Device for realizing negative carbon emission and co-production of lime

Abstract

The utility model discloses a device for realizing negative carbon emission and co-production of lime, which can be used for feeding high-temperature CO2 waste gas produced by a lime kiln into a CO2 conversion device to be converted into CO gas, dedusting and purifying the high-temperature CO2 waste gas in a calcining zone of the lime kiln and then feeding the high-temperature CO2 waste gas into a fuel generation conversion device to be converted into combustible gas containing CO. The combustible gas obtained through conversion is fed into the lime kiln to be combusted and heat is supplied to calcine the limestone, so that the high-temperature CO2 waste gas in lime production is used as a heat source and is subjected to decarburization conversion with biomass waste carbon or other carbon-containing fuel through a one-step method to generate the combustible gas and co-produce the lime; by applying the device disclosed by the invention, the problems of high external energy consumption, long conversion time and high conversion cost for converting CO2 into CO can be solved, the efficient industrialization realization of a negative carbon technology is promoted, and the aims of saving energy, reducing emission, replacing fossil fuel and realizing value-added, zero carbonization and negative carbonization are fulfilled.

Description

Technical Field

[0001] The present application relates to the field of lime kiln technology, in particular to the recovery and application of CO2 in lime kilns, and specifically to a device that can reduce production energy consumption, simplify production process flow, and achieve negative carbon emissions and co-produce lime. Background Art

[0002] Carbon dioxide resources can be comprehensively utilized through the following approaches: (1) conversion of carbon dioxide into useful chemicals; (2) production of organic compounds through electrochemical, photoelectrochemical, and photochemical reactions; (3) production of carbon dioxide polymers; (4) production of fuel carbon; and (5) supercritical carbon dioxide extraction. Supercritical CO2 extraction primarily utilizes the chemical inertness of CO2. However, the current technology for using CO2 as a reactant is not mature enough, and the conversion and utilization rate of CO2 is quite low.

[0003] At present, negative carbon technology is the key to achieving net zero carbon dioxide emissions and is also the most promising technology. It can integrate the technical points and advantages of multiple applications such as renewable resource utilization, clean energy production, and carbon dioxide emission reduction, and has huge advantages in creating and increasing negative carbon emissions.

[0004] Among these, carbon dioxide chemical utilization technology is the most typical negative carbon technology. Characterized by a chemical conversion process, it uses CO2 as a carbon and oxygen resource to convert it into other products, and is an industrial technology with certain emission reduction benefits. It not only directly consumes CO2 but also replaces traditional high-carbon raw materials, achieving both direct and indirect emission reduction effects.

[0005] In recent years, C1 chemistry ("C1 chemistry" refers to the chemical processes used to synthesize industrial products using carbon or substances containing a single carbon atom in their molecules, such as CO, CO2, CH4, and CH3OH) as raw materials) has made tremendous progress. CO2 is the cheapest and most abundant resource in the C1 family, and its utilization has naturally become a major topic of concern worldwide. Therefore, a currently feasible approach is to convert CO2 into CO fuel. This conversion method involves degrading CO2 into CO through pyrolysis at high temperatures (873K).

[0006] In traditional CO production methods, using carbon-containing fuels such as coke and coal to reduce CO2 to produce CO is a major production approach and important technology for converting CO2 into chemical raw materials and fuels. This process technology not only collects, captures and utilizes industrial exhaust containing CO2 gas, but also realizes the resource utilization of low-grade fuels such as coal powder and biomass powder.

[0007] At present, in many application research and production of CO production, regardless of whether coke or coal is used, the ideal reaction temperature in the gasification reaction of reducing CO2 is 900-1050℃. The higher the temperature, the shorter the reaction time required. However, the reduction process also requires heating the raw materials to a high temperature, which leads to the high energy consumption required for the above-mentioned CO2 reduction method in actual production. Moreover, the reduction method is carried out in steps, which leads to serious problems of heat loss and energy waste. At the same time, there are also problems such as irrational energy utilization, complex process flow and equipment, which seriously restrict the sustainable development of its technical application.

[0008] Therefore, considering the energy efficiency of the aforementioned CO2 conversion processes, external energy consumption is often required or the high energy consumption results in poor economic efficiency. To protect natural resources and the ecological environment, a sustainable CO2 energy conversion system must be sought. The inventors recognized that effective approaches include reducing energy consumption or achieving energy self-sufficiency by utilizing the production system's own energy and waste heat.

[0009] As a new energy source, biomass energy is known as the "fourth energy source." Furthermore, in new energy applications for industrial production, biomass gasification is considered one of the important ways to utilize biomass energy due to its economical and carbon-neutral nature. It is also one of the important green and clean energy sources for lime production. A series of thermochemical reactions during the biomass gasification process can convert biomass raw materials into gaseous fuels for production, or further into high-value-added renewable liquid fuels or chemicals. The core advantage of CO2 reforming and reduction synthesis gas in biomass gasification and production applications is carbon emission reduction and carbon recovery. This is achieved by recycling the CO2 gas generated after combustion in lime kilns and other industrial furnaces, and then reacting it with biomass solid fuel for water-gas conversion and catalytic conversion into combustible gas for industrial production.

[0010] However, the main challenge in the resource utilization of carbon dioxide is to overcome the strong stability of the carbon dioxide molecule. Breaking C=O requires high energy input. From a thermodynamic point of view, the C=O bond energy is 783kJ / mol, and high temperature (1600-2000K) and high pressure conditions are required to break C=O. Among the currently popular plasma methods, the core gas temperature of the microwave plasma can reach 5000K or even higher, and the temperature of the surrounding area can also reach above 3000K. Obviously, in the current lime production process (calcination temperature 890-1100℃), both the temperature and pressure environment and the energy consumption are unbearable. Therefore, it is urgent to propose a technical solution that can use the production system's own energy and waste heat energy to achieve energy self-sufficiency to meet the energy requirements of the CO2 conversion process, thereby reducing the energy consumption in the CO2 conversion process, achieving the goals of replacing fossil fuels, value-added, zero carbonization, and negative carbonization, and realizing sustainable development. Utility Model Content

[0011] The present application provides a device for achieving negative carbon emissions and co-producing lime, which is used to solve the problems of high external energy consumption, long conversion time and high conversion cost required for converting CO2 into CO by traditional negative carbon technology.

[0012] In order to achieve the above objectives, this application provides the following technical solutions:

[0013] The present application provides a device for achieving negative carbon emissions and co-producing lime, comprising a lime kiln, a CO2 conversion device, and / or a fuel generation and conversion device, wherein:

[0014] The lime kiln has a kiln top gas collecting pipe, which can send the CO2 gas produced by the lime kiln into the kiln top flue gas dust reduction and purification device for dust reduction and purification treatment, and the treated flue gas enters the CO2 conversion device through the descending flue gas conveying pipe;

[0015] The CO2 conversion device includes a low-temperature CO2 flue gas pressurizing device and a high-speed internal heating conversion device. The low-temperature CO2 flue gas pressurizing device is used to pressurize the CO2 gas received from the descending flue gas conveying pipeline, and the high-speed internal heating conversion device is used to convert the pressurized CO2 gas into CO gas, and the converted CO gas is sent into the kiln chamber of the lime kiln to be burned and heat to calcine limestone;

[0016] The fuel generation and conversion device is a closed structure with two sections, the upper section is the cracking section, and the lower section is the conversion section. The cracking section and the conversion section are connected and cut off by a hot air shut-off valve. The top of the cracking section is provided with a biomass fuel inlet and a CO2 gasifying agent inlet, the bottom of the cracking section is provided with a cracking gas outlet, the conversion section has a CO conversion gas outlet and an air pipeline for inputting air gasifying agent, the bottom of the conversion section is provided with a high-temperature CO2 gas inlet, the CO2 gasifying agent inlet and the high-temperature CO2 gas inlet are respectively connected to the air pipeline for inputting The pyrolysis section is connected to a pipeline for high-temperature CO2 waste gas coming out of the calcining zone of the lime kiln. The pyrolysis section is used to pyrolyze the biomass fuel and high-temperature CO2 waste gas fed thereinto into pyrolysis gas containing CO, and the cracked CO is output to the kiln chamber of the lime kiln through the pyrolysis gas outlet; the conversion section is used to receive the remaining biomass fuel (charcoal) after pyrolysis from the pyrolysis section and convert the high-temperature CO2 gas rising from its bottom into CO gas through the biomass fuel (charcoal), and the converted CO gas is output to the kiln chamber of the lime kiln through the CO conversion gas outlet.

[0017] Furthermore, in the above technical solution, the lime kiln is a double-bore vertical kiln or a single-bore vertical kiln.

[0018] Furthermore, a plurality of fuel spray guns are provided around the kiln body of the lime kiln, each of the fuel spray guns is connected to a lime kiln body fuel surrounding pipe provided on the outer wall of the kiln body, the fuel spray guns are used to spray combustible gas into the kiln chamber of the lime kiln, and the lime kiln body fuel surrounding pipe is used to receive the cracking gas discharged from the cracking gas outlet, the CO gas discharged from the CO conversion gas outlet 1, and the CO gas discharged from the CO2 conversion device.

[0019] Furthermore, a lime kiln flue gas circulation channel connected to the kiln chamber is provided on the outer wall of the lime kiln body. The lime kiln flue gas circulation channel is connected to the ash cleaning and conveying pipe through multiple pulse control valves. The ash cleaning and conveying pipe is connected to the ash cleaning and conveying pipeline. The high-temperature exhaust gas from the lime kiln calcining zone is sent into the high-temperature dust reduction device through the lime kiln flue gas circulation channel, pulse control valves, ash cleaning and conveying pipes and ash cleaning and conveying pipelines for dust reduction and purification treatment. The purified high-temperature CO2 exhaust gas is sent to the CO2 gasification agent inlet and the high-temperature CO2 gas inlet.

[0020] Furthermore, the low-temperature CO2 flue gas pressurizing device has a CO2 inlet end, a first CO2 outlet end and a second CO2 outlet end. The CO2 inlet end is connected to the descending flue gas conveying pipeline, the first CO2 outlet end is connected to the CO2 inlet of the high-speed internal heating conversion device through waste gas valve 1, and the second CO2 outlet end is connected to the waste gas external network pipeline 1 through waste gas valve 2.

[0021] Furthermore, the high-speed internal heating conversion device includes a high-speed internal heating conversion device shell, a graphite electrode body is arranged in the high-speed internal heating conversion device shell, the graphite electrode body has a hollow inner cavity, the hollow inner cavity is filled with spherical zirconium-based nano high-entropy porous ultra-high temperature catalytic material, a plurality of electrode vents are arranged on the side wall of the graphite electrode body, and the electrode vents are connected to the high-speed internal heating conversion device shell; the graphite electrode body is electrically connected to the transformer, and the transformer is used to energize the graphite electrode body when the gas passes through the graphite electrode body; the converted CO enters the high-speed internal heating conversion device shell through the electrode vents, and enters the CO delivery pipeline 2 through the CO conversion gas outlet 2 on the high-speed internal heating conversion device shell, and then enters the lime kiln chamber through the lime kiln body fuel surrounding pipe, the CO conversion gas outlet 2 is connected to the CO delivery pipeline 2 through the hot air valve 4, and the CO delivery pipeline 2 is connected to the lime kiln body fuel surrounding pipe.

[0022] Furthermore, the CO2 conversion device also includes a low-speed external heating conversion device, in which several layers of catalysts are arranged in sequence from bottom to top, and the gaps and particle sizes of the catalysts at different levels decrease step by step from bottom to top.

[0023] Furthermore, the several layers of catalyst include a first-level Fe fiber wool catalyst, a first-level heat storage particle catalyst, a second-level Fe fiber wool catalyst, a second-level heat storage particle catalyst, a third-level Fe fiber wool catalyst, a third-level heat storage particle catalyst and a fourth-level Fe fiber wool catalyst, which are arranged in sequence from bottom to top.

[0024] Furthermore, the low-speed external heating conversion device has a first CO inlet, which is close to the bottom of the low-speed external heating conversion device. The first CO inlet is connected to the CO conversion gas outlet of the high-speed internal heating conversion device through a CO conversion gas connecting channel, and a hot air valve five is provided on the CO conversion gas connecting channel.

[0025] Furthermore, a second CO inlet is provided at the bottom of the low-speed external heating conversion device, and the second CO inlet is connected to the high-temperature CO2 gas delivery pipe 2 through the hot air valve 2, and the high-temperature CO2 gas delivery pipe 2 is connected to the high-temperature CO2 gas delivery pipe 1, and the high-temperature CO2 gas delivery pipe 1 is connected to the gas outlet of the high-temperature dust reduction device.

[0026] Furthermore, the high-temperature CO2 gas delivery pipeline 1 is connected to the CO2 gasification agent inlet through the high-temperature CO2 gas delivery pipeline 3, and the high-temperature CO2 gas delivery pipeline 3 is provided with a hot air valve 3; one end of the high-temperature CO2 gas delivery pipeline 1 is connected to the high-temperature CO2 gas inlet through the hot air valve 1.

[0027] Furthermore, a high-temperature electromagnetic induction heating device, a medium-temperature electromagnetic induction heating device and a low-temperature electromagnetic induction heating device are sequentially arranged on the outer wall of the low-speed external heating conversion device from bottom to top. The heating power supplies of the three electromagnetic induction heating devices are respectively controlled by an electronic control device. The three electromagnetic induction heating devices are used to heat the gas in the low-speed external heating conversion device.

[0028] Furthermore, a CO output port is provided at the top of the low-speed external heating conversion device, and the CO output port is connected to the CO delivery pipeline 1 through a CO control valve, and the CO delivery pipeline 1 is connected to the CO delivery pipeline 2 through the cracked gas output pipeline.

[0029] Furthermore, a main pulverized coal spray gun is provided on the top of the fuel generation and conversion device, and a steam gasification agent inlet and a fuel inlet are provided on the main pulverized coal spray gun. An air inlet is opened on the side wall of the fuel generation and conversion device close to the cracking section. A pulverized coal surrounding pipe is provided on the top of the cracking section, and the pulverized coal surrounding pipe is connected to the inner cavity of the cracking section through multiple pulverized coal auxiliary nozzles. The cracking section is divided into a drying layer, a pyrolysis layer, an oxidation layer and a reduction layer from top to bottom.

[0030] Furthermore, three layers of regulating blowing ports are provided on the outer wall of the conversion section from top to bottom, each regulating blowing port is connected to the inner cavity of the conversion section, and each regulating blowing port is connected to a high-temperature CO2 gas delivery pipeline three, and the high-temperature CO2 gas delivery pipeline three performs auxiliary blowing on the conversion section through the regulating blowing port.

[0031] Furthermore, multiple layers of air gasification agent regulating blowing ports are provided on the outer wall of the conversion section from top to bottom, each of the air gasification agent regulating blowing ports is connected to air duct 2, air duct 2 is connected to air duct 1, and air duct 1 is connected to the outlet end of the air pressurizing device.

[0032] Furthermore, the CO gas converted in the conversion section is delivered to the CO delivery pipeline 3 through the CO conversion gas outlet 1, and the CO delivery pipeline 3 is connected to the CO delivery pipeline 2 through the cracked gas output pipeline.

[0033] Furthermore, an ash outlet is formed below the conversion section, and the ash outlet is provided with a heat-resistant rotary sealed ash discharger, which is used to discharge the carbon ash after the biomass fuel is converted into a closed ash storage bin below.

[0034] Furthermore, the ash storage bin is connected to the air pressurizing device through a pipeline, and the air pressurizing device can pneumatically convey the carbon ash in the ash storage bin to the pneumatic conveying ring pipe. The pneumatic conveying ring pipe is connected to the ash storage bin through multiple interfaces, and the pneumatic conveying ring pipe is connected to the lower ash bin of the high-temperature dust reduction device through the pneumatic ash conveying pipeline. A screw conveyor is arranged under the high-temperature dust reduction device, and the screw conveyor is used to convey the fly ash discharged from the high-temperature dust reduction device to the belt conveyor of the ash discharge system at the bottom of the lime kiln.

[0035] Furthermore, the ash storage bin is provided with a water inlet and a water outlet, and water is injected into the ash storage bin through the water inlet and the water level is maintained at the target liquid level position. A slurry pump is provided at the water outlet, and the mixture of carbon ash and water is sucked out by the slurry pump.

[0036] Compared with the prior art, this application has at least the following beneficial effects:

[0037] 1. The present application provides a device for achieving negative carbon emission and co-production of lime. The device can send the high-temperature CO2 gas generated by the production of calcium oxide in the lime kiln into a CO2 conversion device to convert it into CO gas, and / or, send the high-temperature CO2 waste gas from the lime kiln calcination zone into a fuel generation conversion device after dust removal and purification to convert it into a combustible gas containing CO, and send the CO gas converted from the CO2 conversion device and / or the combustible gas containing CO generated from the fuel generation conversion device into the lime kiln for combustion and heat supply to calcine limestone. That is, the present application utilizes the high-temperature CO2 waste gas in lime production as a heat source. The method is to decarbonize and transform biomass waste carbon or other carbon-containing fuels (coal, coke) to generate CO-containing combustible gas that can be used for production and co-produce lime, thereby realizing the conversion and reuse of CO2 waste gas from the lime kiln. Therefore, the device for achieving negative carbon emissions and co-producing lime provided by this application can utilize the high-temperature CO2 waste gas in lime production as a heat source, solving the problems of high external energy consumption, long conversion time and high conversion cost required for traditional negative carbon technology to convert CO2 into CO, promoting the efficient industrialization of negative carbon technology, achieving energy conservation and emission reduction, replacing fossil fuels, and realizing the goals of value-added, zero carbonization and negative carbonization.

[0038] 2. The CO2 conversion device and fuel generation conversion device in this application use graphite electrodes and electromagnetic induction to react with cheap iron-based and zirconium-containing catalysts with CO2 waste gas to generate CO fuel gas for recycling, thereby achieving complete conversion and reuse of CO2 waste gas. This can not only offset the increased electricity cost of electrolysis of CO2, but also significantly reduce the fuel cost of lime production, while also achieving the goal of "negative carbon" emissions of CO2.

[0039] 3. The present application uses biomass solid fuel as energy to provide a carbon and hydrogen source, and the fuel of the carbon and hydrogen source is prepared by catalytic cracking to calcine lime. The high-temperature biochar comes into contact with the high-temperature CO2 waste gas from the lime kiln to produce a reduction reaction. The CO produced can be returned to the lime kiln as fuel to be burned again to calcine lime. That is, the present application can convert more than 90% of the biochar produced in the biomass catalytic cracking process into CO2 fuel, and at the same time, all the waste gas containing about 40% CO2 produced when calcining lime is converted into CO2 fuel, which can achieve the purpose of recycling and converting biochar waste carbon, and also effectively reduce the fuel cost of lime production and carbon emission reduction.

[0040] 4. The fuel generation and conversion device in the present application adopts a two-stage structure, with the upper cracking section (i.e., the reduction device) and the lower conversion section (i.e., the synthesis device) arranged in series up and down. The upper cracking section uses biomass solid fuel as raw material and uses a composite series of coal and biomass to produce fuel gas rich in CO and H2 gas through high-temperature cracking. The lower conversion section uses the high-temperature hot biochar after cracking in the cracking section as the carbon source and heat source. By inputting high-temperature exhaust gas from the lime kiln circulation channel for C1 conversion, more than 90% of the biomass fuel can be converted into CO combustible gas; the external heat source of the lower conversion section is provided by the sensible heat of high-temperature CO2 gas in the range of 1000-1100°C produced by the circulation channel in the middle of the lime kiln chamber, which can greatly reduce the energy consumption required for conversion. Not only does it not require an external energy heat source, but it can also release the carbon energy in the greenhouse gas CO2 and convert it into coal gas energy mainly composed of CO+H2.

[0041] 5. The present application mainly uses biomass fuel, and also provides a way and method of gasifying dry coal powder as raw material (fuel). The reaction temperature can be as high as 1300-1600°C, and it has good adaptability to coal types, can gasify a wide range of coal types, and has low requirements for ash content. Ash content below 30% can be gasified. During the gasification process, the carbon conversion rate is high and no organic pollutants are generated. The process meets the requirements of clean and efficient utilization of coal and environmental protection. The present application adopts a dry coal powder coupled with biomass composite serial method to realize the co-gasification of pulverized coal and biomass composite serial, that is, to achieve high-temperature gasification, and also solve the defects of low calorific value of biomass fuel and low furnace temperature. It is also convenient to realize gasification furnace temperature control and reduce energy consumption and improve efficiency, and also realize the functions of independent use of biomass and independent use of coal powder for production.

[0042] 6. The high-speed internal heating conversion device in the CO2 conversion device in the present application is achieved by arranging a replaceable spherical solid inside the hollow graphite electrode. The high-entropy porous boride catalytic composite material is synthesized with zirconium oxide and zirconium phosphate materials as catalyst carriers and BaTiO3 and ultra-high temperature boride ceramic materials as auxiliary agents. The presence of the filler material increases the gas residence time, enhances the electric field strength and electron energy; and the electric field strength at the contact point of the spherical material is enhanced, the voltage is increased, and more micro-discharges are generated, thereby generating more plasma charges and micro-discharge filaments during discharge; in the conversion process, the factors affecting the conversion rate include the relative dielectric constant, porosity, and surface roughness of the filler material; materials with high porosity and large surface roughness help to enhance the electric field and generate higher current density, thereby improving the CO2 conversion rate and energy efficiency. In addition, the CO2 conversion device of the present application has a simple structure, good airtightness, no dead corners, and is conducive to uniform gas distribution and circulation. CO2 can be directly converted into CO and O2 in the reactor device.

[0043] 7. The low-speed external heating conversion device in the CO2 conversion device of the present application is designed as a filling device, which adopts a pipeline container structure. A certain height of flocculent catalyst and granular solid reactants are set inside the container to ensure that the flow velocity changes when the airflow flows through, thereby forming eddy currents and turbulence. The flocculent catalyst carrier is Fe fiber fleece, and the solid reactant is alumina particles containing zirconium and other components. An electromagnetic induction heating device is set outside the low-speed external heating conversion device. High-frequency magnetic lines are generated in the induction coil in the device, which generate eddy currents on the surface of the conductor workpiece in the induction coil. The heat is generated by self-generated internal resistance, and the heat is transferred to the device material through contact conduction. On the cylinder, the Fe fiber catalyst and the solid reactant carrier inside are heated to the catalytic temperature through the device barrel. When the CO2 gas flows through this area, it is instantly heated to the catalytic temperature, and the CO2 gas is quickly converted into CO gas. The low-speed external heating conversion device in this application has a simple structure, good airtightness, and no dead angle, which is conducive to uniform gas distribution and circulation. The heating temperature is controlled by an external electrical control box connected to the electromagnetic induction heating device. The heating area is segmented, and the power of each area (segment) can be adjusted. The temperature, protection and start-stop are automatically controlled, which improves the overall adaptive automation level of the device and can adapt to the needs of industrial production. BRIEF DESCRIPTION OF THE DRAWINGS

[0044] In order to more clearly illustrate the technical solutions in the embodiments of the present application, the following briefly introduces the drawings required for use in the embodiments. Obviously, the drawings described below are only some embodiments of the present application. For ordinary technicians in this field, other drawings can be obtained based on these drawings without creative work. It should be understood that the specific shapes and structures shown in the drawings should not generally be regarded as limiting conditions for implementing the present application; for example, based on the technical concepts and exemplary drawings disclosed in this application, those skilled in the art are able to easily make routine adjustments or further optimizations to the addition / reduction / attribution division, specific shapes, positional relationships, connection methods, and dimensional ratios of certain units (components).

[0045] Figure 1 This is a schematic diagram of the overall structure of a device for achieving negative carbon emissions and co-producing lime provided by the present application in one embodiment;

[0046] Figure 2 for Figure 1 A display diagram of the drawing in part A;

[0047] Figure 3 for Figure 1 The illustration of the diagram in part B;

[0048] Figure 4 This is a schematic diagram of the overall structure of the fuel generation and conversion device in this application in one embodiment;

[0049] Figure 5 for Figure 4 The display diagram of the drawing in part C;

[0050] Figure 6 for Figure 4 The display diagram of the D part;

[0051] Figure 7 This is a schematic diagram of the overall structure of the CO2 conversion device in this application in one embodiment.

[0052] Description of reference numerals:

[0053] 1. Double-chamber vertical kiln device for lime kiln;

[0054] 2. Fuel generation and conversion device; 2-1. Cracking section; 2-2. Conversion section; 2-3. Biomass fuel inlet; 2-4. CO2 gasifier inlet; 2-5. Pulverized coal main lance; 2-5-1. Steam gasifier inlet; 2-5-2. Pulverized coal surrounding pipe; 2-5-3. Pulverized coal auxiliary nozzle; 2-5-4. Fuel inlet; 2-5-5. Air inlet; 2-6. Hot air shut-off valve; 2-6-1. Cutting and crushing mechanism; 2-7. Pyrolysis gas outlet; 2-8. CO conversion gas Outlet 1; 2-9, high-temperature CO2 gas inlet; 2-10, heat-resistant rotary sealed ash discharger; 2-11, air pressurizing device; 2-12, pneumatic conveying loop pipe; 2-13, slurry pump; 2-14, ash storage bin; 2-14-1, upper sealing plate; 2-14-2, lower sealing plate; 2-14-3, target liquid level; 2-15, air duct 1; 2-15-1, air duct 2; 2-15-2, air gasification agent regulating nozzle; 2-16, water inlet;

[0055] 3. CO2 conversion device; 3-1. Low-temperature CO2 flue gas pressurizing device; 3-2. High-speed internal heating conversion device; 3-2-1. High-speed internal heating conversion device housing; 3-3. Low-speed external heating conversion device; 3-4. Graphite electrode body; 3-4-1. Transformer; 3-5. Electrode vent; 3-6. Zirconium-based nano-high entropy porous ultra-high temperature catalytic material; 3-7. CO conversion gas outlet 2; 3-8. CO conversion gas connecting channel; 3-9. Hot air valve 4; 3-10. Hot air valve 5; 3-11. First-stage Fe fiber velvet catalyst; 3-12, first-stage thermal storage particle catalyst; 3-13, second-stage Fe fiber velvet catalyst; 3-14, second-stage thermal storage particle catalyst; 3-15, third-stage Fe fiber velvet catalyst; 3-16, third-stage thermal storage particle catalyst; 3-17, fourth-stage Fe fiber velvet catalyst; 3-18, high-temperature electromagnetic induction heating device; 3-19, medium-temperature electromagnetic induction heating device; 3-20, low-temperature electromagnetic induction heating device; 3-21, electronic control device; 3-22, CO conversion gas outlet three;

[0056] 4. Kiln roof gas collecting pipe; 5. Kiln roof flue gas dust reduction and purification device; 6. Descending flue gas conveying pipe; 7. CO conveying pipe 1; 8. CO conveying pipe 2; 9. Lime kiln body fuel surrounding pipe; 10. Fuel spray gun; 11. CO conveying pipe 3; 12. Cracking gas output pipe; 13. Lime kiln flue gas circulation channel; 14. Pulse control valve; 15. Ash cleaning conveying surrounding pipe; 16. Ash cleaning conveying pipe; 17. High-temperature dust reduction device; 18. High-temperature CO2 gas conveying pipe 1; 19. Screw conveyor; 20. High-temperature CO2 gas conveying pipe 2; 21. High-temperature CO2 gas conveying pipe 3; 21-1. Adjustable blowing port; 22. Hot air valve 1; 23. Hot air valve 2; 24. Hot air valve 3; 25. Pneumatic ash conveying pipe; 26. Exhaust gas valve 1; 27. Exhaust gas valve 2; 28. CO control valve; 29. ​​Exhaust gas external network pipe 1. DETAILED DESCRIPTION

[0057] The following specific embodiments illustrate the implementation of this application. Those familiar with the art can easily understand the other advantages and functions of this application from the content disclosed in this specification. Obviously, the described embodiments are part of the embodiments of this application, but not all of them. Based on the embodiments in this application, all other embodiments obtained by ordinary technicians in this field without making creative efforts are within the scope of protection of this application.

[0058] The present application will be further described below in detail through specific embodiments in conjunction with the accompanying drawings.

[0059] In the description of this application: unless otherwise specified, "plurality" means two or more. Terms in this application such as "pipeline one" and "pipeline two" are intended to distinguish the objects referred to and do not have any special meaning in terms of technical connotation (for example, they should not be understood as emphasizing the degree of importance or order, etc.). Expressions such as "including", "comprising", and "having" also mean "not limited to" (certain units, components, materials, steps, etc.).

[0060] Terms such as "upper," "lower," "left," "right," and "center" used in this application are generally intended to facilitate intuitive understanding when compared with the accompanying drawings and are not intended to be absolute limitations on positional relationships in actual products. Changes to these relative positional relationships are considered within the scope of this application without departing from the technical concepts disclosed herein.

[0061] In order to solve the problems existing in the prior art, the inventors proposed that the development of applicable heating and catalytic methods and high-performance catalysts is the key to solving the above problems, combining the requirements of lime production process, CO2 conversion conditions, and various energy supply methods. Common catalytic research systems can be divided into: electrocatalysis, thermal catalysis, photocatalysis, and a combination of the three. Graphite heating is a technology commonly used in heating, smelting, and sublimation processes, which can play an important role in different catalytic research systems. On this basis, the inventors proposed that graphite can be used as a resistive heating material. When electricity is applied, the resistance generates heat energy, thereby heating the surrounding objects. In addition, the inventors also proposed that electromagnetic induction self-heating technology can be used. Electromagnetic induction is a technology based on high-frequency alternating magnetic fields to generate induced eddy currents or relaxation oscillations inside ferromagnetic and paramagnetic materials, thereby achieving material self-heating. It has the advantages of fast heating speed and precise energy transmission.

[0062] The present application provides a method for producing lime by utilizing high-temperature CO2 waste gas from lime production as a heat source without adding external energy and heat. The method decarbonizes the waste carbon from biomass or other carbon-containing fuels (coal, coke) in a one-step process and converts it into C1 new energy. The method also utilizes graphite electrodes and electromagnetic induction to react with the CO2 waste gas with inexpensive iron-based and zirconium-containing catalysts to generate CO2 fuel gas for recycling, thereby achieving complete conversion and reuse of the CO2 waste gas, replacing fossil fuels, increasing value, and achieving zero carbonization and negative carbonization. The technical route of the present application is described below:

[0063] Route 1: Using solid biomass fuel as an energy source to provide a hydrocarbon source, the fuel is first catalytically cracked to produce a hydrocarbon source (primarily CO and H2) for lime calcination. This calcination process produces high-temperature CO2 waste gas at 950-1200°C, enriched in 25-42% CO2. During the biomass catalytic cracking process, a high-temperature biochar (waste carbon) ranging from 8-40% (adjustable) is produced. This high-temperature biochar is then reacted with the equally high-temperature CO2 waste gas from the lime kiln exhaust recirculation system in a sealed reactor for a reduction reaction. By manipulating the reaction temperature, reaction time, and waste gas flow rate, high-quality CO2 gas fuel is produced. The resulting CO2 is then returned to the lime kiln for further combustion in lime calcination. This route converts over 90% of the biochar produced during the biomass catalytic cracking process into CO2 fuel, while also converting approximately 40% of the CO2 waste gas produced during lime calcination into CO2 fuel. This not only recycles and converts the biochar waste carbon, but also effectively reduces fuel costs and carbon emissions in lime production.

[0064] Route 2: In order to balance and convert the CO2 gas generated by re-combustion, an electrolytic reduction reaction device is set up, using low-cost iron-based and zirconium-containing catalysts, and generating induced eddy currents through graphite electrode method + electromagnetic induction heating, thereby achieving self-heating of the material and converting the remaining CO2 into CO combustible gas for lime calcination production.

[0065] Therefore, this application can fully recover the CO2 gas in lime production through the above-mentioned route 1 and route 2 and convert it into combustible gas fuel with C1 as the main component, which can not only offset the increased electricity cost of electrolysis of CO2, but also significantly reduce the fuel cost of lime production, while also achieving the goal of CO2 "negative carbon" emissions.

[0066] The process technology means and measures adopted in this application are described in detail below.

[0067] 1. Reaction mechanism of water gas (cracking gasification)

[0068] Carbon monoxide (CO) and hydrogen (H2) are both combustible gases. This mixture is called "water gas" in industry. This is because a water (H2O) molecule contains one oxygen (O) atom and two hydrogen (H) atoms. When water meets hot coal (C), the oxygen atom is immediately captured by the coal (C), resulting in the formation of carbon monoxide (CO) and hydrogen (H2).

[0069] Water gas is a low-calorific value coal gas, traditionally produced by reacting steam with hot carbon-containing fuels (such as coal or coke) or biomass. This application uses solid biomass fuels instead of coal or coke to produce water gas. The main components are hydrogen and carbon monoxide, and in actual production, it may also contain small amounts of carbon dioxide, nitrogen, and methane. The content of each component depends on the raw materials used and the gasification conditions.

[0070] In the gasifier, the carbon in the biomass fuel and the steam mainly undergo the following water-gas reaction:

[0071] C+H2O→CO+H2

[0072] C+2H2O→CO2+2H2

[0073] The above reactions are all endothermic reactions, so heat must be supplied to the gasifier.

[0074] 2. Reverse Water Gas Shift (RWGS) Reaction Mechanism

[0075] The RWGS reaction is the reverse reaction of the water-gas shift (WGS) reaction. CO2 can be converted into more active CO gas through the RWGS reaction.

[0076] The reverse water-gas shift reaction equation is as follows:

[0077] CO2+H2=CO+H2OΔH 0 298 =+42.1KJ / mol

[0078] This reaction is a reversible, endothermic, equimolar reaction, and high temperatures favor the reverse water-gas shift reaction. Optimal conditions for the RWGS reaction are selected to achieve optimal reaction performance. In this application, the key to regulating reaction conditions is controlling the molar ratio of CO₂ to H₂ in the reaction gas under atmospheric conditions.

[0079] Experiments have shown that the catalyst temperature gradient has a crucial influence on the RWGS reaction. In practice, ideal reaction conditions are achieved when the temperature is between 80°C and 400°C, the pressure is between 1 atm (0.101 MPa) and 18 atm (1.81 MPa), and the gas flow rate is a 1:1 molar ratio of H2 to CO2.

[0080] 3. Application of electromagnetic induction heating technology

[0081] Electromagnetic induction is a technology that uses a high-frequency alternating magnetic field to generate induced eddy currents or relaxation oscillations inside ferromagnetic and paramagnetic materials, thereby achieving self-heating of the materials. It has the advantages of fast heating speed and precise energy transmission.

[0082] The use of electromagnetic induction heating technology to drive the selective reduction of CO2 to produce CO can achieve electron enrichment on the catalyst surface in a high-frequency electromagnetic environment. The electron-rich surface of the catalyst helps to activate CO2 molecules, thereby promoting the reaction along a path with lower activation energy.

[0083] 4. Application of new low-cost iron-based catalytic materials

[0084] In the method of reducing CO2 to CO by electromagnetic induction heating, the present invention uses Fe fiber fleece as a catalyst carrier to prepare a monolithic catalytic material, and utilizes Ru 3+ Ruthenium nanoparticles (RuNPs) are modified onto the surface of Fe fibers through a replacement reaction with metallic Fe. Crucially, Fe fiber fleece is a common and inexpensive abrasive for mechanical polishing. Furthermore, the fibers' self-supporting structure makes the catalyst structure strong and easy to shape. This allows for the formation of a monolithic catalytic material, effectively reducing gas resistance and meeting the practical needs of industrial applications.

[0085] 5. Application of Graphite Electrode Heating Plasma Conversion to CO2 Technology

[0086] Plasma is the fourth state of matter. It is a collection of particles such as electrons, ions, atoms (ground state or excited state), molecules (ground state or excited state), and free radicals formed by the dissociation and ionization of gas molecules by heat or external electric fields, radiation, and other energy excitations. The plasma mentioned in this application is mainly produced by gas discharge ionization. During the discharge, free electrons gain energy from the given electric field and then lose energy by colliding with neutral gas molecules. The molecules gain energy and produce chemical substances such as metastable molecules, atoms, free radicals, and ions.

[0087] Graphite electrode is a high-temperature resistant graphite conductive material made from petroleum coke and pitch coke as aggregates and coal tar as binder, through the process of raw material calcination, crushing and grinding, batching, kneading, molding, roasting, impregnation, graphitization and mechanical processing. In addition, the melting point of graphite is 3850±50℃ and the boiling point is 4250℃. Even after ultra-high arc burning, the weight loss is very small and the thermal expansion coefficient is also very small. In particular, the strength of graphite increases with increasing temperature. At 2000℃, the strength of graphite doubles, making it very suitable for the high temperature (1600-2000K) conditions and environment required for CO2 pyrolysis.

[0088] 6. Application of zirconium-based nano-high entropy porous ultra-high temperature catalytic materials

[0089] The high-entropy porous boride catalytic composite material synthesized with zirconium oxide and zirconium phosphate materials as catalyst carriers and BaTiO3 and ultra-high temperature boride ceramic materials as additives has the characteristics of high temperature resistance, large specific surface area and surface charge density, and can be used for ion exchange; it also has strong thermal stability, chemical stability and mechanical strength, and strong acid and alkali resistance; in particular, its high-entropy porous and stable layered structure is not destroyed after the guest is introduced into the interlayer, and as a mesoporous material carrier, different metal ions and organics can continue to be embedded into it, further improving the activity and selectivity of the original catalyst.

[0090] In particular, the ultra-high temperature boride ceramic material YB4 has a melting point of up to 2800°C, and its oxidation product is Y2O3, which also has a melting point of up to 2145°C. In addition, YB4 also has a low density (4.36g / cm 3 ) and a low elastic modulus (350GPa). It fully meets the high temperature (1600-2000K) conditions and environment required for CO2 pyrolysis.

[0091] 7. CO2 to CO temperature balance control

[0092] The reaction of CO2 reducing CO adopts the Boudouard method, and the reaction formula is:

[0093] CO2+C=2CO-162.4Mj / kmol

[0094] During the reaction, the key factors affecting the reduction rate are temperature and the quality of the carbon source. Carbon sources are typically biomass (charcoal), coke, or coal (anthracite). The reduction rate is directly proportional to temperature. At low temperatures below 800°C, the reaction time often exceeds tens of seconds or even longer, making it difficult to achieve equilibrium in the reduction reaction. The ideal controlled temperature range is 1000°C to 1100°C. At 1000°C, the CO2-to-CO conversion rate can reach over 99%, and at 1100°C, the conversion rate approaches 100%. The CO2 conversion rates at different temperatures are shown in Table 1 below.

[0095] Table 1 Conversion rates of CO2 and CO at different temperatures

[0096] Temperature (℃) 450 600 700 750 800 850 900 1000 1100 <![CDATA[CO2(%)]]> 98.1 65.3 42.6 23.9 11.9 5.7 3.1 0.85 0.06 CO (%) 1.9 34.7 57.4 76.1 88.1 94.3 96.9 99.15 99.94

[0097] When the reaction temperature is at the optimal reaction temperature of 1100°C, the properties of the carbon source (fuel) are also critical to the reaction rate of CO2 reduction of CO. Table 2 below lists the reaction activity and reaction rate of different fuel properties.

[0098] Table 2 Comparison of reactivity and reaction rate of different fuel properties

[0099] Time (seconds) 0 5 10 15 20 25 30 35 40 Charcoal (co%) 40-88 92-100 Coke (co%) 40-50 63-74 74-85 85-90 90-93 93-94 94-95 95 95 Coal (co%) 40-65 64-73 74-78 78-82 82-83 83 83 83

[0100] The data in the table show that charcoal can complete 88% CO conversion within 5 seconds and 100% CO conversion within 10 seconds, while coke has a CO conversion rate of only 40-50% within 5 seconds, a conversion rate of only 74-85% within 10 seconds, and a maximum conversion rate of only 95% within 40 seconds. Coal does not convert CO within 5 seconds, has a conversion rate of only 64-72% within 10 seconds, and a maximum conversion rate of only 82% within 40 seconds. Therefore, in terms of both reaction activity and reaction speed, charcoal > coke > coal. Therefore, this application prefers charcoal (biomass) as the carbon source.

[0101] 8. Coal and Biomass Serial Composite Gasification

[0102] Coal gasification, a key component of clean coal conversion and utilization, is also the most effective path for clean and efficient coal conversion. The combined gasification of coal and biomass fuels fully leverages the unique characteristics of both energy sources, effectively enhancing and improving the quality of syngas. It also overcomes challenges associated with traditional biomass gasification processes, achieving clean and efficient utilization of both biomass and coal resources.

[0103] This application mainly uses biomass fuel, and also provides a way and method of gasifying by using dry coal powder as raw material (fuel). The reaction temperature is as high as 1300℃~1600℃, and it has good adaptability to coal types, can gasify a wide range of coal types, and has low requirements for ash content. Any coal with an ash content of less than 30% can be gasified. During the gasification process, the carbon conversion rate is high and no organic pollutants are generated. Its process meets the requirements of clean and efficient utilization of coal and environmental protection. In this application, the dry coal powder is coupled with biomass composite serial to achieve the co-gasification of pulverized coal and biomass composite serial, that is, to achieve high-temperature gasification, and also solve the defects of low calorific value and low furnace temperature of biomass fuel. It is also convenient to realize gasifier temperature control and reduce energy consumption and improve efficiency, and also realize the functions of independent use of biomass and independent use of coal powder for production.

[0104] The energy conversion benefits brought about by this application are analyzed and calculated below.

[0105] 1. Energy conversion from charcoal directly to CO

[0106] The traditional biomass gasification process can produce 8-40% waste carbon residue (charcoal) after gasification, which cannot be consumed by the biomass itself and needs to be exported or processed. This wastes resources, increases environmental protection management, and also results in low energy conversion efficiency.

[0107] In this application, the charcoal residue produced during the gasification process is directly converted in the furnace, and the C1 component in the charcoal is fully converted into CO gas through the high-temperature thermochemical reaction of CO2 / charcoal. On average, 1 kg of charcoal (waste carbon) can produce 3.50 m 3 More than CO gas fuel.

[0108] According to the calculation of heat energy in lime production, the theoretical energy consumption of one ton of ash is 890,000Kcal heat energy. The conversion of biomass heat energy (maximum 4200Kcl / kg) requires 210kg of biomass fuel, which can produce 45kg (average) of charcoal after gasification. According to 1kg of charcoal, 3.50m3 of 3 (Average) CO can be calculated as:

[0109] 45kg×3.50m 3 =157.5m 3 / ton ash

[0110] According to the calorific value of carbon monoxide (gas) 3500~4700Kcal / Nm 3 (air pressure is 1.0Kpa) calculation, the heat energy can be obtained:

[0111] 157.5m 3 / ton ash×(3500~4700Kcal / Nm 3 )=551250~740250Kcal

[0112] According to the calculation that one ton of ash requires 890,000Kcal of heat energy: 551,250~740,250Kcal / 890,000Kcal

[0113] The available energy is 0.62 to 0.83 tons of ash heat.

[0114] 2. Utilization of waste carbon thermal energy

[0115] In the traditional gasification process, when waste carbon is discharged from the furnace, it needs to be water-quenched in the furnace to achieve the purpose of liquid slag discharge. This not only consumes a large amount of water resources and wastes a lot of thermal energy resources, but also causes water pollution and is difficult to manage for environmental protection.

[0116] This application utilizes a high-temperature (900-1100°C) conversion method in the lower section (synthesis section) of the furnace. This fully recovers and utilizes the charcoal's own heat from the upper section of the furnace and the sensible heat of the converted raw coal gas, resulting in high thermal efficiency. Furthermore, by fully utilizing the sensible heat of the high-temperature (1000-1200°C) CO2 waste gas from the lime kiln circulation channel for C1 conversion, over 98% of the charcoal can be converted to CO gas, while achieving "zero" external energy supply. Because the majority of the waste carbon is converted, only 2-5% of carbon-free ash (i.e., the ash in the raw material) is discharged, compared to the 8-40% waste carbon slag produced in traditional gasification processes.

[0117] 3. Energy Balance of CO2 to CO

[0118] The chemical equation for the reduction of carbon monoxide (coal gas) by carbon dioxide is:

[0119] C+1 / 2O2=CO+110.5kJ

[0120] C+O2=CO2+393.5kJ

[0121] CO + 1 / 2O2 = CO2 + 283 kJ

[0122] From the Gays' law, we know that: combining the first and second equations above and eliminating the O2 term (i.e., equation 1×2-equation 2), we get: C+CO2=2CO-172.5kJ

[0123] Therefore, it can be concluded that 1 mol of C reacts with 1 mol of CO2 and absorbs 172.5KJ of heat.

[0124] Calculate the energy cost required to convert 1 ton of CO2 using the formula:

[0125] Conversion energy = reaction molar energy * 10^6 / molecular molar mass

[0126] Substituting the molar mass of CO2 as 44g / mol, it is calculated that the energy required to convert 1 ton of CO2 into CO and H2O is 3900000KJ (equivalent to 932100Kcal).

[0127] Energy of converted CO:

[0128] The calorific value of CO is 12.64MJ / Nm 3 , converted into mass calorific value is 10.112MJ / kg, equal to 10112KJ / kg, equivalent to 10112000KJ per ton (equivalent to: 2416768Kcal).

[0129] 4. Recovery of high-temperature CO2 energy from lime kiln

[0130] A large amount of high-temperature CO2 waste gas waste heat output from the waste gas circulation channel of the lime kiln calcining zone is directly converted into CO with charcoal without gas separation. The mass ratio of CO2 to charcoal is 3.62:1, that is, it is converted into synthesis gas mainly composed of CO+H2. The thermal energy in the conversion process comes from the sensible heat of the CO2 waste gas at a temperature of 900-1300℃ in the lime kiln. This temperature is the decomposition temperature of the lime calcined in the lime kiln, which is exactly the cracking temperature required for CO2 to convert to CO. The reaction time is determined by the CO2 waste gas temperature, flow rate, and the height of the carbon reaction layer, and is generally adjusted within 5-40 seconds.

[0131] The following describes the key equipment and measures used to implement the production process of this application.

[0132] 1. Lime kiln calcining device

[0133] An off-kiln channel-supported double-chamber lime kiln with dual functions of mixing and blowing disclosed in the Chinese utility model patent CN202321555958.8 authorized by the applicant on November 17, 2023 can be used as a production device for producing lime (calcium oxide) and CO2 gas.

[0134] 2. Fuel generation and conversion device (segmented serial reduction integrated generation device)

[0135] The device adopts a two-stage structure, with an upper reduction device (cracking section, i.e., a reducing gas generating device) and a lower synthesis device (conversion section, i.e., a synthesis gas device) arranged in series up and down. The upper reduction gas generating device uses biomass solid fuel as raw material and adopts a composite series of coal and biomass to produce CO and H2-rich fuel gas through high-temperature cracking. The lower synthesis gas device uses the high-temperature hot biochar after cracking of the reducing gas generating device as a carbon source and heat source. By inputting high-temperature exhaust gas from the lime kiln circulation channel for C1 conversion, more than 90% of the charcoal can be converted into CO combustible gas.

[0136] The external heat source of the synthesis gas device in the lower section is provided by the sensible heat of high-temperature CO2 gas in the range of 1000-1100℃ produced by the circulation channel in the middle of the lime kiln, which greatly reduces energy consumption. Not only does it not require an external energy heat source, but it can also release the carbon energy in the greenhouse gas CO2 and convert it into coal gas energy mainly composed of CO+H2.

[0137] 3. High-speed internal heating conversion device (internal heating electrolysis CO2 conversion CO device)

[0138] The device's heating method utilizes hollow graphite electrodes. The graphite core of the graphite electrodes is composed of carbon atoms, exhibiting excellent electrical and thermal conductivity and high-temperature resistance. Thermal conductivity is crucial for graphite heating, effectively transferring heat energy to surrounding objects, heating them. When current is applied to the electrodes, resistance is generated, generating heat energy that heats the surrounding objects. Furthermore, graphite's strong infrared absorption capacity allows it to absorb high-intensity infrared radiation, enabling rapid heating of surrounding objects, a key factor in its effectiveness in the heating process.

[0139] Inside the hollow graphite electrode, a replaceable, spherical solid is placed. This high-entropy porous boride catalytic composite material, synthesized using zirconium oxide and zirconium phosphate as catalyst carriers and BaTiO3 and ultra-high-temperature boride ceramic materials as additives, is synthesized. The presence of the filler material increases gas residence time, enhancing the electric field strength and electron energy. Furthermore, the electric field strength and voltage at the contact points of the spherical material increase, generating more microdischarges and, consequently, more plasma charges and microdischarge filaments during discharge. During the conversion process, factors such as the filler material's relative dielectric constant, porosity, and surface roughness influence the conversion rate. Materials with high porosity and surface roughness help enhance the electric field, generating higher current density, thereby improving CO2 conversion and energy efficiency.

[0140] The conversion method utilizes plasma catalysis technology, which uses any combination of plasma and catalyst to improve the conversion rate of reactants, the selectivity of target products, and enhance energy efficiency. Adding a catalyst to the reaction system enhances the plasma reaction and activates the catalyst within the plasma region. In the CO2 conversion process, the primary purpose of adding a catalyst is to improve the energy efficiency of the reaction.

[0141] When the reaction gas CO2 passes through the inside of the electrode, when a sufficiently high voltage is applied to the electrode, the gas is broken down, forming a discharge channel that enables the plasma to produce a large number of high-energy active particles, and the discharge is uniform and stable. The high-energy active particles are activated and catalyzed by a high-entropy porous boride catalytic composite material synthesized with zirconium oxide and zirconium phosphate materials as catalyst carriers and BaTiO3 and ultra-high temperature boride ceramic materials as auxiliary agents, which is arranged inside the hollow graphite electrode, thereby achieving a thorough cracking of CO2 and generating CO gas. The reactor of the present application has a simple structure, good airtightness, no dead angles, and is conducive to uniform gas distribution and circulation. CO2 can be directly converted into CO and O2 in the reactor device.

[0142] 4. Low-speed external heating conversion device (externally heated adjustable CO2 electromagnetic induction conversion CO reactor)

[0143] The reaction device adopts a filling device and a pipeline container structure. The interior of the container is filled with a certain height of filamentous catalyst and granular solid reactants, ensuring that the flow rate changes when the airflow flows through, thereby forming eddies and turbulence. The filamentous catalyst carrier is Fe fiber wool, and the solid reactant is alumina particles containing zirconium and other components. An electromagnetic induction heating device is set outside the reactor. The induction coil in the device generates high-frequency magnetic lines of force, which cause eddy currents to be generated on the surface of the conductor workpiece inside the induction coil and generate heat by self-generated internal resistance. The heat is transferred to the barrel by contact conduction, and then the internal Fe fiber wool catalyst and solid reactant carrier are heated to the catalytic temperature through the barrel. When CO2 gas flows through this area, it is instantly heated to the catalytic temperature and the CO2 gas is converted into CO gas. The reactor structure of the present application is simple, airtight, and has no dead angles, which is conducive to uniform gas distribution and circulation. The heating temperature is controlled by an external electric control box connected to the electromagnetic induction heating device. The heating area is segmented, the power of each area (segment) is adjustable, and the temperature, protection and start-stop are automatically controlled.

[0144] The structural principle and process flow of the solution provided in this application are described in detail below.

[0145] This application provides a device for achieving negative carbon emissions and co-producing lime, primarily comprising: a double-chamber vertical kiln unit 1, a fuel generation and conversion unit 2, and a CO2 conversion unit 3. The production process flow achieved using this device can be divided into three systems, enabling both integrated closed-loop production of all three systems and independent production of each system. These three systems are: a) an independent double-chamber vertical kiln production system; b) an independent fuel generation and conversion production system; and c) an independent CO2-to-CO production system.

[0146] The process principle of the closed-loop production of the three systems is as follows:

[0147] Limestone begins initial decomposition at 890°C in a double-chamber lime kiln and is completely decomposed at 950-1100°C. During the decomposition process, the limestone produces 35-44% carbon dioxide (CO2) gas. This gas enters the kiln's flue gas dust reduction and purification device through the lime kiln's top gas collection pipe. From there, it enters the CO2 conversion unit through the descending flue gas pipeline, where it converts the CO2 to CO. The converted CO2 gas then flows through the pipeline into the kiln's fuel enclosure pipe, where it is distributed to the fuel injection guns and transported to the kiln for combustion and heat to calcine the limestone. Pyrolysis gas produced by the fuel conversion unit also enters the kiln's fuel enclosure pipe through the CO2 pipeline, where it mixes with the CO gas and enters the fuel injection guns.

[0148] During the ash cleaning process, the 1100℃ high-temperature and high-pressure (30-35KPa) flue gas in the flue gas circulation channel of the lime kiln body is transported to the CO2 conversion device in the lower section of the fuel generation and conversion device through the ash cleaning conveying pipe, ash cleaning conveying pipeline and high-temperature dust suppression device to convert CO2 and waste carbon into CO. The generated CO fuel also enters the fuel pipe of the lime kiln body through the conveying pipeline, completing the entire closed-loop fuel conversion process.

[0149] A high-temperature powder ash collection device can be installed on the ash cleaning and conveying pipeline to collect lime powder (dust). After collection, the powder is transported by a screw conveyor to the belt conveyor below the ash discharge device at the bottom of the lime kiln, and transported together with the finished lime.

[0150] In the present application, the fuel generation and conversion device is a two-stage closed structure. The upper and lower sections are controlled by electric (or hydraulic, pneumatic) hot air shut-off valves, which can realize both composite serial production of the upper and lower sections and independent operation and production of the upper and lower sections. The upper section is a cracking device, which adopts a downdraft structure and is divided into four areas from top to bottom: drying layer, pyrolysis layer, oxidation layer, and reduction layer. The biomass fuel and the reducing gas are in a parallel downward flow mode, the pyrolysis layer temperature is controlled in the range of 500-600°C, and the final oxidation layer formation temperature can reach a high temperature of 1000°C.

[0151] The lower section, the generator, employs an updraft structure. Its feedstock is waste carbon, primarily solid granular biochar, generated after biomass pyrolysis in the upper section. Its entry into the lower section is controlled by a hot air shutoff valve between the upper and lower sections. Once in the lower section, the waste carbon slowly descends, undergoing countercurrent heat exchange with the rising CO2 reducing gas, converting it to CO. This conversion process requires no external heat source, deriving entirely from waste heat within the production system. This waste heat primarily comes from three sources: 1. 900-1000°C heat energy from the waste carbon itself; 2. 1100°C high-temperature CO2 waste gas from the lime kiln's flue gas circulation duct; and 3. The combined combustion temperature of these three sources precisely meets the required temperature for waste carbon conversion, achieving a balanced heat supply. The resulting waste carbon ash (furnace ash) represents only approximately 3% of the weight of the waste carbon before conversion. It flows through an ash discharger at the bottom of the fuel generator / conversion unit and into an ash storage bin. From there, it is transported by pneumatic conveying or a slurry pump to the lime kiln's bottom ash discharge system or other downstream devices.

[0152] The structure and main process flow of the solution provided in this application are described in detail below with reference to the accompanying drawings and specific embodiments.

[0153] Example 1

[0154] This application provides a device for achieving negative carbon emissions and co-producing lime. This device utilizes waste heat from a lime kiln, biomass waste carbon, graphite electrodes, and electromagnetic induction to directly produce CO2 fuel and co-produce lime. This example details the process flow for integrated closed-loop production using this device.

[0155] See also Figures 1 to 3 When lime is produced by the double-chamber vertical kiln device 1, the primary CO2 gas with a concentration of 35-44% is obtained and enters the kiln top flue gas dust reduction and purification device 5 through the kiln top gas collecting pipe 4 for dust reduction and purification treatment. The temperature of the treated flue gas is in the range of 70-250℃, and the particulate matter in the flue gas is less than 50mg / m 3 The flue gas enters the low-temperature CO2 flue gas pressurizing device 3-1 along the descending flue gas conveying pipe 6, and the pressurized CO2 gas enters the high-speed internal heating conversion device 3-2 for CO gas conversion. Figure 7During the conversion process, the gas first enters the graphite electrode body 3-4. The interior of the graphite electrode body 3-4 is hollow and filled with spherical zirconium-based nano-high entropy porous ultra-high temperature catalytic materials 3-6. A plurality of electrode vents 3-5 are provided on the electrode body. When the gas passes through the graphite electrode body 3-4, the transformer 3-4-1 energizes the graphite electrode body 3-4. After energization, the graphite electrode body quickly reaches a temperature greater than 1800°C within 1 to 2 seconds. At the same time, the zirconium-based nano-high entropy porous ultra-high temperature catalytic materials 3-6 in the graphite electrode body also reach the same temperature, catalyzing the CO2 gas and instantly converting it into a gas with a CO content greater than 90%. The converted gas enters the interior of the high-speed internal heating conversion device shell 3-2-1 through several electrode vents 3-5. See Figure 1 The gas then enters the CO delivery pipeline 2 8 through the CO conversion gas outlet 2 3-7, and then enters the kiln chamber (kiln chamber 1 and kiln chamber 2) of the lime kiln double-chamber vertical kiln device 1 through the lime kiln body fuel surrounding pipe 9.

[0156] When the converted CO gas needs to be further increased in content, it enters the low-speed external heating conversion device 3-3 through the CO conversion gas connection channel 3-8 for further conversion. Figure 7 Inside the low-speed external heating conversion device 3-3, there are arranged catalytic materials of different heights and quantities, such as a first-level Fe fiber fleece catalyst 3-11, a first-level heat storage particle catalyst 3-12, a second-level Fe fiber fleece catalyst 3-13, a second-level heat storage particle catalyst 3-14, a third-level Fe fiber fleece catalyst 3-15, a third-level heat storage particle catalyst 3-16, and a fourth-level Fe fiber fleece catalyst 3-17. The gaps and particle sizes of the catalysts at different levels are different, decreasing from bottom to top. Among them, the fiber fleece catalyst is a flocculent body of different diameters, and the heat storage particle catalyst is a round particle. The combination of the two objects forms a material space with different resistances to meet the gas residence time and heat storage and catalytic time. During the heating process, the gas passes through the entire interior of the container from bottom to top, and its gas flow, pressure, and opening and closing are controlled by hot air valve four 3-9 and hot air valve five 3-10. The overall heating of the low-speed external heating conversion device 3-3 is achieved by a three-stage heating device: a high-temperature electromagnetic induction heating device 3-18, a medium-temperature electromagnetic induction heating device 3-19, and a low-temperature electromagnetic induction heating device 3-20. The three-stage heating device is separate and gradually heats and regulates from bottom to top. It can also be heated in a single stage. Its heating power supply is controlled by an electronic control device 3-21. The content of CO gas after conversion can reach more than 99%. The converted CO gas fuel enters the CO delivery pipeline 2 8 through the CO conversion gas outlet 3 3-22 and the CO delivery pipeline 1 7.

[0157] The fuel (heat energy) required by the double-chamber vertical kiln device 1 comes from the fuel generation and conversion device 2, see Figures 4 to 6The fuel generation and conversion device 2 is configured as two areas with different functions, the cracking section 2-1 and the conversion section 2-2. The two areas control the material downward flow and opening and closing through the hot air shut-off valve 2-6. A cutting and crushing mechanism 2-6-1 is provided at the connection between the two areas.

[0158] Granular biomass fuel (which can be charcoal with a particle size of 30-100 mm) enters through biomass fuel inlet 2-3, CO2 gasifier enters through CO2 gasifier inlet 2-4, and steam gasifier enters through steam gasifier inlet 2-5-1. Steam gasifier inlet 2-5-1 serves as a backup and is used when pulverized coal gasification is employed. CO2 gasifier is the primary gasifier used in production. The biomass fuel entering through biomass fuel inlet 2-3 slowly descends, entering the drying layer, pyrolysis layer, oxidation layer, and reduction layer, from top to bottom. During the biomass fuel cracking process, the biomass fuel and reducing gas flow in parallel and downward. The main components of the cracked gas (average values ​​for different biomass fuels) are: 15.27% hydrogen, 3.12% oxygen, 56.22% nitrogen, 1.57% methane, 9.76% carbon monoxide, 13.75% carbon dioxide, 0.10% ethylene, 0.13% ethane, 0.03% propane, and 0.05% propylene, totaling 100%. The cracked gas enters the cracked gas output pipeline 12 from the cracked gas outlet 2-7 and is also transported to the CO delivery pipeline 8.

[0159] The remaining charcoal after cracking accounts for about 8 to 40% of the dry weight of the fuel (which can be adjusted according to the production process). It enters the upper part of the hot air shut-off valve 2-6 through the charcoal's own gravity and the positive pressure inside the device. Opening and adjusting different channel areas of the hot air shut-off valve 2-6 can control its descending speed and enter the conversion section 2-2. The charcoal slowly descends from top to bottom in the conversion section 2-2 and undergoes combustion heat exchange with the high-temperature CO2 waste gas in the range of more than 1000 to 1200°C from the high-temperature CO2 gas transmission pipeline 18. During the exchange process, the CO2 gas is converted into CO gas.

[0160] The conversion process uses air and CO2 gas as gasifying agents, adopts bottom blowing method, and high-temperature CO2 waste gas enters the device through high-temperature CO2 gas inlet 2-9. The high-temperature CO2 gasifying agent entering the conversion section 2-2 is high-temperature CO2 waste gas in the range of 950-1200℃, which comes from the high-temperature waste gas in the lime kiln calcining zone (i.e., the temperature of the lime kiln decomposing limestone). Figure 1 、 2The flue gas enters the ash cleaning and conveying pipe 15 through the lime kiln flue gas circulation channel 13 that is interconnected between the lime kiln body 1 and the kiln body 2. A plurality of pulse control valves 14 are arranged on the ash cleaning and conveying pipe 15 to communicate with the lime kiln flue gas circulation channel 13. The flue gas flow and pressure in the ash cleaning and conveying pipe 15 are controlled by controlling the opening number and opening and closing times of the pulse control valves 14. The flue gas then enters the ash cleaning and conveying pipe 16 and is conveyed to the high-temperature dust reduction device 17 for dust reduction and purification treatment. The purified high-temperature CO2 waste gas is conveyed to the CO2 gasification agent inlet 2-4 through the high-temperature CO2 gas conveying pipe 18. High-temperature CO2 gas delivery pipeline 1 18 is also provided with high-temperature CO2 gas delivery pipeline 2 20 and high-temperature CO2 gas delivery pipeline 3 21. High-temperature CO2 gas delivery pipeline 2 20 is controlled and regulated by hot air valve 2 23 to deliver a portion of the CO2 gas to the low-speed external heating conversion device 3-3 for conversion. The gas in high-temperature CO2 gas delivery pipeline 3 21 enters high-temperature CO2 gas delivery pipeline 3 21 through hot air valve 3 24, with a portion entering the CO2 gasifying agent inlet 2-4 and a portion entering the conversion section 2-2. Figure 3 The high-temperature CO2 gas transmission pipeline 3 21 is provided with three layers of regulating injection ports 21-1 at the upper, middle and lower levels to assist the injection of the conversion section 2-2 device, thereby achieving the purpose of regulation and optimization control. Figure 3 The air gasifier enters through the air pipe 1 2-15, and the air source is provided by the air pressurizing device 2-11. The air pipe 1 2-15 is provided with a branch pipe air pipe 2 2-15-1, and is also provided with upper, middle and lower three-layer adjustable blowing ports 2-15-2 for auxiliary blowing of air and oxygen.

[0161] The remaining charcoal ash (slag) after the charcoal is fully converted accounts for about 2 to 3% of the dry weight of the fuel. Its particle size is relatively fine and is discharged into the ash storage bin through the heat-resistant rotary sealed ash discharger 2-10. Figure 6 An upper sealing plate 2-14-1 is provided on the upper part of the ash storage bin, and a lower sealing plate 2-14-2 is provided on the lower part, forming an independent sealed space to ensure that gas and dust do not leak out. When pneumatically conveying dust, the high-pressure air source is provided by the air pressurizing device 2-11, which is blown into the ash storage bin through the pipeline, forming a high-pressure airflow of dust and gas mixed and boiling, and then blown into the pneumatic conveying ring pipe 2-12. The pneumatic conveying ring pipe 2-12 is provided with multiple interfaces connected to the ash storage bin 2-14, forming a pressure-equalized airflow that is discharged into the pneumatic ash conveying pipeline 25 and then enters the lower ash bin of the high-temperature dust reduction device 17. Together with the dust-removed surface ash, it is transported by the screw conveyor 19 to the upper part of the ash discharge belt at the bottom of the lime kiln, and then transported to the downstream system together with the finished lime. When the slurry ash discharge method is adopted, water is injected through the water inlet 2-16 and the water level is maintained at the target liquid level position 2-14-3, and then the slurry pump 2-13 is turned on to suck the mixture of carbon ash and water out of the device, and then stored or transported.

[0162] All CO gas that has completed the conversion process in the conversion section 2-2 is output from the CO conversion gas outlet 1 2-8 outside the device, enters the cracked gas output pipeline 12 through the CO delivery pipeline 3 11, and is mixed and then delivered to the CO delivery pipeline 2 8.

[0163] All the converted combustible gases enter the CO conveying pipe 2 8 for mixing, and the mixed gas enters the fuel surrounding pipe 9 of the lime kiln body, and then is sprayed into the double-bore vertical kiln device 1 of the lime kiln by several fuel injection guns 10 arranged around the lime kiln body to calcine the lime. The CO2 gas decomposed during the calcination process enters the gas collecting pipe 4 on the kiln top, and the powdered ash (dust) purified in the high-temperature dust reduction device 17 enters the screw conveyor 19 from its bottom, and is transported to the belt conveyor of the ash discharge system at the bottom of the lime kiln, and is transported to downstream users together with the finished lime. At this point, the production cycle of the entire system is completed.

[0164] Example 2

[0165] Based on a device for achieving negative carbon emission and co-production of lime provided in this application, this embodiment describes the process of using this device to carry out closed-loop production of a lime kiln double-chamber vertical kiln device 1 and a fuel generation and conversion device 2.

[0166] The CO2 outlet of the low-temperature CO2 flue gas pressurizing device 3-1 is connected to the CO2 inlet of the high-speed internal heating reformer 3-2 via an exhaust valve 26. A hot air valve 3-9 is installed at the CO2 reformed gas outlet 3-7 at the bottom of the high-speed internal heating reformer 3-2. The bottom of the low-speed external heating reformer 3-3 is connected to the high-temperature CO2 gas delivery pipeline 20 via a hot air valve 23. The top of the low-speed external heating reformer 3-3 is connected to the CO delivery pipeline 7 via a CO control valve 28.

[0167] In this embodiment, based on the process described in Example 1, the exhaust gas valve 1 26, the hot air valve 4 3-9, the hot air valve 2 23 and the CO control valve 28 are closed to stop the exhaust gas from entering the CO2 conversion device 3 and stop the output of CO gas, and the exhaust gas valve 2 27 is opened to allow the exhaust gas to enter the exhaust gas external network pipe 1 29 and then be discharged into a separately provided chimney or other emission facilities, so that the lime kiln double-chamber vertical kiln device 1 and the fuel generation and conversion device 2 form an independent closed-loop production system.

[0168] Example 3

[0169] Based on the device for achieving negative carbon emissions and co-producing lime provided in this application, this embodiment describes the process of using this device to produce synthesis gas in series by combining biomass and coal powder.

[0170] When the fuel generation and conversion device 2 is operating normally with biomass fuel, pulverized coal fuel is introduced into the furnace, and the coal and air undergo combustion reaction to release heat. This stage is mainly to increase the temperature in the furnace. First, the pulverized coal main spray gun 2-5, the pulverized coal surrounding pipe 2-5-2, the pulverized coal auxiliary nozzle 2-5-3, the fuel inlet 2-5-4 and the air inlet 2-5-5 are turned on to carry out composite serial production of pulverized coal injection and biomass fuel. When the temperature rises to the predetermined parameter, the air inlet 2-5-5 is closed to stop the air supply and the furnace is turned on. The CO2 gasifier inlet 2-4 and the steam gasifier inlet 2-5-1 are opened to cause a gasification reaction with the unburned coal char flowing downward, and then react with the pyrolyzed biomass char to produce medium-calorific value combustible gas rich in CO and H2. Since the gasification reaction is an endothermic reaction, the furnace temperature will gradually decrease. When the furnace temperature reaches the preset value, the system will open the air inlet 2-5-5 again to continue supplying air to increase the furnace temperature. In this way, the two-stage reciprocating cycle to produce gas constitutes a coal and biomass composite serial gasification process.

[0171] Example 4

[0172] Based on the device for achieving negative carbon emissions and co-producing lime provided in this application, this embodiment describes the process of independently using biomass fuel to produce cracking gas using this device.

[0173] In the process described in Example 3, the single-row gasification process using biomass fuel can be restored by closing the main pulverized coal lance 2-5, the pulverized coal surrounding pipe 2-5-2, the auxiliary pulverized coal nozzle 2-5-3, the fuel inlet 2-5-4 and the air inlet 2-5-5.

[0174] Compared with the prior art, the solution provided by this application has at least the following beneficial effects:

[0175] (1) This application uses biomass raw materials (charcoal) with "zero carbon" properties to gasify into CO2-based gas to produce lime, changing the production method of traditional lime shaft kilns using petrochemical energy such as anthracite or coke, and realizing the transformation of traditional energy to green energy application.

[0176] (2) The present application adopts the production of gasification gas and synthesis gas in the same device, which solves the problem that the traditional gasification process and coal gas production process require different devices, resulting in large equipment footprint, complicated process and high equipment cost. That is, it simplifies the production process flow and energy loss, and also greatly reduces equipment investment.

[0177] (3) This application realizes the composite serial cracking and gasification of biomass and coal by directly injecting coal powder and other fuels during the biomass gasification and cracking process, thereby achieving the purpose of multi-path application of fuel and realizing two functions in the same device, thereby achieving the purpose of reducing equipment investment.

[0178] (4) The present application uses the high-temperature CO2 gas in the lime kiln circulation channel as a high-calorific value gas fuel for reforming with biomass coke (charcoal) to generate CO, which not only saves the external heat energy consumption required in the conversion process, but also solves the problem of "black pollution" caused by the large amount of "waste coke" generated in the traditional biomass cracking production method that cannot be treated. This is one of the original innovation cores of the present application.

[0179] (5) Compared with traditional biomass gasifiers, due to the reforming effect of "waste charcoal", more than 95% of biomass fuel is gasified into high calorific value combustible gases such as CO, and the calorific value of the gas can be increased by more than 15%. The calorific value of biomass gas is increased from the original ≥1200Kcal / Nm 3 Increased to ≥1800Kcal / Nm 3 .

[0180] (6) In this application, since CO2 waste gas is converted into CO fuel and directly mixed with biomass cracking gas for lime calcination production, its calorific value is increased from ≥1800Kcal / Nm 3 Increase again to ≥3000Kcal / Nm of mixed gas 3 Calorific value, saving a lot of energy consumption in lime production.

[0181] (7) The internal heating electrode high voltage electricity + plasma technology adopted in this application converts CO2 into CO fuel, and uses high-energy electrons and active species generated by high-voltage discharge to activate energy small molecules, thereby rapidly cracking CO2, achieving rapid breaking of CO2's inert chemical bonds and improving the catalytic reaction ability. In particular, the application of high-entropy porous boride catalytic composite materials synthesized with zirconium oxide and zirconium phosphate materials as catalyst carriers and BaTiO3 and ultra-high temperature boride ceramic materials as auxiliary agents reduces reaction energy consumption and reaction time, and the materials are easily available and inexpensive, which is also one of the original innovation cores of this application.

[0182] (8) The present application adopts the external heating electromagnetic induction method + staged product circulation cracking to separate CO2 into CO fuel. Through the reasonable distribution of the temperature inside the reactor and the staged temperature adjustment and the timely withdrawal of the product, the complete cracking of CO2 is achieved, and the production of high-purity CO and the recycling of CO2 raw material gas are achieved. In addition, sufficient reaction time is required for the CO2 cracking process. In particular, the cheap and easily available silk floc catalyst carrier is selected as Fe fiber wool, which greatly reduces the catalytic cost. This is also one of the original innovation cores of the present application.

[0183] (9) In the "electrolysis" method of the present application, since the converted CO2 gas is directly used to produce lime, its electrical energy and thermal energy consumption is replaced by the converted CO2 gas, achieving energy consumption balance and surplus, without increasing costs due to external energy.

[0184] (10) The present application has the advantages of simple structure, controllable and easy electric conversion intensity, large flue gas treatment flux, and good CO2 cracking effect.

[0185] (11) In this application, all CO2 waste gas is converted into CO gas for lime calcination, realizing the circular application within the production system and achieving the true purpose of "zero carbon emissions". In addition, the remaining CO gas can also be stored and used externally or sold, realizing the "negative carbon" emissions of lime production.

[0186] (12) Compared with the traditional method of calcining lime with coal, this application adopts a closed-loop production method and does not require the investment in environmental treatment equipment such as bag filters, desulfurization and denitrification, which can effectively reduce the investment in environmental treatment equipment.

[0187] (13) This application adopts a variety of different production methods to realize a lime production system, a gas preparation system, and a CO2 conversion system that can operate independently, which facilitates production management and operation.

[0188] (14) The device in this application is also suitable for the transformation and application of traditional lime kilns, and is easier to promote industrialization.

[0189] (15) The principles and application solutions of this application can also be expanded to other waste carbon conversions and gaseous product conversion processes dominated by technologies such as electrolysis, and are easy to industrially convert and apply.

[0190] The technical features of the above embodiments can be combined arbitrarily (as long as there is no contradiction in the combination of these technical features). In order to make the description concise, not all possible combinations of the technical features in the above embodiments are described; these embodiments that are not explicitly written should also be considered to be within the scope of this specification.

[0191] The present application has been described in a relatively specific and detailed manner through general explanations and specific embodiments. It should be understood that, based on the technical concept of the present application, several conventional adjustments or further innovations may be made to these specific embodiments; however, as long as they do not depart from the technical concept of the present application, the technical solutions obtained by such conventional adjustments or further innovations also fall within the scope of protection of the claims of the present application.

Claims

1. A device for achieving negative carbon emissions and co-production of lime, characterized by: The invention comprises a lime kiln, a CO2 conversion device (3) and / or a fuel generation conversion device (2), wherein: The lime kiln has a kiln top gas collecting pipe (4), which can convey the CO2 gas produced by the lime kiln into the kiln top flue gas dust reduction and purification device (5) for dust reduction and purification treatment, and the treated flue gas enters the CO2 conversion device (3) along the descending flue gas conveying pipe (6); The CO2 conversion device (3) includes a low-temperature CO2 flue gas pressurizing device (3-1) and a high-speed internal heating conversion device (3-2), wherein the low-temperature CO2 flue gas pressurizing device (3-1) is used to pressurize the CO2 gas received from the descending flue gas conveying pipeline (6), and the high-speed internal heating conversion device (3-2) is used to convert the pressurized CO2 gas into CO gas, and the converted CO gas is sent into the kiln chamber of the lime kiln to be burned and heat-provided to calcine limestone; The fuel generation and conversion device (2) is a closed structure with two sections, the upper section is a cracking section (2-1), and the lower section is a conversion section (2-2). The cracking section (2-1) and the conversion section (2-2) are connected and cut off by a hot air shut-off valve (2-6). The top of the cracking section (2-1) is provided with a biomass fuel inlet (2-3) and a CO2 gasifying agent inlet (2-4). The bottom of the cracking section (2-1) is provided with a cracking gas outlet (2-7). The conversion section (2-2) has a CO conversion gas outlet (2-8) and an air pipeline for inputting an air gasifying agent. The bottom of the conversion section (2-2) is provided with a high-temperature CO2 gas inlet (2-9). The O2 gasifying agent inlet (2-4) and the high-temperature CO2 gas inlet (2-9) are respectively connected to the pipeline for outputting the high-temperature CO2 waste gas from the lime kiln calcining zone. The cracking section (2-1) is used to crack the biomass fuel and high-temperature CO2 waste gas fed therein into cracking gas containing CO, and the cracked CO is output to the kiln chamber of the lime kiln through the cracking gas outlet (2-7); the conversion section (2-2) is used to receive the remaining biomass fuel after cracking from the cracking section (2-1) and convert the high-temperature CO2 gas rising from its bottom into CO gas through the biomass fuel, and the converted CO gas is output to the kiln chamber of the lime kiln through the CO conversion gas outlet (2-8).

2. The device for achieving negative carbon emissions and co-production of lime according to claim 1, characterized in that: The lime kiln is a double-bore vertical kiln or a single-bore vertical kiln; A plurality of fuel spray guns (10) are provided around the kiln body of the lime kiln, each of the fuel spray guns (10) being connected to a lime kiln body fuel surrounding pipe (9) provided on the outer wall of the kiln body, the fuel spray gun (10) being used to spray combustible gas into the kiln chamber of the lime kiln, the lime kiln body fuel surrounding pipe (9) being used to receive the cracked gas discharged from the cracked gas outlet (2-7), the CO gas discharged from the CO conversion gas outlet 1 (2-8), and the CO gas discharged from the CO2 conversion device (3); A lime kiln flue gas circulation channel (13) communicating with the kiln chamber is provided on the outer wall of the lime kiln body. The lime kiln flue gas circulation channel (13) is communicated with the ash cleaning and conveying enclosure pipe (15) through a plurality of pulse control valves (14). The ash cleaning and conveying enclosure pipe (15) is connected to the ash cleaning and conveying pipeline (16). The high-temperature exhaust gas from the lime kiln calcining zone is sent into the high-temperature dust reduction device (17) through the lime kiln flue gas circulation channel (13), the pulse control valve (14), the ash cleaning and conveying enclosure pipe (15) and the ash cleaning and conveying pipeline (16) for dust reduction and purification treatment. The purified high-temperature CO2 exhaust gas is sent to the CO2 gasifying agent inlet (2-4) and the high-temperature CO2 gas inlet (2-9).

3. The device for achieving negative carbon emissions and co-production of lime according to claim 2, characterized in that: The low-temperature CO2 flue gas pressurizing device (3-1) has a CO2 inlet, a first CO2 outlet, and a second CO2 outlet. The CO2 inlet is connected to the descending flue gas conveying pipe (6). The first CO2 outlet is connected to the CO2 inlet of the high-speed internal heating conversion device (3-2) through a waste gas valve (26). The second CO2 outlet is connected to a waste gas external network pipe (29) through a waste gas valve (27). The high-speed internal heating conversion device (3-2) includes a high-speed internal heating conversion device shell (3-2-1), a graphite electrode body (3-4) is arranged in the high-speed internal heating conversion device shell (3-2-1), the graphite electrode body (3-4) has a hollow inner cavity, the hollow inner cavity is filled with spherical zirconium-based nano high-entropy porous ultra-high temperature catalytic material (3-6), a plurality of electrode vents (3-5) are arranged on the side wall of the graphite electrode body (3-4), the electrode vents (3-5) are connected to the high-speed internal heating conversion device shell (3-2-1); the graphite electrode body (3-4) is electrically connected to the transformer (3-4-1), and the transformer (3- 4-1) is used to energize the graphite electrode body (3-4) when the gas passes through the graphite electrode body (3-4); the converted CO enters the high-speed internal heating conversion device shell (3-2-1) through the electrode vent (3-5), and enters the CO delivery pipe (8) through the CO conversion gas outlet (3-7) on the high-speed internal heating conversion device shell (3-2-1), and then enters the lime kiln through the lime kiln body fuel surrounding pipe (9). The CO conversion gas outlet (3-7) is connected to the CO delivery pipe (8) through the hot air valve (3-9), and the CO delivery pipe (8) is connected to the lime kiln body fuel surrounding pipe (9).

4. The device for achieving negative carbon emissions and co-production of lime according to claim 3, characterized in that: The CO2 conversion device (3) further comprises a low-speed external heating conversion device (3-3), wherein a plurality of layers of catalysts are sequentially arranged from bottom to top in the low-speed external heating conversion device (3-3), and the gaps and particle sizes of the catalysts at different layers decrease step by step from bottom to top; The several layers of catalysts include a first-level Fe fiber fleece catalyst (3-11), a first-level heat storage particle catalyst (3-12), a second-level Fe fiber fleece catalyst (3-13), a second-level heat storage particle catalyst (3-14), a third-level Fe fiber fleece catalyst (3-15), a third-level heat storage particle catalyst (3-16) and a fourth-level Fe fiber fleece catalyst (3-17), which are arranged in sequence from bottom to top.

5. The device for achieving negative carbon emission and co-production of lime according to claim 4, characterized in that: The low-speed external heating reformer (3-3) has a first CO inlet, which is close to the bottom of the low-speed external heating reformer (3-3). The first CO inlet is connected to the CO conversion gas outlet of the high-speed internal heating reformer (3-2) through a CO conversion gas connecting channel (3-8). The CO conversion gas connecting channel (3-8) is provided with a hot air valve five (3-10); A second CO inlet is provided at the bottom of the low-speed external heating conversion device (3-3), and the second CO inlet is connected to a second high-temperature CO2 gas delivery pipe (20) through a second hot air valve (23), and the second high-temperature CO2 gas delivery pipe (20) is connected to a first high-temperature CO2 gas delivery pipe (18), and the first high-temperature CO2 gas delivery pipe (18) is connected to the gas outlet of the high-temperature dust suppression device (17); The high-temperature CO2 gas delivery pipeline 1 (18) is connected to the CO2 gasification agent inlet (2-4) through the high-temperature CO2 gas delivery pipeline 3 (21), and the high-temperature CO2 gas delivery pipeline 3 (21) is provided with a hot air valve 3; one end of the high-temperature CO2 gas delivery pipeline 1 (18) is connected to the high-temperature CO2 gas inlet (2-9) through the hot air valve 1 (22).

6. The device for achieving negative carbon emission and co-production of lime according to claim 5, characterized in that: A high-temperature electromagnetic induction heating device (3-18), a medium-temperature electromagnetic induction heating device (3-19), and a low-temperature electromagnetic induction heating device (3-20) are sequentially arranged on the outer wall of the low-speed external heating conversion device (3-3) from bottom to top, and the heating power supplies of the three electromagnetic induction heating devices are respectively controlled by an electric control device (3-21). The three electromagnetic induction heating devices are used to heat the gas in the low-speed external heating conversion device (3-3); A CO output port is provided on the top of the low-speed external heating conversion device (3-3), and the CO output port is connected to the CO delivery pipeline 1 (7) through a CO control valve (28), and the CO delivery pipeline 1 (7) is connected to the CO delivery pipeline 2 (8) through a cracked gas output pipeline (12).

7. The device for achieving negative carbon emissions and co-production of lime according to claim 1, characterized in that: A pulverized coal main lance (2-5) is provided on the top of the fuel generation and conversion device (2), a steam gasification agent inlet (2-5-1) and a fuel inlet (2-5-4) are provided on the pulverized coal main lance (2-5), an air inlet (2-5-5) is provided on the side wall of the fuel generation and conversion device (2) close to the cracking section (2-1), a pulverized coal surrounding pipe (2-5-2) is provided on the top of the cracking section (2-1), the pulverized coal surrounding pipe (2-5-2) is connected to the inner cavity of the cracking section (2-1) through multiple pulverized coal auxiliary nozzles (2-5-3), and the cracking section (2-1) is divided into a drying layer, a pyrolysis layer, an oxidation layer and a reduction layer from top to bottom.

8. The device for achieving negative carbon emissions and co-production of lime according to claim 1, characterized in that: Three layers of regulating blowing ports (21-1) are provided on the outer wall of the conversion section (2-2) from top to bottom, each regulating blowing port (21-1) is communicated with the inner cavity of the conversion section (2-2), and each regulating blowing port (21-1) is communicated with a high-temperature CO2 gas delivery pipeline three (21), and the high-temperature CO2 gas delivery pipeline three (21) performs auxiliary blowing on the conversion section (2-2) through the regulating blowing ports (21-1); The outer wall of the conversion section (2-2) is further provided with multiple layers of air gasification agent regulating injection ports (2-15-2) from top to bottom, each of the air gasification agent regulating injection ports (2-15-2) is connected to the second air duct (2-15-1), the second air duct (2-15-1) is connected to the first air duct (2-15), and the first air duct (2-15) is connected to the outlet end of the air pressurizing device (2-11); The CO gas converted in the conversion section (2-2) is transported to the CO delivery pipeline three (11) through the CO conversion gas outlet one (2-8), and the CO delivery pipeline three (11) is connected to the CO delivery pipeline two (8) through the cracked gas output pipeline (12).

9. The device for achieving negative carbon emission and co-production of lime according to claim 8, characterized in that: An ash outlet is formed below the conversion section (2-2), and a heat-resistant rotary sealed ash discharger (2-10) is provided at the ash outlet. The heat-resistant rotary sealed ash discharger (2-10) is used to discharge the carbon ash after the biomass fuel is converted into a sealed ash storage bin (2-14) below. The ash storage bin (2-14) is connected to the air pressurizing device (2-11) through a pipeline. The air pressurizing device (2-11) can pneumatically convey the carbon ash in the ash storage bin (2-14) to the pneumatic conveying ring pipe (2-12). The pneumatic conveying ring pipe (2-12) is connected to the ash storage bin (2-14) through multiple interfaces. The pneumatic conveying ring pipe (2-12) is connected to the lower ash bin of the high-temperature dust reduction device (17) through a pneumatic ash conveying pipeline (25). A screw conveyor (19) is provided below the high-temperature dust reduction device (17). The screw conveyor (19) is used to convey the powdered ash discharged from the high-temperature dust reduction device (17) to the belt conveyor of the ash discharge system at the bottom of the lime kiln; The ash storage bin (2-14) is provided with a water inlet (2-16) and a water outlet. Water is injected into the ash storage bin (2-14) through the water inlet (2-16) and the water level is maintained at a target liquid level position (2-14-3). A slurry pump (2-13) is provided at the water outlet. The mixture of carbon ash and water is sucked out by the slurry pump (2-13).

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