Poly-generation system and method for enhancing pyrolusite reduction through co-pyrolysis of low-rank coal and biomass

Abstract

According to the poly-generation system and method for enhancing pyrolusite reduction through co-pyrolysis of the low-rank coal and the biomass, through the two-section bed design of a pyrolysis reactor and a pyrolusite reduction reactor, reducing gases such as H2, CO and CH4 generated through co-pyrolysis of the low-rank coal and the biomass are directionally guided into the pyrolusite reduction reactor, and pyrolusite conversion is achieved. Pyrolysis gas, tar and semicoke products are synchronously produced at the temperature of 500-800 DEG C in the pyrolysis stage, and MnO2 is efficiently converted into MnO and Mn3O4 at the temperature of 400-600 DEG C in the reduction stage. The pyrolysis reactor and the reduction reactor are separately arranged, so that the pyrolysis temperature and the reduction temperature are independently regulated and controlled, the reduction gas yield is increased through biomass alkali metal catalysis, pyrolusite reduction activation energy is cooperatively reduced, the advantages of efficient resource conversion and low carbon emission are achieved, and the method is suitable for industrial production. And a new path is provided for collaborative utilization of low-rank coal, biomass and manganese ore resources.

Description

Technical Field

[0001] The present invention relates to the technical field of energy chemical industry and comprehensive utilization of mineral resources, and in particular to a polygeneration system and method for enhancing pyrolusite reduction by co-pyrolysis of low-rank coal and biomass. Background Art

[0002] With the transformation of the global energy structure and the increasing demand for efficient resource utilization, the high-value utilization of low-rank coal and the development of low-grade manganese ore resources have become important research directions. Low-rank coal has the characteristics of high volatility, high oxygen content, and poor thermal stability. Its direct combustion efficiency is low and it is highly polluting. Although its pyrolysis technology can be converted into high-value-added products such as tar and coal gas, pyrolysis alone has problems such as many heavy components in tar and low carbon conversion rate. At the same time, biomass, as a renewable carbon source, can release active hydrogen and light volatiles during its pyrolysis process. When co-pyrolyzed with low-rank coal, it can significantly improve the quality of pyrolysis products through hydrogen supply effect and synergistic reaction. However, existing co-pyrolysis technologies mostly focus on fuel co-production, and lack systematic integration of the multi-path utilization of reducing pyrolysis gas.

[0003] On the other hand, pyrolusite, a significant manganese resource in my country, primarily consists of MnO₂. Traditional reduction processes rely on high-temperature or strong-acid leaching, resulting in high energy consumption and significant pollution. In recent years, biomass-based reducing agents have garnered significant attention due to their low-carbon properties. However, the reduction of pyrolusite using biomass coke alone suffers from low reaction rates, insufficient manganese reduction rates (<85%), and poor solid-solid mass transfer efficiency. Notably, the reducing gases (such as CO, H₂, and CH₄) and active hydrogen produced by the co-pyrolysis of low-rank coal and biomass possess strong reducing power. Directly utilizing these gases for pyrolusite reduction would not only achieve efficient utilization of pyrolysis gas but also replace traditional fossil-based reducing agents, reducing the process's carbon footprint. Existing patents and literature, such as biomass coke roasting for pyrolusite reduction and low-rank coal pyrolysis polygeneration, have partially addressed the single-feedstock utilization issue but have yet to fully integrate the pyrolysis-reduction-product separation process. For example, traditional heat transfer methods are prone to tar carryover and reactor clogging, while fixed-bed or rotary kiln reduction systems struggle to meet the high throughput requirements of rapid pyrolysis gas. In addition, the lack of integrated design for the catalytic cracking of macromolecular aromatics in pyrolysis tar and the high-value utilization of MnO products restricts the economic efficiency of the system.

[0004] Therefore, it is urgent to develop a multi-product system for the co-pyrolysis of low-rank coal and biomass to enhance the reduction of pyrolusite. Through infrared rapid heating, gas-solid reactor optimization and product cascade utilization, the efficient reduction of pyrolusite by pyrolysis gas, catalytic upgrading of tar and resource utilization of semi-coke can be achieved simultaneously, forming a new clean production model of "waste treatment and energy-quality coupling". Summary of the Invention

[0005] The present invention aims to provide a multi-product system and method for enhancing pyrolusite reduction through the co-pyrolysis of low-rank coal and biomass. This system generates high-concentration reducing gases through the co-cracking reaction of oxygenated volatiles in biomass with the aromatic structures of low-rank coal. Rapid infrared heating technology and a graded temperature control strategy lower the pyrolusite reduction temperature to 350-550°C. A specially designed two-stage reactor achieves directional transport of reducing gas and selective conversion of manganese oxides, simultaneously producing high-quality pyrolysis oil and gaseous products. This technology integrates the pyrolysis heating, mineral reduction, and pollution control steps of traditional processes into a closed-loop system, reducing overall energy consumption by over 42% compared to existing technologies. This technology creates a new path for synergistic efficiency enhancement through the graded conversion of solid fuels and low-carbon smelting of strategic metals.

[0006] To achieve the above objectives, the present invention provides the following technical solution: a polygeneration system for enhancing pyrolusite reduction by co-pyrolysis of low-rank coal and biomass, comprising a gas distribution system, a pyrolysis system, a reduction system, and a product recovery system, the specific structure and connection relationship of which are as follows:

[0007] The gas distribution system includes a high-pressure gas cylinder, a gas pressure reducing valve and a gas flow controller, which are connected in sequence with a silicone hose with an inner diameter of 6 mm. The gas distribution system is used to pass inert gas into the pyrolysis reactor and the reduction reactor to maintain an inert atmosphere in the reactor;

[0008] The pyrolysis system includes a feed inlet, a solid residue discharge port and a pyrolysis reactor, wherein the feed inlet and the solid residue discharge port are connected to the pyrolysis reactor by welding, and the pyrolysis reactor is used to perform a pyrolysis reaction on a mixture of low-rank coal and biomass;

[0009] The reduction system includes a reduction reactor, an air inlet pipe, a solid residue discharge port, and a solid residue reduction reactor. The air inlet pipe and the solid residue discharge port are connected to the reduction reactor by welding. The solid residue discharge port is connected to the solid residue reduction reactor by welding. The reduction reactor is used to perform a reduction reaction on pyrolusite. The air inlet pipe is used to transport the reducing gas generated by the pyrolysis reactor to the reduction reactor. The solid residue reduction reactor is used to perform a secondary reduction reaction on the coke generated by the pyrolysis reactor and the pyrolusite in the reduction reactor.

[0010] The product recovery system includes a condensing device, a gas filter, a wet flow meter, a gas collecting tank and a pyrolusite separation device, which are connected in sequence with a silicone hose with an inner diameter of 6 mm. The condensing device is used to collect pyrolysis tar, the gas filter is used to dry the pyrolysis gas, the wet flow meter is used to monitor the gas flow, the gas collecting tank is used to collect the gas products after the reduction reaction, and the pyrolusite separation device is used to separate the reduced coke from the pyrolusite.

[0011] In the gas distribution system, the inert gas is nitrogen, and the gas flow rate is controlled at 0.5-1 L / min.

[0012] The pyrolysis reactor is heated by infrared radiation with a heating rate of 10-40 °C / s.

[0013] The reduction reactor adopts a fluidized bed structure and the temperature is controlled at 400-600 °C.

[0014] The temperature of the solid residue reduction reactor is controlled at 400-600 °C, and the stirring device is turned on during the reaction.

[0015] The product recovery system further includes a condenser, a refrigerator, a liquid collection bottle, a gas washing bottle, a gas filter and a wet flow meter, which are sequentially connected by a silicone hose with an inner diameter of 6 mm.

[0016] A polygeneration method for enhancing pyrolusite reduction by co-pyrolysis of low-rank coal and biomass comprises the following steps:

[0017] (1) crushing and pre-treating low-rank coal, biomass and pyrolusite, and mixing the pre-treated low-rank coal and biomass in proportion. When the low-rank coal and biomass are co-pyrolyzed, a synergistic hydrogen supply effect is generated;

[0018] (2) The low-rank coal and biomass mixture is loaded into an infrared pyrolysis reactor, and the pyrolusite powder is placed in a fluidized bed reduction reactor, and the two reactors are connected by a high-temperature resistant metal pipe;

[0019] (3) Connect the gas distribution system, pyrolysis reactor, reduction reactor, and product recovery system, set the pyrolysis zone temperature to 500-800 °C, the reduction zone temperature to 400-600 °C, and maintain the reaction time at 30 min;

[0020] (4) Open the gas distribution system to introduce nitrogen into the reactor to maintain an inert atmosphere in the reactor;

[0021] (5) Start the pyrolysis reactor temperature rising program and condensation device, the low-rank coal and biomass undergo pyrolysis reaction at high temperature, and the reducing gas generated is carried to the fluidized bed reduction reactor filled with manganese ore by the carrier gas;

[0022] (6) The reducing gas containing H2, CO, and CH4 generated by pyrolysis is transported to the fluidized bed reduction reactor via a carrier gas, and undergoes a gas-solid phase reduction reaction with pyrolusite, with a reaction contact time of 8-25 seconds;

[0023] (7) The solid residues in the pyrolysis reactor and the reduction reactor are transported to the solid residue reactor through a pipeline, and the two are fully mixed and then subjected to a secondary reduction reaction;

[0024] (8) The pyrolysis tar is collected in a condensation device. After the reaction is completed, the solid matter is separated using a pyrolusite separation device, and the gaseous products are collected in a gas collection system.

[0025] The biomass is agricultural and forestry waste, the moisture content of which is controlled at 8%-15%, and is co-pyrolyzed with low-rank coal to produce a synergistic hydrogen supply effect.

[0026] The particle size of the low-rank coal and biomass is less than 100 mesh, the particle size of the pyrolusite is 100-300 mesh, and the pretreatment is drying at 100°C for 2 h.

[0027] The mixing ratios of the low-rank coal and biomass are 1:3, 1:1, and 3:1.

[0028] The pyrolysis reactor and the reduction reactor are both heated by infrared radiation, with a heating rate of 10-40 °C / s.

[0029] The beneficial effects of the present invention are:

[0030] 1. Through the synergistic co-pyrolysis of low-rank coal and biomass, combining the hydrogen-rich characteristics of biomass with the high volatile matter advantage of low-rank coal, the tar yield and light component content in the pyrolysis products are significantly improved, while reducing the generation of macromolecular products.

[0031] 2. Utilize the reducing gas generated by co-pyrolysis to achieve efficient reduction of manganese ore, forming a resource polygeneration model, which not only improves energy utilization but also reduces pollution emissions.

[0032] 3. Temperature gradient control and reactor separation design optimize the synergy between pyrolysis and reduction reactions, enhancing the overall system efficiency and product quality.

[0033] 4. The system's product separation module reduces energy consumption while achieving clean co-production of multi-form products, combining environmental benefits with resource recycling advantages. BRIEF DESCRIPTION OF THE DRAWINGS

[0034] Figure 1 This is a process schematic diagram of the polygeneration system for co-pyrolysis of low-rank coal and biomass to enhance pyrolusite reduction according to the present invention.

[0035] Marked in the figure are: gas distribution system 1, high-pressure steel cylinder 1-1, gas pressure reducing valve 1-2, gas flow controller 1-3, pyrolysis system 2, feed inlet 2-1, pyrolysis reactor 2-2, solid residue discharge port 2-3, reduction system 3, reduction reactor 3-1, air inlet pipe 3-2, solid residue discharge port 3-3, solid residue reduction reactor 3-4, product recovery system 4, condensing device 4-1, gas filter 4-2, wet flow meter 4-3, gas collecting tank 4-4, pyrolusite separation device 4-5. DETAILED DESCRIPTION

[0036] The technical solution of the present invention is further described in detail below through the accompanying drawings and embodiments.

[0037] First, it should be noted that, in the description of the present invention, unless otherwise expressly specified or limited, the terms "connected" and "connection" should be understood broadly. For example, they may refer to fixed connections, detachable connections, or integral connections; they may be mechanical connections or electrical connections; and they may be direct connections or indirect connections through an intermediary. Those skilled in the art will understand the specific meanings of the above terms in the present invention based on specific circumstances.

[0038] Example 1

[0039] This embodiment is a polygeneration system for enhancing pyrolusite reduction by co-pyrolysis of low-rank coal and biomass according to the present invention, comprising a gas distribution system 1, a pyrolysis system 2, a reduction system 3, and a product recovery system 4. The specific structure and connection relationship are as follows:

[0040] The gas distribution system 1 includes a high-pressure gas cylinder 1-1, a gas pressure reducing valve 1-2, and a gas flow controller 1-3, which are connected in sequence with a silicone hose with an inner diameter of 6 mm. The gas distribution system 1 is used to pass inert gas into the pyrolysis reactor 2-2 and the reduction reactor 3-1 to maintain an inert atmosphere in the reactor;

[0041] The pyrolysis system 2 includes a feed port 2-1 and a pyrolysis reactor 2-2, which are connected by welding. The pyrolysis reactor 2-2 is used to perform a pyrolysis reaction on the low-rank coal and biomass mixture;

[0042] The reduction system 3 includes a reduction reactor 3-1, an air inlet pipe 3-2, a solid residue discharge port 3-3 and a solid residue reactor 3-4. The air inlet pipe 3-2 and the solid residue discharge port 3-3 are connected to the reduction reactor 3-1 by welding, and the solid residue discharge port 3-3 is connected to the solid residue reduction reactor 3-4 by welding. The reduction reactor 3-1 is used to reduce pyrolusite, the air inlet pipe 3-2 is used to transport the reducing gas generated by the pyrolysis reactor 2-2 to the reduction reactor 3-1, and the solid residue reactor 3-4 is used to perform secondary reduction on the solid residue generated by the pyrolysis reactor 2-2 and the reduction reactor 3-2 through the solid residue discharge port 3-3;

[0043] The product recovery system 4 includes a condensing device 4-1, a gas filter 4-2, a wet flow meter 4-3, a gas collecting tank 4-4, and a pyrolusite separation device 4-5, which are connected in sequence with a silicone hose with an inner diameter of 6 mm. The coolant in the condensing device 4-1 is ethylene glycol, which can be cooled to below -20 ° C. The gas filter 4-2 is connected to the wet flow meter 4-3, and the wet flow meter 4-3 is connected to the gas collecting tank 4-4 and the gas product analyzer. The pyrolusite separation device 4-5 is used to separate the reduced coke from the pyrolusite.

[0044] The condensing device 4-1 is used to collect pyrolysis tar, and the gas collecting tank 4-4 is used to collect gas products after the reduction reaction. In the gas distribution system 1, the inert gas is nitrogen, and the gas flow rate is controlled at 0.5-1 L / min.

[0045] The pyrolysis reactor 2-2 is heated by infrared radiation with a heating rate of 10-40 °C / s.

[0046] The reduction reactor 3-1 adopts a fluidized bed structure, and the temperature is controlled at 400-600 °C.

[0047] Example 2

[0048] This embodiment is an example of the polygeneration method for enhancing pyrolusite reduction by co-pyrolysis of low-rank coal and biomass, comprising the following steps:

[0049] (1) Pretreatment and mixing: Low-rank coal with a particle size of 5 mm and corn straw with a particle size of 3 mm were crushed in accordance with the particle size requirements of claim 8, and then mixed in a mass ratio of 1:1 (corresponding to the mixing ratio of claim 10), and the crushed pretreated sample was dried at 100°C for 2 h.

[0050] (2) Material filling: The mixed material is fed into the infrared pyrolysis reactor 2-2 from the feed port 2-1, and the pyrolusite powder is filled into the fluidized bed reduction reactor 3-1. The two reactors are connected by a high-temperature resistant metal pipe.

[0051] (3) System connection and parameter setting: The gas distribution system, pyrolysis reactor, reduction reactor, and product recovery system were connected as in Example 1. The pyrolysis temperature was set to 500°C, which meets the temperature requirement of claim 6. The temperature of the reduction reactor 3-1 was set to 400°C, which meets the temperature requirement of claim 4. The reaction residence time was 30 min, which meets the time requirement of claim 6.

[0052] (4) Introducing inert gas: Open the high-pressure cylinder 1-1 and introduce nitrogen, which meets the inert gas requirements of claim 2. Adjust the gas flow rate to 800 ml / min, i.e., 0.8 L / min, which meets the range of 0.5-1 L / min of claim 2, to maintain an inert atmosphere in the reactor.

[0053] (5) Start the pyrolysis reaction: Start the pyrolysis reactor heating program at a heating rate of 20 °C / s, and turn on the condensation device at the same time; low-rank coal and biomass are pyrolyzed at 500 °C, and the generated reducing gas is carried into the fluidized bed reduction reactor 3-1 by the carrier gas.

[0054] (6) Gas-solid phase reduction reaction: The pyrolysis gas is introduced into the reduction reactor 3-1 at 400 °C to undergo a reduction reaction with the pyrolusite. In this example, the total residence time is 30 min.

[0055] (7) Secondary reduction reaction: The solid residues in the pyrolysis reactor and the reduction reactor are transported to the solid residue reactor through a pipeline. The temperature of the solid residue reactor is set to 500 °C. After the two are fully mixed, a secondary reduction reaction is carried out.

[0056] (8) Product recovery: The pyrolysis tar is collected through a condensation device, the reduced solid matter is separated by a pyrolusite separation device, and the gas product is collected into a gas collection system; under this condition, the pyrolusite reduction rate is 78%, the tar yield is 32%, and the gas calorific value is 12MJ / m 3 .

[0057] Example 3

[0058] This embodiment is another example of the polygeneration method for enhancing pyrolusite reduction by co-pyrolysis of low-rank coal and biomass, comprising the following steps:

[0059] (1) Pretreatment and mixing: Low-rank coal with a particle size of 5 mm and pine sawdust with a particle size of 5 mm were crushed in accordance with the particle size requirements of the claim, and then mixed in a mass ratio of 1:2, corresponding to the mixing ratio of claim 10, and the crushed pretreated sample was dried at 100 °C for 2 h.

[0060] (2) Material filling: The mixed material is fed into the infrared pyrolysis reactor 2-2 from the feed port 2-1, and the pyrolusite powder is filled into the fluidized bed reduction reactor 3-1. The two reactors are connected by a high-temperature resistant metal pipe.

[0061] (3) System connection and parameter setting: The gas distribution system, pyrolysis reactor, reduction reactor, and product recovery system were connected as in Example 1. The pyrolysis temperature was set to 700 °C, which met the temperature requirement of the pyrolysis zone in the claims. The temperature of the reduction reactor 3-1 was set to 500 °C, which met the temperature requirement of the reduction zone in the claims. The reaction residence time was set to 25 min, which met the time requirement in the claims.

[0062] (4) Introducing inert gas: Open the high-pressure cylinder 1-1 and introduce nitrogen, which meets the inert gas requirements of the claims. Adjust the gas flow rate to 500 ml / min, i.e. 0.5 L / min, to maintain an inert atmosphere in the reactor.

[0063] (5) Start the pyrolysis reaction: Start the pyrolysis reactor heating program at a heating rate of 20 °C / s, and turn on the condensation device at the same time; low-rank coal and pine sawdust are pyrolyzed at 700 °C, and the generated reducing gas is carried into the fluidized bed reduction reactor 3-1 by the carrier gas.

[0064] (6) Gas-solid phase reduction reaction: The pyrolysis gas is introduced into the reduction reactor 3-1 at 500 °C to undergo a reduction reaction with the pyrolusite. In this example, the total residence time is 25 min.

[0065] (7) Secondary reduction reaction: The solid residues in the pyrolysis reactor and the reduction reactor are transported to the solid residue reactor through a pipeline. The temperature of the solid residue reactor is set to 500 °C. After the two are fully mixed, a secondary reduction reaction is carried out.

[0066] (8) Product recovery: The pyrolysis tar is collected through a condensation device, the reduced solid matter is separated by a pyrolusite separation device, and the gaseous products are collected in a gas collection system; under this condition, the pyrolusite reduction rate reaches 88%, the proportion of benzene compounds in the tar increases by 20%, and the system energy efficiency ratio increases by 15%.

[0067] It is particularly noted that the pyrolysis reactor 2-2, reduction reactor 3-1, solid residue reduction reactor 3-4, condensing device 4-1, gas filter 4-2, wet flow meter 4-3, gas collecting tank 4-4 and pyrolusite separation device 4-5 described in the present invention are not fixed values, and their sizes can be specifically determined according to experimental conditions.

[0068] 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 polygeneration system for enhancing pyrolusite reduction by co-pyrolysis of low-rank coal and biomass, characterized in that: It includes gas distribution system, pyrolysis system, reduction system and product recovery system. The specific structure and connection relationship are as follows: The gas distribution system includes a high-pressure gas cylinder, a gas pressure reducing valve and a gas flow controller, which are connected in sequence with a silicone hose with an inner diameter of 6 mm. The gas distribution system is used to introduce inert gas into the pyrolysis reactor and the reduction reactor to maintain an inert atmosphere in the reactor; The pyrolysis system includes a feed inlet, a solid residue discharge port and a pyrolysis reactor, wherein the feed inlet and the solid residue discharge port are connected to the pyrolysis reactor by welding, and the pyrolysis reactor is used to perform a pyrolysis reaction on a mixture of low-rank coal and biomass; The reduction system includes a reduction reactor, an air inlet pipe, a solid residue discharge port, and a solid residue reduction reactor. The air inlet pipe and the solid residue discharge port are connected to the reduction reactor by welding. The solid residue discharge port is connected to the solid residue reduction reactor by welding. The reduction reactor is used to perform a reduction reaction on pyrolusite. The air inlet pipe is used to transport the reducing gas generated by the pyrolysis reactor to the reduction reactor. The solid residue reduction reactor is used to perform a secondary reduction reaction on the coke generated by the pyrolysis reactor and the pyrolusite in the reduction reactor. The product recovery system includes a condensing device, a gas filter, a wet flow meter, a gas collecting tank and a pyrolusite separation device, which are connected in sequence with a silicone hose with an inner diameter of 6 mm. The condensing device is used to collect pyrolysis tar, the gas filter is used to dry the pyrolysis gas, the wet flow meter is used to monitor the gas flow, the gas collecting tank is used to collect the gas products after the reduction reaction, and the pyrolusite separation device is used to separate the reduced coke from the pyrolusite.

2. The polygeneration system for enhancing pyrolusite reduction by co-pyrolysis of low-rank coal and biomass according to claim 1, characterized in that: In the gas distribution system, the inert gas is nitrogen, and the gas flow rate is controlled at 0.5-1 L / min.

3. The polygeneration system for enhancing pyrolusite reduction by co-pyrolysis of low-rank coal and biomass according to claim 1, characterized in that: The pyrolysis reactor is heated by infrared radiation with a heating rate of 10-40 °C / s.

4. The polygeneration system for enhancing pyrolusite reduction by co-pyrolysis of low-rank coal and biomass according to claim 1, characterized in that: The reduction reactor adopts a fluidized bed structure and the temperature is controlled at 400-600 °C.

5. The polygeneration system for enhancing pyrolusite reduction by co-pyrolysis of low-rank coal and biomass according to claim 1, characterized in that: The temperature of the solid residue reduction reactor is controlled at 400-600 °C, and the stirring device is turned on during the reaction.

6. A polygeneration method for enhancing pyrolusite reduction by co-pyrolysis of low-rank coal and biomass, characterized in that: The following steps are involved: (1) crushing and pre-treating low-rank coal, biomass and pyrolusite, and mixing the pre-treated low-rank coal and biomass in proportion; (2) The low-rank coal and biomass mixture is loaded into an infrared pyrolysis reactor, and the pyrolusite powder is placed in a fluidized bed reduction reactor, and the two reactors are connected by a high-temperature resistant metal pipe; (3) Connect the gas distribution system, pyrolysis reactor, reduction reactor, and product recovery system, set the pyrolysis zone temperature to 500-800 °C, the reduction zone temperature to 400-600 °C, and maintain the reaction time for 30 min; (4) Open the gas distribution system to introduce nitrogen into the reactor to maintain an inert atmosphere in the reactor; (5) Start the pyrolysis reactor temperature rising program and condensation device, the low-rank coal and biomass undergo pyrolysis reaction at high temperature, and the reducing gas generated is carried to the fluidized bed reduction reactor filled with manganese ore by the carrier gas; (6) The reducing gas containing H2, CO, and CH4 generated by pyrolysis is transported to the fluidized bed reduction reactor via a carrier gas, and undergoes a gas-solid phase reduction reaction with pyrolusite, with a reaction contact time of 8-25 seconds; (7) The solid residues in the pyrolysis reactor and the reduction reactor are transported to the solid residue reactor through a pipeline, and the two are fully mixed and then subjected to a secondary reduction reaction; the pyrolysis reactor and the reduction reactor are both heated by infrared radiation, with a heating rate of 10-40 °C / s; (8) The pyrolysis tar is collected in a condensation device. After the reaction is completed, the solid matter is separated using a pyrolusite separation device, and the gaseous products are collected in a gas collection system.

7. The polygeneration method of co-pyrolysis of low-rank coal and biomass to enhance pyrolusite reduction according to claim 6, characterized in that: The biomass is agricultural and forestry waste, the moisture content of which is controlled at 8%-15%, and is co-pyrolyzed with low-rank coal to produce a synergistic hydrogen supply effect.

8. The polygeneration method of co-pyrolysis of low-rank coal and biomass to enhance pyrolusite reduction according to claim 6, characterized in that: The particle size of the low-rank coal and biomass is below 100 mesh, the particle size of the pyrolusite is 100-300 mesh, and the pretreatment is drying at 100°C for 2 hours.

9. The polygeneration method of co-pyrolysis of low-rank coal and biomass to enhance pyrolusite reduction according to claim 6, characterized in that: The mixing ratios of the low-rank coal and biomass are 1:3, 1:1, and 3:1.

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