A pyrolysis recovery system and method for chopped glass fibers from wind turbine blades

Abstract

This invention discloses a pyrolysis recovery system and method for chopped glass fibers in wind turbine blades. A dual-chamber pyrolysis reactor is formed by stacking a pyrolysis chamber and an oxidation reaction chamber. After the wind turbine blade enters the reactor, it undergoes pyrolysis at high temperatures. The resulting gaseous components are condensed and separated by a pyrolysis oil recovery system to obtain pyrolysis gas and pyrolysis oil. The completely pyrolyzed material falls into the oxidation reactor under the rotation of a sealed feeding device. The rising hot air in the oxidation reaction chamber heats the pyrolysis chamber, while the high-temperature flue gas generated after the combustion of the pyrolysis gas heats the oxidation reaction chamber through a second heat exchanger, thus completing the pyrolysis process. All flue gas is treated by dust removal and purification devices before being discharged, achieving the harmless treatment of retired wind turbine blades.

Description

Technical Field

[0001] This invention relates to the field of resource recycling technology, and in particular to a pyrolysis recycling system and method for chopped glass fibers from wind turbine blades. Background Technology

[0002] Wind turbine blades are a crucial component of wind turbine units. The design life of wind turbine units is typically 20-25 years, and the ever-increasing installed capacity of wind power will inevitably lead to the replacement of a large number of decommissioned wind turbine blades. Therefore, the disposal, treatment, and recycling of decommissioned wind turbine blades are urgently needed.

[0003] Currently, the disposal and recycling of thermosetting composite materials such as wind turbine blades mainly rely on traditional methods such as landfill and incineration, which result in significant secondary pollution and resource waste. Pyrolysis, on the other hand, involves heating the raw materials to medium-high temperatures under anaerobic or oxygen-deficient conditions, causing the matrix material to decompose into small molecules such as alkanes and olefins, thus achieving in-situ dissociation of the reinforcing material from the matrix material. Compared with other methods, pyrolysis has advantages such as large processing capacity, good fiber recovery performance, significant volume reduction, thorough harmlessness, and high resource recovery rate, making it a technology with great application and promotion potential in the current resource-based disposal technology for wind turbine blades.

[0004] However, since wind turbine blades are composed of glass fibers and thermosetting resins, with the thermosetting resins having a complex three-dimensional network structure and strong chemical bonds between molecules, it is difficult to achieve efficient separation of resin and fiber during recycling. Therefore, the pyrolysis device needs to have high heat transfer performance and heat exchange efficiency. In addition, the coke produced after pyrolysis will accumulate on the surface of the glass fibers, reducing the mechanical properties of the recycled glass fibers and becoming a major obstacle to the recycling process. Therefore, the pyrolysis device needs to be able to remove carbon deposits on the fiber surface as much as possible during the reaction to avoid degradation of the mechanical properties of the recycled fibers.

[0005] Patent CN 113046107A effectively pyrolyzes composite materials in decommissioned wind turbine blades using a circulating fluidized bed and recovers the pyrolysis oil generated during the pyrolysis process. However, due to the intense collision between the crushed waste wind turbine blades and the bed material during the reaction in the circulating fluidized bed, the mechanical properties of the glass fiber significantly decrease, severely affecting the mechanical properties of the regenerated fiber and greatly reducing its reuse value. Patent CN 113217936A uses a rotary kiln pyrolysis reactor to simultaneously pyrolyze and oxidize decommissioned wind turbine blades. Although this reduces the process flow to some extent, the direct oxidation results in the direct oxidation of the pyrolysis gas and oil phase products. On the one hand, this increases the local heating temperature of the regenerated fiber, exacerbating the thermal effect on the mechanical properties of the glass fiber. On the other hand, the complete oxidation of the pyrolysis gas and oil phase products fails to meet the requirements for multi-component resource utilization of decommissioned wind turbine blades.

[0006] Therefore, there is a need to provide a novel pyrolysis recovery system and method for chopped glass fibers from wind turbine blades to solve the above problems. Summary of the Invention

[0007] The main objective of this invention is to provide a novel pyrolysis recycling system and method for chopped glass fibers in wind turbine blades. This invention aims to address the shortcomings of existing pyrolysis reactors in processing decommissioned wind turbine blades, such as low system efficiency, uneven heat transfer, and poor raw material adaptability. In particular, it addresses the difficulty in overcoming carbon buildup and mechanical property degradation during fiber recycling, thus hindering the efficient disposal of decommissioned wind turbine blades. Ultimately, this invention achieves efficient and clean pyrolysis treatment of decommissioned wind turbine blades and efficient recycling of regenerated fibers.

[0008] To achieve the above objectives, the present invention provides a pyrolysis recovery system for chopped glass fibers in wind turbine blades, comprising a pyrolysis reactor, an oxidation reactor, a flue gas purification system, a first heat exchanger, a second heat exchanger, a pyrolysis oil recovery system, and a burner; the pyrolysis reactor is stacked above the oxidation reactor, wherein:

[0009] The pyrolysis reactor includes a first shell and an upper conveyor chain plate disposed on the bottom surface inside the first shell. The inner cavity of the first shell forms a pyrolysis chamber. A pyrolysis gas outlet is provided above the first shell. The pyrolysis oil recovery system is connected to the pyrolysis chamber through the pyrolysis gas outlet. A discharge port is provided at the material drop end of the first shell near the upper conveyor chain plate, and a feeding port is provided at the material inlet end of the first shell corresponding to the upper conveyor chain plate.

[0010] The first heat exchange device is disposed in the pyrolysis chamber. The first heat exchange device includes multiple first heat exchange tubes arranged around the upper conveyor chain plate. The upper end of the first heat exchange tube is connected to the flue gas purification system, and the lower end of the first heat exchange tube is connected to the oxidation reactor. The first heat exchange tube is not connected to the gas in the pyrolysis chamber.

[0011] The oxidation reactor includes a second shell and a lower conveyor chain plate mounted inside the second shell. The inner cavity of the second shell forms an oxidation reaction chamber. An inlet is provided on the second shell near the discharge port. The loading end of the lower conveyor chain plate is located below the inlet. An outlet is provided on the second shell near the discharge end of the lower conveyor chain plate. An oxidation gas outlet is provided on the top of the second shell. The oxidation gas outlet is connected to the lower opening of the first heat exchange tube. The lower part of the oxidation reaction chamber is connected to an air supply system, which provides upward airflow to the oxidation reaction chamber.

[0012] The second heat exchange device is disposed above the lower conveyor chain plate. The second heat exchange device includes multiple second heat exchange tubes arranged along the conveying direction of the lower conveyor chain plate. The second heat exchange tube includes an air inlet and an air outlet. The air inlet is connected to the burner, and the air outlet is directly or indirectly connected to the lower opening of the first heat exchange tube.

[0013] The pyrolysis oil recovery system includes a condenser and a pyrolysis oil collection tank connected to the condensate outlet of the condenser. The air inlet of the condenser is connected to the pyrolysis gas outlet, and the air outlet of the condenser is connected to the burner.

[0014] The burner is used to burn the passing gas and deliver it to the air inlet;

[0015] A sealed material discharge device is provided between the discharge port and the inlet, and between the outlet and the outside.

[0016] Optionally, it also includes a pulverizer located next to the air compressor. The pulverizer includes a third housing and pulverizing rollers located inside the third housing. An inlet is provided above the third housing, and a conveyor belt is provided below the third housing and connected to the feeding port.

[0017] Optionally, the upper conveyor chain plate and the lower conveyor chain plate are arranged to overlap in the vertical direction and have opposite conveying directions.

[0018] Optionally, the discharge port and the inlet are connected to form a first discharge channel, and a second discharge channel is formed between the discharge port and the outside. Both the first and second discharge channels include cylindrical channels that are open at the top and bottom and extend laterally along their axes. The sealed discharge device includes two circular end plates arranged opposite each other and cross-shaped blades connected between the two end plates. The end plates are all vertically arranged and can be inserted into the ends of the cylindrical channels one by one. The cross-shaped blades include four blades arranged in a cross shape along the axial direction of the sealed discharge device. The radial diameter of the cross-shaped blades is adapted to the inner diameter of the corresponding cylindrical channel. The axial length of the sealed discharge device is greater than or equal to the length of the corresponding cylindrical channel. The sealed discharge device is rotatably disposed in the corresponding cylindrical channel along its central axis.

[0019] Preferably, the width of the pyrolysis chamber is 1000mm-4000mm, the width-to-length ratio is 1 / 4 to 1 / 8, and the width-to-height ratio is 1 / 1 to 2 / 1; the width of the oxidation reaction chamber is 1000mm-4000mm, the width-to-length ratio is 1 / 5 to 1 / 9, and the width-to-height ratio is 1 / 1 to 2 / 1.

[0020] Optionally, the lower part of the oxidation reaction chamber is connected to an air supply system, which provides upward airflow to the oxidation reaction chamber.

[0021] Optionally, an air distribution device is provided below the lower conveyor chain plate, and an air chamber is formed between the air distribution device and the bottom surface of the second housing. The air supply system is connected to the air chamber, and the air supply system includes an air compressor. The air distribution device is a guide plate with uniform holes or multiple upward air-supplying guide wheels.

[0022] Optionally, the first heat exchange device further includes an upper gas collecting cover and a lower gas collecting cover arranged opposite to each other. Both the upper and lower gas collecting covers are hollow plates. The bottom surface of the upper gas collecting cover has multiple upper openings corresponding to the first heat exchange tubes, and the upper opening of the first heat exchange tubes is connected to the upper openings. The top surface of the lower gas collecting cover has multiple lower openings corresponding to the first heat exchange tubes, and the lower opening of the first heat exchange tubes is connected to the lower openings. The upper gas collecting cover is located above the upper conveyor chain plate, and the lower gas collecting cover is located below the upper conveyor chain plate. The bottom surface of the lower gas collecting cover has a first gas port communicating with the oxidation gas outlet. The lower gas collecting cover also has a second gas port communicating with the gas outlet of the second heat exchange tube.

[0023] Optionally, both the upper conveyor chain and the lower conveyor chain are chain-type conveyor devices, and the conveyor chain of the chain-type conveyor device is provided with ventilation holes.

[0024] Optionally, the second heat exchange device includes multiple heat exchange sub-tube assemblies. Each heat exchange sub-tube assembly includes an inlet main pipe, multiple second heat exchange tubes arranged on a plane along the conveying direction of the lower conveyor chain plate, and an outlet main pipe. One end of the inlet main pipe is connected to the inlet port, and the other end is connected to the inlet end of each second heat exchange tube. One end of the outlet main pipe is connected to the outlet port, and the other end is connected to the outlet end of each second heat exchange tube.

[0025] The present invention also provides a method for pyrolysis recovery of chopped glass fibers from wind turbine blades based on the pyrolysis recovery system described in any of the preceding claims, comprising the steps of:

[0026] S1, during initial startup, delivers combustible gas to the burner and, after combustion, transfers it to the second heat exchange device so that the temperature of the oxidation reaction chamber reaches 500℃-700℃ and the reaction temperature of the pyrolysis chamber reaches 400℃-500℃.

[0027] S2, the crushed wind turbine blades are fed through the feeding port at a feeding rate of 0t / h-2t / h, and the transmission rate of the upper conveyor chain is controlled to make the pyrolysis time of the wind turbine blades in the pyrolysis chamber 0.5-2h, and the transmission rate of the lower conveyor chain is controlled to make the oxidation time of the wind turbine blades in the oxidation reaction chamber 0.5-2h. After the temperature of the pyrolysis chamber and the oxidation reaction chamber stabilizes, the supply of combustible gas to the burner is stopped.

[0028] S3, start the flue gas purification system and pyrolysis oil recovery system;

[0029] S4, start the sealed feeding device so that the wind turbine blades that have completed pyrolysis in the pyrolysis chamber continuously fall into the oxidation reaction chamber, and the glass fibers that have completed oxidation and decarbonization are discharged through the discharge port.

[0030] The pyrolysis recovery system and method for chopped glass fibers in wind turbine blades, as described in this invention, are based on a dual-chamber pyrolysis reactor formed by stacking a pyrolysis chamber and an oxidation reaction chamber. After the wind turbine blades pass through a pulverizer and enter the pyrolysis reactor, they undergo pyrolysis at high temperatures. The gaseous components of the pyrolysis are condensed by a pyrolysis oil recovery system. The completely pyrolyzed material at the rear of the upper conveyor chain falls into the oxidation reactor under the rotation of a sealed feeding device, thereby promoting the effective separation of organic and inorganic components from the wind turbine blades. The beneficial effects of this invention include at least the following:

[0031] (1) Compact structure: The arrangement of two conveyor belts connected vertically (and in opposite directions) effectively improves space utilization efficiency;

[0032] (2) High-efficiency heat transfer: The high-temperature pyrolysis gas generated by the pyrolysis reaction in the pyrolysis chamber is condensed and separated into pyrolysis oil. The remaining non-condensable gas is fully combusted by the burner and then introduced into the second heat exchange device in the oxidation reaction chamber to provide heat for the oxidation reaction in the oxidation reaction chamber. The heat and flue gas generated by the oxidation reaction in the oxidation reaction chamber are introduced into the first heat exchange device in the pyrolysis chamber together with the gas of the second heat exchange device to provide heat for the pyrolysis reaction. They are isolated from each other and can also be used for heat recycling, which further improves the thermal efficiency of the system.

[0033] (3) Wide range of raw materials applicable and flexible and adjustable reaction process: By adjusting the transmission speed of the upper and lower conveyor chain plates, the temperature of the flue gas generated by the burner, and the position and angle of the air distribution device and fan outside each stage of the flue, the working state of the reaction chamber can be flexibly changed to adapt to the efficient pyrolysis of retired wind turbine blades of different parts and different components.

[0034] (4) High quality of regenerated fiber: The pyrolysis and oxidation processes are combined in stages to achieve in-situ decarbonization of regenerated fiber, which effectively inhibits the degradation of fiber strength and mechanical properties.

[0035] (5) High degree of product resource utilization: In addition to recycling glass fiber, the pyrolysis gas generated by the pyrolysis of retired wind turbine blades can be used for combustion to provide heat for reactor pyrolysis and realize the self-heating pyrolysis process; after condensation, liquid products are obtained, which can be used as liquid fuel or further purified to synthesize high-value chemicals.

[0036] (6) Clean emissions: All flue gas generated is treated by dust removal and purification devices before being discharged, achieving the harmless treatment of retired wind turbine blades. Attached Figure Description

[0037] To more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on the structures shown in these drawings without creative effort.

[0038] Figure 1 This is a cross-sectional structural schematic diagram of a pyrolysis and recycling system for chopped glass fibers in wind turbine blades according to an embodiment of the present invention;

[0039] Figure 2 for Figure 1 Left view of the pyrolysis recovery system in the image;

[0040] Figure 3 for Figure 1 Top view of the pyrolysis recovery system in the middle;

[0041] Figure 4 This is a schematic diagram of the structure of the heat exchange tube assembly of the second heat exchange device provided in an embodiment of the present invention;

[0042] Figure 5 This is a schematic diagram of the structure of a sealed material feeding device according to an embodiment of the present invention;

[0043] Figure 6 This is a schematic diagram of the structure of a first heat exchange device provided in an embodiment of the present invention;

[0044] Figure 7 for Figure 6 A schematic diagram of the internal structure of the first heat exchanger in the diagram;

[0045] Figure 8 This is a partial structural schematic diagram of an oxidation reactor provided in an embodiment of the present invention.

[0046] Label Explanation:

[0047] Feed port 1;

[0048] Dust collector 2;

[0049] Flue gas purification system 3, flue gas purifier 31;

[0050] Oxidation reactor 4, oxidation reaction chamber 400, sealed material feeding device 401, lower conveyor chain plate 402, ventilation hole 4021, air distribution device 403, hole 4031, gas chamber 404, second shell 405, feed inlet 41, discharge outlet 42, oxidation gas outlet 43;

[0051] Second heat exchange device 5, second heat exchange tube 51, air inlet 511, air outlet 512, heat exchange sub-tube assembly 50, air inlet main pipe 501, air outlet main pipe 502;

[0052] Crusher 6, third housing 61, crushing rollers 62, lifting conveyor belt 63;

[0053] The pyrolysis reactor 7, pyrolysis chamber 700, sealed material feeding device 701, first heat exchange tube 702, upper conveyor chain plate 703, first shell 704, material discharge port 705, first heat exchange device 71, upper gas collecting cover 721, lower gas collecting cover 722, first gas port 723, second gas port 724, and third gas port 725 are included.

[0054] End plate 761, cross shaft blade 762;

[0055] Pyrolysis gas outlet 81, pyrolysis gas channel 8;

[0056] Burner 9;

[0057] Pyrolysis oil recovery system 100, condenser 10, pyrolysis oil collection box 11;

[0058] Air compressor 12.

[0059] The objectives, features, and advantages of this invention will be further explained in conjunction with the embodiments and with reference to the accompanying drawings. Detailed Implementation

[0060] The technical solutions in this embodiment will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention.

[0061] It should be noted that all directional indicators (such as up, down, left, right, front, back, etc.) in this embodiment are only used to explain the relative positional relationship and movement of each component in a specific posture (as shown in the attached figure). If the specific posture changes, the directional indicator will also change accordingly.

[0062] Furthermore, in this invention, descriptions involving "first," "second," etc., are for descriptive purposes only and should not be construed as indicating or implying their relative importance or implicitly specifying the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one of that feature. In the description of this invention, "a plurality of" means at least two, such as two, three, etc., unless otherwise explicitly specified.

[0063] In this invention, unless otherwise explicitly specified and limited, the terms "connection," "fixed," etc., should be interpreted broadly. For example, "fixed" can mean a fixed connection, a detachable connection, or an integral part; it can mean a mechanical connection or an electrical connection; it can mean a direct connection or an indirect connection through an intermediate medium; it can mean the internal communication of two components or the interaction between two components, unless otherwise explicitly limited. Those skilled in the art can understand the specific meaning of the above terms in this invention according to the specific circumstances.

[0064] Furthermore, the technical solutions of the various embodiments of the present invention can be combined with each other, but only if they are feasible for those skilled in the art. If the combination of technical solutions is contradictory or cannot be implemented, it should be considered that such combination of technical solutions does not exist and is not within the scope of protection claimed by the present invention.

[0065] It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.

[0066] Please combine Figure 1-8 As shown, the pyrolysis recovery system provided by the present invention includes a pyrolysis reactor 7, an oxidation reactor 4, a flue gas purification system 3, a first heat exchange device 71, a second heat exchange device 5, a pyrolysis oil recovery system 100, and a burner 9.

[0067] The pyrolysis reactor 7 is stacked on top of the oxidation reactor 4.

[0068] The pyrolysis reactor 7 includes a first shell 704 and an upper conveyor chain plate 703 disposed on the bottom surface inside the first shell. The inner cavity of the first shell forms a pyrolysis chamber 700. A pyrolysis gas outlet 81 is provided above the first shell. The pyrolysis oil recovery system 100 is connected to the pyrolysis chamber 700 through the pyrolysis gas outlet 81. A discharge port 705 is provided at the discharge end of the first shell near the upper conveyor chain plate 703, and a feeding port 1 is provided at the feed end of the first shell corresponding to the upper conveyor chain plate 703. The conveyor chain plate can be a chain conveyor belt.

[0069] Furthermore, in a preferred embodiment, the pyrolysis oil recovery system 100 is disposed on one side of the pyrolysis reactor 4, and the pyrolysis gas outlet 81 is connected to the pyrolysis oil recovery system 100 via a pyrolysis gas pipeline 8. There can be multiple pyrolysis gas outlets 81.

[0070] Those skilled in the art can also, as needed, appropriately install an exhaust fan on the pyrolysis gas pipeline 8 to provide suction pressure for the pyrolysis gas to flow from the pyrolysis chamber 700 to the pyrolysis oil recovery system 100, which will not be elaborated here. Furthermore, in other parts of this embodiment, blower and exhaust devices can be installed as needed to provide the necessary pneumatic power for the gas circulation of the entire pyrolysis recovery system. The specific embodiments mainly describe the technical features that address the actual technical problem to be solved by this invention. Contents related to the pyrolysis recovery system that overlap with existing technologies and can be selected by those skilled in the art as needed are not described in detail; however, this does not mean that the technical solution of the pyrolysis recovery system in this invention is incomplete.

[0071] The first heat exchange device 71 is disposed in the pyrolysis chamber 700. The first heat exchange device 71 includes a plurality of first heat exchange tubes 702 arranged around the upper conveyor chain plate 703. One end of the first heat exchange tube 702 (e.g., the upper opening of the first heat exchange tube 702) is connected to the flue gas purification system 3, and the other end of the first heat exchange tube 702 (e.g., the lower opening of the first heat exchange tube 702) is connected to the oxidation reactor 4. The first heat exchange tube 702 is not in communication with the gas in the pyrolysis chamber 700.

[0072] Furthermore, in a specific example, the upper end of the first heat exchange tube 702 can be connected to the flue gas purification system 3 set outside the pyrolysis reactor 4 through a pipe, as long as the overall airtightness of the pyrolysis chamber 700 is ensured.

[0073] Please combine them together Figure 8 The oxidation reactor 4 includes a second shell 405 and a lower conveyor chain plate 402 disposed within the second shell. The inner cavity of the second shell forms an oxidation reaction chamber 400. An inlet 41 is provided on the second shell near the discharge port 705. The feeding end of the lower conveyor chain plate 402 is located below the inlet 41. An outlet 42 is provided on the second shell near the discharge end of the lower conveyor chain plate 402. An oxidation gas outlet 43 is provided on the upper part of the second shell. The oxidation gas outlet 43 is connected to the lower opening of the first heat exchange tube 702. The lower part of the oxidation reaction chamber 400 is connected to an air supply system, which provides upward airflow to the oxidation reaction chamber 400.

[0074] Please combine them together Figure 4The second heat exchange device 5 is disposed above the lower conveyor chain plate 402. The second heat exchange device 5 includes multiple second heat exchange tubes 51 arranged along the conveying direction of the lower conveyor chain plate 402. The second heat exchange tube 51 includes an air inlet 511 and an air outlet 512. The air inlet 511 is connected to the burner 9, and the air outlet 512 is directly or indirectly connected to the lower opening of the first heat exchange tube 702.

[0075] The gas discharged from the second heat exchange tube 51 through the outlet 512 can be connected to the first heat exchange tube 702 through a separate pipe, or it can be directly discharged into the oxidation reaction chamber 400 and flow together with the flue gas after oxidation reaction through the oxidation gas outlet 43 to the first heat exchange tube 702.

[0076] The pyrolysis oil recovery system 100 includes a condenser 10 and a pyrolysis oil collection tank 11 connected to the condensate outlet of the condenser 10. The air inlet of the condenser 10 is connected to the pyrolysis gas outlet 81, and the air outlet of the condenser 10 is connected to the burner 9.

[0077] The burner 9 is used to burn the passing gas and deliver it to the inlet 511 of the second heat exchange tube 51.

[0078] A closable, sealed material discharge device is provided between the discharge port 705 and the inlet port 41, and between the outlet port 42 and the outside. Among these, in... Figure 1 In the middle, the sealing discharge device 701 is located between the discharge port 705 and the feed port 41, and the sealing discharge device 401 is located between the discharge port 42 and the outside.

[0079] During initial startup, combustible gas is supplied to the burner 9 to provide initial heat to the overall pyrolysis recovery system. After the pyrolysis reaction begins, the pyrolysis gas enters the condenser 10 (which can be a shell-and-tube heat exchanger) through the pyrolysis gas channel 8 for condensation, thereby separating into pyrolysis oil and non-condensable gas. The non-condensable gas typically includes combustible gases such as hydrogen and methane. No additional fuel supply is required afterward, and the pyrolysis reaction can continuously maintain the pyrolysis energy and oxidation reaction energy required by the pyrolysis recovery system.

[0080] The high-temperature flue gas from burner 9 undergoes heat exchange in oxidation reaction chamber 400 via second heat exchange tube 51, raising the temperature of oxidation reaction chamber 400 to 500℃-700℃. Powered by the air supply system, the pyrolyzed wind turbine blades on the lower conveyor chain 402 come into full contact with oxygen at high temperature, reacting through oxidation and carbon removal, leaving behind glass fiber. The high-temperature reaction flue gas from oxidation reaction chamber 400 is then transported by airflow through oxidation gas outlet 43 into first heat exchange tube 702. First heat exchange tube 702 exchanges heat with pyrolysis chamber 700, maintaining the temperature of pyrolysis chamber 400 at 400℃-500℃. The wind turbine blades on upper conveyor chain 703 undergo pyrolysis, and the pyrolyzed solid material enters oxidation reaction chamber 400 through discharge port 705 and inlet 41. Pyrolysis gas is discharged to pyrolysis oil recovery system 100.

[0081] The working principle of the pyrolysis recovery system is explained below through a specific workflow.

[0082] First, during initial startup, combustible gas is supplied to the burner 9, generating high-temperature flue gas of 800℃-1000℃. This flue gas enters the second heat exchange tube 51 of the second heat exchange device 5 through the inlet 511, and then heats the oxidation reaction chamber 400 of the oxidation reactor 4 through heat exchange. By adjusting the burner 9 and the air supply system, the high-temperature reaction flue gas in the oxidation reaction chamber 400 is transported by wind through the oxidation gas outlet 43 into the first heat exchange tube 702. The first heat exchange tube 702 exchanges heat with the pyrolysis chamber 700, raising the temperature of the pyrolysis chamber 700 to 400℃-500℃. Crushed wind turbine blades are then fed through the feed inlet 1 at a feed rate of 0t / h-2t / h. The upper conveyor chain plate 703 moves at a uniform speed according to the designed speed, and the wind turbine blades are uniformly heated and decomposed in the pyrolysis chamber 700. The generated pyrolysis gas enters the condenser 10 through the pyrolysis gas outlet 81, where it is separated into pyrolysis oil and non-condensable gas. After passing through the pyrolysis reactor 7, the pyrolysis products of the decommissioned wind turbine blades fall onto the lower conveyor chain plate 402 through the opening of the sealed feeding device 701, and are oxidized and decarbonized under aerobic conditions. The high-temperature gas generated after oxidation is heat-exchanged through the first heat exchange tube 702 to help maintain the temperature of the pyrolysis chamber 700. After the decommissioned wind turbine blades are completely oxidized in the oxidation reaction chamber, the remaining recycled glass fiber is discharged to the external solid collection device through the sealed feeding device 401. In addition, the non-condensable gas obtained after pyrolysis separation is used as fuel gas and burned in the burner 9 to continuously generate high-temperature flue gas to heat the second heat exchange device 5, thereby maintaining the temperature of the pyrolysis and oxidation reactions required by the pyrolysis recovery system.

[0083] Optionally, in this embodiment, the pyrolysis recovery system further includes a crusher 6. The crusher 6 may include a third housing 61 and crushing rollers 62 disposed within the third housing. An inlet is provided at the top of the third housing, and a lifting conveyor belt 63 is provided at the bottom outlet of the third housing 61. The material discharge end of the lifting conveyor belt 63 is connected to the feeding port 1 to transport material from the bottom outlet of the third housing 61 to the feeding port 1 for feeding. By selecting appropriate crushing rollers, the size of the wind turbine blades to be pyrolyzed that ultimately enter the pyrolysis chamber 700 can be adjusted, thereby controlling the completeness of the reaction.

[0084] Optionally, in this embodiment, the upper conveyor chain 703 and the lower conveyor chain 402 are arranged to overlap vertically, and their conveying directions are opposite. This arrangement achieves a design that minimizes the footprint.

[0085] Meanwhile, the sizes of the pyrolysis reactor 7 and the oxidation reactor 4 can be set as needed. The main reference quantities for the design can be calculated based on their respective reaction temperatures and the transmission rates of the upper and lower conveyor chains. The two can be designed to be similar in size or to have different sizes.

[0086] In this embodiment, the pyrolysis chamber 700 has a width of 1000mm-4000mm, a width-to-length ratio of 1 / 4 to 1 / 8, and a width-to-height ratio of 1 / 1 to 2 / 1; the oxidation reaction chamber 400 has a width of 1000mm-4000mm, a width-to-length ratio of 1 / 5 to 1 / 9, and a width-to-height ratio of 1 / 1 to 2 / 1.

[0087] Optionally, please combine them together. Figure 5In this embodiment, the discharge port 705 and the inlet port 41 are connected to form a first discharge channel, and a second discharge channel is formed between the outlet port 42 and the outside. Both the first and second discharge channels include cylindrical channels that are open at the top and bottom and extend laterally along the axis. The sealed discharge device includes two circular end plates 761 arranged opposite each other and a cross-shaped blade 762 connected between the two end plates. The end plates are all vertically arranged and can be inserted into the ends of the cylindrical channels one by one. The cross-shaped blade 762 includes four blades arranged in a cross shape along the axial direction of the sealed discharge device. The radial diameter of the cross-shaped blade 762 is adapted to the inner diameter of the corresponding cylindrical channel. The axial length of the sealed discharge device is greater than or equal to the length of the corresponding cylindrical channel. The sealed discharge device is rotatably arranged in the corresponding cylindrical channel along the central axis. The openings at the top and bottom of the cylindrical channel are slightly larger than the openings formed between adjacent blades. In use, the material first falls between any pair of adjacent blades. At this time, the free ends of at least one pair of blades will abut against the inner circumference of the cylindrical channel to form a sealing effect. Then, the sealed material feeding device rotates along its own axis, allowing the material to fall downwards under the action of gravity.

[0088] It is understood that, in a specific example, the sealing material feeding device and the cylindrical channel can be coupled in various ways. For example, the housing of the cylindrical channel can be configured as a detachable mechanism to accommodate the installation of the sealing material feeding device; alternatively, through holes suitable for the cylindrical channel can be opened at corresponding positions of the first and second housings, allowing the sealing material feeding device to be directly inserted and installed; and a drive handle or drive shaft hole can be reserved at an appropriate position (e.g., end plate) of the sealing material feeding device for manual or mechanical drive. Specifically, openings can be formed at the positions of the first and second housings corresponding to the ends of the cylindrical channel for inserting and installing the sealing material feeding device into the cylindrical channel, and a drive mechanism for driving the rotation of the sealing material feeding device can be installed at the openings.

[0089] In a preferred embodiment, the sealed material feeding devices 401 and 701 have a length of 1000mm-4000mm and a diameter of 100mm-400mm.

[0090] It is understandable that the structure of the sealed material discharge device can also be in other ways. For example, by using two doors set at the top and bottom and opening them in a staggered manner, it is possible to ensure the sealing between the pyrolysis chamber 700 and the oxidation reaction chamber 400 while realizing the conveying of decommissioned wind turbine blades from the pyrolysis chamber 700 to the oxidation reaction chamber 400 under airtight conditions.

[0091] In a preferred embodiment, the distance between the pyrolysis chamber 700 and the upper conveyor chain plate 703 is no more than 10 mm; the distance between the oxidation reaction chamber 400 and the lower conveyor chain plate 402 is no more than 10 mm.

[0092] Optionally, in this embodiment, the flue gas purification system 3 may include a dust collector 2 and a flue gas purifier 31; wherein, the flue gas purifier may be selected and configured as needed by those skilled in the art, for example, according to the proportion of nitrogen and sulfur in the flue gas, as well as the proportion of other harmful components such as carbon dioxide.

[0093] Optionally, in this embodiment, an air distribution device 403 is provided below the lower conveyor chain plate 402, and an air chamber 404 is formed between the air distribution device 403 and the bottom surface of the second housing. The air supply system is connected to the air chamber 404, and the air supply system includes an air compressor 12. In this embodiment, the air distribution device 403 is an air guide plate with uniformly spaced holes 4031. In other embodiments, the air distribution device 403 may also be multiple upward-directing air guide wheels, etc.

[0094] Please combine them together Figure 6 and Figure 7 Optionally, in this embodiment, the first heat exchange device 71 further includes an upper gas collecting cover 721 and a lower gas collecting cover 722 disposed opposite to each other. Both the upper gas collecting cover 721 and the lower gas collecting cover 722 are hollow plates. The bottom surface of the upper gas collecting cover 721 has multiple upper openings corresponding to the first heat exchange tube 702, and the upper opening of the first heat exchange tube 702 is connected to the upper opening (e.g., by welding). The top surface of the lower gas collecting cover 722 has multiple lower openings corresponding to the first heat exchange tube 702, and the lower opening of the first heat exchange tube 702 is connected to the lower opening (e.g., by welding). The bottom surface of the lower gas collecting cover 722 has a first gas port 723 communicating with the oxidation gas outlet 43. The lower gas collecting cover 722 also has a second gas port 724 communicating with the gas outlet 512 of the second heat exchange tube 51. The upper gas collecting cover 721 also has a third gas port 725 communicating with the flue gas purification system 3.

[0095] The upper gas collecting cover 721 is located above the upper conveyor chain plate 703, and the lower gas collecting cover 722 is located below the upper conveyor chain plate 703; optionally, the lower gas collecting cover 722 is located below the bottom surface of the first housing below the upper conveyor chain plate 703, or the top surface of the lower gas collecting cover 722 is shared as the bottom surface of the first housing.

[0096] It is understandable that, during the design process, the upper gas collecting cover 722 cannot block the material transfer between the feeding port 1 and the upper conveyor chain plate 703; for example, the feeding end of the upper conveyor chain plate 703 extends to the outside of the first heat exchange device 71, or a through hole is opened on the upper gas collecting cover 722 or a material channel is added so that the material can fall from the feeding port 1 onto the upper conveyor chain plate 703.

[0097] Optionally, in this embodiment, both the upper conveyor chain plate 703 and the lower conveyor chain plate 402 are chain plate type conveying devices, and the conveyor chain plate of the chain plate type conveying device is provided with ventilation holes 4021.

[0098] Alternatively, as a preferred embodiment of the chain plate, the conveying surfaces of the upper conveyor chain plate 703 and the lower conveyor chain plate 402 described in the above embodiments are arranged horizontally.

[0099] Optionally, in this embodiment, the second heat exchange device 5 may include multiple heat exchange sub-tube assemblies 50. Each heat exchange sub-tube assembly 50 includes an inlet main pipe 501, multiple second heat exchange tubes 51 arranged on a plane along the conveying direction of the lower conveyor chain plate, and an outlet main pipe 502. One end of the inlet main pipe 501 is connected to the inlet port 511, and the other end is connected to the inlet end of each second heat exchange tube 51. One end of the outlet main pipe 502 is connected to the outlet port 512, and the other end is connected to the outlet end of each second heat exchange tube 51. The multiple heat exchange sub-tube assemblies 50 may be arranged overlapping and / or side-by-side. The multiple heat exchange sub-tube assemblies 50 may share a single inlet main pipe 501 and outlet main pipe 502, or each heat exchange sub-tube assembly 50 may include its own independent inlet main pipe 501 and outlet main pipe 502.

[0100] The present invention also provides a pyrolysis recovery method for chopped glass fibers from wind turbine blades based on the pyrolysis recovery system described above, comprising the following steps:

[0101] S1, during initial startup, delivers combustible gas to the burner and, after combustion, transfers it to the second heat exchange device so that the temperature of the oxidation reaction chamber reaches 500℃-700℃ and the reaction temperature of the pyrolysis chamber reaches 400℃-500℃.

[0102] S2, the crushed wind turbine blades are fed through the feeding port at a feeding rate of 0t / h-2t / h, and the transmission rate of the upper conveyor chain plate 703 is controlled to make the pyrolysis time of the wind turbine blades in the pyrolysis chamber 0.5-2h, and the transmission rate of the lower conveyor belt is controlled to make the oxidation time of the wind turbine blades in the oxidation reaction chamber 0.5-2h. After the temperature of the pyrolysis chamber and the oxidation reaction chamber stabilizes, the supply of combustible gas to the burner is stopped.

[0103] S3, start the flue gas purification system and pyrolysis oil recovery system;

[0104] S4, start the sealed feeding device so that the wind turbine blades that have completed pyrolysis in the pyrolysis chamber continuously fall into the oxidation reaction chamber, and the glass fibers that have completed oxidation and decarbonization are discharged through the discharge port.

[0105] Specifically, during initial startup, combustible gas is supplied to the burner 9, generating high-temperature flue gas of 800℃-1000℃. This flue gas enters the second heat exchange tube 51 of the second heat exchange device 5 through the inlet 511, heating the oxidation reaction chamber 400 of the oxidation reactor 4. By adjusting the burner 9 and the air supply system, the high-temperature flue gas in the oxidation reaction chamber 400 is transported by the airflow through the oxidation gas outlet 43 into the first heat exchange tube 702. The first heat exchange tube 702 exchanges heat with the pyrolysis chamber 700, thus improving the heat exchange efficiency of the pyrolysis chamber 700. The temperature of the pyrolysis reactor reaches 400℃-500℃; the flue gas purification system 3 and the pyrolysis oil recovery system 10 are started; then the decommissioned wind turbine blades are fed into the crusher 6 at a feed rate of 0t / h-2t / h, and the power of the crusher 6 is adjusted so that the crushed wind turbine blades fall onto the upper conveyor chain plate 703 in the pyrolysis reactor 7 through the feed port 1 at a certain feed rate. The upper conveyor chain plate 703 moves at a uniform speed according to the design, and the transmission speed of the upper conveyor chain plate 703 is controlled so that the wind turbine blades are in the pyrolysis chamber 70. The pyrolysis time in chamber 700 is 0.5-2 hours. The decommissioned wind turbine blades are uniformly heated and decomposed within the pyrolysis chamber 700. The generated pyrolysis gas enters the condenser 10 through the pyrolysis gas channel 8, where it is separated into pyrolysis oil and non-condensable gas. The decommissioned wind turbine blades, after pyrolysis on the upper conveyor chain plate 703, fall into the oxidation reactor 4 under the rotation of the sealed material discharge device 701, where they undergo oxidation and decarbonization under aerobic conditions. By controlling the transmission rate of the lower conveyor belt 402, the oxidation time of the wind turbine blades in the oxidation reaction chamber 400 is kept to 0.5-2 hours. The high-temperature gas generated is then exchanged through the second heat exchange tube 702 to help maintain the temperature of the pyrolysis chamber 700. After the decommissioned wind turbine blades are completely oxidized in the oxidation reaction chamber 400, the remaining recycled glass fibers are discharged to the external solid collection device through the sealed discharge device 401. In addition, the non-condensable gas obtained after pyrolysis separation is used as fuel gas and fed into the burner 9 for combustion and heating to continuously generate high-temperature flue gas to heat the second heat exchange device 5 and maintain the temperature of the pyrolysis and oxidation reactions required by the pyrolysis recovery system.

[0106] The pyrolysis recovery system and method for chopped glass fibers in wind turbine blades, as described in this invention, are based on a dual-chamber pyrolysis reactor formed by stacking a pyrolysis chamber and an oxidation reaction chamber. After the wind turbine blades pass through a pulverizer and enter the pyrolysis reactor, they undergo pyrolysis at high temperatures. The gaseous components of the pyrolysis are condensed by a pyrolysis oil recovery system. The completely pyrolyzed material at the rear of the upper conveyor chain falls into the oxidation reactor under the rotation of a sealed feeding device, thereby promoting the effective separation of organic and inorganic components from the wind turbine blades. The beneficial effects of this invention include at least the following:

[0107] (1) Compact structure: The arrangement of two conveyor belts connected vertically (and in opposite directions) effectively improves space utilization efficiency;

[0108] (2) High-efficiency heat transfer: The high-temperature pyrolysis gas generated by the pyrolysis reaction in the pyrolysis chamber is condensed and separated into pyrolysis oil. The remaining non-condensable gas is fully combusted by the burner and then introduced into the second heat exchange device in the oxidation reaction chamber to provide heat for the oxidation reaction in the oxidation reaction chamber. The heat and flue gas generated by the oxidation reaction in the oxidation reaction chamber are introduced into the first heat exchange device in the pyrolysis chamber together with the gas of the second heat exchange device to provide heat for the pyrolysis reaction. They are isolated from each other and can also be used for heat recycling, which further improves the thermal efficiency of the system.

[0109] (3) Wide range of raw materials applicable and flexible and adjustable reaction process: By adjusting the transmission speed of the upper and lower conveyor belts, the temperature of the flue gas generated by the burner, and the position and angle of the air distribution device and fan outside each stage of the flue, the working state of the reaction chamber can be flexibly changed to adapt to the efficient pyrolysis of retired wind turbine blades of different parts and different components.

[0110] (4) High quality of regenerated fiber: The pyrolysis and oxidation processes are combined in stages to achieve in-situ decarbonization of regenerated fiber, which effectively inhibits the degradation of fiber strength and mechanical properties.

[0111] (5) High degree of product resource utilization: In addition to recycling glass fiber, the pyrolysis gas generated by the pyrolysis of retired wind turbine blades can be used for combustion to provide heat for reactor pyrolysis and realize the self-heating pyrolysis process; after condensation, liquid products are obtained, which can be used as liquid fuel or further purified to synthesize high-value chemicals.

[0112] (6) Clean emissions: All flue gas generated is treated by dust removal and purification devices before being discharged, achieving the harmless treatment of retired wind turbine blades.

[0113] The above are merely preferred embodiments of the present invention and do not limit the scope of the patent. Any equivalent structural or procedural transformations made based on the description and drawings of the present invention, or direct or indirect applications in other related technical fields, are similarly included within the scope of patent protection of the present invention.

Claims

1. A pyrolysis recovery system for chopped glass fibers in wind turbine blades, characterized in that, It includes a pyrolysis reactor, an oxidation reactor, a flue gas purification system, a first heat exchanger, a second heat exchanger, a pyrolysis oil recovery system, and a burner; the pyrolysis reactor is stacked on top of the oxidation reactor, wherein: The pyrolysis reactor includes a first shell and an upper conveyor chain plate disposed on the bottom surface inside the first shell. The inner cavity of the first shell forms a pyrolysis chamber. A pyrolysis gas outlet is provided above the first shell. The pyrolysis oil recovery system is connected to the pyrolysis chamber through the pyrolysis gas outlet. A discharge port is provided at the material drop end of the first shell near the upper conveyor chain plate, and a feeding port is provided at the material inlet end of the first shell corresponding to the upper conveyor chain plate. The first heat exchange device is disposed in the pyrolysis chamber. The first heat exchange device includes multiple first heat exchange tubes arranged around the upper conveyor chain plate. The upper end of the first heat exchange tube is connected to the flue gas purification system, and the lower end of the first heat exchange tube is connected to the oxidation reactor. The first heat exchange tube is not connected to the gas in the pyrolysis chamber. The oxidation reactor includes a second shell and a lower conveyor chain plate mounted inside the second shell. The inner cavity of the second shell forms an oxidation reaction chamber. An inlet is provided on the second shell near the discharge port. The loading end of the lower conveyor chain plate is located below the inlet. An outlet is provided on the second shell near the discharge end of the lower conveyor chain plate. An oxidation gas outlet is provided on the top of the second shell. The oxidation gas outlet is connected to the lower opening of the first heat exchange tube. The lower part of the oxidation reaction chamber is connected to an air supply system, which provides upward airflow to the oxidation reaction chamber. The second heat exchange device is disposed above the lower conveyor chain plate. The second heat exchange device includes multiple second heat exchange tubes arranged along the conveying direction of the lower conveyor chain plate. The second heat exchange tube includes an air inlet and an air outlet. The air inlet is connected to the burner, and the air outlet is directly or indirectly connected to the lower opening of the first heat exchange tube. The pyrolysis oil recovery system includes a condenser and a pyrolysis oil collection tank connected to the condensate outlet of the condenser. The air inlet of the condenser is connected to the pyrolysis gas outlet, and the air outlet of the condenser is connected to the burner. The first heat exchange device further includes an upper gas collecting cover and a lower gas collecting cover disposed opposite to each other, the lower gas collecting cover being located below the upper conveyor chain plate; both the upper and lower gas collecting covers are hollow plates, the bottom surface of the upper gas collecting cover has multiple upper openings corresponding to the first heat exchange tubes, the upper opening of the first heat exchange tubes being connected to the upper openings; the top surface of the lower gas collecting cover has multiple lower openings corresponding to the first heat exchange tubes, the lower opening of the first heat exchange tubes being connected to the lower openings; the upper gas collecting cover is located above the upper conveyor chain plate, and the lower gas collecting cover is located below the upper conveyor chain plate; the bottom surface of the lower gas collecting cover has a first gas port communicating with the oxidation gas outlet; the lower gas collecting cover also has a second gas port communicating with the gas outlet of the second heat exchange tube. The burner is used to burn the passing gas and deliver it to the air inlet. Heat exchange occurs in the oxidation reaction chamber via the second heat exchange tube, so that the temperature of the oxidation reaction chamber reaches 500℃-700℃. The high-temperature reaction flue gas in the oxidation reaction chamber is transported into the first heat exchange tube through the oxidation gas outlet under the action of wind. The gas discharged from the second heat exchange tube through the outlet is connected to the first heat exchange tube. The first heat exchange tube exchanges heat with the pyrolysis chamber, so that the temperature of the pyrolysis chamber is maintained at 400℃-500℃. A sealed material discharge device is provided between the discharge port and the inlet, and between the outlet and the outside.

2. The pyrolysis recovery system according to claim 1, characterized in that, It also includes a crusher, which includes a third housing and crushing rollers disposed within the third housing. The third housing has an inlet at its upper part and a lifting conveyor belt at its lower outlet. The material discharge end of the lifting conveyor belt is connected to the feeding port.

3. The pyrolysis recovery system according to claim 1, characterized in that, The upper and lower conveyor chains are arranged to overlap vertically and in opposite directions.

4. The pyrolysis recovery system according to claim 1, characterized in that, The discharge port and the inlet are connected to form a first discharge channel, and a second discharge channel is formed between the discharge port and the outside. Both the first and second discharge channels include cylindrical channels that are open at the top and bottom and extend laterally along their axes. The sealed discharge device includes two circular end plates arranged opposite each other and cross-shaped blades connected between the two end plates. The end plates are all vertically arranged and can be inserted into the ends of the cylindrical channels one by one. The cross-shaped blades include four blades arranged in a cross shape along the axial direction of the sealed discharge device. The radial diameter of the cross-shaped blades is adapted to the inner diameter of the corresponding cylindrical channel. The axial length of the sealed discharge device is greater than or equal to the length of the corresponding cylindrical channel. The sealed discharge device is rotatably disposed in the corresponding cylindrical channel along its central axis.

5. The pyrolysis recovery system according to claim 1, characterized in that, The pyrolysis chamber has a width of 1000mm-4000mm, a width-to-length ratio of 1 / 4 to 1 / 8, and a width-to-height ratio of 1 / 1 to 2 / 1; the oxidation reaction chamber has a width of 1000mm-4000mm, a width-to-length ratio of 1 / 5 to 1 / 9, and a width-to-height ratio of 1 / 1 to 2 / 1.

6. The pyrolysis recovery system according to claim 1, characterized in that, An air distribution device is provided below the lower conveyor chain plate, and an air chamber is formed between the air distribution device and the bottom surface of the second housing. The air supply system is connected to the air chamber and includes an air compressor. The air distribution device is a guide plate with uniform holes or multiple upward air-supplying guide wheels.

7. The pyrolysis recovery system according to claim 1, characterized in that, Both the upper and lower conveyor chains are chain-type conveyor devices, and the conveyor chains of the chain-type conveyor devices are provided with ventilation holes.

8. The pyrolysis recovery system according to claim 1, characterized in that, The second heat exchange device includes multiple heat exchange sub-tube assemblies. Each heat exchange sub-tube assembly includes an inlet main pipe, multiple second heat exchange tubes arranged on a plane along the conveying direction of the lower conveyor chain plate, and an outlet main pipe. One end of the inlet main pipe is connected to the inlet port, and the other end is connected to the inlet end of each second heat exchange tube. One end of the outlet main pipe is connected to the outlet port, and the other end is connected to the outlet end of each second heat exchange tube.

9. A method for pyrolysis recovery of chopped glass fibers from wind turbine blades based on a pyrolysis recovery system as described in any one of claims 1-8, characterized in that, Including the following steps: S1, during initial startup, delivers combustible gas to the burner and, after combustion, transfers it to the second heat exchange device so that the temperature of the oxidation reaction chamber reaches 500℃-700℃ and the reaction temperature of the pyrolysis chamber reaches 400℃-500℃. S2, the crushed wind turbine blades are fed through the feeding port at a feeding rate of 0t / h-2t / h, and the transmission rate of the upper conveyor chain is controlled to make the pyrolysis time of the wind turbine blades in the pyrolysis chamber 0.5-2h, and the transmission rate of the lower conveyor chain is controlled to make the oxidation time of the wind turbine blades in the oxidation reaction chamber 0.5-2h. After the temperature of the pyrolysis chamber and the oxidation reaction chamber stabilizes, the supply of combustible gas to the burner is stopped. S3, start the flue gas purification system and pyrolysis oil recovery system; S4, start the sealed feeding device so that the wind turbine blades that have completed pyrolysis in the pyrolysis chamber continuously fall into the oxidation reaction chamber, and so that the glass fibers that have completed oxidation and decarbonization are discharged through the discharge port.

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