Thermal decomposition reactor and carbon fiber and glass fiber recovery device comprising same

Abstract

The invention relates to a thermal decomposition reactor and a carbon fiber and glass fiber recovery device comprising the same. The thermal decomposition reactor comprises a shell, at least one moving module and at least one stirring module. The moving module may be provided with a helical blade attached to the inner wall of the case and expanding in the longitudinal direction of the case. The stirring module may be provided with a plurality of plate-shaped swirlers which are attached to the inner wall of the housing at right angles and extend in the longitudinal direction of the housing. The stirring modules may be alternately arranged with the moving modules. The moving module enables the waste composite material to move in the inner shell, and the stirring module enables the waste composite material to be mixed with hot air in the inner shell. According to the invention, the heat is effectively transferred to the waste composite material through the stirring module, so that the time required by the thermal decomposition process can be shortened.

Description

Technical Field

[0001] The present invention relates to a pyrolysis reactor and a recovery device for carbon fiber and glass fiber including the same. Background Art

[0002] Wind power generation refers to a power generation method in which the kinetic energy of wind is used to rotate blades and converted into mechanical energy and then the mechanical energy is converted into electrical energy. As an alternative to existing power generation methods that mainly use fossil fuels, its application is increasing.

[0003] A wind turbine has a plurality of blades installed on the rotating shaft of the generator. In order to generate more electrical energy, the blades are made long and wide. The larger the size of the blade, the greater the weight of the blade. However, for energy efficiency, the blade must be made light. In addition, since the blade continuously collides with the wind, the strength of the blade must also be increased to ensure durability. To solve this problem, carbon fiber reinforced plastic or glass fiber reinforced plastic is used as the material of the blade. Composite materials containing carbon fiber and glass fiber are not only light but also have high strength, so they are applied to various fields such as the automotive field and the aviation field in addition to blades.

[0004] However, after the blades of the wind turbine are damaged or their lifespan is exhausted, the disposal of waste blades becomes a problem. Generally, composite materials such as carbon fiber reinforced plastic or glass fiber reinforced plastic are difficult to reuse, so in most cases they are landfilled. However, it is impossible to keep landfilling more and more composite waste, and the need for treatment methods other than landfilling or methods that can be reused is constantly emerging.

[0005] Therefore, it is necessary to develop a reactor and a recovery device that can effectively recover carbon fiber or glass fiber from exhausted waste blades. In addition, in addition to waste blades, it is necessary to develop devices and methods that can recover carbon fiber and glass fiber in waste composite materials discharged from the automotive industry, the aviation industry, etc.

[0006] Prior Art Documents

[0007] Patent Document 1: Korean Patent No. 10-1810284 (Title: Method for Separating Carbon Fiber from Waste Carbon Fiber Reinforced Plastic) Summary of the Invention

[0008] An object of the present invention is to provide a pyrolysis reactor and a recovery device for carbon fiber and glass fiber that can recover and reuse fibers in a short time by maximizing heat transfer efficiency.

[0009] An object of the present invention is to provide a pyrolysis reactor and a recovery device for carbon fiber and glass fiber that can prevent waste composite materials from accumulating inside the reactor when the reactor rotates.

[0010] A pyrolysis reactor according to an embodiment of the present invention includes a shell, at least one moving module, and at least one stirring module. The shell is cylindrical. The moving module may include spiral blades installed on the inner wall of the shell and extending in the length direction of the shell. The stirring module may include a plurality of plate-shaped cyclones installed at right angles to the inner wall of the shell and extending in the length direction of the shell. The stirring module and the moving module may be alternately arranged.

[0011] In a pyrolysis reactor according to an embodiment of the present invention, the cyclone may include a flat plate portion with a short side in the radial direction of the shell, and an inclined portion inclined at a predetermined angle with respect to the flat plate portion.

[0012] In a pyrolysis reactor according to an embodiment of the present invention, the angle between the flat plate portion and the inclined portion may be 90 to 170°.

[0013] In a pyrolysis reactor according to an embodiment of the present invention, the end of the inclined portion may face the rotation direction of the shell.

[0014] In a pyrolysis reactor according to an embodiment of the present invention, the length ratio of the short sides of the flat plate portion and the inclined portion may be 1:1 to 1:0.3.

[0015] A pyrolysis reactor according to an embodiment of the present invention may further include a heating furnace having a burner and accommodating the shell therein.

[0016] A pyrolysis reactor according to an embodiment of the present invention may further include a charging portion disposed on one side of the heating furnace and connected to one end of the shell.

[0017] In a pyrolysis reactor according to an embodiment of the present invention, the charging portion may include a first valve located on the upstream side, a second valve located on the downstream side, and a gas inlet located between the first valve and the second valve.

[0018] A pyrolysis reactor according to an embodiment of the present invention may supply combustion gas at 400 to 500 °C into the shell.

[0019] In a pyrolysis reactor according to an embodiment of the present invention, the distance between adjacent blades in the spiral blades may be 0.1 to 0.3 m.

[0020] A pyrolysis reactor according to another embodiment of the present invention includes a shell, a moving module, and a stirring module. The shell is formed in a cylindrical shape. The moving module may include spiral blades installed on the inner wall of the shell and extending in the length direction of the shell. The stirring module may include a plurality of plate-shaped cyclones installed at right angles to the inner wall of the shell, with one side inserted into the spiral blades and extending in the length direction of the shell.

[0021] In a pyrolysis reactor according to another embodiment of the present invention, the cyclone may include a flat plate portion having a short side in the radial direction of the shell, and an inclined portion inclined at a predetermined angle with respect to the flat plate portion. The angle between the flat plate portion and the inclined portion may be 90 to 170°.

[0022] A carbon fiber and glass fiber recovery device according to an embodiment of the present invention includes: a waste composite material supply unit, a reaction unit for heating the waste composite material supplied from the waste composite material supply unit, a heat supply unit for supplying heat to the reaction unit, a modification unit for separating the pyrolysis gas discharged from the reaction unit into gas and oil, and a separation unit having a separation portion for separating the product of the reaction unit into a first substance and a second substance, a first chamber for accommodating the first substance, and a second chamber for accommodating the second substance. The reaction unit may include at least one pyrolysis reactor. The pyrolysis reactor includes a shell, at least one moving module, and at least one stirring module. The shell is cylindrical. The moving module may include a spiral blade installed on the inner wall of the shell and extending in the length direction of the shell. The stirring module may include a plurality of plate-shaped cyclones installed at right angles to the inner wall of the shell and extending in the length direction of the shell. The stirring module may be alternately arranged with the moving module.

[0023] In a carbon fiber and glass fiber recovery device according to an embodiment of the present invention, the cyclone may include a flat plate portion having a short side in the radial direction of the shell, and an inclined portion inclined at a predetermined angle with respect to the flat plate portion.

[0024] In a carbon fiber and glass fiber recovery device according to an embodiment of the present invention, the angle between the flat plate portion and the inclined portion may be 90 to 170°.

[0025] In a carbon fiber and glass fiber recovery device according to an embodiment of the present invention, the end of the inclined portion may face the rotation direction of the shell.

[0026] In a carbon fiber and glass fiber recovery device according to an embodiment of the present invention, the length ratio of the short sides of the flat plate portion and the inclined portion may be 1:1 to 1:0.3.

[0027] In a carbon fiber and glass fiber recovery device according to an embodiment of the present invention, the pyrolysis reactor may further include a heating furnace having a burner and accommodating the shell therein.

[0028] In a carbon fiber and glass fiber recovery device according to an embodiment of the present invention, the pyrolysis reactor may further include a charging portion disposed on one side of the heating furnace and connected to one end of the shell.

[0029] In a carbon fiber and glass fiber recovery device according to an embodiment of the present invention, the charging portion may include a first valve located on the upstream side, a second valve located on the downstream side, and a gas inlet located between the first valve and the second valve.

[0030] The carbon fiber and glass fiber recycling device according to an embodiment of the present invention can supply combustion gas at 400 to 500 °C to the inside of the shell.

[0031] In the carbon fiber and glass fiber recycling device according to an embodiment of the present invention, the distance between adjacent blades in the spiral blade can be 0.1 to 0.3 m.

[0032] According to an embodiment of the present invention, by maximizing the heat transfer efficiency, fibers can be recycled in a short time.

[0033] According to an embodiment of the present invention, it is possible to prevent waste composite materials from accumulating inside the reactor when the reactor rotates. BRIEF DESCRIPTION OF THE DRAWINGS

[0034] Figure 1 FIG. is a view showing a pyrolysis reactor according to an embodiment of the present invention.

[0035] Figure 2 FIG. is a view showing a pyrolysis reactor according to an embodiment of the present invention.

[0036] Figure 3 FIG. is a view showing a moving module in a pyrolysis reactor according to an embodiment of the present invention.

[0037] Figure 4 FIG. is a view showing a stirring module in a pyrolysis reactor according to an embodiment of the present invention.

[0038] Figure 5 FIG. is a view showing a cyclone in a pyrolysis reactor according to an embodiment of the present invention.

[0039] Figure 6 FIG. is a view showing a transverse cross-section of a pyrolysis reactor according to an embodiment of the present invention.

[0040] Figure 7 (a) and (b) of FIG. are views showing a pyrolysis reactor according to an embodiment of the present invention.

[0041] Figure 8 FIG. is a view showing a moving module and a stirring module in a pyrolysis reactor according to an embodiment of the present invention.

[0042] Figure 9 FIG. is a view showing a pyrolysis reactor according to an embodiment of the present invention.

[0043] Figure 10 FIG. is a view schematically showing a carbon fiber and glass fiber recycling device according to an embodiment of the present invention.

[0044] Figure 11It is a diagram showing that two thermal decomposition reactors are stacked according to an embodiment of the present invention.

[0045] Figure 12 It is a diagram showing that two thermal decomposition reactors are stacked according to an embodiment of the present invention. Detailed Description of the Invention

[0046] The present invention can be subjected to various transformations and can have various embodiments. Specific embodiments are illustrated below and will be described in detail in the detailed description. However, this is not intended to limit the present invention to a specific embodiment, but should be understood to include all transformations, equivalents, and substitutes included in the spirit and technical scope of the present invention.

[0047] The terms used in the present invention are merely used to describe specific embodiments and are not intended to limit the present invention. Singular expressions include plural expressions unless clearly indicated otherwise in the context. It should be understood that terms such as "comprising" or "having" in the present invention are used to specify the existence of features, numbers, steps, actions, components, parts, or combinations thereof described in the specification, and do not preclude the existence or additional possibility of one or more other features, numbers, steps, actions, components, accessories, or combinations thereof.

[0048] Hereinafter, preferred embodiments of the present invention will be described in detail with reference to the accompanying drawings. At this time, it should be noted that the same components in the drawings are denoted by the same reference numerals as much as possible. In addition, detailed descriptions of well-known functions and configurations that may affect the gist of the present invention are omitted. For the same reason, some components in the drawings are exaggerated, omitted, or shown approximately.

[0049] Figure 1 It is a diagram showing a thermal decomposition reactor according to an embodiment of the present invention. Figure 2 It is a diagram showing a thermal decomposition reactor according to an embodiment of the present invention. Figure 3 It is a diagram showing a moving module in a thermal decomposition reactor according to an embodiment of the present invention. Figure 4 It is a diagram showing a stirring module in a thermal decomposition reactor according to an embodiment of the present invention. Figure 5 It is a diagram showing a cyclone in a thermal decomposition reactor according to an embodiment of the present invention. Figure 6 It is a diagram showing a transverse cross-section of a thermal decomposition reactor according to an embodiment of the present invention.

[0050] As Figure 1 and 2 shown, the thermal decomposition reactor 1000 according to the present invention includes a shell 1100, a moving module 1200, and a stirring module 1300.

[0051] The shell 1100 is formed in a cylindrical shape. The waste composite material is thermally decomposed inside the shell 1100. For the mixing of the waste composite material, the shell 1100 can rotate in one direction. When the waste composite material is thermally decomposed, in order to maintain a reducing atmosphere, combustion gas is injected into the shell 1100 and combustion gas is discharged from the shell 1100. Combustion gas at 400 - 500 °C can be injected into the shell 1100.

[0052] A reducing atmosphere can be maintained inside the shell 1100. In order to maintain the reducing atmosphere, the gas discharged from the shell 1100 can be recycled into the shell 1100. The discharged gas consists of nitrogen, carbon dioxide, etc. One or more oxygen measurement sensors can be arranged inside the shell 1100. By continuously measuring the oxygen concentration inside the shell 1100, the oxygen concentration inside the shell 1100 is controlled to be less than 10%.

[0053] The shell 1100 has a length capable of ensuring the residence time of the waste composite material. The residence time can be at least 2 hours or more.

[0054] The moving module 1200 moves the waste composite material inside the shell 1100 as the shell 1100 rotates. As Figure 3 shown, the moving module 1200 is equipped with a spiral blade 1210. The spiral blade 1210 is fixed to the inner wall of the shell 1100.

[0055] The width of the spiral blade 1210 can be adjusted according to the design specifications. For example, the width of the spiral blade 1210 can be 10 - 15 cm. The spacing between adjacent spiral blades 1210 can be set differently according to the target residence time. For example, the spacing between the spiral blades 1210 can be 0.1 - 0.3 m.

[0056] The spacing between the spiral blades 1210 and the rotation speed of the shell 1100 can be adjusted to adjust the residence speed of the waste composite material and the state of the reactants.

[0057] The material of the spiral blade 1210 can be a metal with high thermal conductivity. The waste composite material can receive heat transfer by contacting the spiral blade 1210.

[0058] The stirring module 1300 mixes the waste composite material with hot air inside the shell 1100. The cyclone of the stirring module 1300 can effectively transfer heat to the waste composite material during the mixing process of the waste composite material.

[0059] As Figure 4 shown, the stirring module 1300 is equipped with a plurality of cyclones 1310. The plurality of cyclones 1310 can be arranged on the inner wall of the shell 1100 at equal angular intervals. 2 - 4 cyclones 1310 can be arranged along the inner circumferential surface of the shell 1100.

[0060] The cyclone 1310 has a rectangular plate shape. The cyclone 1310 has a long side extending in the longitudinal direction of the shell 1100 and a short side spreading in the radial direction of the shell. One end of the cyclone 1310 is fixed to the inner wall of the shell 1100, and the other end spreads toward the inside of the shell 1100.

[0061] The cyclone 1310 can be bent by a specified angle on one side in the spreading direction ( Figure 5 ). As the other end side of the cyclone 1310 bends, the cyclone 1310 has a flat plate portion 1311 and an inclined portion 1312. One end of the flat plate portion 1311 is fixed to the inner wall of the shell 1100, and the other end faces the radial direction of the shell 1100. One end of the inclined portion 1312 is connected to the flat plate portion 1311 and is inclined by a specified angle with respect to the flat plate portion 1311. The angle (θ) between the flat plate portion 1311 and the inclined portion 1312 can be 90 to 170°, preferably 90 to 120°.

[0062] When the shell 1100 rotates, more heat is transferred to the waste composite material through the cyclone 1310. When the shell 1100 rotates, the flow of the waste composite material located at the lower part of the shell 1100 is restricted by the cyclone 1310. When the cyclone 1310 is located at a position above a specified height due to the rotation of the shell 1100, the waste composite material divided by the cyclone 1310 falls. At this time, the inclined portion 1312 of the cyclone 1310 restricts the fall of the waste composite material in contact with the flat plate portion 1311, preventing the waste composite material from directly falling to the lower part of the shell 1100. The waste composite material contacts the cyclone 1310 through the inclined portion 1312 for a longer time, so that heat transfer can be effectively obtained.

[0063] At this time, the larger the angle between the flat plate portion 1311 and the inclined portion 1312, the faster the waste composite material in contact with the cyclone 1310 falls to the lower part of the shell 1100, so the mixing degree of the waste composite material becomes larger. On the contrary, if the angle between the flat plate portion 1311 and the inclined portion 1312 becomes smaller, the fall of the waste composite material is restricted, and the waste composite material contacts the cyclone 1310 for a longer time, so that more heat is transferred. The angle between the flat plate portion 1311 and the inclined portion 1312 can be selected according to the design specifications.

[0064] The long sides of the flat plate portion 1311 and the inclined portion 1312 extend along the longitudinal direction of the shell 1100 and have the same length. On the contrary, the short sides of the flat plate portion 1311 and the inclined portion 1312 can have different lengths. As Figure 5As shown, the length of the short side of the flat part 1311 can be l1, and the length of the short side of the inclined part 1312 can be l2. The length ratio of l1 to l2 can be from 1:1 to 1:0.3, preferably 1:0.5. The longer l1 is, the more area there is for the waste composite material to contact when the shell 1100 rotates, and more heat can be transferred to the waste composite material. When the size of the waste composite material 2000 undergoing thermal decomposition is large or the amount of the waste composite material 2000 is large, l1 can be made long so that a larger amount of the waste composite material 2000 contacts a larger area of the flat part 1311.

[0065] The length ratio of the flat part 1311 to the inclined part 1312 can be selected according to the desired design specifications. The material of the cyclone 1310 can be a metal with high thermal conductivity.

[0066] On the other hand, as Figure 6 shown, the inclination direction of the inclined part 1312 can be towards the rotation direction of the shell 1100. By making the inclined part 1312 face the rotation direction of the shell 1100, it is possible to limit the fallen waste composite material divided from falling below the cyclone 1310.

[0067] By having the inclined part 1312, the cyclone 1310 of the present invention prevents the waste composite material 2000 from being clamped or fixed to the cyclone 1310 when the shell 1100 rotates. In addition, through the cyclone 1310, not only is heat better transferred to the waste composite material 2000, but also the waste composite material 2000 is better mixed with the high-temperature air during the process of the waste composite material falling from the cyclone 1310 to the bottom surface of the shell 1100. Thus, the heat transfer efficiency to the waste composite material can be maximized.

[0068] The waste composite material is located at the lower part of the shell 1100, and it is difficult for the inside of the shell 1100 to be uniformly heated. However, the moving module 1200 and the stirring module 1300 can effectively transfer heat to the waste composite material during the process of moving and mixing the waste composite material. At least one moving module 1200 and at least one stirring module 1300 can be alternately arranged. In Figure 2 the illustrated embodiment, 3 moving modules 1200 and 2 stirring modules 1300 are alternately arranged, but it is not limited thereto, and moving modules 1200 and stirring modules 1300 with various lengths and numbers can be alternately arranged.

[0069] The length of the stirring module 1300 can be adjusted to adjust the residence time of the waste composite material. The length of the stirring module 1300 is designed considering the residence time during the thermal decomposition reaction, and the residence time is determined by the entire length and rotation speed of the shell 1100 and the length of the stirring module 1300. The materials of the moving module 1200 and the stirring module 1300 can be metals with high thermal conductivity.

[0070] Figure 7 Figures (a) and (b) are diagrams showing a thermal decomposition reactor according to an embodiment of the present invention. Figure 8 It is a diagram showing a moving module and a stirring module in a thermal decomposition reactor according to an embodiment of the present invention.

[0071] In another embodiment, the moving module 1300 and the stirring module 1400 can be configured to continuously extend along the length direction of the axis and overlap with each other within the shell 1100.

[0072] The moving module 1200 moves the waste composite material within the shell 1100 as the shell 1100 rotates. As shown in Figure 7 Figures (a) and (b), the moving module 1200 includes a spiral blade 1210'. The spiral blade 1210' is fixed to the inner wall of the shell 1100 and continuously extends along the length direction of the shell 1100.

[0073] The width of the spiral blade 1210' can be adjusted according to the design specifications. For example, the width of the spiral blade 1210' can be 10 - 15 cm. The spacing between adjacent spiral blades 1210' can be set differently according to the target residence time. For example, the spacing between the spiral blades 1210' can be 0.1 - 0.3 m.

[0074] The spacing between the spiral blades 1210' and the rotation speed of the shell 1100 can be adjusted to regulate the residence speed of the waste composite material and the state of the reactants.

[0075] The material of the spiral blade 1210' can be a metal with high thermal conductivity. The waste composite material can be in contact with the spiral blade 1210' to transfer heat.

[0076] The stirring module 1300 mixes the waste composite material with hot air within the shell 1100. The cyclone 1310' of the stirring module 1300 can effectively transfer heat to the waste composite material during the mixing process.

[0077] As shown in Figure 8 , the stirring module 1300 includes a plurality of cyclones 1310'. The cyclone 1310' is in the shape of a plate, one side is fixed to the inner wall of the shell 1100, and it continuously extends in the length direction of the shell 1100. The plurality of cyclones 1310' can be arranged on the inner wall of the shell 1100 at equal angular intervals. The cyclone 1310' can be arranged 2 - 4 along the inner circumferential surface of the shell 1100.

[0078] The cyclone 1310' has a rectangular plate shape. The cyclone 1310' has a long side extending in the length direction of the shell 1100 and a short side spreading in the radial direction of the shell. One end of the cyclone 1310' is fixed to the inner wall of the shell 1100, and the other end extends towards the inside of the shell 1100.

[0079] The cyclone 1310' can be bent by a specified angle on one side in the radial direction. As the other end side of the cyclone 1310' bends, the cyclone 1310' has a flat portion and an inclined portion. One end of the flat portion is fixed to the inner wall of the shell 1100, and the other end thereof faces the radial direction of the shell 1100. One end of the inclined portion is connected to the flat portion and is inclined by a specified angle with respect to the flat portion. The angle (θ) between the flat portion and the inclined portion can be 90 to 170°, preferably 90 to 120°.

[0080] When the shell 1100 rotates, more heat is transferred to the waste composite material through the cyclone 1310'. When the shell 1100 rotates, the flow of the waste composite material located at the lower part of the shell 1100 is restricted by the cyclone 1310'. When the cyclone 1310' is located at a position above a specified height due to the rotation of the shell 1100, the waste composite material divided by the cyclone 1310' falls. At this time, the inclined portion of the cyclone 1310' restricts the fall of the waste composite material in contact with the flat portion, preventing the waste composite material from directly falling to the lower part of the shell 1100. The waste composite material contacts the cyclone 1310' through the inclined portion for a longer time, so that heat transfer can be effectively obtained.

[0081] At this time, the larger the angle between the flat portion and the inclined portion, the faster the waste composite material in contact with the cyclone 1310' falls to the lower part of the shell 1100, so the mixing degree of the waste composite material becomes larger. On the contrary, if the angle between the flat portion and the inclined portion becomes smaller, the fall of the waste composite material is restricted, and the waste composite material contacts the cyclone 1310' for a longer time, so that more heat is transferred. The angle between the flat portion and the inclined portion can be selected according to the design specifications.

[0082] The long sides of the flat portion and the inclined portion extend along the length direction of the shell 1100 and have the same length. On the contrary, the short sides of the flat portion and the inclined portion can have different lengths. The length of the short side of the flat portion can be l1, and the length of the short side of the inclined portion can be l2. The length ratio of l1 to l2 can be 1:1 to 1:0.3, preferably 1:0.5. The longer l1 is, the more area there is for the waste composite material to contact when the shell 1100 rotates, and more heat can be transferred to the waste composite material. When the size of the thermally decomposed waste composite material 2000 is large or the amount of the waste composite material 2000 is large, l1 can be made long so that a larger amount of the waste composite material 2000 contacts a larger area of the flat portion.

[0083] The length ratio of the flat portion to the inclined portion can be selected according to the desired design specifications. The material of the cyclone 1310' can be a metal with high thermal conductivity.

[0084] On the other hand, the inclination direction of the inclined portion can be towards the rotation direction of the housing 1100. By making the inclined portion face the rotation direction of the housing 1100, it is possible to restrict the fallen waste composite material divided from falling below the cyclone 1310'.

[0085] By providing the cyclone 1310' of the present invention with an inclined portion, it is possible to prevent the waste composite material 2000 from being clamped or fixed to the cyclone 1310' when the housing 1100 rotates. In addition, through the cyclone 1310', not only is heat better transferred to the waste composite material 2000, but the waste composite material 2000 is better mixed with the high-temperature air during the process of the waste composite material falling from the cyclone 1310' to the bottom surface of the housing 1100. Thereby, the heat transfer efficiency to the waste composite material can be maximized.

[0086] The materials of the moving module 1200 and the stirring module 1300 can be metals with high thermal conductivity.

[0087] Figure 9 It is a diagram showing a thermal decomposition reactor according to an embodiment of the present invention.

[0088] As Figure 9 shown, the thermal decomposition reactor 1000 according to the present invention may further include a heating furnace 1400, a charging portion 1500, and a discharging portion 1600.

[0089] The heating furnace 1400 supplies heat to the waste composite material. High-temperature gas can flow into the heating furnace 1400. The heating furnace 1400 indirectly heats the waste composite material using the high-temperature gas.

[0090] The high-temperature gas can be generated by a burner (not shown) disposed outside the heating furnace 1400. The burner burns the thermal decomposition gas and LNG to generate combustion gas. The generated high-temperature combustion gas can be supplied into the heating furnace 1400. The temperature of the combustion gas can be 400 - 500 °C.

[0091] On the other hand, a plurality of burners 1410 may also be provided in the heating furnace 1400. The burners 1410 are disposed outside the housing 1100 and can be disposed in the area where the stirring module 1300 is disposed. The stirring module 1300 serves to mix the waste composite material and transfer heat to the waste composite material. By further supplying heat from the outside of the housing 1100, more heat can be transferred to the waste composite material. The heat source of the burners 1410 can be the thermal decomposition gas and LNG.

[0092] The charging portion 1500 transfers the crushed waste composite material to the housing 1100. The charging portion 1500 is connected to one end of the housing 1100.

[0093] The input section 1500 includes a hopper 1510, a first valve 1520, a second valve 1530, a gas inlet 1540, and a gas outlet 1550. The upper end of the hopper 1510 is open, and waste composite materials are supplied through the upper end of the hopper 1510. To facilitate the reception of waste composite materials, the hopper 1510 may have a frustum shape with a larger diameter at the upper end and a smaller diameter towards the lower part. A tubular passage extends downward from the hopper 1510.

[0094] To maintain a fixed air composition inside the shell 1100 for the thermal decomposition of waste composite materials. However, when the input section 1500 is opened to supply waste composite materials, outside air will flow in together, causing a change in the gas composition inside the shell 1100. To prevent this, the input section 1500 is provided with a first valve 1520 and a second valve 1530. The first valve 1520 is arranged on the upstream side of the passage, and the second valve 1530 is arranged on the downstream side of the passage.

[0095] The first valve 1520 and the second valve 1530 are controlled to be opened sequentially rather than simultaneously. The first valve 1520 and the second valve 1530 can be opened in a sliding manner, and the degree of opening can be adjusted according to the amount of waste composite materials to be input. In this embodiment, the input section 1500 forms a double structure through the first valve 1520 and the second valve 1530, but it is not limited thereto. The input section side may also be provided with more than three valves. Each valve can move within a specified range. As the multiple valves are opened respectively, a desired amount of crushed waste composite materials can be input into the interior of the shell 1100. In addition, through this double valve, waste composite materials can be continuously input into the shell 1100, and the inflow of oxygen can be minimized during input.

[0096] The first valve 1520 can be opened with the second valve 1530 closed. After opening the first valve 1520 and inputting a specified amount of crushed waste composite materials, when the first valve 1520 is closed and the input section 1500 is sealed, the second valve 1530 is opened. While the second valve 1530 is opened, flue gas can be injected through the gas inlet 1540. Flue gas is supplied to the passage of the input section 1500 during the opening of the second valve 1530, and when the second valve 1530 is closed again, the flue gas is discharged through the gas outlet 1550. Through the opening of the second valve 1530, the waste composite materials are input into the shell 1100. To facilitate the introduction of the waste composite materials into the shell 1100, the passage of the input section 1500 may have an inclined surface that slopes towards the shell 1100. Through the double valve and the supply of flue gas, the inflow of oxygen into the interior of the shell 1100 can be minimized.

[0097] The carbon fiber, glass fiber, and char after pyrolysis are discharged through the discharge unit 1600. The discharge unit 1600 is connected to the other end of the housing 1100. An outlet is provided on one side of the discharge unit 1600 to enable the pyrolysis reaction products transferred from the inside of the housing 1100 to be discharged. To discharge the pyrolysis reaction products, an opening or a cut surface may be formed on the end side of the housing 1100.

[0098] One end of the housing 1100 is rotatably connected to the input unit 1500, and the other end of the housing 1100 is rotatably connected to the discharge unit 1600. For the rotation of the housing 1100, a motor (not shown) may be disposed on the input unit 1500 side or the discharge unit 1600 side, or may be disposed on both sides of the input unit 1500 and the discharge unit 1600.

[0099] The pyrolysis reaction products discharged from the discharge unit 1600 may move to a reaction product recovery unit (not shown). The reaction product recovery unit accommodates the pyrolysis reaction products. The reaction product recovery unit is connected to the discharge unit 1600. The reaction product recovery unit may be inclined on the side adjacent to the discharge unit 1600 so that the pyrolysis products discharged from the discharge unit 1600 do not collide violently with the bottom surface of the reaction product recovery unit.

[0100] To prevent damage to the recycled fibers caused by a sharp temperature drop, the reaction product recovery unit may have a flue gas atmosphere of 100 °C or higher. Carbon fiber, glass fiber, and char are collected in the reaction product recovery unit.

[0101] Figure 10 FIG. is a diagram schematically showing a carbon fiber and glass fiber recovery device according to an embodiment of the present invention. Figure 11 FIG. is a diagram showing that two pyrolysis reactors are stacked according to an embodiment of the present invention. Figure 12 FIG. is a diagram showing that two pyrolysis reactors are stacked according to an embodiment of the present invention.

[0102] As Figure 10 shown, the carbon fiber and glass fiber recovery device 3000 includes a waste composite material supply unit 3100, a reaction unit 3200, a heat supply unit 3300, a modification unit 3400, and a separation unit 3500.

[0103] The waste composite material supply unit 3100 supplies the waste composite material to the reaction unit 3200. The waste composite material supply unit 3100 may preprocess the waste composite material into a state suitable for pyrolysis and then supply it to the reaction unit 3200.

[0104] The waste composite material supply unit 3100 includes a crushing module, a conveying module, a storage module, and a feeding module. The crushing module crushes the recycled waste composite material into a specified size and moves it to the storage module through the conveying module. The crushing module can crush the waste composite material cut to a specified length into a thickness of less than 20 mm. On the other hand, the crushing module can adjust the crushing size of the cut waste composite material. The crushing size of the waste composite material can be adjusted according to the target state and final product of the waste composite material. When long fibers can be recycled, the crushing size of the waste blades can be increased.

[0105] In the recycling process, a conveyor can be used to convey the waste composite material to each unit and each module. Multiple conveyors can be arranged continuously or side by side along the moving path of the waste composite material. The waste composite material can be screened during transportation.

[0106] In order to reduce the generation of water vapor during the thermal decomposition of the waste composite material, hot air can be supplied to the storage module to dry the stored waste composite material.

[0107] The feeding module feeds the waste composite material into the thermal decomposition reactor 1000 of the reaction unit 3200. In order to feed the crushed waste composite material, a single-screw feeder can be used. The feeding module can feed the waste composite material into the feeding part 1500 of the thermal decomposition reactor 1000 once or continuously.

[0108] On the other hand, it is necessary to reduce the temperature of the waste composite material placed in the feeding module. Cooling jackets can be arranged on the bottom and side surfaces of the feeding module to cool the waste composite material. The thermal decomposition reactor connected to the lower part of the feeding part is in a high-temperature state due to the high-temperature gas flowing inside. By arranging cooling jackets on the bottom and side surfaces of the feeding module, it is possible to prevent the heat released from the thermal decomposition reactor from being transferred to the feeding module, resulting in a fire of the waste blades located in the feeding module before being fed into the thermal decomposition reactor. The cooling jacket can receive cold water from the cooling tower of the modification unit to reduce the temperature of the fed waste composite material.

[0109] The reaction unit 3200 receives the waste composite material from the waste composite material supply unit 3100 and performs thermal decomposition. The reaction unit 3200 includes at least one thermal decomposition reactor 1000. The thermal decomposition reactor 1000 can include a shell 1100, a moving module 1200, a stirring module 1300, a heating furnace 1400, a feeding part 1500, and a discharging part 1600.

[0110] The thermal decomposition reactor 1000 has been described above, so the description is omitted.

[0111] The waste composite material introduced into the pyrolysis reactor 1000 is pyrolyzed within the pyrolysis reactor 1000. The pyrolysis process can go through the first pyrolysis step and the second pyrolysis step. Through the first pyrolysis, resins such as epoxy resin and wood contained in the waste composite material are gasified. Through the second pyrolysis, the resins and char residues remaining in the carbon fiber and glass fiber blocks are decomposed. During the first and second pyrolysis, the internal temperature of the pyrolysis reactor 1000 can be 400 - 600 °C.

[0112] The first pyrolysis and the second pyrolysis can be carried out by the pyrolysis reactor 1000. Considering the residence time of the waste composite material in the reactor, the size of the introduced waste composite material, etc., two or more pyrolysis reactors can be connected for use. For example, the reaction unit 3200 can include one first pyrolysis reactor 1000 and one second pyrolysis reactor 1000'. Or, in order to ensure the residence time during the first pyrolysis, the reaction unit 3200 can also include two first pyrolysis reactors 1000 and one second pyrolysis reactor 1000'.

[0113] The first pyrolysis reactor 1000 for the first pyrolysis and the second pyrolysis reactor 1000' for the second pyrolysis can be connected horizontally or vertically. As Figure 11 shown, when multiple pyrolysis reactors are connected vertically, the advantage is that the size of the entire device can be reduced and the degree of freedom in design can be improved.

[0114] When two pyrolysis reactors 1000, 1000' are vertically arranged, the rotation directions of the shells 1100, 1100' in the two pyrolysis reactors 1000, 1000' can be in opposite directions. As Figure 12 shown, it can be that the first pyrolysis reactor 1000 rotates in the clockwise direction and the second pyrolysis reactor 1000' rotates in the counterclockwise direction. At this time, the unfolding directions of the inclined parts 1312 of the cyclone 1310 can be in opposite directions.

[0115] The oxygen concentration inside the first pyrolysis reactor 1000 during the first pyrolysis should be maintained below 10%. A sensor can be arranged inside the first pyrolysis reactor 1000 to continuously measure the oxygen concentration. In another embodiment, a sensor can also be arranged in the discharge line to measure the oxygen concentration in the discharged gas.

[0116] The residence time of the crushed waste composite material in the first pyrolysis reactor 1000 during the first pyrolysis can be 9 hours or less. If the residence time is 9 hours or more, the reactants may be over-carbonized. The temperature inside the first pyrolysis reactor 1000 can be 400 - 500 °C.

[0117] After the first thermal decomposition, in the thermal decomposition reactor 1000, resins such as epoxy resin and wood contained in the waste composite material are gasified, leaving carbon fiber and glass fiber blocks as products. At this time, the resin that has not been gasified in time is carbonized (charred matter, char) and remains on the surfaces of the carbon fiber and glass fiber.

[0118] As products of the first thermal decomposition process, in addition to gas and charred matter (Char), oil mist is also generated. The oil mist is cooled during the process of passing through the modification unit 3400, so that part of it can be extracted as gas and part of it can be extracted as oil. The oil mist can be cooled by water. The gas generated from the oil mist has calorific value and can flow to the gas tank of the heat supply unit 3300 to be used as an indirect heat source for the second thermal decomposition.

[0119] The second thermal decomposition can be carried out in the second thermal decomposition reactor 1000'. The second thermal decomposition is a combustion reaction. The carbon fiber and glass fiber blocks with part of the charred matter removed are moved to the second thermal decomposition reactor 1000'. The carbon fiber and glass fiber in this step may have charred matter sticking between the fibers. During the second thermal decomposition process, the combustion gas containing about 10% oxygen causes the remaining epoxy resin and charred matter to burn. Through the second thermal decomposition process, that is, the combustion process, the remaining epoxy resin and charred matter are removed, leaving only carbon fiber and glass fiber.

[0120] The heat source for the second thermal decomposition can be combustion gas. The temperature of the combustion gas injected into the second thermal decomposition reactor 1000' can be 500 - 600 °C, preferably 500 °C. The oxygen concentration in the combustion gas can be approximately 10%. Through the combustion reaction in the second thermal decomposition reactor 1000', the resin and charred matter remaining on the carbon fiber and glass fiber blocks are decomposed.

[0121] The residence time of the carbon fiber and glass fiber blocks in the second thermal decomposition reactor 1000' can be 3 hours or less. At this time, if the oxygen concentration in the second thermal decomposition reactor 1000' is high, oxidation of the heating object may occur, so the oxygen concentration is maintained below 10%.

[0122] After the second thermal decomposition, high-purity carbon fiber and glass fiber are left.

[0123] The heat supply unit 3300 can include a burner, a heat exchanger, a blower, a scrubber, and a chimney. The thermal energy required for the thermal decomposition reaction can be supplied by the burner. The burner can supply combustion gas to the external shell in an indirect heating form. The burner can use thermal decomposition gas and LNG as fuel. The blower injects external air into the heat exchanger to conduct heat exchange with the external air. The external air is heated by the heat exchanger and supplied to the storage module.

[0124] The scrubber treats the exhaust gas. As the scrubber, a dust collection device using an aqueous NaOH solution can be used. In this embodiment, although a clean dust collection device using an aqueous NaOH solution is used, it is not limited thereto, and a scrubber such as a filtration method or an electrostatic method can also be used. The chimney finally discharges the exhaust gas and by-products.

[0125] The modification unit 3400 can include a catalyst tower, a heat exchanger, a separation tank, a cleaning tank, and a pressure control tank. The modification unit 3400 converts the pyrolysis gas into oil. Approximately 30% of the entire pyrolysis gas can be converted into pyrolysis oil. Thereby, the fuel amount of the pyrolysis furnace can be saved.

[0126] As the catalyst tower, a zeolite series commercial catalyst such as ZSM-5 can be used, but it is not limited thereto. The pyrolysis gas is modified while flowing from the lower part into the catalyst tower and upward. The heat exchanger cools the pyrolysis gas passing through the catalyst tower and atomizes the oil mist.

[0127] The separation tank separates the condensed pyrolysis gas into gas and oil. The cooled pyrolysis gas moves to the separation tank. The pyrolysis gas in a gaseous state is discharged from the upper part of the separation tank, and the oil condenses and is discharged from the lower part of the separation tank. The condensed oil can be stored in the pyrolysis oil storage tank.

[0128] The pyrolysis gas discharged from the upper part of the separation tank flows into the cleaning tank, and impurities in the gaseous pyrolysis gas are removed. The cleaning tank neutralizes the pyrolysis gas to reduce the amount of hydrogen chloride (HCl) in the pyrolysis gas, and the neutralized pyrolysis gas flows to the pressure control tank. The pressure control tank is arranged to prevent the reflux of the pyrolysis gas before the pyrolysis gas is supplied to the burner. The pyrolysis gas discharged from the pressure control tank can be supplied to the burner.

[0129] The modified pyrolysis gas is used again as fuel for heating the first pyrolysis reactor 1000 and the second pyrolysis reactor 1000'. By using the pyrolysis gas as fuel again, the overall fuel consumption can be reduced, and pollutant emissions can be reduced.

[0130] The separation unit 3500 may include a washing section, a separation section, a first chamber, a second chamber, a carding module, and a granulation module. The washing section receives the second pyrolysis product and washes it in such a way that lumps of carbon fiber and glass fiber remain. The separation section separates the second pyrolysis product into r-CF (recycled carbon fiber) and r-GF (recycled glass fiber). r-CF and r-GF can be separated using the density difference. As methods using the density difference, there are a dry method and a wet method. The dry method utilizes the flow of air, causing the flow of air to the second pyrolysis product moving on the conveyor to move the light carbon fiber.

[0131] The wet method is a method of separating carbon fiber and glass fiber using a liquid having a density between the densities of carbon fiber and glass fiber.

[0132] The carbon fiber and glass fiber separated by the separation section can be moved to the first chamber and the second chamber respectively. The separation operation of the carbon fiber and glass fiber can be carried out on the conveyor.

[0133] The carbon fiber and glass fiber stored in the first chamber and the second chamber respectively can be post-processed and shipped out.

[0134] The carding module combs r-CF and r-GF having a specified length. The length of r-CF and r-GF after removing the resin is 50 mm or less. Since the fiber length of r-CF and r-GF is short, they are combed for post-processing. The combed r-CF and r-GF are pressed and processed into non-woven fabric. When the length of r-CF and r-GF is 5 mm or less, since it is difficult to comb, they are not fed into the carding module. Before the recycled r-CF and r-GF are fed into the carding module, r-CF and r-GF having a length of 5 mm or less can be separated using a sieve or the like.

[0135] The granulation module melts and mixes the recycled r-CF, r-GF, and resin to make pellets. The granulation module cuts the non-woven fabric generated in the carding module into a specified size and mixes it with the molten resin. The r-CF and r-GF non-woven fabric whose structure has become hard by pressing is cured together with the resin and shipped out.

[0136] r-CF and r-GF having a length of 5 mm or less flow directly into the granulation module respectively. r-CF and r-GF having a length of 5 mm or less are directly mixed with the resin and granulated.

[0137] The control unit can receive the size of the waste composite material particles input into the pyrolysis reactor from the waste composite material supply module 3100, and determine whether the carbon fiber and glass fiber stored in the first chamber and the second chamber respectively move to the granulation module through the carding module or directly move to the granulation module. It can also adjust the crushing size of the waste composite material in the crushing step according to the user's needs.

[0138] The waste composite material of the present invention can be subjected to processes from crushing to pyrolysis and separation of carbon fiber and glass fiber in one process, and is moved to each unit through a conveyor. One or more conveyors can be connected to adjust the residence time in each unit.

[0139] Above, an embodiment of the present invention has been described. However, those skilled in the art can make various modifications and changes to the present invention by adding, changing, deleting or adding components, etc., within the scope not departing from the idea of the present invention described in the claims, and this is also included in the scope of the present invention's rights.

[0140] Explanation of reference numerals

[0141] 1000: Pyrolysis reactor 1100: Shell

[0142] 1200: Moving module 1210: Screw blade

[0143] 1300: Stirring module 1310: Cyclone

[0144] 1311: Flat part 1312: Inclined part

[0145] 1320: Heating part 1400: Heating furnace

[0146] 1410: Burner 1500: Feeding part

[0147] 1510: Hopper 1520: First valve

[0148] 1530: Second valve 1540: Gas inlet

[0149] 1550: Gas discharge port 1600: Discharge part.

Claims

1. A thermal decomposition reactor, characterized in that, Comprising: A cylindrical shell; At least one moving module, having a spiral blade installed on the inner wall of the shell and extending in the length direction of the shell; and At least one stirring module, having a plurality of plate-shaped cyclones installed at right angles on the inner wall of the shell and extending in the length direction of the shell, and being alternately arranged with the moving module.

2. The thermal decomposition reactor according to claim 1, characterized in that, The cyclone comprises: a flat plate portion, the short side having the radial direction of the shell; and an inclined portion, inclined at a specified angle with respect to the flat plate portion.

3. The thermal decomposition reactor according to claim 2, characterized in that, The angle between the flat plate portion and the inclined portion is 90 to 170°.

4. The thermal decomposition reactor according to claim 2, characterized in that, The end of the inclined portion faces the rotation direction of the shell.

5. The thermal decomposition reactor according to claim 2, characterized in that, The length ratio of the short sides of the flat plate portion and the inclined portion is 1:1 to 1:0.

3.

6. The thermal decomposition reactor according to claim 1 or 2, characterized in that, Further comprising: A heating furnace, having a burner and accommodating the shell therein.

7. The thermal decomposition reactor according to claim 6, characterized in that, Further comprising: A charging portion, arranged on one side of the heating furnace and connected to one end of the shell.

8. The thermal decomposition reactor according to claim 7, characterized in that, The charging portion comprises: A first valve located on the upstream side; A second valve located on the downstream side; and A gas inlet located between the first valve and the second valve.

9. The thermal decomposition reactor according to claim 1 or 2, characterized in that, A combustion gas at 400 to 500 °C is supplied into the shell.

10. The thermal decomposition reactor according to claim 1 or 2, characterized in that, The distance between adjacent blades of the spiral blade is 0.1 to 0.3 m.

11. A thermal decomposition reactor, characterized in that, Comprising: A cylindrical shell; A moving module, having a spiral blade installed on the inner wall of the shell and extending in the length direction of the shell; and A stirring module, having a plurality of plate-shaped cyclones installed at right angles on the inner wall of the shell, and one side being inserted into the spiral blade and extending in the length direction of the shell.

12. The thermal decomposition reactor according to claim 11, wherein, The cyclone comprises: a flat plate portion, the short side having the radial direction of the shell; and an inclined portion, inclined at a specified angle with respect to the flat plate portion, The angle between the flat plate portion and the inclined portion is 90 to 170°.

13. A carbon fiber and glass fiber recycling device, characterized in that, Comprising: A waste composite material supply unit; A reaction unit, heating the waste composite material supplied from the waste composite material supply unit; A heat supply unit, providing heat to the reaction unit; A modification unit, separating the thermal decomposition gas discharged from the reaction unit into gas and oil; and A separation unit, comprising a separation section that separates the product of the reaction unit into a first substance and a second substance, a first chamber that accommodates the first substance, and a second chamber that accommodates the second substance. The reaction unit includes at least one pyrolysis reactor, and The pyrolysis reactor includes: A cylindrical shell; At least one moving module, having a spiral blade installed on the inner wall of the shell and extending in the length direction of the shell; and At least one stirring module, having a plurality of plate-shaped cyclones installed perpendicular to the inner wall of the shell and extending in the length direction of the shell, and being alternately arranged with the moving module.

14. The carbon fiber and glass fiber recycling device according to claim 13, wherein The cyclone includes: a flat plate portion, the short side of which has the radial direction of the shell; and an inclined portion, which is inclined at a predetermined angle with respect to the flat plate portion.

15. The carbon fiber and glass fiber recycling device according to claim 14, wherein The angle between the flat plate portion and the inclined portion is 90 to 170°.

16. The carbon fiber and glass fiber recycling device according to claim 14, wherein The end of the inclined portion faces the rotation direction of the shell.

17. The carbon fiber and glass fiber recycling device according to claim 14, wherein The length ratio of the short sides of the flat plate portion and the inclined portion is 1:1 to 1:0.

3.

18. The carbon fiber and glass fiber recycling device according to claim 13 or 14, wherein The pyrolysis reactor further includes: A heating furnace, having a burner and accommodating the shell inside.

19. The carbon fiber and glass fiber recycling device according to claim 18, wherein The pyrolysis reactor further includes: A feeding portion, disposed on one side of the heating furnace and connected to one end of the shell.

20. The carbon fiber and glass fiber recycling device according to claim 19, wherein The feeding portion includes: A first valve located on the upstream side; A second valve located on the downstream side; and A gas inlet located between the first valve and the second valve.

21. The carbon fiber and glass fiber recycling device according to claim 13 or 14, wherein Combustion gas at 400 to 500 °C is supplied into the shell.

22. The carbon fiber and glass fiber recycling device according to claim 13 or 14, wherein The distance between adjacent blades of the spiral blade is 0.1 to 0.3 m.

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