A self-heating pyrolysis co-generation system

Abstract

This invention provides a self-heating pyrolysis char co-production system. The main body of the system is a pyrolysis reactor, which consists of five sections: a feeding section, a drying section, a transition section, a pyrolysis section, and a cooling section. It is used for the entire process of processing biomass such as logs from feeding, drying, pyrolysis to cooling. The pyrolysis gas produced is sent to a pyrolysis gas burner to produce flue gas. Part of the flue gas heats the drying and pyrolysis processes in the reactor, while another part is sent to a waste heat boiler to produce steam. The flue gas after waste heat utilization is purified by a series of flue gas purification devices before being discharged. Furthermore, during the cooling of the pyrolyzed char, heat is exchanged with nitrogen. The generated hot nitrogen exchanges heat with water in a nitrogen cooler to produce hot water. The cooled nitrogen is then sent back to the cooling section to achieve nitrogen circulation. This system not only significantly improves the quality, production efficiency, and capacity of the pyrolyzed char but also co-produces steam and hot water, resulting in significant economic benefits.

Description

Technical Field

[0001] This invention belongs to the field of charcoal burning technology, and specifically relates to a self-heating pyrolysis co-generation system. Background Technology

[0002] Under the strategic backdrop of "peak carbon and carbon neutrality," the efficient and clean utilization of forestry biomass resources has become a key pathway to reduce dependence on fossil fuels. Pyrolysis, as an important biomass energy conversion pathway, has received widespread attention and in-depth research in recent years. Converting forestry biomass resources into high-value-added biochar through pyrolysis can achieve carbon sequestration and replace coal-fired heating, meeting the dual policy requirements of circular economy and pollution control. Most existing biochar is machine-made, which uses loose agricultural and forestry waste such as wood chips, straw, sawdust, bamboo shavings, and peanut shells as raw materials, processed into high-density columnar or block solid fuel through "pretreatment-forming-pyrolysis carbonization" or "pretreatment-pyrolysis carbonization-forming." However, machine-made biochar produced through these processes often suffers from poor quality due to the addition of binders during production. In contrast, biochar produced using whole or naturally shaped biomass such as logs is of higher quality. Therefore, how to achieve biochar production from logs is a core technical challenge that urgently needs to be overcome in the field of high-value utilization of forestry biomass resources. It is also a key path to promote the upgrading of biochar from "fuel grade" to "high-quality functional grade" and better match the dual needs of carbon sequestration and clean heating.

[0003] Traditional raw charcoal production equipment mainly consists of earthen kilns and vehicle-mounted retorts. Earthen kilns work by loading wood into the kiln and controlling the oxygen supply to allow the wood to slowly pyrolyze under anaerobic conditions, ultimately forming charcoal. This process has a long production cycle, taking more than ten days from loading to charcoal output. Furthermore, this method relies heavily on manual experience, making precise control of temperature and oxygen levels difficult, which can lead to inconsistent product quality. Additionally, the flue gas generated during the pyrolysis process in earthen kilns is emitted directly without treatment, causing environmental pollution. Vehicle-mounted retorts employ an intermittent production mode, requiring a series of processes including loading, heating, cooling, and unloading for each production run. This results in low production efficiency and cannot meet the large-scale demands of modern industry for raw charcoal.

[0004] It is evident that traditional log charcoal production equipment is insufficient to meet the demands of large-scale industrial production. Furthermore, existing equipment focuses solely on the pyrolysis and carbonization process itself, lacking a systematic consideration of the overall production process. The utilization rate of pyrolysis gas is low; a large amount of combustible gas generated during pyrolysis is not fully and effectively recovered and reused, resulting in significant energy waste. In addition, excessively high charcoal exit temperatures can easily lead to smoldering, which not only threatens equipment safety but may also cause a decline in product quality. To address the problems of traditional processes and existing equipment, there is an urgent need to develop a self-heating pyrolysis cogeneration system to achieve a highly efficient, continuous, environmentally friendly, and economical log charcoal pyrolysis production process, meeting the ever-evolving needs of the energy and environmental protection sectors. Summary of the Invention

[0005] To address the aforementioned technical problems, this invention provides a self-heating pyrolysis charcoal cogeneration system, which enables continuous production of raw charcoal while simultaneously producing steam and hot water, resulting in significant economic benefits.

[0006] To achieve the above objectives, the technical solution of the present invention is as follows:

[0007] A self-heating pyrolysis cogeneration system, characterized in that the system comprises: a pyrolysis reactor, a pyrolysis gas burner, a waste heat boiler, an SCR device, an economizer, a flue gas dust collector, an integrated desulfurization chimney, a drying gas cooler, a nitrogen cooler, and a drying gas dust collector.

[0008] The pyrolysis reactor is used for drying raw materials, pyrolysis treatment, and cooling of pyrolysis char.

[0009] The pyrolysis gas burner is connected to the pyrolysis reactor and is used to receive the pyrolysis gas generated by the pyrolysis reactor. Part of the flue gas generated by the combustion of the pyrolysis gas is sent to the pyrolysis reactor to provide energy for the drying and pyrolysis process in the pyrolysis reactor. The remaining part of the flue gas is sent to the waste heat boiler for steam production.

[0010] The waste heat boiler is connected to the pyrolysis reactor and the pyrolysis gas burner, and is used to receive flue gas and use the heat of the flue gas to produce steam.

[0011] The SCR device is connected to the waste heat boiler and is used for the denitrification treatment of flue gas after waste heat utilization.

[0012] The economizer is connected to the SCR device and is used to heat the demineralized water using the waste heat of the flue gas at the outlet of the SCR device to supply water to the waste heat boiler, while reducing the exhaust gas temperature.

[0013] The flue gas dust collector is connected to the economizer and is used for flue gas dust removal;

[0014] The desulfurization chimney integrated machine is connected to the flue gas dust collector and is used for flue gas desulfurization and flue gas emission.

[0015] Preferably, the pyrolysis reactor is a multi-stage self-heating pyrolysis charcoal production pyrolysis furnace, the main body of which is a furnace body. The furnace body is divided into 5 sections, including a feeding section, a drying section, a transition section, a pyrolysis section, and a cooling section arranged sequentially and connected to each other. A movable trolley for carrying raw materials is installed inside the lower part of the pyrolysis reactor furnace body.

[0016] Preferably, the pyrolysis reactor is provided with liftable furnace doors between the feed section and the drying section, between the drying section and the transition section, between the transition section and the pyrolysis section, and between the pyrolysis section and the cooling section. The left end of the feed section and the right end of the cooling section are provided with liftable furnace doors for overall sealing of the pyrolysis reactor.

[0017] Preferably, the drying section has several parallel drying flue gas inlets below it, which are connected to the pyrolysis gas burner. The drying flue gas inlets directly supply the flue gas generated by the combustion of pyrolysis gas in the pyrolysis gas burner to provide heat for the drying process. The top of the drying section has a drying gas outlet for discharging the drying gas mixture of flue gas and steam generated during drying. The top of the drying section is also equipped with a temperature detector for detecting the temperature inside the drying section, which is 100-200℃.

[0018] Preferably, the drying gas is discharged from the drying gas outlet of the drying section and then sent into the drying gas cooler for cooling. The cooled drying gas is then sent into the drying gas dust collector for dust removal before being discharged.

[0019] Preferably, the pyrolysis section is the place where raw materials are pyrolyzed to produce pyrolytic char. A plurality of parallel pyrolysis flue gas inlets are provided on one side below the pyrolysis section. One end of each pyrolysis flue gas inlet is connected to the pyrolysis gas burner, and the other end is connected to one end of a heating coil located in the pyrolysis section. The other end of the heating coil is connected to one end of a plurality of pyrolysis flue gas outlets located on the other side below the pyrolysis section. The other ends of the plurality of pyrolysis flue gas outlets are connected to the waste heat boiler. The flue gas generated by the pyrolysis gas burner burning pyrolysis gas is sent into the heating coil in the pyrolysis section through the plurality of pyrolysis flue gas inlets, and then sent into the waste heat boiler after passing through the plurality of pyrolysis flue gas outlets, thus completing the heating of the pyrolysis section by the flue gas.

[0020] Preferably, the other end of the pyrolysis flue gas inlet is connected to the pyrolysis gas burner, through which flue gas generated by the combustion of pyrolysis gas by the pyrolysis gas burner is introduced. The introduced flue gas enters the heating coil, and the heating coil heats the raw material dried in the drying section within the pyrolysis section through radiative heat transfer. Several pyrolysis gas outlets are provided above the pyrolysis section, and the pyrolysis gas generated by pyrolysis is sent to the pyrolysis gas burner through the pyrolysis gas outlets. A temperature detector is also provided at the top of the pyrolysis section for detecting the internal temperature of the pyrolysis section, and the temperature of the pyrolysis section is 500-600℃.

[0021] Preferably, the cooling section is the place where the pyrolytic carbon produced by the pyrolysis of the raw materials in the pyrolysis section is cooled by nitrogen gas.

[0022] The cooling section has several parallel cold nitrogen inlets on one side below it, several parallel supplementary nitrogen inlets on the other side below it, and several parallel hot nitrogen outlets on the top of it. The cold nitrogen inlets are connected to the top of the nitrogen cooler, the supplementary nitrogen inlets are connected to an external nitrogen source, and the hot nitrogen outlets are connected to the bottom of the nitrogen cooler.

[0023] When the pyrolysis reactor is started, nitrogen gas is introduced into the cooling section through the supplementary nitrogen inlet; after the pyrolysis char is sent out from the pyrolysis section, it enters the cooling section and exchanges heat with the nitrogen gas sent back from the cold nitrogen inlet to cool down, and then it is sent out from the cooling section to complete the cooling of the pyrolysis char.

[0024] The nitrogen gas supplied through the supplementary nitrogen inlet exchanges heat with the pyrolytic carbon and is heated to become hot nitrogen gas, which is then discharged from the cooling section through the hot nitrogen outlet and sent to the nitrogen cooler for cooling.

[0025] Preferably, the nitrogen cooler is a spray tower structure, in which hot nitrogen is cooled by spraying cold water, and the hot nitrogen is cooled by exchanging heat with the sprayed cold water to become cold nitrogen, which is then sent into the cooling section through the cold nitrogen inlet to complete the nitrogen circulation; the cold water sprayed by the nitrogen cooler exchanges heat with the hot nitrogen generated in the cooling section to become hot water.

[0026] Preferably, the nitrogen circulation occurring within the cooling section includes the following steps:

[0027] S1: When the pyrolysis reactor is started, only the supplementary nitrogen inlet is opened, and an external nitrogen source is introduced into the cooling section through the supplementary nitrogen inlet to establish an inert atmosphere;

[0028] S2: After the start-up stage is completed, the supplementary nitrogen inlet is closed and the cold nitrogen inlet is opened to enter the normal operation stage. After the pyrolysis carbon is sent out from the pyrolysis section, it enters the cooling section and exchanges heat with the nitrogen gas sent back from the cold nitrogen inlet to cool down. Then it is sent out from the cooling section to complete the cooling of the pyrolysis carbon.

[0029] S3: When the furnace is started, the nitrogen gas supplied through the supplementary nitrogen inlet exchanges heat with the pyrolytic carbon and becomes hot nitrogen gas, which is discharged from the cooling section through the hot nitrogen outlet and fed into the nitrogen cooler from the bottom. The hot nitrogen gas flows from the bottom of the nitrogen cooler to the top of the nitrogen cooler, during which it exchanges heat with the sprayed cold water to perform a cooling treatment. The cooled nitrogen gas is then sent back to the cooling section through the cold nitrogen inlet.

[0030] The beneficial effects of this invention are as follows:

[0031] 1. This invention proposes a self-heating pyrolysis charcoal cogeneration system, which addresses the technical limitations of traditional log pyrolysis charcoal and machine-made charcoal production, achieving continuous production throughout the entire process of log and other biomass feeding, drying, pyrolysis, and charcoal cooling. This system not only significantly improves the production efficiency and capacity of log pyrolysis charcoal but also stably produces high-quality log charcoal;

[0032] 2. The system innovatively integrates co-generation of char and heat. During the pyrolysis of biomass such as logs that are intact or in their natural form, in addition to generating the main product, pyrolysis char, it also simultaneously produces pyrolysis gas rich in combustible components. The flue gas generated by the combustion of the pyrolysis gas in the pyrolysis gas burner can not only provide heat for the drying and pyrolysis processes, but can also be sent to the waste heat boiler to produce steam, effectively broadening the system's output categories.

[0033] 3. By implementing a closed-loop circulation of hot and cold nitrogen between the cooling section of the pyrolysis reactor and the nitrogen cooler, highly efficient coupling of high-temperature pyrolysis char cooling and waste heat recovery is achieved. While ensuring the production of high-quality pyrolysis char in the pyrolysis reactor, hot water is produced through the nitrogen cooler. This design transforms the cooling process from an energy-consuming stage to a production-generating stage, further improving the system's economic efficiency. Attached Figure Description

[0034] Figure 1 This is a schematic diagram of the self-heating pyrolysis co-generation system provided in Embodiment 1 of the present invention;

[0035] Figure 2 This is a schematic diagram of the drying section of the pyrolysis reactor in the self-heating pyrolysis cogeneration system provided in Embodiment 1 of the present invention;

[0036] Figure 3 This is a schematic diagram of the pyrolysis section of the pyrolysis reactor in the self-heating pyrolysis cogeneration system provided in Embodiment 1 of the present invention;

[0037] Figure 4 This is a schematic diagram of the cooling section of the pyrolysis reactor in the self-heating pyrolysis cogeneration system provided in Embodiment 1 of the present invention;

[0038] Figure 5This is a schematic diagram of the overall assembly of the pyrolysis reactor in the self-heating pyrolysis cogeneration system provided in Embodiment 2 of the present invention;

[0039] Figure 6 This is a schematic diagram of the feed section of the pyrolysis reactor in the self-heating pyrolysis cogeneration system provided in Embodiment 2 of the present invention;

[0040] Figure 7 This is a schematic diagram of the drying section of the pyrolysis reactor in the self-heating pyrolysis cogeneration system provided in Embodiment 2 of the present invention;

[0041] Figure 8 This is a schematic diagram of the transition section of the pyrolysis reactor in the self-heating pyrolysis cogeneration system provided in Embodiment 2 of the present invention;

[0042] Figure 9 This is a schematic diagram of the pyrolysis section of the pyrolysis reactor in the self-heating pyrolysis cogeneration system provided in Embodiment 2 of the present invention;

[0043] Figure 10 This is a schematic diagram of the cooling section of the pyrolysis reactor in the self-heating pyrolysis cogeneration system provided in Embodiment 2 of the present invention;

[0044] Figure 11 A schematic diagram of the pyrolysis reactor trolley of the self-heating pyrolysis cogeneration system provided in an embodiment of the present invention;

[0045] Figure 12 A schematic diagram of the heating coil of the pyrolysis section of the pyrolysis reactor in the self-heating pyrolysis cogeneration system provided in an embodiment of the present invention;

[0046] Figure 13 This is a schematic diagram of the control system of the self-heating pyrolysis co-generation system provided in Embodiment 3 of the present invention;

[0047] Figure 14 The control logic of the control unit for the BP neural network of the drying section provided in Embodiment 3 of the present invention;

[0048] Figure 15 The control logic of the control unit of the pyrolysis-carbon cogeneration system provided in Embodiment 3 of the present invention;

[0049] Figure 16 The control unit provided in Embodiment 3 of the present invention provides the bidirectional LSTM neural network control logic for the pyrolysis section;

[0050] Figure 17 The control logic of the control unit for the cooling section of the present invention is provided in Embodiment 3 of the present invention.

[0051] Figure 18The control logic of the control unit for the flue gas purification unit provided in Embodiment 3 of the present invention is a multi-task BP neural network.

[0052] Figure 19 The control logic of the control unit for the incineration and waste heat utilization unit provided in Embodiment 3 of the present invention is the LSTM+BP neural network control logic.

[0053] Figure label:

[0054] 1: Pyrolysis reactor; 1-1: Feed section; 1-2: Drying section; 1-2-1: Drying flue gas inlet; 1-2-2: Drying gas outlet; 1-3: Transition section; 1-4: Pyrolysis section; 1-4-1: Pyrolysis flue gas inlet; 1-4-2: Heating coil; 1-4-3: Pyrolysis flue gas outlet; 1-4-4: Pyrolysis gas outlet; 1-5: Cooling section; 1-5-1: Cold nitrogen inlet; 1-5-2: Supplementary nitrogen inlet; 1-5-3: Hot nitrogen outlet; 1-6: Trolley; 2: Pyrolysis gas burner; 3: Waste heat boiler; 4: SCR device; 5: Economizer; 6: Flue gas dust collector; 7: Desulfurization chimney integrated unit; 8: Drying gas cooler; 9: Nitrogen cooler; 10: Drying gas dust collector. Detailed Implementation

[0055] To make the technical problems, technical solutions and advantages of the present invention clearer, a detailed description will be given below in conjunction with the accompanying drawings and specific embodiments.

[0056] Example 1:

[0057] like Figure 1 As shown, an embodiment of the present invention provides a self-heating pyrolysis cogeneration system, comprising: a pyrolysis reactor 1, a pyrolysis gas burner 2, a waste heat boiler 3, an SCR device 4, an economizer 5, a flue gas dust collector 6, a desulfurization chimney integrated machine 7, a drying gas cooler 8, a nitrogen cooler 9, and a drying gas dust collector 10.

[0058] The pyrolysis reactor 1 is used for drying raw materials, pyrolysis treatment, and cooling of pyrolysis char. The pyrolysis gas burner 2 is connected to the pyrolysis reactor 1 and is used to receive the pyrolysis gas generated by the pyrolysis reactor 1. Part of the flue gas generated from the combustion of the pyrolysis gas is fed into the pyrolysis reactor 1 to supply energy for the drying and pyrolysis processes carried out in the pyrolysis reactor 1. The remaining part of the flue gas is sent to the waste heat boiler 3 for steam production. The waste heat boiler 3 is connected to both the pyrolysis reactor 1 and the pyrolysis gas burner 2 and is used to receive the flue gas... The flue gas is heated and its heat is used to produce steam. The SCR device 4 is connected to the waste heat boiler 3 for denitrification of the flue gas after waste heat utilization. The economizer 5 is connected to the SCR device 4 for heating demineralized water using the waste heat of the flue gas at the outlet of the SCR device 4 to supply water to the waste heat boiler 3, while reducing the exhaust gas temperature. The flue gas dust collector 6 is connected to the economizer 5 for flue gas dust removal. The desulfurization chimney integrated machine 7 is connected to the flue gas dust collector 6 for flue gas desulfurization and flue gas emission.

[0059] Furthermore, the pyrolysis reactor 1 is a multi-stage self-heating pyrolysis charcoal production pyrolysis furnace, the main body of which is the furnace body. The furnace body is divided into 5 sections, including a feeding section 1-1, a drying section 1-2, a transition section 1-3, a pyrolysis section 1-4, and a cooling section 1-5 arranged sequentially and connected to each other. A movable trolley 1-6 for carrying raw materials is provided on the lower inner side of the furnace body of the pyrolysis reactor 1.

[0060] Furthermore, the pyrolysis reactor 1 is provided with liftable furnace doors between the feed section 1-1 and the drying section 1-2, between the drying section 1-2 and the transition section 1-3, between the transition section 1-3 and the pyrolysis section 1-4, and between the pyrolysis section 1-4 and the cooling section 1-5. The left end of the feed section 1-1 and the right end of the cooling section 1-5 are provided with liftable furnace doors for the overall sealing of the pyrolysis reactor 1.

[0061] like Figure 2 As shown, several parallel drying flue gas inlets 1-2-1 are provided below the drying section 1-2. The drying flue gas inlets 1-2-1 are connected to the pyrolysis gas burner 2. The drying flue gas inlets 1-2-1 directly enter the pyrolysis gas burner 2 to burn the flue gas generated by the pyrolysis gas, providing heat for the drying process. The top of the drying section is provided with a drying gas outlet 1-2-2, which is used to discharge the drying gas mixed with the steam generated during drying. The top of the drying section 1-2 is also provided with a temperature detector, which is used to detect the temperature inside the drying section 1-2. The internal temperature of the drying section 1-2 is 100-200℃.

[0062] Furthermore, after the drying gas is discharged from the drying gas outlet 1-2-2 of the drying section 1-2, it is sent into the drying gas cooler 8 for cooling. The cooled drying gas is then sent into the drying gas dust collector 10 for dust removal before being discharged.

[0063] like Figure 3 and Figure 12 As shown, the pyrolysis section 1-4 is the site where pyrolysis of raw materials produces pyrolytic char. Several parallel pyrolysis flue gas inlets 1-4-1 are located on one side below the pyrolysis section 1-4. One end of each pyrolysis flue gas inlet 1-4-1 is connected to the pyrolysis gas burner 2, and the other end is connected to one end of a heating coil 1-4-2 located within the pyrolysis section 1-4. The other end of the heating coil 1-4-2 is connected to one end of several pyrolysis flue gas outlets 1-4-3 located on the other side below the pyrolysis section 1-4. The other ends of the several pyrolysis flue gas outlets 1-4-3 are connected to the waste heat boiler 3. The flue gas generated by the pyrolysis gas burner 2 is fed into the heating coil 1-4-2 within the pyrolysis section 1-4 via the several pyrolysis flue gas inlets 1-4-1, and then into the waste heat boiler 3 after passing through the several pyrolysis flue gas outlets 1-4-3, thus completing the heating of the pyrolysis section 1-4 by the flue gas.

[0064] Furthermore, the other end of the pyrolysis flue gas inlet 1-4-1 is connected to the pyrolysis gas burner 2, through which flue gas generated by the combustion of pyrolysis gas by the pyrolysis gas burner 2 is introduced. The introduced flue gas enters the heating coil 1-4-2, and the heating coil 1-4-2 heats the raw material dried in the drying section 1-2 within the pyrolysis section 1-4 through radiative heat transfer. Several pyrolysis gas outlets 1-4-4 are provided above the pyrolysis section 1-4, through which the pyrolysis gas generated by pyrolysis is sent to the pyrolysis gas burner 2. A temperature detector is also provided at the top of the pyrolysis section 1-4 to detect the internal temperature of the pyrolysis section 1-4, which is 500-600℃.

[0065] like Figure 4As shown, cooling section 1-5 is the cooling area for the pyrolytic carbon produced from the pyrolysis raw materials in pyrolysis section 1-4. The pyrolytic carbon is cooled by nitrogen gas. Several parallel-arranged cold nitrogen inlets 1-5-1 are located on one side below cooling section 1-5, and several parallel-arranged supplementary nitrogen inlets 1-5-2 are located on the other side below cooling section 1-5. Several parallel-arranged hot nitrogen outlets 1-5-3 are located at the top of cooling section 1-5. The cold nitrogen inlets 1-5-1 are connected to the top of the nitrogen cooler 9, the supplementary nitrogen inlets 1-5-2 are connected to an external nitrogen source, and the hot nitrogen outlets 1-5-3... 3 is connected to the bottom of the nitrogen cooler 9; when the pyrolysis reactor 1 is started, nitrogen is introduced into the cooling section 1-5 through the supplementary nitrogen inlet 1-5-2; after the pyrolysis carbon is sent out from the pyrolysis section 1-4, it enters the cooling section 1-5 and exchanges heat with the nitrogen introduced from the supplementary nitrogen inlet 1-5-2 to cool down, and then is sent out of the cooling section 1-5 to complete the cooling of the pyrolysis carbon; the hot nitrogen gas that is heated by the nitrogen introduced from the supplementary nitrogen inlet 1-5-2 after exchanging heat with the pyrolysis carbon is discharged from the cooling section 1-5 through the hot nitrogen outlet 1-5-3 and sent into the nitrogen cooler 9 for cooling treatment.

[0066] Furthermore, the nitrogen cooler 9 is a spray tower structure, which cools the hot nitrogen by spraying cold water. The hot nitrogen exchanges heat with the sprayed cold water and is cooled into cold nitrogen, which is then sent into the cooling section 1-5 through the cold nitrogen inlet 1-5-1 to complete the nitrogen circulation. The cold water sprayed by the nitrogen cooler 9 exchanges heat with the hot nitrogen generated in the cooling section 1-5 to become hot water.

[0067] It is understood that, in this embodiment, the nitrogen circulation occurring in the cooling section 1-5 includes the following steps: S1: When the pyrolysis reactor 1 is started, only the supplementary nitrogen inlet 1-5-2 is opened, and an external nitrogen source introduces nitrogen into the cooling section 1-5 through the supplementary nitrogen inlet 1-5-2 to establish an inert atmosphere; S2: After the start-up stage is completed, the supplementary nitrogen inlet 1-5-2 is closed, and the cold nitrogen inlet 1-5-1 is opened to enter the normal operation stage. After the pyrolysis char is sent out from the pyrolysis section 1-4 and enters the cooling section 1-5, it circulates with the nitrogen from the cold nitrogen inlet 1-5-1. The returned nitrogen gas is cooled by heat exchange and then sent out of the cooling section 1-5 to complete the cooling of the pyrolytic carbon; S3: When the furnace is started, the nitrogen gas sent in by the supplementary nitrogen inlet 1-5-2 exchanges heat with the pyrolytic carbon and becomes hot nitrogen gas, which is discharged from the cooling section 1-5 through the hot nitrogen outlet 1-5-3 and sent into the nitrogen cooler 9 from the bottom. The hot nitrogen gas flows from the bottom of the nitrogen cooler 9 to the top of the nitrogen cooler (9), and exchanges heat with the sprayed cold water during the process to perform cooling treatment. The cooled nitrogen gas is sent back to the cooling section 1-5 through the cold nitrogen inlet 1-5-1.

[0068] Example 2:

[0069] like Figures 5 to 12 As shown, in order to more clearly illustrate the technical solution and advantages of the present invention, adjustments have been made to the multi-stage self-heating pyrolysis charcoal production device in the previous embodiment, as follows:

[0070] A multi-stage self-heating pyrolysis charcoal production device includes a feeding section 1-1, a drying section 1-2, a transition section 1-3, a pyrolysis section 1-4, a cooling section 1-5, a trolley 1-6, and a track for carrying raw materials and restricting the movement of the trolley 1-6.

[0071] In this embodiment, the main body of the feeding section 1-1 is a furnace body consisting of three interconnected feeding sections. Each feeding section furnace body consists of left and right furnace walls, a furnace top perpendicular to the left and right furnace walls, and two lower edges of the furnace body perpendicular to the left and right furnace walls. The inner sides of the lower ends of the left and right furnace walls of the feeding section furnace body are respectively provided with sealing grooves, and the inner sides of the lower edges of the furnace body perpendicular to the left and right furnace walls of the feeding section are respectively provided with sealing grooves.

[0072] Comparison Figure 2 In a preferred embodiment, the drying section of the pyrolysis reactor 1 is mainly composed of four interconnected drying section furnace bodies. Each drying section furnace body consists of left and right furnace walls, a furnace top perpendicular to the left and right furnace walls, and two lower edges of the furnace body perpendicular to the left and right furnace walls. Sealing grooves are respectively provided on the inner side of the lower end of the left and right furnace walls of the drying section furnace body, and sealing grooves are respectively provided on the inner side of the lower edge of the furnace body perpendicular to the left and right furnace walls.

[0073] Those skilled in the art can also, as needed, introduce the pyrolysis flue gas from the pyrolysis flue gas outlet 1-4-3 into the drying section 1-2 through the drying flue gas inlet 1-2-1, while simultaneously separating the drying flue gas from the drying gas generated during the drying process. A flue gas inlet is opened on the outer side of the lower right furnace wall of the four drying section furnace bodies. The flue gas inlet is connected to one end of the drying flue gas inlet 1-2-1, and the other end of the drying flue gas inlet 1-2-1 is connected to a connecting flue pipe. The connecting flue pipe extends from the beginning of the first drying section furnace body of the drying section 1-2 to the last section of the pyrolysis section 1-4. The tail end of the drying section furnace body is provided; a smoke outlet is opened on the outer side of the lower end of the left furnace wall of each drying section furnace body, and the smoke outlet is connected to the drying flue gas outlet; a drying section heating coil is also provided on the inner side of the left and right furnace walls of each drying section furnace body, and the drying flue gas flows and exchanges heat in the drying section heating coil before being discharged, realizing the separation of drying flue gas and drying gas. The two ends of the drying section heating coil are respectively connected to the smoke inlet and the smoke outlet; a drying gas outlet 1-2-2 is opened in the middle of the furnace top of each drying section furnace body, and the drying gas outlet 1-2-2 is connected to the drying gas manifold, which is connected to the drying gas dust collector 10.

[0074] It is understood that in this embodiment, the pyrolysis gas generated by the pyrolysis of logs or other intact or naturally shaped biomass in the pyrolysis section 1-4 is sent to the pyrolysis gas burner 2 for combustion to produce high-temperature flue gas. A portion of the flue gas is sent from the pyrolysis flue gas inlet 1-4-1 to the heating coil 1-4-2, then through the pyrolysis flue gas outlet 1-4-3 into the connecting flue pipe, and subsequently sent to the drying section 1-2 to provide heat for the drying section.

[0075] In this embodiment, the main body of the transition section 1-3 is a three-section transition section furnace body. Each transition section furnace body includes left and right furnace walls, a furnace top perpendicular to the left and right furnace walls, and two lower edges of the furnace body perpendicular to the left and right furnace walls. The inner side of the lower end of the left and right furnace walls of each transition section furnace body is provided with a sealing groove, and the lower edge of each transition section furnace body is provided with a sealing groove.

[0076] Furthermore, each transition section furnace body has a nitrogen outlet at the lower end of the left and right furnace walls, which is connected to the transition section nitrogen outlet pipe; each transition section furnace body has a nitrogen purging hole at the middle position of the furnace top, which is connected to the transition section nitrogen inlet pipe.

[0077] In this embodiment, the main body of the pyrolysis section 1-4 is a four-section pyrolysis furnace body. Each pyrolysis furnace body includes left and right furnace walls, a furnace top perpendicular to the left and right furnace walls, and two lower edges perpendicular to the left and right furnace walls. Sealing grooves are respectively provided on the inner side of the lower end of the left and right furnace walls of each pyrolysis furnace body, and sealing grooves are also provided on the inner side of the lower edge of each pyrolysis furnace body. A flue gas inlet is opened on the outer side of the lower end of the left furnace wall of each pyrolysis furnace body, and the flue gas inlet is connected to one end of the pyrolysis flue gas inlet 1-4-1. A flue gas outlet is opened on the outer side of the lower end of the right furnace wall of each pyrolysis furnace body, and the flue gas outlet is connected to the pyrolysis flue gas inlet 1-4-1. One end of the gas outlet 1-4-3 and the other end of the pyrolysis flue gas inlet 1-4-1 are connected to the communication flue pipe; the inner sides of the left and right furnace walls of each pyrolysis section furnace body are also provided with pyrolysis section heating coils 1-4-2, the two ends of which are respectively connected to the pyrolysis flue gas inlet 1-4-1 and the pyrolysis flue gas outlet 1-4-3; the middle of the furnace top of each pyrolysis section furnace body is provided with a pyrolysis gas outlet 1-4-4, the pyrolysis gas outlet 1-4-4 is connected to one end of the pyrolysis gas manifold, and the other end of the pyrolysis gas manifold is connected to the pyrolysis gas burner 2.

[0078] In this embodiment, the main body of the cooling section 1-5 is a four-section cooling section furnace body. Each cooling section furnace body includes left and right furnace walls, a furnace top perpendicular to the left and right furnace walls, and two lower edges of the furnace body perpendicular to the left and right furnace walls. The inner side of the lower end of the left and right furnace walls of each cooling section furnace body is provided with a sealing groove, and the inner side of the lower edge of each cooling section furnace body is provided with a sealing groove. A nitrogen inlet hole is opened on the outer side of the lower end of the left and right furnace walls of each cooling section furnace body. The nitrogen inlet hole is connected to one end of the cold nitrogen inlet 1-5-1, and the other end of the cold nitrogen inlet 1-5-1 is connected to the bottom end of the nitrogen cooler 9. A hot nitrogen outlet 1-5-3 is opened in the middle of the furnace top of each cooling section furnace body. The hot nitrogen outlet 1-5-3 is connected to the top end of the nitrogen cooler 9.

[0079] In this embodiment, each drying section 1-2 furnace body, each transition section 1-3 furnace body, each pyrolysis section 1-4 furnace body, and each cooling section 1-5 furnace body are provided with a heat insulation layer, the heat insulation layer being made of aluminum silicate fiber; the lengths of each drying section furnace body, each transition section furnace body, each pyrolysis section furnace body, and each cooling section furnace body are equal.

[0080] In this embodiment, trolleys 1-6 were also adjusted. Each trolley consists of a platform, a sealing plate, a partition, wheels, and a baffle plate. The platform, which contacts the raw materials, is made of refractory brick. Below the platform is the sealing plate, made of steel plate and connected to the platform via metal anchors. The front end of the sealing plate is flush with the platform, and its length is equal to the lengths of the drying section furnace, the transition section furnace, the pyrolysis section furnace, and the cooling section furnace. The length of the sealing plate is 3-5 mm longer than the platform. A 3-5 mm thick partition plate is connected to the rear end of the sealing plate. The upper end of the partition plate is spaced far from the raw materials. The furnace tops of the feeding section furnace body, the drying section furnace body, the transition section furnace body, the pyrolysis section furnace body, and the cooling section furnace body are 1-3 mm apart. The left and right ends of the partition plate are 1-3 mm away from the left and right furnace walls of the feeding section furnace body, the drying section furnace body, the transition section furnace body, the pyrolysis section furnace body, and the cooling section furnace body. Two flow-blocking plates are also connected to the left and right sides of the lower end face of the sealing plate. The partition plate, the sealing plate, and the left and right furnace walls and the furnace top of the feeding section furnace body, the drying section furnace body, the transition section furnace body, the pyrolysis section furnace body, and the cooling section furnace body form an independent sealed space. The wheel is connected below the sealing plate.

[0081] Furthermore, the sealing plates and flow-blocking plates of the trolleys 1-6 respectively form a labyrinth seal with the sealing grooves on the inner sides of the left and right walls of each furnace body and the sealing grooves on the inner side of the lower edge of the furnace body.

[0082] In some embodiments, a method of using any multi-stage self-heating pyrolysis charcoal production apparatus is provided, comprising the following steps:

[0083] S1: Place logs or other whole or naturally shaped biomass onto each of the trolleys 1-6;

[0084] S2: Place each of the trolleys 1-6 on the track, and push the trolleys 1-6 to pass through the feeding section 1-1 and enter the drying section 1-2. The trolleys 1-6 are fully heated in the drying section 1-2 to complete the drying of the raw materials.

[0085] S3: Push each of the trolleys 1-6 through the transition section 1-3 and into the pyrolysis section 1-4. The dried raw material is fully pyrolyzed and carbonized in the pyrolysis section 1-4 to produce pyrolysis carbon.

[0086] S4: Push each of the trolleys 1-6 to send the pyrolytic carbon into the cooling section 1-5. In the cooling section, the pyrolytic carbon exchanges heat with the cold nitrogen gas sent to the inside of the cooling section through the cold nitrogen inlet 1-5-1 to achieve the cooling of the pyrolytic carbon. After the pyrolytic carbon is cooled, it is sent out of the device. The nitrogen gas after heat exchange is discharged through the hot nitrogen outlet 1-5-3.

[0087] S5: The pyrolysis gas generated from the pyrolysis of the raw material in the pyrolysis section 1-4 is sent to the pyrolysis gas burner 2 through the pyrolysis gas outlet 1-4-4 to generate high-temperature flue gas. The high-temperature flue gas is sent to the heating coil 1-4-2 through the pyrolysis flue gas inlet 1-4-1, and after exchanging heat with the raw material, it is discharged from the pyrolysis section through the pyrolysis flue gas outlet 1-4-3. It is then sent to the drying flue gas inlet 1-2-1 through the connecting flue pipe, and then enters the drying section heating coil to heat the drying section. The heated drying flue gas is discharged through the drying section flue gas outlet and sent to the SCR device 4 for purification treatment.

[0088] Example 3:

[0089] like Figure 13 and Figure 14 As shown, in order to more clearly illustrate the technical solution and advantages of the present invention, based on Embodiment 1 and Embodiment 2, a control system based on the above-mentioned self-heating pyrolysis co-generation system and multi-stage self-heating pyrolysis char production pyrolysis device with a multi-neural network optimization algorithm is provided.

[0090] Specifically, the control unit, based on data collected by sensors, centrally controls the pyrolysis reactor 1, the pyrolysis gas burner 2, the waste heat boiler 3, the SCR device 4, the economizer 5, the flue gas dust collector 6, and the desulfurization chimney integrated machine 7 through a multi-neural network collaborative control strategy. It predicts the output of charcoal, steam, and hot water through a multi-neural network calculation method involving parameter input, model building, decision-making, execution feedback, and output strategy. Based on the difference between the predicted output and quality and the target output and quality, it adjusts the parameters of each device in the pyrolysis reactor 1, the pyrolysis gas burner 2, the waste heat boiler 3, the SCR device 4, the economizer 5, the flue gas dust collector 6, and the desulfurization chimney integrated machine 7.

[0091] Furthermore, the feed section 1-1 of the pyrolysis reactor 1 is equipped with a feed rate sensor and a raw material moisture content detection device, and the signals of the feed rate sensor and the raw material moisture content detection device are electrically connected to the control unit;

[0092] Furthermore, the drying section 1-2 of the pyrolysis reactor 1 is equipped with a temperature sensor for real-time monitoring of the internal temperature of the drying section 1-2, and the temperature sensor of the drying section 1-2 is electrically connected to the control unit;

[0093] Furthermore, the pyrolysis section 1-4 of the pyrolysis reactor 1 is equipped with a temperature sensor for real-time monitoring of the internal temperature of the pyrolysis section 1-4. The temperature sensor of the pyrolysis section 1-4 is electrically connected to the control unit. The pyrolysis gas generated by the pyrolysis of the raw material in the pyrolysis section 1-4 is transported to the pyrolysis gas burner 2 for combustion through the pyrolysis gas outlet 1-4-4. The pyrolysis gas outlet 1-4-4 is equipped with a pyrolysis gas oxygen content detector for detecting the oxygen content of the pyrolysis gas.

[0094] Furthermore, the cooling section 1-5 is equipped with a temperature sensor for monitoring the internal temperature of the cooling section 1-5, and the temperature sensor of the cooling section 1-5 is electrically connected to the control unit; the cooling section 1-5 is connected to the nitrogen cooler 9 through the cold nitrogen inlet 1-5-1 and the hot nitrogen outlet 1-5-3, and the cooling section 1-5 uses cold nitrogen to cool the pyrolytic carbon produced by the pyrolysis of the pyrolysis section 1-4. After heat exchange, the cold nitrogen becomes hot nitrogen and is sent into the nitrogen cooler 9 through the hot nitrogen outlet 1-5-3;

[0095] Furthermore, after hot nitrogen enters the nitrogen cooler 9, it exchanges heat with cold water to become cold nitrogen, which is then transported back to the cooling section 1-5 through the cold nitrogen inlet 1-5-1. The cold nitrogen inlet 1-5-1 is equipped with a flow sensor for detecting the flow rate of cold nitrogen and a temperature sensor for detecting the temperature of cold nitrogen. Supplemental nitrogen is transported to the cooling section 1-5 through the supplemental nitrogen inlet 1-5-2, which is equipped with a flow sensor for detecting the flow rate of supplemental nitrogen.

[0096] Furthermore, the pyrolysis gas burner 2 is used to burn the pyrolysis gas generated by the pyrolysis of raw materials in the pyrolysis section. After the pyrolysis gas is burned, high-temperature flue gas is generated and transported in three directions. One direction is pyrolysis heating flue gas, which is sent to the pyrolysis section 1-4 to provide heat for the pyrolysis process. Another direction is drying heating flue gas, which is sent to the drying section 1-2 to provide heat for the drying process. The remaining high-temperature flue gas is sent to the waste heat boiler 3 to produce steam.

[0097] Furthermore, the drying flue gas inlet 1-2-1 is equipped with a flow sensor and a temperature sensor to detect the flow rate and temperature of the drying flue gas; the pyrolysis flue gas inlet 1-4-1 is equipped with a flow sensor and a temperature sensor to detect the flow rate and temperature of the pyrolysis flue gas.

[0098] Furthermore, such as Figures 15 to 19 As shown, the multi-neural network control strategy of the control unit includes a BP network for the drying section, a bidirectional LSTM network for the pyrolysis section, a GRU-BP hybrid network for the cooling section, a multi-task BP network for flue gas purification, and an LSTM-BP fusion network for waste heat utilization. The control logic of the control unit is to collect the parameters of the entire process flow through the input layer, process them through the multi-neural network optimization algorithm of the model layer, fuse and optimize them by the decision layer and generate execution instructions, then adjust the parameters through the execution feedback layer, and finally drive the system to complete the production of raw charcoal by the output layer, realizing closed-loop optimization control of the entire process.

[0099] Furthermore, such as Figure 15 As shown, the control objective of the drying section 1-2 is to stabilize the moisture content of the dried raw material at 10-15%. The BP network of the drying section adopts the forward propagation formula:

[0100] in, The input vector includes the feed rate, initial moisture content of the raw material, temperature of the drying heating flue gas, flow rate of the drying heating flue gas, and temperature inside the drying furnace. and These are the output vectors of hidden layer 1 and hidden layer 2. , The weights of hidden layer 1 and hidden layer 2, and The biases for hidden layer 1 and hidden layer 2; The output vector contains the moisture content of the dried raw material, the discharge temperature, and the required drying time.

[0101] The control logic of the control unit for the drying section 1-2 is as follows: First, parameters such as feed rate, initial moisture content of raw material, temperature of drying heating flue gas, flow rate of drying heating flue gas, and temperature inside the drying furnace are collected by the feed rate sensor, raw material moisture content detector, drying heating flue gas temperature sensor, drying heating flue gas flow sensor, and drying section temperature sensor, respectively, and sent to the input layer. After the parameters are initially extracted by the hidden layer 1, the hidden layer 2 performs in-depth feature mapping, and finally the predicted values ​​of moisture content, discharge temperature, and required drying time are obtained through the output layer, providing data basis for the regulation of the drying process.

[0102] Furthermore, such as Figure 16 As shown, the bidirectional LSTM network in the pyrolysis section uses the cell state update formula:

[0103] in, This is a forget gate, used to indicate the forgetting of previously recorded data. It is the Sigmoid activation function. The input vector for the pyrolysis section includes temperature, oxygen content in the pyrolysis gas, flow rate of the pyrolysis heating flue gas, and temperature data of the pyrolysis heating flue gas over a 20-minute period. For the The weight matrix, Let be the hidden state vector of the previous time step in the pyrolysis section. for Weight, For the bias term of the forget gate; For input gate, For the The input weight matrix, for Weight, This is the bias term for the input gate; For candidate state vectors, For Tanh activation function, For the The weight matrix, for Weight, The bias term for the candidate state; Let be the cell state vector. The data from the previous time step is filtered using element-wise multiplication; It is an output gate, that is, it controls the output of the cell state to... proportion, For the The weight matrix, for Weight, This is the bias term for the output gate; The hidden state vector is the output of the prediction results of the input vector for the temperature change, oxygen content of pyrolysis gas and composition of pyrolysis gas in the next 10 minutes.

[0104] The control unit's control logic for the pyrolysis sections 1-4 first collects parameters such as temperature, oxygen content, flow rate, and temperature of the pyrolysis section over 20 minutes using a pyrolysis section temperature sensor, a pyrolysis gas oxygen content detector, a pyrolysis heating flue gas temperature sensor, and a pyrolysis heating flue gas flow sensor, respectively, and sends them to the input layer. Secondly, it reads data "from front to back" to record data changes and "from back to front" to predict expected data changes. By merging, filtering, and processing the data, it extracts the patterns of these parameter changes, organizes the patterns, and outputs the bidirectional LSTM network prediction results to guide the control system.

[0105] Furthermore, such as Figure 17 As shown, the control target for cooling sections 1-5 is that the temperature of the pyrolytic carbon after cooling is ≤50ºC. The cooling section adopts the GRU-BP update formula:

[0106] in, To reset the gate output, The input vector for the cooling section includes the cold nitrogen flow rate, the cooling section temperature, the pyrolytic carbon mass, and the oxygen content of the cooling section. For the reset door The input weight matrix, The weight matrix for the reset door's hidden state. Let be the hidden state vector of the cooling section at the previous moment. To reset the door's bias; To update the gate output, For the update gate The input weight matrix, The updated gate hidden state weight matrix, To update the gate's bias term, For candidate state vectors, For the input weight matrix, Here is the hidden state weight matrix. To adjust the tendency of candidate states; This is the final hidden state;

[0107] The control logic of the control unit for the cooling sections 1-5 is as follows: dynamic and safety parameters such as cold nitrogen flow rate, cooling section temperature, and cooling section oxygen content are collected by the cold nitrogen flow sensor, cooling section temperature sensor, and cold nitrogen oxygen content detector and sent to the input layer. The weight of pyrolyzed char from the output layer of the pyrolysis section is extracted and sent to the input layer of the cooling section. The GRU layer captures the timing patterns such as "flow rate change-temperature fluctuation", "nitrogen replenishment flow rate-oxygen content delay change", and "oxygen content abnormality-temperature abnormality". The BP hidden layer optimizes the control strategy of "flow rate adjustment-char outlet temperature". Then, the output layer generates control commands for the heat exchange cold water flow rate and hot nitrogen flow rate to adjust the cooling effect and generates control commands for replenishing nitrogen flow rate to maintain the nitrogen balance of the cooling section and compensate for nitrogen leakage. Finally, the actuator is driven to adjust the corresponding parameters.

[0108] Furthermore, such as Figure 18 As shown, the multi-task BP network for flue gas purification is used to control the SCR device 4, the flue gas dust collector 6, and the integrated desulfurization chimney machine 7, and adopts a multi-task loss function:

[0109] in , as well as The losses are respectively for the sub-tasks of denitrification, desulfurization, dust removal, and energy consumption. , , as well as These are the weights of the four tasks;

[0110] The control logic of the control unit for the SCR device 4, the flue gas dust collector 6, and the integrated desulfurization chimney 7 is as follows: First, real-time parameters of SCR inlet temperature, NH3 flow rate, filtration velocity, and alkali flow rate are collected from the waste heat boiler tail flue gas temperature sensor, NH3 flow meter, dust collector anemometer, and alkali flow sensor, respectively, and sent to the input layer. After being input into the neural network, the general feature of "flue gas characteristics-reaction efficiency" is extracted through the shared hidden layer. Then, this feature is split into four BP branches: denitrification, dust removal, desulfurization, and energy consumption. Each branch learns the nonlinear law of the corresponding target, and finally outputs NO. x Emissions, outlet dust concentration, SO x The emission and system energy consumption prediction results are input into a multi-task loss function. The weighted calculation of the difference between each parameter and the emission standard and the optimal energy consumption forms a comprehensive loss value. The control system aims to minimize the comprehensive loss value and adjusts the weight parameters of the shared layer and each BP branch in reverse to reduce energy consumption while ensuring compliance with emission standards.

[0111] Furthermore, such as Figure 19As shown, the waste heat boiler 3 uses an LSTM+BP fusion network function:

[0112] in, The output feature vector of the LSTM layer. To input dynamic timing parameters, The output feature vector of the fusion layer. This is a vector concatenation function. To input static timing parameters, This is the output vector of the fusion layer's feature vector in the BP hidden layer. For the bias term of the BP hidden layer, For the final control output, This is the output layer weight matrix. For the bias term of the final output layer;

[0113] The control unit's control logic for the waste heat boiler 3 collects dynamic time-series parameters of flue gas temperature and flow rate, as well as static slow-varying parameters of economizer inlet cold water temperature and feedwater flow rate, from the pyrolysis gas burner tail temperature sensor, flow sensor, economizer inlet cold water temperature sensor, and cold water flow meter. These parameters are then fed to the input layer, along with the required steam pressure setpoint. The LSTM layer learns the time-series pattern of "flue gas fluctuation - heat change," and the fusion layer then splices the dynamic features and static parameters output by the LSTM to form a complete input. Subsequently, the BP hidden layer learns the nonlinear relationship between heat change and steam output, economizer outlet temperature, and energy consumption. The output layer then obtains the predicted results for steam output, economizer outlet temperature, and energy consumption.

[0114] In the description of this invention, "a number" refers to a quantity greater than or equal to 2, that is, a quantity of at least 2. The terms "upper," "lower," "left," "right," "inner," "outer," "front," and "rear," etc., indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings, and are only for the convenience of describing the invention and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation, and should not be construed as a limitation of the invention; unless otherwise expressly specified and limited, the term "connection" should be interpreted broadly, for example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a direct connection or an indirect connection through an intermediate medium. Those skilled in the art can understand the specific meaning of the above terms in this invention according to the specific circumstances.

[0115] The above are merely preferred embodiments of the present invention. It should be noted that those skilled in the art can make various modifications and improvements without departing from the inventive concept of the present invention, and these all fall within the protection scope of the present invention. Commonly known structures and characteristics in the above embodiments of the present invention have not been described in detail.

Claims

1. A self-heating pyrolysis cogeneration system, characterized in that, The system includes: a pyrolysis reactor (1), a pyrolysis gas burner (2), a waste heat boiler (3), an SCR device (4), an economizer (5), a flue gas dust collector (6), a desulfurization chimney integrated machine (7), a drying gas cooler (8), a nitrogen cooler (9), and a drying gas dust collector (10). The pyrolysis reactor (1) is used for drying raw materials, pyrolysis treatment and cooling of pyrolysis char; The pyrolysis gas burner (2) is connected to the pyrolysis reactor (1) and is used to receive the pyrolysis gas generated by the pyrolysis reactor (1), and send part of the flue gas generated by the combustion of the pyrolysis gas into the pyrolysis reactor (1) to provide heat for the drying and pyrolysis process in the pyrolysis reactor (1), and send the remaining part of the flue gas to the waste heat boiler (3) for steam production. The waste heat boiler (3) is connected to the pyrolysis reactor (1) and the pyrolysis gas burner (2) to receive flue gas and use the heat of the flue gas to produce steam. The SCR device (4) is connected to the waste heat boiler (3) and is used for the denitrification treatment of flue gas after waste heat utilization; The economizer (5) is connected to the SCR device (4) and is used to heat the demineralized water by using the waste heat of the flue gas at the outlet of the SCR device (4) to supply water to the waste heat boiler (3) and at the same time reduce the exhaust temperature. The flue gas dust collector (6) is connected to the economizer (5) and is used for flue gas dust removal; The desulfurization chimney integrated machine (7) is connected to the flue gas dust collector (6) and is used for flue gas desulfurization and flue gas emission.

2. The self-heating pyrolysis cogeneration system according to claim 1, characterized in that, The pyrolysis reactor (1) is a multi-stage self-heating pyrolysis charcoal production device. The main body is a furnace body, which is divided into 5 sections, including a feeding section (1-1), a drying section (1-2), a transition section (1-3), a pyrolysis section (1-4), and a cooling section (1-5) arranged in sequence and connected to each other. A movable trolley (1-6) for carrying raw materials is installed inside the lower part of the furnace body of the pyrolysis reactor (1).

3. The self-heating pyrolysis cogeneration system according to claim 2, characterized in that, The pyrolysis reactor (1) is provided with liftable furnace doors between the feed section (1-1) and the drying section (1-2), between the drying section (1-2) and the transition section (1-3), between the transition section (1-3) and the pyrolysis section (1-4), and between the pyrolysis section (1-4) and the cooling section (1-5). The left end of the feed section (1-1) and the right end of the cooling section (1-5) are provided with liftable furnace doors for the overall sealing of the pyrolysis reactor (1).

4. The self-heating pyrolysis cogeneration system according to claim 2, characterized in that, The drying section (1-2) is provided with several parallel drying flue gas inlets (1-2-1) below it. The drying flue gas inlets (1-2-1) are connected to the pyrolysis gas burner (2). The drying flue gas inlets (1-2-1) are directly fed into the pyrolysis gas burner (2) to burn the flue gas generated by the pyrolysis gas, which provides heat for the drying process. The top of the drying section is provided with a drying gas outlet (1-2-2) to discharge the drying gas mixed with the steam generated by the drying process. The top of the drying section (1-2) is also provided with a temperature detector to detect the temperature inside the drying section (1-2). The internal temperature of the drying section (1-2) is 100-200℃.

5. The self-heating pyrolysis cogeneration system according to claim 4, characterized in that, After the drying gas is discharged from the drying gas outlet (1-2-2) of the drying section (1-2), it is sent into the drying gas cooler (8) for cooling. After cooling, the drying gas is sent into the drying gas dust collector (10) for dust removal and then discharged.

6. The self-heating pyrolysis cogeneration system according to claim 2, characterized in that, The pyrolysis section (1-4) is the site where pyrolytic carbon is produced by the pyrolysis of raw materials. Several parallel pyrolysis flue gas inlets (1-4-1) are provided on one side below the pyrolysis section (1-4). One end of each pyrolysis flue gas inlet (1-4-1) is connected to the pyrolysis gas burner (2), and the other end is connected to one end of a heating coil (1-4-2) located within the pyrolysis section (1-4). The other end of the heating coil (1-4-2) is connected to several pyrolysis flue gas inlets located on the other side below the pyrolysis section (1-4). One end of the outlet (1-4-3) is connected, and the other end of the plurality of pyrolysis flue gas outlets (1-4-3) is connected to the waste heat boiler (3). The flue gas generated by the combustion of pyrolysis gas by the pyrolysis gas burner (2) is sent into the heating coil (1-4-2) in the pyrolysis section (1-4) through the plurality of pyrolysis flue gas inlets (1-4-1), and then sent into the waste heat boiler (3) after passing through the plurality of pyrolysis flue gas outlets (1-4-3), thus completing the heating of the pyrolysis section (1-4) by the flue gas.

7. The self-heating pyrolysis cogeneration system according to claim 6, characterized in that, The other end of the pyrolysis flue gas inlet (1-4-1) is connected to the pyrolysis gas burner (2), through which flue gas generated by the combustion of pyrolysis gas by the pyrolysis gas burner (2) is introduced. The introduced flue gas enters the heating coil (1-4-2), and the heating coil (1-4-2) heats the raw material dried in the pyrolysis section (1-4) through the drying section (1-2) by radiative heat transfer. Several pyrolysis gas outlets (1-4-4) are provided above the pyrolysis section (1-4), and the pyrolysis gas generated by the pyrolysis of the raw material is sent into the pyrolysis gas burner (2) through the pyrolysis gas outlets (1-4-4). A temperature detector is also provided at the top of the pyrolysis section (1-4) to detect the temperature inside the pyrolysis section (1-4), and the temperature of the pyrolysis section (1-4) is 500-600℃.

8. The self-heating pyrolysis cogeneration system according to claim 2, characterized in that, The cooling section (1-5) is the place where the pyrolytic carbon produced by the pyrolysis of the raw materials in the pyrolysis section (1-4) is cooled by nitrogen gas. The cooling section (1-5) has several parallel cold nitrogen inlets (1-5-1) on one side below it, and several parallel supplementary nitrogen inlets (1-5-2) on the other side below it. The cooling section (1-5) has several parallel hot nitrogen outlets (1-5-3) on the top. The cold nitrogen inlets (1-5-1) are connected to the top of the nitrogen cooler (9), the supplementary nitrogen inlets (1-5-2) are connected to an external nitrogen source, and the hot nitrogen outlets (1-5-3) are connected to the bottom of the nitrogen cooler (9). When the pyrolysis reactor (1) is started, nitrogen gas is introduced into the cooling section (1-5) through the supplementary nitrogen inlet (1-5-2); after the pyrolysis carbon is sent out from the pyrolysis section (1-4), it enters the cooling section (1-5) and exchanges heat with the nitrogen gas sent back from the cold nitrogen inlet (1-5-1) to cool down, and then it is sent out from the cooling section (1-5) to complete the cooling of the pyrolysis carbon; The nitrogen gas supplied through the supplementary nitrogen inlet (1-5-2) is heated by exchanging heat with the pyrolytic carbon and becomes hot nitrogen gas, which is discharged from the cooling section (1-5) through the hot nitrogen outlet (1-5-3) and sent to the nitrogen cooler (9) for cooling treatment.

9. The self-heating pyrolysis cogeneration system according to claim 8, characterized in that, The nitrogen cooler (9) is a spray tower structure. It cools the hot nitrogen by spraying cold water. The hot nitrogen exchanges heat with the sprayed cold water and is cooled into cold nitrogen. After being sent into the cooling section (1-5) through the cold nitrogen inlet (1-5-1), the nitrogen circulation is completed. The nitrogen cooler (9) sprays cold water and exchanges heat with the hot nitrogen generated in the cooling section (1-5) to become hot water.

10. The self-heating pyrolysis cogeneration system according to claim 8, characterized in that, The nitrogen circulation occurring within the cooling section (1-5) includes the following steps: S1: When the pyrolysis reactor (1) is started, only the supplementary nitrogen inlet (1-5-2) is opened, and the external nitrogen source is introduced into the cooling section (1-5) through the supplementary nitrogen inlet (1-5-2) to establish an inert atmosphere; S2: After the start-up stage is completed, the supplementary nitrogen inlet (1-5-2) is closed and the cold nitrogen inlet (1-5-1) is opened to enter the normal operation stage. After the pyrolysis carbon is sent out from the pyrolysis section (1-4), it enters the cooling section (1-5) and exchanges heat with the nitrogen gas sent back from the cold nitrogen inlet (1-5-1) to cool down. Then it is sent out from the cooling section (1-5) to complete the cooling of the pyrolysis carbon. S3: When the furnace is started, the nitrogen gas supplied by the supplementary nitrogen inlet (1-5-2) exchanges heat with the pyrolytic carbon and becomes hot nitrogen gas, which is discharged from the cooling section (1-5) through the hot nitrogen outlet (1-5-3) and sent into the nitrogen cooler (9) from the bottom. The hot nitrogen gas flows from the bottom of the nitrogen cooler (9) to the top of the nitrogen cooler (9), and exchanges heat with the sprayed cold water during the process to perform cooling treatment. The cooled nitrogen gas is sent back to the cooling section (1-5) through the cold nitrogen inlet (1-5-1).

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