Carbon-based resource staged polygeneration conversion system and method

Abstract

The application discloses a carbon-based resource hierarchical multi-element conversion system and method, a plasma hydrogen radical catalysis module is used for receiving hydrogen gas discharged by an electrolytic water module and is used for catalytically generating plasma hydrogen radicals from the hydrogen gas; a pyrolyzer is used for performing a hydrogenation pyrolysis reaction on solid carbon-based resources and the plasma hydrogen radicals to generate gaseous products and solid products; a plasma thermal cracking gasification module is used for converting the solid products discharged from a second outlet end into H2 / CO synthesis gas; a multi-phase product fine separation module is in communication with the first outlet end and is used for separating the gaseous products discharged from the first outlet end into gaseous phase products and liquid phase products; and a renewable energy power generation module is used for supplying power to the electrolytic water module, the plasma hydrogen radical catalysis module and the plasma thermal cracking gasification module. The application introduces hydrogen radicals into a pyrolysis reaction, significantly improves tar yield and quality, and simultaneously replaces a conventional gasification heat supply path with plasma to efficiently convert semicoke.

Description

Technical Field

[0001] This application belongs to the field of solid carbon-based resource utilization technology, specifically relating to a hierarchical multi-element conversion system and method for carbon-based resources. Background Technology

[0002] Currently, solid carbon-based resources such as coal and biomass remain a crucial foundation of my country's energy and chemical industry system. Traditional utilization methods mainly include direct combustion and single gasification processes. While direct combustion equipment is mature, it suffers from the problem of converting high-grade chemical energy into low-grade thermal energy, resulting in significant irreversible losses and high emission intensity, leading to high levels of CO2 and NOx emissions. x The current system suffers from severe particulate matter emissions; gasification processes typically rely on the self-combustion of some raw materials for heating, resulting in low energy efficiency and still high carbon emissions. Furthermore, the system cannot achieve high-value utilization of raw materials through differentiated processing. In addition, the high-value-added components, such as aromatics, abundant in solid carbon-based resources are often destroyed during high-temperature combustion or gasification, leading to resource waste and hindering the achievement of diversified and graded utilization goals. Meanwhile, with the large-scale integration of renewable energy sources such as wind and solar power, their volatility and intermittency are becoming increasingly prominent, causing grid connection difficulties and frequent instances of wind and solar power curtailment. Existing technologies lack effective pathways to convert fluctuating green electricity into stable chemical products, failing to establish a highly efficient utilization platform that deeply couples green electricity with carbon-based resources, thus limiting the overall flexibility and carbon reduction capacity of the energy system. Therefore, there is an urgent need for an integrated system that can achieve both high-value utilization of solid carbon-based resources through differentiated processing and synergistic absorption of fluctuating green electricity and its conversion into stable chemical energy products, in order to overcome the bottlenecks of existing technologies in energy efficiency, product structure, and carbon emission control. Summary of the Invention

[0003] The purpose of this application is to provide a graded multi-element conversion system and method for carbon-based resources, so as to realize the high-value utilization of solid carbon-based resources in different grades, and to synergistically absorb fluctuating green electricity and convert it into stable chemical energy products.

[0004] To achieve the above objectives, this application provides a carbon-based resource hierarchical multi-element conversion system, comprising:

[0005] An electrolysis water module is used to electrolyze water to obtain hydrogen and oxygen. The electrolysis water module includes a hydrogen outlet for discharging hydrogen and an oxygen outlet for discharging oxygen. The plasma hydrogen radical catalytic module is used to receive hydrogen gas discharged from the water electrolysis module and to catalyze the hydrogen gas to generate plasma hydrogen radicals. The pyrolyzer includes a first inlet end, a second inlet end, a first outlet end, and a second outlet end. The first inlet end is used to input solid carbon-based resources from the outside. The second inlet end is connected to the plasma hydrogen radical catalytic module and is used to receive plasma hydrogen radicals. The second outlet end is connected to the plasma thermal cracking gasification module. The pyrolyzer is used to perform hydrogen pyrolysis reaction on solid carbon-based resources and plasma hydrogen radicals to generate gaseous products and solid products. The plasma pyrolysis gasification module is used to convert the solid products discharged from the second outlet into H2 / CO syngas. The multiphase product fine separation module is connected to the first outlet end and is used to separate the gaseous product discharged from the first outlet end into gaseous product and liquid product. The renewable energy power generation module is used to power the water electrolysis module, the plasma hydrogen radical catalysis module, and the plasma thermal cracking gasification module.

[0006] In some embodiments, the pyrolyzer further includes a third inlet and a third outlet. The carbon-based resource graded multi-element conversion system also includes a heat carrier oxidizer. The heat carrier oxidizer includes a first gaseous reactant inlet, a solid reactant inlet, and a solid product outlet. The first gaseous reactant inlet is connected to an oxygen outlet pipe, and the solid reactant inlet is connected to the third outlet to transport semi-coke at a first preset temperature discharged from the third outlet to the heat carrier oxidizer via the solid reactant inlet. The solid product outlet is connected to the third inlet of the pyrolyzer to supply semi-coke at a second preset temperature to the pyrolyzer, wherein the first preset temperature is lower than the second preset temperature.

[0007] In some embodiments, the heat carrier oxidizer includes a second gaseous reactant inlet, and the carbon-based resource graded multi-element conversion system also includes a carbon dioxide enrichment and recycling module. The outlet of the carbon dioxide enrichment and recycling module is connected to the second gaseous reactant inlet to transport the generated high-concentration carbon dioxide into the second gaseous reactant inlet of the heat carrier oxidizer. The inlet of the carbon dioxide enrichment and recycling module is connected to the first outlet of the waste heat cascade recovery module.

[0008] In some embodiments, the carbon dioxide enrichment and recycling module includes an integrated series-connected cooler, separator, and compressor. The cooler is used to cool the flue gas delivered from the first outlet of the waste heat recovery module, the separator is used to perform gas-liquid separation on the cooled flue gas to obtain carbon dioxide, and the compressor is used to compress the carbon dioxide to obtain a high concentration of carbon dioxide.

[0009] In some embodiments, when the semi-coke at a first preset temperature is burned in the heat carrier oxidizer, the volume ratio of carbon dioxide to oxygen in the heat carrier oxidizer ranges from 3:1 to 7:1, and the temperature range of the semi-coke at a second preset temperature output from the heat carrier oxidizer is from 600°C to 1050°C.

[0010] In some embodiments, the pyrolyzer is a riser-type rapid hydrogenation pyrolysis reactor with a rapid mixing and heating zone. The rapid mixing and heating zone is used to mix solid carbon-based resources with semi-coke at a second preset temperature delivered from the solid product outlet. The residence time of the solid carbon-based resources in the riser is 2s to 7s. The mass ratio of hydrogen to solid carbon-based resources at the first gaseous reactant inlet of the pyrolyzer is in the range of 0.05 to 0.30.

[0011] In some embodiments, the carbon-based resource hierarchical multi-element conversion system is characterized by further including a waste heat cascade recovery module, a heat carrier oxidizer further including a gaseous product outlet, a plasma thermal cracking gasification module including a gaseous outlet, and the gaseous product outlet and the gaseous outlet being connected to the inlet of the waste heat cascade recovery module, so that the flue gas generated by the gaseous product outlet and the syngas generated by the gaseous outlet are both input into the waste heat cascade recovery module for recovery, and the recovered heat is used to preheat the water in the water electrolysis module.

[0012] In some embodiments, the water electrolysis module is a solid oxide electrolyzer, and the water entering the water electrolysis module is preheated to 500°C to 700°C by a waste heat recovery module, and the electrolysis temperature is maintained at 700°C to 1000°C.

[0013] A second aspect of this application provides a method for hierarchical and multi-element conversion of carbon-based resources, applied to the above-mentioned system, wherein the conversion method includes: The renewable energy power generation module is activated to supply power to the water electrolysis module, the plasma hydrogen radical catalysis module, and the plasma pyrolysis gasification module. Hydrogen generated by the water electrolysis module is transported to the plasma hydrogen radical catalysis module to generate plasma hydrogen radicals. Solid carbon-based resources are input into the pyrolyzer through the first inlet end, so that the solid carbon-based resources and plasma hydrogen radicals undergo hydrogenation pyrolysis reaction in the pyrolyzer to generate gaseous products and solid products. The solid products generated by the pyrolysis unit are transported to the plasma thermal pyrolysis gasification module, where they are converted into H2 / CO syngas in a high-temperature plasma environment. The gaseous products generated by the pyrolysis unit are transported to the multiphase product fine separation module for separation into gaseous and liquid products.

[0014] In some implementations, the conversion method further includes: The oxygen generated by the water electrolysis module, the semi-coke at the first preset temperature generated by the pyrolyzer, and the high-concentration carbon dioxide output from the carbon dioxide enrichment and recycling module are all transported to the heat carrier oxidizer so that the semi-coke at the first preset temperature is burned in a mixed atmosphere of oxygen and carbon dioxide, while heating the heat carrier to generate flue gas and semi-coke at the second preset temperature. The semi-coke at the second preset temperature is fed back into the pyrolyzer to provide energy for the pyrolysis reaction; The flue gas is transported to the waste heat recovery module for heat recovery.

[0015] In some implementations, the conversion method further includes: The syngas produced by the gaseous outlet of the plasma pyrolysis gasification module and the flue gas produced by the gaseous product outlet of the heat carrier oxidizer are transported to the waste heat cascade recovery module for recovery. The heat recovered by the waste heat recovery module is used to preheat the water in the water electrolysis module; The remaining flue gas from the waste heat recovery module is transported to the carbon dioxide enrichment and recycling module for reuse, while the remaining syngas is discharged to the outside.

[0016] Through the above technical solution, the water electrolysis module is used to electrolyze water to obtain hydrogen and oxygen. The water electrolysis module includes a hydrogen outlet for discharging hydrogen and an oxygen outlet for discharging oxygen. The plasma hydrogen radical catalytic module is used to receive the hydrogen discharged from the water electrolysis module and to catalyze the hydrogen to generate plasma hydrogen radicals. The pyrolyzer includes a first inlet, a second inlet, a first outlet, and a second outlet. The first inlet is used to input solid carbon-based resources from the outside. The second inlet is connected to the plasma hydrogen radical catalytic module and is used to receive plasma hydrogen radicals. The second outlet... The system is connected to a plasma pyrolysis gasification module. The pyrolyzer is used to perform hydrogenation pyrolysis reactions on solid carbon-based resources and plasma hydrogen radicals to generate gaseous and solid products. The plasma pyrolysis gasification module converts the solid products discharged from the second outlet into H2 / CO syngas. A multiphase product fine separation module is connected to the first outlet and is used to separate the gaseous products discharged from the first outlet into gaseous and liquid products. A renewable energy power generation module supplies power to the water electrolysis module, the plasma hydrogen radical catalysis module, and the plasma pyrolysis gasification module. This system utilizes green electricity to drive the electrolysis of water to produce hydrogen / oxygen, plasma radical catalysis, and high-temperature pyrolysis processes. Introducing hydrogen radicals into the pyrolysis reaction significantly improves tar yield and quality. Simultaneously, plasma replaces the traditional gasification heating path for efficient conversion of semi-coke. The system achieves high-value utilization of resources while simultaneously addressing the challenges of green electricity consumption and carbon emission reduction.

[0017] Other features and advantages of the embodiments of this application will be described in detail in the following detailed description section. Attached Figure Description

[0018] The accompanying drawings are provided to further illustrate the embodiments of this application and form part of the specification. They are used together with the following detailed description to explain the embodiments of this application, but do not constitute a limitation on the embodiments of this application. For those skilled in the art, other drawings can be obtained based on the structures shown in these drawings without any inventive effort. In the drawings: Figure 1 This is a schematic diagram of the principle structure of the carbon-based resource hierarchical multi-element conversion system of this application; Figure 2 This is a flowchart illustrating the graded and multi-element conversion method for carbon-based resources proposed in this application.

[0019] Explanation of reference numerals in the attached figures Detailed Implementation

[0020] The specific embodiments of this application will be described in detail below with reference to the accompanying drawings. It should be understood that the specific embodiments described herein are for illustration and explanation only and are not intended to limit this application.

[0021] The following description, with reference to the accompanying drawings, describes a system and method for graded multi-element conversion of carbon-based resources according to this application.

[0022] like Figure 1 As shown, this application proposes a graded multi-element conversion system for carbon-based resources, including a water electrolysis module 2, a plasma hydrogen radical catalysis module 8, a pyrolyzer 6, a plasma pyrolysis gasification module 3, a multiphase product fine separation module 5, and a renewable energy power generation module 1. The water electrolysis module 2 is used to electrolyze water to obtain hydrogen and oxygen, and includes a hydrogen outlet for discharging hydrogen and an oxygen outlet for discharging oxygen. The plasma hydrogen radical catalysis module 8 is used to receive the hydrogen discharged from the water electrolysis module 2 and to catalyze the hydrogen to generate plasma hydrogen radicals. The pyrolyzer 6 includes a first inlet, a second inlet, a first outlet, and a second outlet. The first inlet is used to input solid carbon-based resources from the outside. The second inlet is connected to the plasma hydrogen radical catalysis module 8 and is used to receive plasma hydrogen radicals. The second outlet is connected to the plasma pyrolysis gasification module 3. The pyrolyzer 6 is used to perform hydrogenation pyrolysis reaction on solid carbon-based resources and plasma hydrogen radicals to generate gaseous and solid products. The plasma pyrolysis gasification module 3 is used to convert the solid products discharged from the second outlet into H2 / CO synthesis gas. The multiphase product fine separation module 5 is connected to the first outlet and is used to separate the gaseous products discharged from the first outlet into gaseous and liquid products. The renewable energy power generation module 1 is used to supply power to the water electrolysis module 2, the plasma hydrogen radical catalysis module 8 and the plasma pyrolysis gasification module 3.

[0023] In this embodiment, the water electrolysis module 2 electrolyzes water to generate hydrogen and oxygen. The generated hydrogen is transported from the hydrogen outlet to the plasma hydrogen radical catalytic module 8 for catalytic reaction and to generate plasma hydrogen radicals. The generated plasma hydrogen radicals are output from the plasma hydrogen radical catalytic module to the pyrolyzer 6. External solid carbon-based resources are input from the first inlet of the pyrolyzer 6. Thus, the solid carbon-based resources and plasma hydrogen radicals undergo a hydrogenation pyrolysis reaction in the pyrolyzer 6 to produce gaseous products (S3 oil gas) and solid products (S2 semi-coke). The gaseous product S3 enters the multiphase product fine separation module 5 through a pipeline for separation to form a gaseous product (pyrolysis gas) and a liquid product (S17 tar). The solid product S2 enters the plasma pyrolysis gasification module 3 through a pipeline for high-temperature pyrolysis reaction to form syngas (S14). Throughout the solid carbon-based conversion process, the renewable energy power generation module 1 includes a photovoltaic array, a wind turbine generator, and a matching energy storage device, thereby stably and continuously supplying power to the water electrolysis module 2, the plasma hydrogen radical catalysis module 8, and the plasma thermal cracking gasification module 3. The aforementioned renewable energy power generation module 1 can generate fluctuating green electricity. This application utilizes this fluctuating green electricity simultaneously in three key electrochemical / electrothermal units, achieving a three-level coupling of electro-thermal-chemical energy. This allows the system to drive water electrolysis, plasma catalysis, and high-temperature gasification processes with green electricity, achieving high-value conversion of resources and output of multiple products. Plasma gasification directly provides a high temperature of 1400℃~1600℃ using electricity, replacing the "burning carbon-based resources for heating" step in traditional gasification, reducing carbon emissions and simultaneously decreasing pure oxygen consumption.

[0024] Among them, plasma hydrogen radical catalysis module 8 is a low-temperature plasma catalytic reactor with a specific energy consumption of 2kWh to 5kWh kg. -1 H2, with a free radical yield of not less than 10%, is used to activate hydrogen obtained from the water electrolysis module 2 to generate hydrogen free radicals and transport them to the pyrolyzer 6 to improve the pyrolysis reaction rate and tar yield. In this application, the plasma hydrogen free radical catalytic module 8 uses dielectric barrier discharge plasma to activate H2, forming a high concentration of H free radicals, thereby achieving hydrogenation pyrolysis and improving tar yield and quality.

[0025] Furthermore, the multiphase product fine separation module 5 is a combination of a gas-solid separator, a condenser, a cyclone separator, and a distillation / filtration device, used to separate the mixed product stream discharged from the first outlet end of the pyrolysis unit 6 into gaseous products (pyrolysis gas) and liquid products (tar).

[0026] In addition, this application uses plasma integration for hydrogen radical activation and high-temperature cracking of semi-coke, which improves tar yield and quality on the one hand, and avoids the carbon resource self-ignition heating path in traditional gasification on the other hand, reducing carbon emissions while reducing pure oxygen consumption and generating H2 / CO-rich syngas.

[0027] Furthermore, in Figure 1 In the equation, S1 is solid carbon-based resource, temperature 25 ℃, pressure 1.01 bar, mass flow rate 140695 kg / h; S2 is semi-coke, temperature 550 ℃, pressure 1.01 bar, mass flow rate 90105 kg / h; S3 is oil and gas, temperature 550 ℃, pressure 1.01 bar, mass flow rate 42098 kg / h; S4 is semi-coke at the first preset temperature, temperature 550 ℃, pressure 1.01 bar, mass flow rate 461939 kg / h; S5 is semi-coke at the second preset temperature, temperature 700 ℃, pressure 1.01 bar, mass flow rate 450224 kg / h; S6 is hydrogen, temperature 75 ℃, pressure 7.00 bar, mass flow rate 3223 kg / h; S7 is oxygen, temperature 75 ℃, pressure 7.00 bar, mass flow rate 25389 kg / h; S8 is flue gas, temperature 700 ℃... S10 is carbon dioxide, temperature 75 ℃, pressure 7.00 bar, mass flow rate 316451 kg / h; S11 is carbon dioxide, temperature 25 ℃, pressure 7 bar, mass flow rate 32309 kg / h; S12 is flue gas, temperature 25 ℃, pressure 7.00 bar, mass flow rate 316451 kg / h; S13 is gasifying agent, temperature 25 ℃, pressure 30.00 bar, mass flow rate 50863 kg / h; S14 is syngas, temperature 1400 ℃, pressure 30.00 bar, mass flow rate 158989 kg / h; S15 is syngas, temperature 1400 ℃, pressure 30.00 bar, mass flow rate 158989 kg / h. kg / h; S16 is pyrolysis gas, temperature 25 ℃, pressure 1.01 bar, mass flow rate 13490 kg / h; S17 is tar, temperature 25 ℃, pressure 1.01 bar, mass flow rate 25385 kg / h; P1 is electrical energy, 155197 kW; P2 is electrical energy, 9632 kW; P3 is electrical energy, 161517 kW.

[0028] In some embodiments, the pyrolyzer 6 further includes a third inlet and a third outlet. The carbon-based resource graded multi-element conversion system also includes a heat carrier oxidizer 7. The heat carrier oxidizer 7 includes a first gaseous reactant inlet, a solid reactant inlet, and a solid product outlet. The first gaseous reactant inlet is connected to an oxygen outlet pipe, and the solid reactant inlet is connected to the third outlet to transport semi-coke at a first preset temperature discharged from the third outlet to the heat carrier oxidizer 7 via the solid reactant inlet. The solid product outlet is connected to the third inlet of the pyrolyzer 6 to supply semi-coke at a second preset temperature to the pyrolyzer 6, wherein the first preset temperature is lower than the second preset temperature.

[0029] In this embodiment, in the pyrolyzer 6, when the solid carbon-based resources and hydrogen entering from the water electrolysis module 2 undergo a hydrogenation pyrolysis reaction, the resulting low-temperature semi-coke enters the heat carrier oxidizer 7 from the third outlet end for heating reaction. The high-temperature semi-coke generated after the low-temperature semi-coke is heated in the heat carrier oxidizer 7 is recycled back into the pyrolyzer 6, thereby providing energy for the pyrolysis reaction.

[0030] In some embodiments, the heat carrier oxidizer 7 includes a second gaseous reactant inlet, and the carbon-based resource graded multi-element conversion system also includes a carbon dioxide enrichment and recycling module 9. The outlet of the carbon dioxide enrichment and recycling module 9 is connected to the second gaseous reactant inlet to transport the generated high-concentration carbon dioxide to the second gaseous reactant inlet of the heat carrier oxidizer 7. The inlet of the carbon dioxide enrichment and recycling module 9 is connected to the first outlet of the waste heat cascade recovery module 4.

[0031] In this embodiment, the oxygen outlet of the water electrolysis module 2 enters the thermal carrier oxidizer 7, and the high-concentration carbon dioxide generated from the outlet of the carbon dioxide enrichment and recycling module 9 also enters the thermal carrier oxidizer 7. Thus, the oxygen byproduct of the water electrolysis module 2 is mixed with the CO2 recovered by the system and sent to the thermal carrier oxidizer 7 as a fluidizing medium to generate high-concentration CO2 flue gas. When the semi-coke at the first temperature enters the thermal carrier oxidizer 7, it is heated by the high-concentration CO2 flue gas to form semi-coke at the second preset temperature. Therefore, the high-purity O2 byproduct of the water electrolysis module 2 is directly used in the combustion process in the thermal carrier oxidizer 7, combined with the recycled CO2 from the carbon dioxide enrichment and recycling module 9 to form an O2 / CO2 working medium, increasing the CO2 volume fraction in the flue gas to 90-95%, significantly reducing the load on subsequent CO2 capture and separation. 。

[0032] In some embodiments, the carbon dioxide enrichment and recycling module 9 includes an integrated series-connected cooler, separator, and compressor. The cooler is used to cool the flue gas delivered from the first outlet of the waste heat recovery module 4, the separator is used to perform gas-liquid separation on the flue gas cooled by the cooler to obtain carbon dioxide, and the compressor is used to compress the carbon dioxide to obtain high-concentration carbon dioxide.

[0033] In this embodiment, the carbon dioxide enrichment and recycling module 9 is used to separate carbon dioxide from pyrolysis gas and syngas. Specifically, during carbon dioxide capture, the cooler cools the flue gas S12 output from the waste heat recovery module 4. The cooled flue gas undergoes gas-liquid separation to obtain carbon dioxide. The carbon dioxide is then compressed by a compressor to obtain high-concentration carbon dioxide. Part of the captured high-concentration carbon dioxide is recycled to the heat carrier oxidizer 7 to mix with oxygen to form a CO2 / O2-rich atmosphere, while the remainder is compressed and stored or supplied externally.

[0034] In some embodiments, when the semi-coke at a first preset temperature is burned in the heat carrier oxidizer 7, the volume ratio of carbon dioxide to oxygen in the heat carrier oxidizer 7 is in the range of 3:1 to 7:1, and the temperature range of the semi-coke at a second preset temperature output from the heat carrier oxidizer 7 is 600°C to 1050°C.

[0035] As an inert diluent, CO2 can significantly reduce local oxygen concentration, suppress the violent combustion reaction of semi-coke, and maintain the reaction temperature within a suitable range, thus avoiding structural damage to the semi-coke caused by local hot spots and excessively high temperatures. In the heat carrier oxidizer 7, a CO2 / O2 volume ratio of 3:1 to 7:1 can stabilize the outlet semi-coke temperature between 600℃ and 1050℃, ensuring sufficient sensible heat for the semi-coke recycled back to the pyrolysis unit, providing a stable heat source for the rapid heating and pyrolysis reaction of solid carbon-based resources. Combustion in a CO2 circulating atmosphere can significantly increase the CO2 volume fraction in the flue gas (typically reaching over 90%), which is beneficial for subsequent carbon dioxide separation, compression, and storage or utilization, reducing energy consumption in the carbon capture process. Furthermore, CO2 as a circulating gas can improve the gas-solid fluidization state within the heat carrier oxidizer, ensuring uniform heating of the semi-coke particles, improving gas-solid heat transfer efficiency, and thus enhancing the overall thermal efficiency of the pyrolysis system. Therefore, controlling the volume ratio of CO2 to O2 within the range of 3:1 to 7:1 can achieve synergistic optimization in terms of combustion temperature control, stable heat supply of the heat carrier, and CO2 enrichment and recovery.

[0036] In some embodiments, the pyrolyzer 6 is a riser-type rapid hydrogenation pyrolysis reactor with a rapid mixing and heating zone. The rapid mixing and heating zone is used to mix solid carbon-based resources with semi-coke at a second preset temperature conveyed from the solid product outlet. The residence time of the solid carbon-based resources in the riser is 2s to 7s. The mass ratio of hydrogen to solid carbon-based resources at the first gaseous reactant inlet of the pyrolyzer 6 is in the range of 0.05 to 0.30.

[0037] In this embodiment, since the riser reactor is a fast reaction system, controlling the residence time within the range of 2s to 7s ensures that the solid carbon-based resources can rapidly heat up and complete the main pyrolysis reaction, while avoiding excessive secondary cracking reactions. Furthermore, due to the high-speed gas-solid two-phase flow and high heat transfer coefficient within the riser, coal particles can rapidly heat up to the pyrolysis temperature and complete the main volatile matter release within the 2s to 7s residence time range, allowing the reaction with hydrogen to be completed in a short time. Introducing hydrogen during pyrolysis can stabilize the free radicals generated during pyrolysis, inhibiting secondary condensation and polymerization reactions of tar, thereby increasing tar yield and the proportion of light aromatics and stabilizing components. Further, the appropriate amount of hydrogen participating in the reaction can hydrogenate and terminate active free radicals, reducing the further condensation of aromatic structures to form semi-coke or coke, thereby increasing the yield of liquid products. When the mass ratio of hydrogen to solid carbon-based resources is controlled within the range of 0.05 to 0.30, sufficient hydrogen source can be provided for the free radical stabilization reaction, while avoiding excessive hydrogen consumption and reduced system economy.

[0038] In some embodiments, the carbon-based resource hierarchical multi-element conversion system is characterized by further including a waste heat cascade recovery module 4, a heat carrier oxidizer 7 further including a gaseous product outlet, a plasma thermal pyrolysis gasification module 3 including a gaseous outlet, and both the gaseous product outlet and the gaseous outlet are connected to the inlet of the waste heat cascade recovery module 4, so that the flue gas generated by the gaseous product outlet and the syngas generated by the gaseous outlet are input into the waste heat cascade recovery module 4 for recovery, and the recovered heat is used to preheat the water in the water electrolysis module 2.

[0039] In this embodiment, the waste heat recovery module 4 is a combination of a heat exchanger group, a steam generator, and a heat storage unit. It is used to recover the sensible heat of the high-temperature flue gas / syngas discharged from the plasma pyrolysis gasification module 3 and the heat carrier oxidizer 7. Specifically, the syngas generated from the gaseous outlet of the plasma pyrolysis gasification module 3 and the flue gas generated from the gaseous product outlet of the heat carrier oxidizer 7 also enter the waste heat recovery module 4 for sensible heat recovery. The obtained heat is then used sequentially for preheating the inlet water of the water electrolysis module 2, drying the solid feed, and other low-temperature heat requirements. The system waste heat is used for water electrolysis preheating through cascade recovery, thereby reducing the power consumption of the electrolysis process.

[0040] In some embodiments, the water electrolysis module 2 is a solid oxide electrolyzer used to electrolyze water to generate hydrogen and oxygen. The inlet water of the water electrolysis module 2 is preheated to 500°C to 700°C by the recovered heat from the waste heat recovery module 4, and the electrolysis temperature is maintained at 700°C to 1000°C. When the water electrolysis module 2 electrolyzes to produce hydrogen within the above-mentioned electrolysis temperature and inlet water preheating temperature range, the power consumption for hydrogen production can be reduced. The preheating of the inlet water is achieved through the thermal integration of the water electrolysis module 2 and the waste heat recovery module to reduce power consumption.

[0041] In addition, the plasma pyrolysis gasification module 3 adopts a DC non-transfer arc plasma torch with a working current of 200A to 800A, and the plasma gas is a mixture of CO2 and H2O with a gasification temperature of 1300℃ to 1600℃.

[0042] like Figure 2 As shown, the second aspect of this application provides a method for hierarchical multi-element conversion of carbon-based resources, applied to the system described above. The conversion method includes: S10: Start the renewable energy power generation module 1 to supply power to the water electrolysis module 2, the plasma hydrogen radical catalysis module 8 and the plasma thermal cracking gasification module 3 and start them up; S20: The hydrogen generated by the water electrolysis module 2 is delivered to the plasma hydrogen radical catalytic module 8 to generate plasma hydrogen radicals; S30: Solid carbon-based resources are input into pyrolyzer 6 through the first inlet end, so that the solid carbon-based resources and plasma hydrogen radicals undergo hydrogenation pyrolysis reaction in pyrolyzer 6 to generate gaseous products and solid products. S40: The solid products generated by the pyrolyzer 6 are transported to the plasma thermal pyrolysis gasification module 3 and converted into H2 / CO syngas in a high-temperature plasma environment; S50: The gaseous products generated by the pyrolysis unit 6 are transported to the multiphase product fine separation module 5 for separation into gaseous products and liquid products.

[0043] In this embodiment, such as Figure 1As shown by the blue line, the renewable energy power generation module 1 supplies power to the water electrolysis module 2, the plasma hydrogen radical catalysis module 8, and the plasma pyrolysis gasification module 3. After the water electrolysis module 2 starts working, it electrolyzes water to generate hydrogen and oxygen. The hydrogen gas S9 is then transported to the plasma hydrogen radical catalysis module for a catalytic reaction to generate plasma hydrogen radicals. The plasma hydrogen radicals S6 enter the pyrolyzer 6. External solid carbon-based resources S1 are also input into the pyrolyzer 6 and undergo a hydrogenation pyrolysis reaction with the plasma hydrogen radicals. The gaseous product S3 generated after the hydrogenation pyrolysis reaction in the pyrolyzer 6 enters the multiphase product fine separation module 5 for separation to form gaseous and liquid products. The solid product enters the plasma pyrolysis gasification module 3 and undergoes a high-temperature pyrolysis reaction to form H2 / CO syngas S14. To address the technical challenges of traditional combustion-gasification routes, such as low thermodynamic efficiency, high carbon emissions, difficulty in absorbing fluctuating renewable energy sources, and loss of high-value aromatic products, this invention proposes a carbon-based multi-element resource conversion system driven by renewable energy electricity and deeply coupling electrochemical and thermochemical processes. It integrates a closed-loop energy-mass cycle of "green electricity - H2 / O2 - pyrolysis - oxygen-enriched combustion - plasma gasification" to efficiently convert fluctuating renewable electricity into stable, high-energy-density chemical energy. Furthermore, the use of plasma hydrogen radical low-temperature hydrogenation pyrolysis significantly improves the yield of high-value components in tar.

[0044] In some implementations, the conversion method further includes: The oxygen generated by the water electrolysis module 2, the semi-coke at the first preset temperature generated by the pyrolyzer 6, and the high-concentration carbon dioxide output by the carbon dioxide enrichment and recycling module 9 are all transported to the heat carrier oxidizer 7 so that the semi-coke at the first preset temperature is burned in a mixed atmosphere of oxygen and carbon dioxide, while heating the heat carrier to generate flue gas and the semi-coke at the second preset temperature. The semi-coke at the second preset temperature is fed back into the pyrolysis unit 6 and provides energy for the pyrolysis reaction. The flue gas is transported to the waste heat recovery module 4 for heat recovery.

[0045] In this embodiment, the oxygen S7 generated by the water electrolysis module 2, the semi-coke S4 at a first preset temperature generated by the pyrolyzer 6, and the high-concentration carbon dioxide S10 generated by the carbon dioxide enrichment and recycling module 9 are all fed into the heat carrier oxidizer 7, so that the semi-coke at the first preset temperature is burned in a mixture of oxygen and carbon dioxide, producing semi-coke at a higher temperature (second preset temperature) and flue gas. Then, the flue gas S8 is fed back to the waste heat recovery module 4 for heat recycling, and the semi-coke S5 at the second preset temperature enters the pyrolyzer 6 to provide energy for the pyrolysis reaction. The addition of the carbon dioxide enrichment and recycling module 9 in this application can reduce CO2 emissions through an integrated CO2 enrichment-recycled combustion-storage scheme.

[0046] In some implementations, the conversion method further includes: The syngas produced by the gaseous outlet of the plasma pyrolysis gasification module 3 and the flue gas produced by the gaseous product outlet of the heat carrier oxidizer 7 are transported to the waste heat cascade recovery module 4 for recovery. The heat recovered by the waste heat recovery module 4 is used to preheat the water in the water electrolysis module 2; The remaining flue gas from the waste heat recovery module 4 is transported to the carbon dioxide enrichment and recycling module 9 for recycling, and the remaining syngas is discharged to the outside.

[0047] In this embodiment, a waste heat recovery module 4 is used to recover the syngas generated by the plasma thermal pyrolysis gasification module 3 and the flue gas generated by the heat carrier oxidizer 7, and the recovered heat is used to preheat the water in the water electrolysis module 2. The waste heat of the system is used for water electrolysis preheating through cascade recovery, which reduces the power consumption of the electrolysis process and realizes the high-value utilization of resources.

[0048] In the description of this application, it should be understood that the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of technical features indicated. Therefore, a feature defined as "first" or "second" may explicitly or implicitly include at least one of that feature. In the description of this application, "multiple" means at least two, such as two, three, etc., unless otherwise explicitly specified.

[0049] In this application, unless otherwise expressly specified and limited, the terms "installation," "connection," "linking," and "fixing," etc., should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral part; they can refer to a mechanical connection, an electrical connection, or a connection that allows communication between components; they can refer to a direct connection or an indirect connection through an intermediate medium; they can refer to the internal communication of two components or the interaction between two components, unless otherwise expressly limited. Those skilled in the art can understand the specific meaning of the above terms in this application based on the specific circumstances.

[0050] In the description of this specification, the references to terms such as "one embodiment," "some embodiments," "example," "specific example," or "some examples," etc., refer to specific features, structures, materials, or characteristics described in connection with that embodiment or example, which are included in at least one embodiment or example of this application. In this specification, the illustrative expressions of the above terms do not necessarily refer to the same embodiment or example. Furthermore, the specific features, structures, materials, or characteristics described may be combined in any suitable manner in one or more embodiments or examples. Moreover, without contradiction, those skilled in the art can combine and integrate the different embodiments or examples described in this specification, as well as the features of different embodiments or examples.

[0051] Although embodiments of this application have been shown and described above, it is understood that the above embodiments are exemplary and should not be construed as limiting this application. Those skilled in the art can make changes, modifications, substitutions and variations to the above embodiments within the scope of this application.

Claims

1. A graded multi-element conversion system for carbon-based resources, characterized in that, include: An electrolysis water module (2) is used to electrolyze water to obtain hydrogen and oxygen. The electrolysis water module (2) includes a hydrogen outlet for discharging hydrogen and an oxygen outlet for discharging oxygen. The plasma hydrogen radical catalytic module (8) is used to receive the hydrogen gas discharged from the water electrolysis module (2) and to catalyze the hydrogen gas to generate plasma hydrogen radicals. The pyrolyzer (6) includes a first inlet end, a second inlet end, a first outlet end, and a second outlet end. The first inlet end is used to input solid carbon-based resources from the outside. The second inlet end is connected to the plasma hydrogen radical catalytic module (8) and is used to receive plasma hydrogen radicals. The second outlet end is connected to the plasma thermal cracking gasification module (3). The pyrolyzer (6) is used to perform hydrogenation pyrolysis reaction on the solid carbon-based resources and the plasma hydrogen radicals to generate gaseous products and solid products. The plasma thermal pyrolysis gasification module (3) is used to convert the solid products discharged from the second outlet end into H2 / CO syngas; The multiphase product fine separation module (5) is connected to the first outlet end and is used to separate the gaseous product discharged from the first outlet end into gaseous product and liquid product. The renewable energy power generation module (1) is used to supply power to the water electrolysis module (2), the plasma hydrogen radical catalysis module (8) and the plasma thermal cracking gasification module (3).

2. The carbon-based resource hierarchical multi-element conversion system according to claim 1, characterized in that, The pyrolyzer (6) further includes a third inlet and a third outlet. The carbon-based resource hierarchical multi-element conversion system further includes a heat carrier oxidizer (7). The heat carrier oxidizer (7) includes a first gaseous reactant inlet, a solid reactant inlet and a solid product outlet. The first gaseous reactant inlet is connected to the oxygen outlet pipe. The solid reactant inlet is connected to the third outlet to transport semi-coke at a first preset temperature discharged from the third outlet to the heat carrier oxidizer (7) via the solid reactant inlet. The solid product outlet is connected to the third inlet of the pyrolyzer (6) to supply semi-coke at a second preset temperature to the pyrolyzer (6). The first preset temperature is lower than the second preset temperature.

3. The carbon-based resource hierarchical multi-element conversion system according to claim 2, characterized in that, The heat carrier oxidizer (7) includes a second gaseous reactant inlet. The carbon-based resource hierarchical multi-element conversion system also includes a carbon dioxide enrichment and recycling module (9). The outlet of the carbon dioxide enrichment and recycling module (9) is connected to the second gaseous reactant inlet to transport the generated high-concentration carbon dioxide to the second gaseous reactant inlet of the heat carrier oxidizer (7). The inlet of the carbon dioxide enrichment and recycling module (9) is connected to the first outlet of the waste heat cascade recovery module (4).

4. The carbon-based resource hierarchical multi-element conversion system according to claim 3, characterized in that, The carbon dioxide enrichment and recycling module (9) includes an integrated series-connected cooler, separator and compressor. The cooler is used to cool the flue gas delivered from the first outlet of the waste heat recovery module (4). The separator is used to perform gas-liquid separation on the flue gas cooled by the cooler to obtain carbon dioxide. The compressor is used to compress the carbon dioxide to obtain high-concentration carbon dioxide.

5. The carbon-based resource hierarchical multi-element conversion system according to claim 3, characterized in that, When the semi-coke at the first preset temperature is burned in the heat carrier oxidizer (7), the volume ratio of carbon dioxide to oxygen in the heat carrier oxidizer (7) is in the range of 3:1 to 7:1, and the temperature range of the semi-coke at the second preset temperature output from the heat carrier oxidizer (7) is 600℃ to 1050℃.

6. The carbon-based resource hierarchical multi-element conversion system according to claim 2, characterized in that, The pyrolysis unit (6) is a riser-type rapid hydrogenation pyrolysis reactor with a rapid mixing and heating zone. The rapid mixing and heating zone is used to mix the solid carbon-based resources with the semi-coke at a second preset temperature delivered from the solid product outlet. The residence time of the solid carbon-based resources in the riser is 2s to 7s. The mass ratio of hydrogen to the solid carbon-based resources at the first gaseous reactant inlet of the pyrolysis unit (6) is in the range of 0.05 to 0.

30.

7. The carbon-based resource hierarchical multi-element conversion system according to any one of claims 1 to 6, characterized in that, The carbon-based resource hierarchical multi-element conversion system also includes a waste heat cascade recovery module (4), the heat carrier oxidizer (7) also includes a gaseous product outlet, the plasma thermal cracking gasification module (3) includes a gaseous outlet, the gaseous product outlet and the gaseous outlet are both connected to the inlet of the waste heat cascade recovery module (4), so that the flue gas generated by the gaseous product outlet and the synthesis gas generated by the gaseous outlet are both input into the waste heat cascade recovery module (4) for recovery, and the recovered heat is used to preheat the water in the water electrolysis module (2).

8. The carbon-based resource hierarchical multi-element conversion system according to claim 7, characterized in that, The water electrolysis module (2) is a solid oxide electrolysis cell. The water entering the water electrolysis module (2) is preheated to 500℃~700℃ by the waste heat recovery module (4), and the electrolysis temperature is maintained at 700℃~1000℃.

9. A method for hierarchical and multi-element conversion of carbon-based resources, characterized in that, The conversion method, applied to the system according to any one of claims 1 to 8, comprises: The renewable energy power generation module (1) is started to supply power to the water electrolysis module (2), the plasma hydrogen radical catalysis module (8) and the plasma thermal cracking gasification module (3) and start them up; The hydrogen generated by the water electrolysis module (2) is transported to the plasma hydrogen radical catalytic module (8) to generate plasma hydrogen radicals; Solid carbon-based resources are input into the pyrolyzer (6) through the first inlet end, so that the solid carbon-based resources and plasma hydrogen radicals undergo hydrogenation pyrolysis reaction in the pyrolyzer (6) to generate gaseous products and solid products; The solid products generated by the pyrolysis unit (6) are transported to the plasma thermal decomposition gasification module (3) and converted into H2 / CO synthesis gas in a high-temperature plasma environment. The gaseous products generated by the pyrolysis unit (6) are transported to the multiphase product fine separation module (5) for separation into gaseous products and liquid products.

10. The method for hierarchical and multi-element conversion of carbon-based resources according to claim 9, characterized in that, The conversion method further includes: The oxygen generated by the water electrolysis module (2), the semi-coke at the first preset temperature generated by the pyrolyzer (6) and the high-concentration carbon dioxide output by the carbon dioxide enrichment and recycling module (9) are all transported to the heat carrier oxidizer (7) so that the semi-coke at the first preset temperature is burned in a mixed atmosphere of oxygen and carbon dioxide, while the heat carrier is heated to generate flue gas and the semi-coke at the second preset temperature. The semi-coke at the second preset temperature is fed back into the pyrolyzer (6) and provides energy for the pyrolysis reaction; The flue gas is transported to the waste heat recovery module (4) for heat recovery.

11. The method for hierarchical and multi-element conversion of carbon-based resources according to claim 9, characterized in that, The conversion method further includes: The syngas generated from the gaseous outlet of the plasma pyrolysis gasification module (3) and the flue gas generated from the gaseous product outlet of the heat carrier oxidizer (7) are transported to the waste heat cascade recovery module (4) for recovery. The heat recovered by the waste heat recovery module (4) is used to preheat the water in the water electrolysis module (2); The remaining flue gas from the waste heat recovery module (4) is transported to the carbon dioxide enrichment and recycling module (9) for recycling, and the remaining syngas is discharged to the outside.

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