical scheme are: carbide slag is an industrial waste residue produced after calcium carbide is hydrolyzed to obtain acetylene gas, and its main components are Ca(OH)2 and calcium oxide; using industrial waste carbide slag as bed material for catalyst bed and adsorbent bed can realize efficient resource utilization of industrial waste.

[0029] Another aspect of the present invention provides a method for co-producing biomass gas, charcoal and oil based on microwave rapid pyrolysis, using the device for co-producing biomass gas, charcoal and oil based on microwave rapid pyrolysis; the specific steps include:

[0030] Step 1: adding biomass into a fluidized bed furnace, and pyrolyzing the biomass in the fluidized bed furnace; controlling the reaction temperature in the fluidized bed furnace by a microwave generator; and collecting heavy carbon powder discharged from a slag discharge port of the fluidized bed furnace by a carbon powder collecting device 1;

[0031] Step 2: The pyrolysis gas generated in the fluidized bed furnace carries the light carbon powder into the cyclone separator to separate the light carbon powder, the carbon powder in the cyclone separator is secondary heated by a microwave generator, and the carbon powder discharged from the slag discharge port of the cyclone separator is collected by a second carbon powder collecting device to serve as a porous carbon electrode material for making a supercapacitor;

[0032] Step 3: The pyrolysis gas in the cyclone separator is transported to a catalytic cracking device, and the reaction temperature in the catalytic cracking device is controlled by a microwave generator. The pyrolysis gas is catalytically reformed through a catalyst bed and then sent to a condensing device to obtain bio-oil liquid;

[0033] Step 4: purifying the non-condensable pyrolysis gas output from the condensing device through an adsorbent bed of the adsorption device; and inputting the purified non-condensable pyrolysis gas into a pressure swing adsorption device for separation and purification to obtain combustible synthesis gas;

[0034] Step 5: inputting the combustible synthesis gas into the SOFC power generation device to generate electricity; using the electricity generated by the SOFC power generation device to power the microwave generator and the adsorbent regeneration device;

[0035] Step six: Take out the used catalyst bed and adsorbent bed and put them into the adsorbent regeneration device, add the heavy carbon powder collected in the carbon powder collection device 1 as a reducing agent into the adsorbent regeneration device, and decompose and reduce the used catalyst bed and adsorbent bed; the adsorbent regeneration device generates CO gas which is sent to the SOFC power generation device for power generation.

[0036] As a further improvement of the above technical solution, in step 2, an activator is added to the cyclone separator through an activator feeding mechanism to simultaneously separate and activate the light carbon powder; and the separated carbon powder and activator are secondary activated at the bottom of the cyclone separator.

[0037] The beneficial effect of the above technical solution is that the carbon powder that has been secondary activated in the cyclone separator can be used as a porous carbon electrode material for making supercapacitors, thereby achieving high-value utilization of pyrolytic carbon.

[0038] As a further improvement of the above technical solution, the pyrolysis temperature of the fluidized bed furnace is controlled at 400-600°C; the temperature in the cyclone separator is controlled at 650°C-750°C; the decomposition temperature of the pyrolysis gas in the catalytic cracking device is controlled at 650°C-750°C; and the reaction temperature in the adsorbent regeneration device is controlled at 750°C-850°C.

[0039] The beneficial effect of the above technical solution is that the temperature in the fluidized bed furnace, the cyclone separator and the catalytic cracking device can be controlled by a microwave generator, so that the temperature can be controlled flexibly, stably and accurately.

[0040] It can be seen from the above technical solutions that, compared with the prior art, the present invention discloses a device and method for biomass gas charcoal oil co-production based on microwave rapid pyrolysis, which has the following advantages and beneficial effects:

[0041] 1. The present invention realizes the synchronous synthesis of three-phase products of biomass through microwave rapid pyrolysis technology, and obtains high-value biomass-derived porous carbon, bio-oil and H2-rich synthesis gas.

[0042] 2. The cyclone separator of the present invention simultaneously separates and activates light carbon powder, and the separated carbon powder and activator are activated for a second time at the bottom of the cyclone separator, and finally a porous carbon electrode material that can be used to make a supercapacitor is obtained.

[0043] 3. The present invention uses industrial waste carbide slag as the bed material for the catalyst bed and the adsorbent bed, thus realizing the resource utilization of industrial waste.

[0044] 4. The present invention utilizes heavy carbon slag or carbon powder produced by pyrolysis as a reducing agent. While achieving the regeneration of the catalyst and the adsorbent, the generated CO gas can be further used for power generation in the SOFC power generation device.

[0045] 5. The present invention obtains high-purity synthesis gas from H2-rich pyrolysis gas through a pressure swing adsorption device, and the combustible synthesis gas is sent to a SOFC power generation device (solid oxide fuel cell) to generate electricity. The generated electricity is used as part of the energy for the microwave generator and the adsorbent regeneration device. BRIEF DESCRIPTION OF THE DRAWINGS

[0046] In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings required for use in the embodiments or the description of the prior art will be briefly introduced below. Obviously, the drawings described below are only embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on the provided drawings without paying creative work.

[0047] Figure 1 A schematic diagram of a device structure for co-production of biomass gas, charcoal and oil based on microwave rapid pyrolysis according to the present invention;

[0048] Figure 2 A schematic top view of a catalyst bed structure of a device for co-producing biomass gas, charcoal and oil based on microwave rapid pyrolysis according to the present invention;

[0049] Figure 3 A schematic side view of a catalyst bed structure of a device for co-producing biomass gas, charcoal and oil based on microwave rapid pyrolysis according to the present invention;

[0050] In the figure: 1. microwave generator; 2. fluidized bed furnace; 21. carbon powder collecting device 1; 211. spiral conveying mechanism 1; 212. collecting container 1; 22. wind hood; 3. cyclone separator; 31. carbon powder collecting device 2; 311. spiral conveying mechanism 2; 312. collecting container 2; 4. catalytic cracking device; 41. catalyst bed; 411. mounting frame; 412. mesh tube; 4121. valve 1; 4122. molded catalyst; 5. condensing device; 51. condenser; 52. oil storage tank; 6. adsorption device; 61. adsorbent bed; 7. pressure swing adsorption device; 71. flue gas discharge port; 8. SOFC power generation device; 9. adsorbent regeneration device; 10. activator feeding mechanism; 11. spiral feeding device; 12. valve. DETAILED DESCRIPTION

[0051] Embodiments of the present invention are described in detail below, examples of which are shown in the accompanying drawings, wherein the same or similar reference numerals throughout represent the same or similar elements or elements having the same or similar functions. The embodiments described below with reference to the accompanying drawings are exemplary and are intended to be used to explain the present invention, and should not be construed as limiting the present invention.

[0052] In the description of the present invention, it is necessary to understand that the terms "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inside", "outside", etc., indicating the orientation or position relationship are based on the orientation or position relationship shown in the drawings, and are only for the convenience of describing the present invention and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore cannot be understood as a limitation on the present invention.

[0053] In addition, the terms "first" and "second" are used for descriptive purposes only and should not be understood as indicating or implying relative importance or implicitly indicating the number of the indicated technical features. Therefore, the features defined as "first" and "second" may explicitly or implicitly include one or more of the features. In the description of the present invention, the meaning of "plurality" is two or more, unless otherwise clearly and specifically defined.

[0054] In the present invention, unless otherwise clearly specified and limited, the terms "installed", "connected", "connected", "fixed" and the like should be understood in a broad sense, for example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be a direct connection or an indirect connection through an intermediate medium, it can be the internal connection of two elements or the interaction relationship between two elements. For ordinary technicians in this field, the specific meanings of the above terms in the present invention can be understood according to specific circumstances.

[0055] According to an embodiment of the present invention, Figures 1 to 3 As shown, a device and method for biomass gas, charcoal and oil co-production based on microwave rapid pyrolysis includes: a microwave generator 1, and a fluidized bed furnace 2, a cyclone separator 3, a catalytic cracking device 4, a condensing device 5, an adsorption device 6, a pressure swing adsorption device 7 (also known as a PSA device), a SOFC power generation device 8 and an adsorbent regeneration device 9, which are sequentially connected through pipelines. There are multiple microwave generators 1.

[0056] A microwave generator 1 for controlling the pyrolysis temperature of biomass in the furnace is installed on the outer wall of the fluidized bed furnace 2, and a carbon powder collecting device 21 is provided at the bottom slag outlet of the fluidized bed furnace 2. The pyrolysis gas outlet of the fluidized bed furnace 2 is connected to the inlet of the cyclone separator 3 through a pipeline to transport the pyrolysis gas carrying light carbon powder; the cyclone separator 3 is provided with a microwave generator 1 for secondary heating of light carbon powder, and a carbon powder collecting device 2 31 is provided at the bottom slag outlet of the cyclone separator 3. A microwave generator 1 for controlling the reaction temperature is provided on the catalytic cracking device 4, and the pyrolysis gas outlet of the cyclone separator 3 is connected to the inlet of the catalytic cracking device 4 through a pipeline to transport the pyrolysis gas; the catalytic cracking device 4 is provided with a detachable catalyst bed 41. The inlet of the condensing device 5 is connected to the outlet of the catalytic cracking device 4 through a pipeline, and an oil storage tank 52 for collecting the bio-oil discharged therefrom is provided at the bottom of the condensing device 5. The outlet of the condensing device 5 is connected to the inlet of the adsorption device 6 through a pipeline to transport the non-condensable pyrolysis gas; the adsorption device 6 is provided with a detachable adsorbent bed 61 for purifying the non-condensable pyrolysis gas. The inlet of the pressure swing adsorption device 7 is connected to the outlet of the adsorption device 6 to separate and purify the non-condensable pyrolysis gas output by the adsorption device 6 and obtain high-concentration combustible gases H2 and CO. The inlet of the SOFC power generation device 8 is connected to the outlet of the pressure swing adsorption device 7 through a pipeline to convert the chemical energy of the combustible gas into electrical energy. The carbon slag in the carbon powder collection device 21 is added to the adsorbent regeneration device 9 as a reducing agent, and the used catalyst bed 41 and adsorbent bed 61 are transferred to the adsorbent regeneration device 9 for decomposition and reduction; the adsorbent regeneration device 9 is used to use the carbon slag collected by the carbon powder collection device 21 as a reducing agent to reduce the used catalyst bed 41 and adsorbent bed 61; the gas outlet of the adsorbent regeneration device 9 transports the combustible gas CO generated by the reduction reaction to the SOFC power generation device 8 through a pipeline for power generation. The SOFC power generation device 8 is electrically connected to the microwave generator 1 and the adsorbent regeneration device 9 for auxiliary power supply.

[0057] When the device for co-production of biomass gas, charcoal and oil based on microwave rapid pyrolysis provided in this embodiment is used, the fluidized bed furnace 2, the cyclone separator 3 and the catalytic cracking device 4 all control the internal reaction temperature through the microwave generator 1; the biomass is added to the fluidized bed furnace 2 for rapid pyrolysis, and the high-temperature pyrolysis gas generated in the furnace carries the light charcoal powder into the cyclone separator 3, and the heavy charcoal powder in the furnace is transported to the charcoal powder collecting device 1 21 through the slag discharge port at the bottom of the furnace for storage and as a reducing agent. The light charcoal powder is separated in the cyclone separator 3, and the charcoal powder is secondary heated by the microwave generator 1 to obtain usable charcoal powder material, and collected in the charcoal powder collecting device 2 31. The high-temperature pyrolysis gas discharged from the cyclone separator 3 is transported to the catalytic cracking device 4 through a pipeline, and the pyrolysis gas is catalytically reformed through the catalyst bed 41 and then passed into the condensing device 5 to obtain light bio-oil. The non-condensable pyrolysis gas discharged from the condensation device 5 is mainly flammable H2 and CO, which are transported to the adsorption device 6 through a pipeline, and then are purified by the adsorbent bed 61 and then merged into the pressure swing adsorption device 7 through a pipeline. The pressure swing adsorption device 7 separates and purifies the flammable H2 and CO to obtain high-purity synthesis gas, which is sent to the SOFC power generation device 8 through a pipeline for power generation, and the generated electricity is used as an auxiliary energy source for the microwave generator 1 and the adsorbent regeneration device 9. The catalyst bed 41 and the adsorbent bed 61 after use are manually disassembled and taken out and placed in the reaction chamber of the adsorbent regeneration device 9 for decomposition and reduction, and the heavy carbon powder in the carbon powder collection device 21 is used as a reducing agent. The CO gas generated in the reduction process in the adsorbent regeneration device 9 is sent to the SOFC power generation device 8 through a pipeline for power generation for utilization.

[0058] Specifically, a plurality of microwave generators 1 are evenly distributed along the circumferential direction on the outer wall of the fluidized bed furnace 2; the bottom of the cyclone separator 3 is conical, and a plurality of microwave generators 1 are evenly distributed along the circumferential direction on its conical outer wall; and a plurality of microwave generators 1 are evenly distributed on the bottom wall of the catalytic cracking device 4.

[0059] Specifically, the biomass gas, charcoal and oil cogeneration system further includes a plurality of valves 12. Valves are installed on the pipeline connecting the pressure swing adsorption device 7 and the SOFC power generation device 8, and the flow rate of the combustible gas input into the SOFC power generation device 8 is regulated by the valves.

[0060] Specifically, the SOFC power generation device 8 is a solid oxide fuel cell that can convert the chemical energy of the combustible gas into electrical energy. A valve 12 is installed on the pipeline connecting the adsorbent regeneration device 9 and the SOFC power generation device 8, and the valve 12 is used to control the flow rate of the CO gas input into the SOFC power generation device 8.

[0061] Specifically, the pressure swing adsorption device 7 has a flue gas discharge port 71 .

[0062] In some embodiments, the biomass gas, charcoal and oil cogeneration system further includes a screw feeding device 11 , the outlet of which is connected to and communicates with the feed port of the fluidized bed furnace 2 to transport the biomass material to be pyrolyzed into the furnace chamber of the fluidized bed furnace 2 .

[0063] Specifically, the screw feeding device 11 can be a screw conveyor.

[0064] In some embodiments, the biomass gas, charcoal and oil co-production system further includes an activator feeding mechanism 10 , which is connected to and communicates with a pipeline between the fluidized bed furnace 2 and the cyclone separator 3 to transport the activator to the cyclone separator 3 .

[0065] The activator is fed into the cyclone separator 3 through the activator feeding mechanism 10, so that the separation and activation of light carbon powder can be carried out simultaneously inside the cyclone separator. The separated carbon powder and activator are secondary activated at the bottom of the cyclone separator, and finally a porous carbon electrode material that can be used for supercapacitors can be obtained, thereby realizing the high-value utilization of pyrolytic carbon.

[0066] Specifically, the activator feeding mechanism 10 includes an activator feeder and a valve 12. The discharge port of the activator feeder is connected through a pipeline and communicates with the pipeline connecting the fluidized bed furnace 2 and the cyclone separator 3; the valve 12 is installed on the pipeline connected to the discharge port of the activator feeder to control the opening and closing state of the pipeline.

[0067] In some embodiments, the carbon powder collecting device 21 includes a screw conveying mechanism 211 and a collecting container 212; the inlet of the screw conveying mechanism 211 is connected to the bottom slag discharge port of the fluidized bed furnace 2, and the outlet of the screw conveying mechanism 211 is connected to the collecting container 212, so as to convey the heavy carbon powder in the fluidized bed furnace 2 to the collecting container 212;

[0068] The carbon powder collecting device 2 31 includes a screw conveying mechanism 2 311 and a collecting container 2 312; the inlet of the screw conveying mechanism 2 311 is connected to the slag discharge port at the bottom of the cyclone separator 3, and the outlet of the screw conveying mechanism 2 311 is connected to the collecting container 2 312 to convey the light carbon powder in the cyclone separator 3 to the collecting container 2 312.

[0069] The spiral conveying mechanism 211 is used to control the heavy carbon slag or carbon powder in the fluidized bed furnace 2 to be input from the bottom slag discharge port thereof to the collecting container 212 for centralized storage, so as to facilitate the manual centralized removal of the heavy carbon slag or carbon powder as a reducing agent from the collecting container 212 and add it to the adsorbent regeneration device 9 for utilization, thereby realizing the high-value utilization of pyrolytic carbon; the spiral conveying mechanism 2 311 is used to control the light carbon powder in the cyclone separator 3 to be transported from the bottom slag discharge port thereof to the collecting container 2 312 for centralized storage, so as to facilitate the centralized removal and use as a porous carbon electrode material for supercapacitors.

[0070] Specifically, the slag discharge port at the bottom of the fluidized bed furnace 2 and the slag discharge port at the bottom of the cyclone separator 3 are both equipped with valves 12 for opening and closing the slag discharge ports.

[0071] In some embodiments, a hood 22 is disposed in the fluidized bed furnace 2 .

[0072] N2 can be introduced into the fluidized bed furnace 2 through a hood 22 disposed in the furnace to maintain an inert atmosphere in the furnace.

[0073] Specifically, the hood 22 is installed at the bottom of the fluidized bed furnace 2 .

[0074] In some embodiments, the condensing device 5 includes a condenser 51 and an oil storage tank 52; the inlet of the condenser 51 is connected to the outlet of the catalytic cracking device 4 through a pipeline, and the outlet of the condenser 51 is connected to the inlet of the adsorption device 6 through a pipeline; the oil storage tank 52 is connected to the condenser 51 through a pipeline to collect oil.

[0075] The condenser 51 can liquefy the condensable pyrolysis gas to obtain light bio-oil and store it in the oil storage tank 52 for centralized recycling; the non-condensable pyrolysis gas is transported from the outlet of the condenser 51 to the adsorption device 6 for purification treatment for easy utilization.

[0076] In some embodiments, the catalyst bed 41 includes a mounting frame 411 and a mesh tube 412 mounted on the mounting frame 411; the mounting frame 411 is detachably connected to the catalytic cracking device 4; the inner cavity of the mesh tube 412 is filled with catalyst, the mouth of the mesh tube 412 is a catalyst access port, and a valve 4121 is provided at the mouth of the mesh tube 412, and the valve 4121 is a T-type valve; the catalyst bed 41 and the adsorbent bed 61 have the same structure.

[0077] The inner cavity of the mesh tube of the catalyst bed 41 and the adsorbent bed 61 is used to fill the catalyst or adsorbent; the mesh tube can achieve full contact between the catalyst, adsorbent and pyrolysis gas; by designing the mounting frame 411 as a detachable structure, it can be easily taken out and placed in the adsorbent regeneration device 9 for reduction of the catalyst and adsorbent, so as to facilitate reuse.

[0078] Specifically, the catalyst bed 41 is inserted into the catalytic cracking device 4 by horizontal sliding. After the side wall door of the catalytic cracking device 4 is opened, the catalyst bed 41 can be pulled out. The adsorbent bed 61 is inserted into the adsorption device 6 by horizontal sliding. After the side wall door of the adsorption device 6 is opened, the adsorbent bed 61 can be pulled out. The catalyst and the adsorbent are put in and taken out through the pipe opening of the mesh tube 412 at the side wall of the corresponding mounting frame 411; the catalyst and the adsorbent are both formed catalysts 4122, and the size of the formed catalyst 4122 is larger than the mesh size of the mesh tube 412.

[0079] In some embodiments, the catalyst in the catalyst bed 41 and the adsorbent in the adsorbent bed 61 are both carbide slag.

[0080] Calcium carbide slag is an industrial waste residue produced after calcium carbide is hydrolyzed to obtain acetylene gas, and its main components are Ca(OH)2 and calcium oxide. Using industrial waste calcium carbide slag as the bed material of the catalyst bed 41 and the adsorbent bed 61 can achieve efficient resource utilization of industrial waste.

[0081] In some embodiments, the outer wall of the pipeline connecting the fluidized bed furnace 2 and the cyclone separator 3 and the outer wall of the pipeline connecting the cyclone separator 3 and the catalytic cracking device 4 are both coated with thermal insulation materials.

[0082] Another embodiment of the present invention provides a method for co-producing biomass gas, charcoal and oil based on microwave rapid pyrolysis, using a device for co-producing biomass gas, charcoal and oil based on microwave rapid pyrolysis; the specific steps include:

[0083] Step 1: adding biomass into the fluidized bed furnace 2, and pyrolyzing the biomass in the fluidized bed furnace 2; controlling the reaction temperature in the fluidized bed furnace 2 by a microwave generator 1; collecting heavy carbon powder discharged from the slag discharge port of the fluidized bed furnace 2 by a carbon powder collecting device 21;

[0084] Step 2: The pyrolysis gas generated in the fluidized bed furnace 2 carries the light carbon powder into the cyclone separator 3 to separate the light carbon powder, the carbon powder in the cyclone separator 3 is secondary heated by the microwave generator 1, and the carbon powder discharged from the slag discharge port of the cyclone separator 3 is collected by the second carbon powder collecting device 31 to serve as a porous carbon electrode material for making a supercapacitor;

[0085] Step 3: The pyrolysis gas in the cyclone separator 3 is transported to the catalytic cracking device 4, and the reaction temperature in the catalytic cracking device 4 is controlled by the microwave generator 1. The pyrolysis gas is catalytically reformed through the catalyst bed 41 and then transported to the condensing device 5 to obtain bio-oil liquid;

[0086] Step 4: purifying the non-condensable pyrolysis gas output from the condensing device 5 through the adsorbent bed 61 of the adsorption device 6; and inputting the purified non-condensable pyrolysis gas into the pressure swing adsorption device 7 for separation and purification to obtain combustible synthesis gas;

[0087] Step 5: inputting the combustible synthesis gas into the SOFC power generation device 8 to generate electricity; using the electricity generated by the SOFC power generation device 8 to power the microwave generator 1 and the adsorbent regeneration device 9;

[0088] Step six: Take out the used catalyst bed 41 and adsorbent bed 61 and put them into the adsorbent regeneration device 9, add the heavy carbon powder collected in the carbon powder collection device 21 as a reducing agent into the adsorbent regeneration device 9, and decompose and reduce the used catalyst bed 41 and adsorbent bed 61; the adsorbent regeneration device 9 generates CO gas which is sent to the SOFC power generation device 8 for power generation.

[0089] In some embodiments, in step 2, an activator is added to the cyclone separator 3 through the activator feeding mechanism 10, and the light carbon powder is separated and activated simultaneously; and the separated carbon powder and the activator are secondary activated at the bottom of the cyclone separator.

[0090] The carbon powder that has undergone secondary activation in the cyclone separator 3 can be used as a porous carbon electrode material for making supercapacitors, thereby achieving high-value utilization of pyrolytic carbon.

[0091] Specifically, the activator is a typical metal salt, such as any one of ZnCl2, K2CO3 and KHCO3.

[0092] In some embodiments, the pyrolysis temperature of the fluidized bed furnace 2 is controlled at 400-600°C; the temperature in the cyclone separator 3 is controlled at 650°C-750°C; the decomposition temperature of the pyrolysis gas in the catalytic cracking device 4 is controlled at 650°C-750°C; and the reaction temperature in the adsorbent regeneration device 9 is controlled at 750°C-850°C.

[0093] By controlling the temperature in the fluidized bed furnace 2, the cyclone separator 3 and the catalytic cracking device 4 through the microwave generator 1, flexible, stable and precise temperature control can be achieved.

[0094] Specifically, the temperature in the cyclone separator 3 can be controlled at 700°C; the decomposition temperature of the pyrolysis gas in the catalytic cracking device 4 is controlled at 700°C; and the reaction temperature in the adsorbent regeneration device 9 is controlled at 800°C.

[0095] Specifically, the inner wall of the cyclone separator 3 is coated with a coating made of corrosion-resistant material; the microwave generator 1 is installed on the outer wall at the bottom of the cyclone separator 3 to heat the carbon powder and activator separated and gathered at the bottom of the cyclone separator 3.

[0096] In some embodiments, the biomass enters the furnace of the fluidized bed furnace 2 through the spiral feed device 11, and the biomass is rapidly pyrolyzed in the fluidized bed furnace 2. The wind cap 22 at the bottom of the fluidized bed furnace 2 introduces N2 to maintain an inert atmosphere in the furnace. The reaction temperature of the fluidized bed furnace 2 is controlled at 400°C. The high-temperature pyrolysis gas generated in the fluidized bed furnace 2 carries the light carbon powder into the cyclone separator 3; the activator is selected as ZnCl2, and the activator is fed into the cyclone separator 3 through the activator feeder. The bottom of the cyclone separator 3 is provided with a corrosion-resistant coating, and the heavy carbon powder in the furnace is transported from the slag discharge port at the bottom of the furnace to the collection container 212 through the spiral conveying mechanism 1 211. In the cyclone separator 3, the carbon powder is secondary heated by the microwave generator 1. The bottom temperature of the cyclone separator 3 is controlled to be maintained at 700°C, and the valve 12 at the slag discharge port at the bottom of the cyclone separator 3 is opened every 30 minutes, and the carbon powder is sent to the collection container 2 312 through the spiral conveying mechanism 2 311. The outlet of the high-temperature pyrolysis gas of the cyclone separator 3 is connected to the inlet of the catalytic cracking device 4, and the reaction temperature of the catalytic cracking device 4 is controlled to be 700°C by the corresponding microwave generator 1; the pyrolysis gas is catalytically reformed through the catalyst bed 41 filled with carbide slag and then passed into the condenser 51, and finally the bio-oil discharged from the condenser 51 is collected by the oil storage tank 52. The non-condensable gas is purified by the adsorbent bed 61 filled with carbide slag and then merged into the pressure swing adsorption device 7 (PSA device) to separate and purify the combustible gas (H2 and CO); the high-purity synthesis gas is generated by the SOFC power generation device 8, and the generated electricity is used as the auxiliary energy of the microwave generator 1 and the adsorbent regeneration device 9. The catalyst bed 41 and the adsorbent bed 61 are taken out from the catalytic cracking device 4 and the adsorption device 6 respectively, and placed in the adsorbent regeneration device 9, the used catalyst and adsorbent are reduced in the adsorbent regeneration device 9, and the carbon slag or carbon powder in the collection container 212 is used as a reducing agent. The CO generated in the adsorbent regeneration device 9 is sent to the SOFC power generation device 8 for power generation.

[0097] In some embodiments, the biomass enters the furnace of the fluidized bed furnace 2 through the spiral feed device 11, and the biomass is rapidly pyrolyzed in the fluidized bed furnace 2. The wind cap 22 at the bottom of the fluidized bed furnace 2 introduces N2 to maintain an inert atmosphere in the furnace. The reaction temperature of the fluidized bed furnace 2 is controlled at 500°C. The high-temperature pyrolysis gas generated in the fluidized bed furnace 2 carries the light carbon powder into the cyclone separator 3; the activator is K2CO3, and the activator is fed into the cyclone separator 3 through the activator feeder. The bottom of the cyclone separator 3 is provided with a corrosion-resistant coating, and the heavy carbon powder in the furnace is transported from the slag discharge port at the bottom of the furnace to the collection container 212 through the spiral conveying mechanism 1 211. In the cyclone separator 3, the carbon powder is secondary heated by the microwave generator 1. The bottom temperature of the cyclone separator 3 is controlled to be maintained at 700°C, and the valve 12 at the slag discharge port at the bottom of the cyclone separator 3 is opened every 30 minutes, and the carbon powder is sent to the collection container 2 312 through the spiral conveying mechanism 2 311. The outlet of the high-temperature pyrolysis gas of the cyclone separator 3 is connected to the inlet of the catalytic cracking device 4, and the reaction temperature of the catalytic cracking device 4 is controlled to be 700°C by the corresponding microwave generator 1; the pyrolysis gas is catalytically reformed through the catalyst bed 41 filled with carbide slag and then passed into the condenser 51, and finally the bio-oil discharged from the condenser 51 is collected by the oil storage tank 52. The non-condensable gas is purified by the adsorbent bed 61 filled with carbide slag and then merged into the pressure swing adsorption device 7 (PSA device) to separate and purify the combustible gas (H2 and CO); the high-purity synthesis gas is generated by the SOFC power generation device 8, and the generated electricity is used as the auxiliary energy of the microwave generator 1 and the adsorbent regeneration device 9. The catalyst bed 41 and the adsorbent bed 61 are taken out from the catalytic cracking device 4 and the adsorption device 6 respectively, and placed in the adsorbent regeneration device 9, the used catalyst and adsorbent are reduced in the adsorbent regeneration device 9, and the carbon slag or carbon powder in the collection container 212 is used as a reducing agent. The CO generated in the adsorbent regeneration device 9 is sent to the SOFC power generation device 8 for power generation.

[0098] In some embodiments, the biomass enters the furnace of the fluidized bed furnace 2 through the spiral feed device 11, and the biomass is rapidly pyrolyzed in the fluidized bed furnace 2. The wind cap 22 at the bottom of the fluidized bed furnace 2 introduces N2 to maintain an inert atmosphere in the furnace. The reaction temperature of the fluidized bed furnace 2 is controlled at 600°C. The high-temperature pyrolysis gas generated in the fluidized bed furnace 2 carries the light carbon powder into the cyclone separator 3; the activator is KHCO3, and the activator is fed into the cyclone separator 3 through the activator feeder. The bottom of the cyclone separator 3 is provided with a corrosion-resistant coating, and the heavy carbon powder in the furnace is transported from the slag discharge port at the bottom of the furnace to the collection container 212 through the spiral conveying mechanism 211. In the cyclone separator 3, the carbon powder is secondary heated by the microwave generator 1. The bottom temperature of the cyclone separator 3 is controlled to be maintained at 700°C, and the valve 12 at the slag discharge port at the bottom of the cyclone separator 3 is opened every 30 minutes, and the carbon powder is sent to the collection container 2 312 through the spiral conveying mechanism 2 311. The outlet of the high-temperature pyrolysis gas of the cyclone separator 3 is connected to the inlet of the catalytic cracking device 4, and the reaction temperature of the catalytic cracking device 4 is controlled to be 700°C by the corresponding microwave generator 1; the pyrolysis gas is catalytically reformed through the catalyst bed 41 filled with carbide slag and then passed into the condenser 51, and finally the bio-oil discharged from the condenser 51 is collected by the oil storage tank 52. The non-condensable gas is purified by the adsorbent bed 61 filled with carbide slag and then merged into the pressure swing adsorption device 7 (PSA device) to separate and purify the combustible gas (H2 and CO); the high-purity synthesis gas is generated by the SOFC power generation device 8, and the generated electricity is used as the auxiliary energy of the microwave generator 1 and the adsorbent regeneration device 9. The catalyst bed 41 and the adsorbent bed 61 are taken out from the catalytic cracking device 4 and the adsorption device 6 respectively, and placed in the adsorbent regeneration device 9, the used catalyst and adsorbent are reduced in the adsorbent regeneration device 9, and the carbon slag or carbon powder in the collection container 212 is used as a reducing agent. The CO generated in the adsorbent regeneration device 9 is sent to the SOFC power generation device 8 for power generation.

[0099] In the description of this specification, the description with reference to the terms "one embodiment", "some embodiments", "example", "specific example", or "some examples" etc. means that the specific features, structures, materials or characteristics described in conjunction with the embodiment or example are included in at least one embodiment or example of the present invention. In this specification, the schematic representations of the above terms do not necessarily refer to the same embodiment or example. Moreover, the specific features, structures, materials or characteristics described may be combined in any one or more embodiments or examples in a suitable manner. In addition, those skilled in the art may combine and combine different embodiments or examples described in this specification.

[0100] Although the embodiments of the present invention have been shown and described above, it is to be understood that the above embodiments are exemplary and are not to be construed as limitations of the present invention. A person skilled in the art may change, modify, replace and vary the above embodiments within the scope of the present invention.

Claims

1. A device for co-production of biomass gas, charcoal and oil based on microwave rapid pyrolysis, characterized in that: include: A microwave generator (1), and a fluidized bed furnace (2), a cyclone separator (3), a catalytic cracking device (4), a condensing device (5), an adsorption device (6), a pressure swing adsorption device (7), a SOFC power generation device (8), and an adsorbent regeneration device (9) which are sequentially connected via pipelines; There are a plurality of microwave generators (1), and the fluidized bed furnace (2), the cyclone separator (3) and the catalytic cracking device (4) are all provided with a microwave generator (1) for controlling the reaction temperature; A first carbon powder collecting device (21) is provided at the bottom slag discharge port of the fluidized bed furnace (2); a second carbon powder collecting device (31) is provided at the bottom slag discharge port of the cyclone separator (3); The catalytic cracking device (4) is provided with a detachable catalyst bed (41); the adsorption device (6) is provided with a detachable adsorbent bed (61); the carbon slag in the carbon powder collecting device (21) is added to the adsorbent regeneration device (9) as a reducing agent, and the used catalyst bed (41) and the adsorbent bed (61) are transferred to the adsorbent regeneration device (9) for decomposition and reduction; the gas outlet of the adsorbent regeneration device (9) transports the combustible gas to the SOFC power generation device (8) through a pipeline to generate electricity; The SOFC power generation device (8) is electrically connected to the microwave generator (1) and the adsorbent regeneration device (9) to supply power.

2. The device for co-production of biomass gas, charcoal and oil based on microwave rapid pyrolysis according to claim 1, characterized in that: It also comprises an activator feeding mechanism (10), wherein the activator feeding mechanism (10) is connected to and communicates with a pipeline communicating between the fluidized bed furnace (2) and the cyclone separator (3) so as to transport the activator into the cyclone separator (3).

3. The device for co-production of biomass gas, charcoal and oil based on microwave rapid pyrolysis according to claim 1, characterized in that: The carbon powder collecting device (21) comprises a screw conveying mechanism (211) and a collecting container (212); the inlet of the screw conveying mechanism (211) is connected to the bottom slag discharge port of the fluidized bed furnace (2), and the outlet of the screw conveying mechanism (211) is connected to the collecting container (212) so as to convey the heavy carbon powder in the fluidized bed furnace (2) to the collecting container (212); The second carbon powder collecting device (31) comprises a second screw conveying mechanism (311) and a second collecting container (312); the inlet of the second screw conveying mechanism (311) is connected to the bottom slag discharge port of the cyclone separator (3), and the outlet of the second screw conveying mechanism (311) is connected to the second collecting container (312) so as to convey the light carbon powder in the cyclone separator (3) to the second collecting container (312).

4. The device for co-production of biomass gas, charcoal and oil based on microwave rapid pyrolysis according to claim 1, characterized in that: The fluidized bed furnace (2) is provided with a hood (22).

5. The device for co-production of biomass gas, charcoal and oil based on microwave rapid pyrolysis according to claim 1, characterized in that: The condensing device (5) comprises a condenser (51) and an oil storage tank (52); the inlet of the condenser (51) is connected to the outlet of the catalytic cracking device (4) through a pipeline, and the outlet of the condenser (51) is connected to the inlet of the adsorption device (6) through a pipeline; the oil storage tank (52) is connected to the condenser (51) through a pipeline to collect oil.

6. The device for co-production of biomass gas, charcoal and oil based on microwave rapid pyrolysis according to claim 1, characterized in that: The catalyst bed (41) comprises a mounting frame (411) and a mesh tube (412) mounted on the mounting frame (411); the mounting frame (411) is detachably connected to the catalytic cracking device (4); the inner cavity of the mesh tube (412) is filled with catalyst, and the tube opening of the mesh tube (412) is a catalyst taking-in and putting-out opening; The catalyst bed (41) and the adsorbent bed (61) have the same structure.

7. The device for co-production of biomass gas, charcoal and oil based on microwave rapid pyrolysis according to claim 1, characterized in that: The catalyst in the catalyst bed (41) and the adsorbent in the adsorbent bed (61) are both carbide slag.

8. A biomass gas, charcoal and oil co-production method based on microwave rapid pyrolysis, characterized in that: Using the device for biomass gas, charcoal and oil co-production based on microwave rapid pyrolysis according to any one of claims 1 to 7; the specific steps include: Step 1: adding biomass into a fluidized bed furnace (2), and pyrolyzing the biomass in the fluidized bed furnace (2); controlling the reaction temperature in the fluidized bed furnace (2) by means of a microwave generator (1); and collecting heavy carbon powder discharged from a slag discharge port of the fluidized bed furnace (2) by means of a carbon powder collecting device (21); Step 2: The pyrolysis gas generated in the fluidized bed furnace (2) carries the light carbon powder into the cyclone separator (3) to separate the light carbon powder, the carbon powder in the cyclone separator (3) is reheated by the microwave generator (1), and the carbon powder discharged from the slag discharge port of the cyclone separator (3) is collected by the second carbon powder collecting device (31) to serve as a porous carbon electrode material; Step 3: The pyrolysis gas in the cyclone separator (3) is transported to the catalytic cracking device (4), the reaction temperature in the catalytic cracking device (4) is controlled by the microwave generator (1), and the pyrolysis gas is catalytically reformed through the catalyst bed (41) and then transported to the condensing device (5) to obtain bio-oil liquid; Step 4: purifying the non-condensable pyrolysis gas output from the condensing device (5) through the adsorbent bed (61) of the adsorption device (6); and inputting the purified non-condensable pyrolysis gas into the pressure swing adsorption device (7) for separation and purification to obtain combustible synthesis gas; Step 5: inputting the combustible synthesis gas into the SOFC power generation device (8) to generate electricity; utilizing the electric energy generated by the SOFC power generation device (8) to power the microwave generator (1) and the adsorbent regeneration device (9); Step 6: The used catalyst bed (41) and adsorbent bed (61) are taken out and placed in an adsorbent regeneration device (9), and the heavy carbon powder collected in the carbon powder collection device (21) is added to the adsorbent regeneration device (9) as a reducing agent to decompose and reduce the used catalyst bed (41) and adsorbent bed (61); the CO gas generated by the adsorbent regeneration device (9) is sent to the SOFC power generation device (8) for power generation.

9. The biomass gas, charcoal and oil co-production method based on microwave rapid pyrolysis according to claim 8, characterized in that: In step 2, an activator is added to the cyclone separator (3) through an activator feeding mechanism (10), and the light carbon powder is separated and activated simultaneously; and the separated carbon powder and activator are secondary activated at the bottom of the cyclone separator.

10. The biomass gas, charcoal and oil co-production method based on microwave rapid pyrolysis according to claim 9, characterized in that: The pyrolysis temperature of the fluidized bed furnace (2) is controlled at 400-600°C; the temperature in the cyclone separator (3) is controlled at 650-750°C; the decomposition temperature of the pyrolysis gas in the catalytic cracking device (4) is controlled at 650-750°C; and the reaction temperature in the adsorbent regeneration device (9) is controlled at 750-850°C.

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