Method for driving pyrolusite reduction and carbon-manganese co-production through rapid coal pyrolysis

Abstract

The invention relates to a method for driving pyrolusite reduction and carbon-manganese co-production through rapid coal pyrolysis, which is characterized in that rapid coal pyrolysis is realized based on an infrared radiation heating technology, and high-activity reductive volatile components in the early stage of pyrolysis are synchronously utilized to carry out reduction reaction with pyrolusite, so that the synergistic preparation of a carbon-based product and a manganese resource is realized. The method comprises the following steps: performing pyrolysis on coal in an infrared pyrolysis reactor under the action of a high-intensity radiation heat source at 500-800 DEG C within milliseconds to second-level time to generate high-reducibility volatile components rich in H2, CO, CH4 and short-chain hydrocarbons and semicoke; the volatile component is directly introduced into a pyrolusite reduction reaction zone and is subjected to a gas-solid reduction reaction with MnO2 in pyrolusite at 600-900 DEG C, high-valence manganese oxide is converted into MnO or manganese metal, and meanwhile semicoke is produced to serve as a high value-added carbon material. According to the method, the reduction potential energy of volatile components is reserved to the maximum extent, more than 90% of active components directionally act on pyrolusite reduction, and the problems of high energy consumption, low reduction efficiency and insufficient added value of products in a traditional process are solved.

Description

Technical Field

[0001] The present invention relates to the technical field of coal chemical industry and comprehensive utilization of mineral resources, and specifically to a method for rapidly pyrolyzing coal to drive pyrolusite reduction and co-producing carbon and manganese, and in particular to a method for realizing efficient pyrolysis of coal, synchronously driving pyrolusite reduction, and synergistically preparing carbon materials and manganese products based on infrared rapid heating technology. Background Art

[0002] Pyrolusite (mainly composed of MnO2) is an important manganese resource, and its efficient reduction is a key step in the preparation of metallic manganese and manganese-based materials. Traditional reduction processes mostly use high-temperature carbon thermal reduction or hydrogen / CO gas reduction, which have problems such as high energy consumption, high reducing agent cost, and tail gas pollution. For example, carbon thermal reduction needs to be carried out at a high temperature of more than 1200 ° C, resulting in energy waste and easy generation of harmful gases; gas reduction relies on high-purity H2 or CO, which is complex and has high safety requirements. In addition, in the prior art, pyrolusite reduction and coal pyrolysis processes are usually operated independently, failing to effectively utilize the reducing volatiles (such as H2, CO, CH4 and short-chain hydrocarbons) produced by coal pyrolysis, resulting in resource waste and low energy efficiency.

[0003] Coal pyrolysis technology is an important approach to clean coal utilization. Its semi-coke product can be further processed into high-value-added carbon materials. However, traditional pyrolysis processes suffer from slow heating rates and severe secondary reactions of volatiles, resulting in low reducing gas yields and unstable semi-coke quality. Especially for high-volatile coals, conventional tubular furnaces or fixed-bed reactors have insufficient heating rates to suppress side reactions such as tar condensation, limiting the release of the reducing potential energy of the pyrolysis products. Furthermore, there is limited research on the coupling of coal pyrolysis and pyrolusite reduction processes, lacking a systematic approach for the targeted utilization of volatiles and the coordinated regulation of temperature zones. Summary of the Invention

[0004] The purpose of the present invention is to provide a method for the rapid pyrolysis of coal to drive the reduction of pyrolusite and its carbon and manganese co-production, which realizes the efficient pyrolysis of coal and the efficient reduction of pyrolusite by infrared rapid heating technology, and simultaneously solves the problems of high energy consumption, low reduction efficiency and insufficient product added value in traditional processes. Without the need for external reducing agents, it avoids the generation of CO2, SO X The exhaust gas can be recycled, meeting the requirements of green chemical industry. It can also process various types of coal (lignite, bituminous coal, etc.) and pyrolusite raw materials (natural ore, industrial manganese slag), realizing the synergy of solid waste resource utilization and energy conversion.

[0005] In order to achieve efficient synergistic conversion of coal and pyrolusite, the present invention provides the following technical solution: coal rapid pyrolysis driven pyrolusite reduction and carbon and manganese co-production method.

[0006] When coal is pyrolyzed alone to drive pyrolusite reduction, the process includes the following steps:

[0007] (1) crushing the coal to a particle size of 1-50 mm and the pyrolusite to a particle size of 0.1-5 mm, and loading them into an infrared pyrolysis reactor and a reduction reactor respectively;

[0008] (2) Connect the gas distribution system, infrared pyrolysis reactor, reduction reactor, and product recovery system in sequence, set the carrier gas flow rate to 50 mL / min~1 L / min, the target temperature of the infrared pyrolysis reactor to 500~800 °C, and the target temperature of the reduction reactor to 600~900 °C;

[0009] (3) The infrared pyrolysis reactor is heated at a rate of 10-40 °C / s, and the coal is rapidly pyrolyzed within milliseconds to seconds to produce highly reducing volatiles and semi-coke rich in H2, CO, CH4, and short-chain hydrocarbons.

[0010] (4) The pyrolysis volatiles are directly transported to the reduction reactor via a carrier gas, where they react with pyrolusite (MnO2 content ≥ 60%) to undergo a gas-solid reduction reaction, reducing MnO2 to MnO or metallic manganese.

[0011] (5) The gaseous products after reduction are recovered after condensation and adsorption treatment, and the semi-coke is used as a porous carbon material (specific surface area ≥ 300 m 2 / g) collected directly.

[0012] When the coal pyrolysis and pyrolusite reduction reactions need to be intensified, the following steps are included:

[0013] a. Pre-install a catalyst (such as Fe2O3, Ni / Al2O3 or natural manganese-based ore) in the reduction reactor, with the mass ratio of the catalyst to pyrolusite being 1:10~10:1;

[0014] b. The volatile matter from coal pyrolysis and pyrolusite undergo a catalytic reduction reaction in a reduction reactor, where the catalyst promotes deep reduction of MnO2 and inhibits side reactions;

[0015] c. The gas after catalytic reduction is subjected to graded condensation (-20℃~-50℃) to separate light hydrocarbons and synthesis gas, and the remaining gas is recycled back to the gas distribution system.

[0016] The infrared pyrolysis reactor and the reduction reactor both use infrared radiation heating, and the temperature zones are independently controlled. The heating rate of the pyrolysis zone is 10-40 °C / s, and the constant temperature time of the reduction zone is 10-60 min.

[0017] The gas distribution system includes a high-pressure gas cylinder, a gas mass flow controller and a high-temperature resistant pipeline (inner diameter 6-10 mm, made of stainless steel or quartz), and the carrier gas is nitrogen, argon or H2 / CO mixture.

[0018] The product recovery system includes a condensing unit (-20°C to -50°C refrigeration), a gas adsorption tower (activated carbon or molecular sieve) and a wet flow meter to achieve efficient separation of gas-liquid-solid products.

[0019] The coal is a high-volatile coal such as lignite and bituminous coal, and the pyrolusite is a natural ore or industrial manganese slag (MnO2 content ≥30%).

[0020] The catalyst is a metal oxide, a natural ore, etc., and can be selected according to different reduction depth requirements.

[0021] A device for rapid pyrolysis of coal to drive pyrolusite reduction and its carbon-manganese co-production, comprising a gas distribution system, an infrared pyrolysis reactor, a reduction reactor and a product recovery system. The gas distribution system includes a high-pressure gas cylinder, a gas pressure reducing valve, a gas mass flow controller and a high-temperature resistant pipeline. The infrared pyrolysis reactor and the reduction reactor both use infrared radiation heating, and the temperature zones are independently controlled. The product recovery system includes a condensing unit, a gas adsorption tower and a wet flow meter.

[0022] The heating rate of the pyrolysis zone of the infrared pyrolysis reactor and the reduction reactor is 10-40 °C / s, and the constant temperature time of the reduction zone is 10-60 min.

[0023] The inner diameter of the high-temperature resistant pipeline is 6-10 mm and the material is stainless steel or quartz.

[0024] The beneficial effects of the present invention are:

[0025] (1) Efficient reduction and resource co-production:

[0026] Through infrared rapid heating technology, efficient coal pyrolysis and pyrolusite reduction are achieved, solving the problems of high energy consumption and low reduction efficiency in traditional processes. The H2 and CO volume ratio of the volatile matter from coal pyrolysis is ≥70%, directly driving pyrolusite reduction with a reduction rate of ≥98%, reducing energy consumption by over 40% compared to traditional carbothermal reduction.

[0027] Co-production of high value-added carbon materials (semi-coke specific surface area ≥300 m 2 / g) and manganese products (MnO or metallic manganese), achieving the goal of efficient resource recycling.

[0028] (2) Process optimization and environmental protection

[0029] The independent temperature control technology of different temperature zones is adopted to match the pyrolysis and reduction kinetics requirements, thus avoiding catalyst deactivation and improving reduction efficiency and product added value.

[0030] By optimizing the process parameters, efficient utilization of highly reducing volatiles was achieved, the reduction rate of pyrolusite was improved, and high value-added carbon materials and manganese products were co-produced.

[0031] Infrared rapid heating inhibits secondary pyrolysis reactions, maximizes the retention of volatile reduction activity, and shortens the reaction time to seconds;

[0032] No external reducing agent is required, tail gas is recycled, and CO2 and harmful gas emissions are reduced.

[0033] (3) Wide applicability

[0034] The technical solution of the present invention has wide applicability and is applicable to various types of coal (lignite, bituminous coal, etc.) as well as low-grade pyrolusite or industrial manganese slag (MnO2 content ≥30%), and can achieve the synergy of solid waste resource utilization and energy utilization.

[0035] Catalysts can be flexibly selected (metal oxides, natural ores, etc.) to meet different reduction depth requirements.

[0036] The technical solution of the present invention can effectively reduce energy consumption, improve reduction efficiency, and co-produce high-value-added carbon materials and manganese products, thus having significant economic and social benefits. BRIEF DESCRIPTION OF THE DRAWINGS

[0037] Figure 1 This is a schematic diagram of the process of rapid pyrolysis of coal to drive pyrolusite reduction according to the present invention.

[0038] Figure 2 This is a schematic diagram of the process of rapid coal pyrolysis coupled with catalytic reduction of pyrolusite according to the present invention.

[0039] Marked in the figure are: gas distribution system 1, high-pressure steel cylinder 1-1, gas pressure reducing valve 1-2, gas mass flow controller 1-3, infrared pyrolysis reactor 2, reduction reactor 3, product recovery system 4, refrigerator 4-1, liquid collection bottle 4-2, condensation tank 4-3, gas washing bottle 4-4, gas filter 4-5, wet flow meter 4-6, gas collecting tank 4-7. DETAILED DESCRIPTION

[0040] The technical solution of the present invention is further described below with reference to the accompanying drawings and examples. It should be noted that the term "connection" herein encompasses conventional methods such as direct welding, flange connection, or sealed butt connection of pipes. All equipment components (such as high-pressure cylinders, reactors, flow meters, etc.) are standard components commonly used in the art or can be manufactured using known techniques.

[0041] Example 1

[0042] This embodiment is a device for coal rapid pyrolysis driven pyrolusite reduction and carbon and manganese co-production according to the present invention, comprising a gas distribution system 1, an infrared pyrolysis reactor 2, a reduction reactor 3, and a product recovery system 4. The specific structure and connection relationship are as follows:

[0043] The gas distribution system 1 includes a high-pressure steel cylinder 1-1, a gas pressure reducing valve 1-2, a gas mass flow controller 1-3 and a high-temperature resistant pipeline; the outlet of the high-pressure steel cylinder 1-1 is connected to the gas pressure reducing valve 1-2 through a pipeline through a flange; the outlet of the gas pressure reducing valve 1-2 is connected to the gas mass flow controller 1-3 through a flange; the outlet of the gas mass flow controller 1-3 is directly connected to the carrier gas inlet of the infrared pyrolysis reactor 2 through a high-temperature resistant pipeline (inner diameter 6-10 mm, stainless steel / quartz).

[0044] The coal inlet of the infrared pyrolysis reactor 2 is located at the top of the reactor, and the pyrolysis volatiles outlet is sealed and connected to the gas inlet of the reduction reactor 3 via a high-temperature resistant pipeline. The gas inlet of the reduction reactor 3 is located at the bottom of the reduction reactor 3, and the pyrolusite is loaded into the reduction reactor 3. The gas outlet pipeline is sealed and connected to the product recovery system 4. The infrared pyrolysis reactor 2 and the reduction reactor 3 are both heated by infrared radiation and independently controlled. The heating rate of the pyrolysis zone is 10-40 ° C / s, and the reduction zone is kept at a constant temperature of 600-900 ° C for 10-60 minutes.

[0045] The product recovery system 4 includes a refrigerator 4-1, a liquid collecting bottle 4-2, a condensation tank 4-3, a gas washing bottle 4-4, a gas filter 4-5, a wet flow meter 4-6 and a gas collecting tank 4-7. The refrigerator 4-1 is directly and sealedly connected to the condensation tank 4-3 through a coolant circulation pipeline, and the gas outlet of the pyrolysis reactor 2 is connected to the inlet of the liquid collecting bottle 4-2 through a high-temperature resistant pipeline for receiving tar-containing volatiles; the liquid collecting bottle 4-2 is immersed in the condensation tank 4-3, and the gas outlet of the liquid collecting bottle 4-2 is directly and sealedly connected to the inlet of the gas washing bottle 4-4. The gas washing bottle 4-4 is filled with an organic solvent (acetone / methanol, etc.), and the gas enters the inlet of the gas filter 4-5 after washing. The gas filter 4-5 is filled with cotton, and the outlet is sealed and connected to the wet flow meter 4-6 to measure the gas flow; the outlet of the wet flow meter 4-6 is directly and sealedly connected to the gas collecting tank 4-7 to temporarily store the recyclable gas.

[0046] Working principle and process:

[0047] Carrier gas introduction: Nitrogen / argon is regulated by the gas distribution system (1) at a flow rate of 50 mL / min-1 L / min and introduced into the infrared pyrolysis reactor (2).

[0048] Coal rapid pyrolysis: Coal particles are heated to 500-800 °C at a rate of 10-40 °C / s under infrared radiation, and pyrolyzed within milliseconds to produce semi-coke and highly reducing volatiles (H2, CO, CH4, etc.).

[0049] Volatile matter reduction of pyrolusite: The pyrolytic volatile matter is carried by the carrier gas into the reduction reactor (3) and undergoes a gas-solid reduction reaction with pyrolusite at 600-900 °C (MnO2→MnO / metallic manganese).

[0050] Example 2

[0051] like Figure 1 As shown, this embodiment is an example of the method for rapid pyrolysis of coal driven pyrolusite reduction and carbon and manganese co-production of the present invention, comprising the following steps:

[0052] The equipment used is as described in Example 1.

[0053] (1) Raw material crushing and filling

[0054] The lignite was crushed to a particle size of 10 mm, and the pyrolusite (MnO2 content 70%) was crushed to a particle size of 1 mm, and loaded into the infrared pyrolysis reactor 2 and the reduction reactor 3 respectively.

[0055] (2) System connection and parameter setting

[0056] Connect the gas distribution system 1 (high-pressure cylinder 1-1, gas pressure reducing valve 1-2, gas mass flow controller 1-3), infrared pyrolysis reactor 2, reduction reactor 3, and product recovery system 4 in sequence. Set the carrier gas (nitrogen) flow rate to 500 mL / min, the target temperature of the infrared pyrolysis reactor to 700 °C, and the target temperature of the reduction reactor to 850 °C.

[0057] (3) Coal rapid pyrolysis

[0058] The infrared pyrolysis reactor heating program was started, and the heating rate was controlled at 10 °C / s. The coal was pyrolyzed within 5 seconds, generating highly reducing volatile matter (H2 and CO accounted for 78% of the total volume) and semi-coke.

[0059] (4) Pyrolusite reduction

[0060] The pyrolysis volatiles are directly transported to the reduction reactor 3 via a carrier gas, with a mass ratio of volatiles to pyrolusite of 3:1, and a gas-solid reduction reaction is carried out at 850°C to produce metallic manganese (purity 98.5%) and a small amount of MnO.

[0061] (5) Product recovery

[0062] The reduced gas is separated into light hydrocarbons by condensation unit 4-1 (-30 °C), and the remaining gas is purified by washing bottle 4-4 and then recovered; the semi-coke is directly collected as a porous carbon material.

[0063] Example 3

[0064] like Figure 2 As shown, this embodiment is another example of the method for rapid pyrolusite reduction driven by coal pyrolysis and carbon-manganese co-production according to the present invention. When the coal pyrolysis and pyrolusite reduction reactions need to be intensified, the equipment used is the same as that in Example 2, including the following steps:

[0065] (1) Raw material crushing and filling

[0066] Bituminous coal (volatile matter 38%) was crushed to a particle size of 20 mm, and pyrolusite (MnO2 content 70%) was crushed to a particle size of 1 mm, and loaded into the infrared pyrolysis reactor 2 and the reduction reactor 3 respectively.

[0067] (2) Catalyst pre-installation

[0068] The Fe2O3 catalyst is pre-installed in the reduction reactor 3, and the mass ratio of the catalyst to the pyrolusite is 1:5.

[0069] (3) System connection and parameter setting

[0070] The carrier gas (nitrogen) flow rate was set at 500 mL / min, the target temperature of the infrared pyrolysis reactor was 750 °C (heating rate 20 °C / s), and the target temperature of the reduction reactor was 800 °C (constant temperature 40 min).

[0071] (4) Catalytic reduction reaction

[0072] The pyrolysis volatiles (H2+CO volume share 82%) and pyrolusite are deeply reduced under the catalysis of Fe2O3, and the generated metallic manganese accounts for 85%.

[0073] (5) Product recovery and tail gas circulation

[0074] The gas after catalytic reduction is subjected to graded condensation (-30 °C) to separate light hydrocarbons and synthesis gas, and the remaining gas is recycled back to the gas distribution system; the semi-coke is directly collected.

[0075] Example 4

[0076] This embodiment is another example of the method for rapid pyrolysis-driven pyrolusite reduction and carbon-manganese co-production according to the present invention. The equipment used is the same as that of Example 2, and the method includes the following steps:

[0077] (1) Raw material crushing and filling

[0078] The lignite (volatile matter 50%) was crushed to a particle size of 30 mm, and the industrial manganese slag (MnO2 content 30%) was crushed to a particle size of 3 mm, and loaded into the infrared pyrolysis reactor 2 and the reduction reactor 3 respectively.

[0079] (2) System connection and parameter setting

[0080] The carrier gas (nitrogen) flow rate was set at 500 mL / min, the target temperature of the infrared pyrolysis reactor was set at 600 °C (heating rate 10 °C / s), and the target temperature of the reduction reactor was set at 700 °C (constant temperature 50 min).

[0081] (3) Coal rapid pyrolysis

[0082] Coal is pyrolyzed within 10 seconds, generating volatile matter (H2 and CO account for 70% of the total volume) and semi-coke.

[0083] (4) Pyrolusite reduction

[0084] The mass ratio of volatile matter to pyrolusite is 2:1, and MnO (accounting for 90%) is generated by reduction at 700 °C.

[0085] (5) Product recovery

[0086] After the gas is condensed, the H2+CO recycling rate reaches 80%; the semi-coke is directly collected.

[0087] It is particularly noted that the high-pressure steel cylinder 1-1, gas pressure reducing valve 1-2, gas mass flow controller 1-3, condensing unit 4-1, etc. described in the present invention are all universal standard parts, and their sizes can be adjusted according to experimental requirements. The pyrolysis reactor 2 and the reduction reactor 3 adopt a temperature zone independent temperature control design, with the temperature range of the pyrolysis zone being 500-800 ° C and the reduction zone being 600-900 ° C, which are suitable for different types of coal and pyrolusite grades. The carrier gas can be nitrogen, argon, or an H2 / CO mixture to optimize the reducing atmosphere. The method does not require the addition of an external reducing agent, and can produce 250 kg of carbon material and 600 kg of manganese product per ton of coal processed, increasing the overall benefit by more than 50%.

[0088] The sizes of the pyrolysis reactor 2, the catalytic pyrolysis reactor 3, the condensation tank 4-3, the liquid collection bottle 4-2 and the gas collecting tank 4-7 of the present invention are not fixed values, and their sizes can be specifically determined according to experimental conditions.

[0089] The present invention may have various embodiments. Without departing from the spirit and essence of the present invention, changes in shape and size made to the disclosure of the present invention shall fall within the scope of protection of the claims of the present invention.

Claims

1. A method for rapid pyrolysis of coal to drive pyrolusite reduction and carbon-manganese co-production method, characterized in that: The following steps are involved: (1) crushing the coal to a particle size of 1-50 mm and the pyrolusite to a particle size of 0.1-5 mm, and loading them into an infrared pyrolysis reactor and a reduction reactor respectively; (2) Connect the gas distribution system, infrared pyrolysis reactor, reduction reactor, and product recovery system in sequence, set the carrier gas flow rate to 50 mL / min~1 L / min, the target temperature of the infrared pyrolysis reactor to 500~800 °C, and the target temperature of the reduction reactor to 600~900 °C; (3) starting the infrared pyrolysis reactor heating program at a heating rate of 10-40 °C / s, causing the coal to be rapidly pyrolyzed within milliseconds to seconds to generate highly reducing volatiles and semi-coke rich in H2, CO, CH4, and short-chain hydrocarbons, wherein the total volume proportion of H2 and CO in the highly reducing volatiles is ≥70%; (4) The pyrolysis volatiles are directly transported to the reduction reactor via a carrier gas, and undergo a gas-solid reduction reaction with pyrolusite having a MnO2 content of ≥60%, thereby reducing MnO2 to MnO or metallic manganese, with the mass ratio of the volatiles to the pyrolusite being 1:2 to 5:1; (5) The gas product after reduction is recovered after condensation and adsorption treatment, and the semi-coke is used as a porous carbon material with a specific surface area of ≥300 m 2 / g.

2. The method for rapid pyrolysis-driven pyrolusite reduction and carbon-manganese co-production thereof according to claim 1, characterized in that: When the coal pyrolysis and pyrolusite reduction reactions need to be intensified, the following steps are included: a. Pre-install a catalyst (such as Fe2O3, Ni / Al2O3 or natural manganese-based ore) in the reduction reactor, with the mass ratio of the catalyst to pyrolusite being 1:10~10:1; b. The volatile matter from coal pyrolysis and pyrolusite undergo a catalytic reduction reaction in a reduction reactor, where the catalyst promotes deep reduction of MnO2 and inhibits side reactions; c. The gas after catalytic reduction is condensed at -20°C to -50°C to separate light hydrocarbons and synthesis gas, and the remaining gas is recycled back to the gas distribution system.

3. The method for rapid pyrolysis-driven pyrolusite reduction and carbon-manganese co-production thereof according to claim 1 or 2, characterized in that: The infrared pyrolysis reactor and the reduction reactor both use infrared radiation heating, and the temperature zones are independently controlled. The heating rate of the pyrolysis zone is 10-40 °C / s, and the constant temperature time of the reduction zone is 10-60 min.

4. The method for rapid pyrolysis-driven pyrolusite reduction and carbon-manganese co-production thereof according to claim 1 or 2, characterized in that: The gas distribution system includes a high-pressure gas cylinder, a gas mass flow controller and a high-temperature resistant pipeline with an inner diameter of 6-10 mm and a material of stainless steel or quartz. The carrier gas is nitrogen, argon or an H2 / CO mixture.

5. The method for rapid pyrolysis-driven pyrolusite reduction and carbon-manganese co-production thereof according to claim 1 or 2, characterized in that: The product recovery system includes a condensing unit with a -20°C to -50°C refrigeration temperature, an activated carbon or molecular sieve gas adsorption tower, and a wet flow meter to achieve efficient separation of gas-liquid-solid products.

6. The method for rapid pyrolysis-driven pyrolusite reduction and carbon-manganese co-production thereof according to claim 1 or 2, characterized in that: The coal is a high-volatile coal such as lignite and bituminous coal, and the pyrolusite is a natural ore or industrial manganese slag with a MnO2 content of ≥30%.

7. The method for rapid pyrolysis-driven pyrolusite reduction and carbon-manganese co-production thereof according to claim 2, characterized in that: The catalyst is a metal oxide or a natural ore, which is selected according to different reduction depth requirements.

8. A device for rapid pyrolysis of coal to drive pyrolusite reduction and carbon and manganese co-production, characterized in that: It includes a gas distribution system, an infrared pyrolysis reactor, a reduction reactor and a product recovery system. The specific structure and connection relationship are as follows: The gas distribution system includes a high-pressure steel cylinder, a gas pressure reducing valve, a gas mass flow controller and a high-temperature resistant pipeline; the outlet of the high-pressure steel cylinder is connected to the gas pressure reducing valve through a pipeline through a flange; the outlet of the gas pressure reducing valve is connected to the gas mass flow controller through a flange; the outlet of the gas mass flow controller is directly connected to the carrier gas inlet of the infrared pyrolysis reactor through a high-temperature resistant pipeline; The infrared pyrolysis reactor is sealed and connected to the gas inlet of the reduction reactor through a high-temperature resistant pipeline. The gas inlet of the reduction reactor is located at the bottom of the reduction reactor, and the gas outlet pipeline of the reduction reactor is sealed and connected to the product recovery system. The infrared pyrolysis reactor and the reduction reactor are both heated by infrared radiation and have independent temperature control. The product recovery system includes a refrigerator, a liquid collection bottle, a condensation tank, a gas washing bottle, a gas filter, a wet flow meter and a gas collecting tank. The refrigerator is directly and sealedly connected to the condensation tank through a coolant circulation pipeline. The gas outlet of the pyrolysis reactor is connected to the inlet of the liquid collection bottle through a high-temperature resistant pipeline for receiving tar-containing volatiles; the liquid collection bottle is immersed in the condensation tank, the gas outlet of the liquid collection bottle is directly and sealedly connected to the inlet of the gas washing bottle, the gas washing bottle is filled with an organic solvent, and the gas enters the inlet of the gas filter after washing. The gas filter is filled with cotton, the gas filter outlet is sealed and connected to the wet flow meter, and the wet flow meter outlet is directly and sealedly connected to the gas collecting tank.

9. The device according to claim 8, characterized in that The heating rate of the pyrolysis zone of the infrared pyrolysis reactor and the reduction reactor is 10-40 °C / s, and the constant temperature time of the reduction zone is 10-60 min.

10. The device according to claim 8, characterized in that The carrier gas in the gas distribution system is nitrogen, argon or H2 / CO mixed gas. The inner diameter of the high-temperature resistant pipeline is 6-10 mm and the material is stainless steel or quartz.

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