Method for operating a chemical manufacturing apparatus, method for manufacturing chemicals, and method for regenerating fillers

Abstract

To provide an operating method for a chemical manufacturing apparatus that can operate stably for long periods of time and efficiently thermally decompose raw materials. [Solution] The method of operating the chemical manufacturing apparatus of the present disclosure comprises a reactor 1, a filler 2 filled inside the reactor 1, a raw material supply unit 3 for supplying raw material M inside the reactor 1, an inert gas supply unit 4 for supplying inert gas G inside the reactor 1, a heating unit 5 for heating the filler 2, and a removal unit 6 for removing chemical product R from the reactor 1, and includes (Sa1) supplying inert gas G inside the reactor 1 by the inert gas supply unit 4, (Sa2) supplying raw material M by the raw material supply unit 3 while heating the reactor by the heating unit 5, (Sa3) removing the chemical product R generated from the raw material M from inside the reactor 1 by the removal unit 6, and (Sa4) and (Sa3) after heating the filler 2 to 400°C to 720°C by the heating unit 5.

Description

[Technical Field]

[0001] This disclosure relates to a method for operating a chemical manufacturing apparatus, a method for manufacturing chemicals, and a method for regenerating fillers. [Background technology]

[0002] One method of recycling waste plastics is chemical recycling, which involves decomposing waste plastics, monomerizing and gasifying them, or using them as blast furnace reducing agents or coke oven raw materials. For example, a fluidized bed reactor is generally used in continuous reactors that use mixed plastics containing polyolefins as raw materials to obtain basic chemicals in a single stage without going through intermediate products such as pyrolysis oils.

[0003] Patent Document 1 discloses that a plastic powder, which is a mixture of polyolefins, polystyrene, polyethylene terephthalate (PET), etc., is supplied to a fluidized bed reactor and decomposed to obtain C2 to C4 olefins, that the heating medium in the fluidized bed is a mixture of used fluid catalytic cracking (FCC) catalyst and ZSM-5, and that these catalysts may contain binder materials such as alumina or silica. [Prior art documents] [Patent Documents]

[0004] [Patent Document 1] Special Publication No. 2016-513147 [Overview of the Initiative] [Problems that the invention aims to solve]

[0005] This disclosure aims to provide a method for operating a chemical manufacturing apparatus that can operate stably for long periods of time and efficiently thermally decompose raw materials. [Means for solving the problem]

[0006] The means for solving the above problems are as follows. That is, <1> A method for operating a chemical manufacturing apparatus, wherein the chemical manufacturing apparatus includes a reactor, fillers filled inside the reactor, a raw material supply unit for supplying a raw material into the reactor, an inert gas supply unit for supplying an inert gas into the reactor, a first heating unit for heating the reactor, a take-out unit for taking out the chemical from the reactor, a first oxygen-containing gas supply unit for supplying an oxygen-containing gas to the reactor, and is provided with (Sa1) supplying the inert gas into the reactor by the inert gas supply unit; (Sa2) while heating the reactor by the first heating unit, supplying the raw material by the raw material supply unit; (Sa3) taking out the chemical produced from the raw material from the inside of the reactor by the take-out unit; (Sa4) after (Sa3), while supplying the oxygen-containing gas from the first oxygen-containing gas supply unit, heating the filler to 400°C to 720°C by the first heating unit; and is a method for operating a chemical manufacturing apparatus including these steps. <2> The method for operating a chemical manufacturing apparatus according to <1>, wherein after (Sa4), (Sa1), (Sa2), and (Sa3) are repeated. <3> The method for operating a chemical manufacturing apparatus according to <1> or <2>, wherein in (Sa1), the inert gas is supplied into the reactor from the inert gas supply unit to flow the filler. <4> The chemical manufacturing apparatus further includes a regeneration furnace provided separately from the reactor, a used filler transfer unit for transferring the filler from the reactor to the inside of the regeneration furnace, A second oxygen-containing gas supply unit that supplies oxygen-containing gas to the inside of the regenerating furnace, A second heating section for heating the aforementioned regeneration furnace, The system further comprises a regenerated filler transfer unit for transferring the filler from the regenerated furnace to the inside of the reactor, (Sa5) Simultaneously with (Sa4) or after (Sa4), the filler is transferred from the reactor to the inside of the regenerating reactor through the used filler transfer unit. (Sa6) The filler is heated to 400°C to 720°C by the second heating unit while the oxygen-containing gas is supplied from the second oxygen-containing gas supply unit, (Sa7) Transferring the filler from the regenerating furnace to the inside of the reactor through the regenerating filler transfer unit, The following further includes <1> from the above <3> This is a method for operating a chemical manufacturing apparatus described in any one of the items. <5> A method for operating a chemical manufacturing apparatus, The chemical manufacturing apparatus is, Reactor and The filler packed inside the reactor, A raw material supply unit that supplies raw materials to the inside of the reactor, An inert gas supply unit that supplies inert gas to the inside of the reactor, The reactor comprises a first heating section for heating the reactor, A removal section for removing the chemical from the reactor, A regenerating reactor is provided separately from the aforementioned reactor, A used filler transfer unit that transfers the filler from the reactor to the inside of the regenerating reactor, A second oxygen-containing gas supply unit that supplies oxygen-containing gas to the inside of the regenerating furnace, A second heating section for heating the aforementioned regeneration furnace, A regenerated filler transfer unit that transfers the filler from the reactor to the inside of the regenerated reactor, Equipped with, (Sb1) The inert gas is supplied into the reactor by the inert gas supply unit, (Sb2) The reaction furnace is heated by the first heating unit while the raw material is supplied by the raw material supply unit, (Sb3) The chemical product produced from the raw materials is removed from the inside of the reactor by the removal unit, (Sb4) Simultaneously with (Sb2) or after (Sb2), the filler is transferred from the reactor to the inside of the regenerating reactor through the used filler transfer unit. (Sb5) The oxygen-containing gas is supplied to the inside of the regenerating furnace by the second oxygen-containing gas supply unit, while the filler is heated to 400°C to 720°C by the second heating unit, (Sb6) Transferring the filler from the regenerating furnace to the inside of the reactor through the regenerating filler transfer unit, This is a method for operating a chemical manufacturing apparatus, including [specific details omitted]. <6> After (Sb5), the above (Sb1), (Sb2), (Sb3), and (Sb4) are repeated. <5> This is the operating method for the chemical manufacturing apparatus described above. <7> In (Sb1) above, the inert gas is supplied into the reactor from the inert gas supply unit to cause the filler to flow, <5> or the above <6> This is the operating method for the chemical manufacturing apparatus described above. <8> The reactor is a fixed bed, <1> or the above <5> This is the operating method for the chemical manufacturing apparatus described above. <9> The filler comprises at least one of silica sand and silicon dioxide. <1> from the above <8> This is a method for operating a chemical manufacturing apparatus described in any one of the items. <10> The aforementioned raw material is a raw material containing plastic, The chemical comprises at least one selected from the group consisting of olefins having 2 to 5 carbon atoms and aromatic hydrocarbons. The aforementioned <1> from the above <9> This is a method for operating a chemical manufacturing apparatus described in any one of the items. <11> A method for manufacturing chemical products, (Sc1) Supplying an inert gas to the inside of the reactor containing the filler, (Sc2) Supplying raw materials including plastic while heating the reactor, (Sc3) Taking out the chemical product produced from the raw materials from inside the reactor, (Sc4) After (Sc3) or simultaneously with (Sc3), the filler is heated to 400°C to 720°C while supplying an oxygen-containing gas. Includes, The method for producing the chemical is characterized in that the chemical contains at least one selected from the group consisting of olefins having 2 to 5 carbon atoms and aromatic hydrocarbons. <12> After (Sc4), the above (Sc1), (Sc2), and (Sc3) are repeated. <11> This is a method for producing the chemicals described. <13> The filler comprises at least one of silica sand and silicon dioxide. <11> or the above <2> This is a method for producing the chemicals described. <14> A method for regenerating fillers, (Sd1) Supplying an inert gas to the inside of the reactor containing the filler, (Sd2) Supplying raw materials while heating the reactor, (Sd3) Taking out the chemical product produced from the raw materials from inside the reactor, (Sd4) After (Sd3) or simultaneously with (Sd3), the filler is heated to 400°C to 720°C while supplying an oxygen-containing gas. This is a method for regenerating fillers, characterized by including [a specific component]. <15> After (Sd4), the above (Sd1), (Sd2), and (Sd3) are repeated. <14> This is the method for regenerating the filler described. <16> The filler comprises at least one of silica sand and silicon dioxide. <14> or the above <15> This is the method for regenerating the filler described. <17> The aforementioned raw material is a raw material containing plastic, The chemical comprises at least one selected from the group consisting of olefins having 2 to 5 carbon atoms and aromatic hydrocarbons. The aforementioned <14> from the above <16> This is a method for regenerating the filler as described in any one of the items. [Effects of the Invention]

[0007] According to embodiments of this disclosure, it is possible to provide a method for operating a chemical manufacturing apparatus that can operate stably for a long period of time and efficiently thermally decompose raw materials. [Brief explanation of the drawing]

[0008] [Figure 1] Figure 1 is a schematic cross-sectional view showing an example of a chemical manufacturing apparatus according to the first embodiment of this disclosure. [Figure 2] Figure 2 is a flowchart showing an example of how to operate a chemical manufacturing apparatus according to the first embodiment of this disclosure. [Figure 3] Figure 3 is a schematic cross-sectional view showing an example of a manufacturing apparatus according to a second embodiment of the chemical product of this disclosure. [Figure 4] Figure 4 is a flowchart showing an example of an operating method for a chemical manufacturing apparatus according to the second embodiment of this disclosure. [Figure 5] Figure 5 is a schematic cross-sectional view showing an example of a chemical manufacturing apparatus according to the third embodiment of this disclosure. [Figure 6] Figure 6 is a flowchart showing an example of an operating method for a chemical manufacturing apparatus according to the third embodiment of this disclosure. [Figure 7] Figure 7 is a schematic cross-sectional view showing an example of a chemical manufacturing apparatus according to the fourth embodiment of this disclosure. [Figure 8A] Figure 8A is a schematic diagram showing an example of a cross-section parallel to the deposition direction of filler 2 in the filler layer 2A of reactor 1. [Figure 8B] Figure 8B is a schematic diagram of the line VIIIB-VIIIB in Figure 8A. [Figure 9] Figure 9 is a schematic cross-sectional view showing an example of a chemical manufacturing apparatus according to the fifth embodiment of this disclosure. [Figure 10]Figure 10 is a schematic cross-sectional view showing an example of a chemical manufacturing apparatus according to the sixth embodiment of this disclosure. [Figure 11] Figure 11 is a flowchart showing an example of a method for producing the chemicals described herein. [Figure 12] Figure 12 is a flowchart showing an example of a filler regeneration method according to this disclosure. [Modes for carrying out the invention]

[0009] The embodiments of this disclosure will be described in detail below. However, the embodiments are not limited to the following description and can be modified as appropriate without departing from the gist of this disclosure. Furthermore, in this specification, the "~" indicating a numerical range means that the numbers before and after it are included as the lower and upper limits, respectively, unless otherwise specified.

[0010] The embodiments shown in this disclosure are illustrative of devices for realizing the technical concept of this disclosure and do not limit this disclosure to the following. Furthermore, the dimensions, materials, shapes, numbers, relative arrangements, etc. of the components described below are merely illustrative examples and are not intended to limit the scope of this disclosure unless otherwise specified. Note that the size, positional relationships, etc. of the members shown in each drawing may be exaggerated for clarity of explanation. In addition, in the following description, the same name and reference numeral indicate the same or similar member, and detailed explanations are omitted as appropriate. In order to avoid making the drawings excessively complex, schematic diagrams that omit the illustration of some elements may be used, or end view diagrams showing only the cut surface may be used as cross-sectional views.

[0011] Furthermore, the following description uses terms to indicate specific directions or positions as needed (e.g., "up," "down," "side," "top surface," "bottom surface," "side," "X," "Y," "Z," and other terms including these terms). However, the use of these terms is solely to facilitate understanding of the invention with reference to the drawings, and the meaning of these terms does not excessively limit the technical scope of the invention. For example, if "top surface" is mentioned, the invention must not always be used in a way that it faces upwards.

[0012] In each figure, the X, Y, and Z axes are defined as follows: the vertical direction is the Y-axis, the direction approximately perpendicular to the Y-axis is the X-axis, and the direction approximately perpendicular to both the X and Y axes is the Z-axis. The X, Y, and Z axes are mutually orthogonal. However, this direction is merely an example, and the direction of the chemical manufacturing apparatus in this disclosure is not limited to this.

[0013] (Operating procedures for chemical manufacturing equipment) The method for operating the chemical manufacturing apparatus of the present disclosure comprises a reactor, a filler filled inside the reactor, a raw material supply unit for supplying raw materials inside the reactor, an inert gas supply unit for supplying inert gas inside the reactor, a first heating unit for heating the reactor, a removal unit for removing the chemical from the reactor, and a first oxygen-containing gas supply unit for supplying oxygen-containing gas to the reactor, and includes: (Sa1) supplying the inert gas inside the reactor by the inert gas supply unit; (Sa2) supplying the raw materials by the raw material supply unit while heating the reactor by the first heating unit; (Sa3) removing the chemical produced from the raw materials from inside the reactor by the removal unit; and (Sa4) after (Sa3), heating the filler to 400°C to 720°C by the first heating unit while supplying oxygen-containing gas from the first oxygen-containing gas supply unit. The operating method of the chemical manufacturing apparatus of this disclosure may further include other processes as necessary. Furthermore, the chemical manufacturing apparatus of this disclosure may further include other components as necessary.

[0014] The method disclosed in Patent Document 1 primarily uses a mixture of FCC (Fluid Catalytic Cracking) catalyst and ZSM-5 for the decomposition of plastics, and does not optimize the reaction conditions of the fluidized bed or fixed bed in the thermal decomposition of plastics.

[0015] Mixed plastics and waste solid fuel (RPF: Refuse-derived paper and plastics densified fuel) tend to produce liquid products such as benzene and styrene during decomposition. In fluidized bed reactions, this can hinder the fluidization of the fluidized bed, leading to poor decomposition efficiency of the plastics. Furthermore, RPF, in particular, does not consist of a fixed set of components, making it difficult to determine the decomposition conditions.

[0016] In response to this, the inventors conducted diligent research and found that the filler used in the decomposition of raw materials reduces the efficiency of plastic decomposition and the yield of useful components, making it difficult to operate the chemical manufacturing equipment stably for long periods of time. To address this problem, they found that by heating the filler used in the decomposition of raw materials to 400°C to 720°C, the yield of useful components does not decrease compared to unused filler, thereby enabling the chemical manufacturing equipment to operate stably for long periods of time and efficiently thermally decompose the raw materials. In other words, they found that by heating the filler used in the decomposition of raw materials to 400°C to 720°C, the filler can be regenerated to a level equivalent to or better than unused filler.

[0017] In this disclosure, "regenerated filler" means that the percentage P of the total yield of useful components when the raw material is decomposed using unused filler that has never been used in the decomposition of the raw material is 95% or higher, preferably 96% or higher, and more preferably 97% or higher, relative to this "reference value". When determining the percentage P, the raw material, filler, and decomposition conditions used are the same whether unused filler is used or filler that has been used at least once in the decomposition of the raw material is used.

[0018] In this disclosure, fillers that have been used at least once to decompose raw materials may be referred to as "used fillers." There are no particular restrictions on the number of times used fillers have been used to decompose raw material M, as long as it has been at least once.

[0019] Furthermore, in this disclosure, fillers obtained by heating used fillers at 400°C to 720°C may be referred to as "recycled fillers."

[0020] [Operation method of the chemical manufacturing apparatus according to the first embodiment] <Chemical manufacturing apparatus according to the first embodiment> First, a first embodiment of the chemical manufacturing apparatus used in the operating method of the chemical manufacturing apparatus of this disclosure will be described with reference to Figure 1. Figure 1 is a schematic cross-sectional view showing an example of the chemical manufacturing apparatus according to the first embodiment of this disclosure.

[0021] The chemical manufacturing apparatus 100 (hereinafter sometimes abbreviated as "manufacturing apparatus 100") comprises a reactor 1, a filler 2 filled inside the reactor 1, a raw material supply unit 3 for supplying raw material M to the inside of the reactor 1, an inert gas supply unit 4 for supplying inert gas G to the inside of the reactor 1, a first heating unit 5 for heating the filler 2, a removal unit 6 for removing chemical product R from the reactor 1, and a first oxygen-containing gas supply unit 7 for supplying oxygen-containing gas to the reactor 1.

[0022] The inert gas G is supplied to the filler 2 through the plug 11 from a direction opposite to the vertical direction in the Y-axis direction. By passing the inert gas G through the filler 2 at a sufficient speed, the filler 2 is suspended and made to behave like a fluid, so that the reactor 1 of the manufacturing apparatus 100 functions as a fluidized bed. Therefore, in the manufacturing apparatus 100, the filler 2 is fluidized sand.

[0023] <<Reactor 1>> The reactor 1 is a component that can accommodate the filler 2 and has a certain internal space to ensure a flow path for the raw materials and inert gas, and is preferably a fluidized bed. In the reactor 1, the filler 2 placed inside the reactor 1 is heated by the first heating unit 5, thereby heating the raw materials M supplied to the inside of the reactor 1.

[0024] The structure, shape, material, and size of the reactor 1 are not particularly limited, as long as they can accommodate the filler 2, are chemically and mechanically stable under reaction conditions, and allow the raw material M to flow through them. They can be appropriately selected according to the purpose.

[0025] The material of the reactor 1 is not particularly limited as long as it is stable in terms of surface temperature and atmosphere on the inside of the reactor 1, that is, on the side of the reactor 1 that contains the raw materials M. For example, inorganic compounds such as alumina (Al2O3), zirconia (ZrO3), silicon carbide (SiC), silicon nitride (Si3N4), mullite (3Al2O3·2SiO2) or ceramics thereof; alloys such as SUS310S, Inconel (INCONEL®), and Hastelloy (HASTELLOY®) can be used.

[0026] Examples of the shape of the reactor 1 include cylindrical, rectangular parallelepiped, conical, frustoconical, and columnar shapes in which the cross-sectional shape perpendicular to the longitudinal direction of the reactor 1 is polygonal.

[0027] Furthermore, regarding the size of the reactor 1, it is preferable that the direction perpendicular to the flow direction of the raw material M, i.e., longer than the inner diameter of the reactor 1, from the viewpoint of allowing the raw material M and the generated chemical product R to flow smoothly and ensuring sufficient contact time between the raw material M and the fluidized bed of filler 2.

[0028] The reactor 1 is capable of circulating an inert gas G, such as quartz wool, and a chemical product R in order to retain the filler 2 inside, and it is preferable to place a stopper 11 inside the reactor 1 (for example, inside a pipe).

[0029] The structure, shape, material, and size of the stopper 11 are not particularly limited, as long as it does not allow the filler 2 to pass through, but does allow the inert gas G, raw material M, or chemical R to pass through. They can be appropriately selected according to the purpose, and examples include quartz wool, a sieve, a mesh, and a dispersion plate. These may be used individually or in combination of two or more types.

[0030] <<Filler 2>> There are no particular restrictions on filler 2, and it can be appropriately selected depending on the purpose. However, it is preferable that the material is stable in the temperature range of thermal decomposition when heated, does not undergo reduction by hydrocarbons, carbon, hydrogen, etc. produced by the thermal decomposition of plastic, and does not react with inert gases.

[0031] Specific examples of filler 2 include silica sand, zirconium oxide, yttria-stabilized zirconium oxide, calcia-stabilized zirconium oxide, magnesium oxide, calcium oxide, silicon carbide, silicon nitride, silicon dioxide (silica), tantalum oxide, niobium oxide, beryllium oxide, lanthanum oxide, manganese(II) oxide, chromium(III) oxide, gallium oxide, forstenite, cordierite, and silica-alumina. Filler 2 may also be a surface-treated version of the above materials for purposes such as surface deactivation or improvement of raw material fluidity. These may be used individually or in combination of two or more. Among these, at least one of silica sand and silicon dioxide, which may be surface-treated, is preferred as filler 2, and silica sand or a surface-treated version thereof is more preferred.

[0032] There are no particular restrictions on the surface-treated filler 2, and it can be appropriately selected depending on the purpose. Examples include granular media having an oxide film on the surface and granular media having a carbon film on the surface. There are no particular restrictions on the method for surface-treating the filler 2, and it can be appropriately selected from known methods.

[0033] The structure of surface-treated filler 2 can be confirmed, for example, by observation using a scanning electron microscope (SEM), a transmission electron microscope (TEM), X-ray photoelectron spectroscopy (XPS), or micro-Raman spectroscopy.

[0034] There are no particular restrictions on the particle size of filler 2; it can be appropriately selected depending on the purpose, for example, 1.7 mm to 0.2 mm, 0.6 mm to 0.07 mm, etc. The particle size of filler 2 is measured by sieving (ISO 2591-1:1988).

[0035] There are no particular restrictions on the pore volume of filler 2, and it can be appropriately selected depending on the purpose, but 0.0001 cm³ is recommended. 3 / g or more 10cm 3 Preferably less than / g, and 0.01cm 3 / g or more 8cm 3More preferably, it is below / g. When the pore volume of Filler 2 is 0.0001 cm 3 / g or more and 8 cm 3 / g or less, it is preferable in that it is easy to maintain a suitable flow state even during long-term operation using easily available materials. The pore volume of Filler 2 is measured in accordance with ISO 15901-2:2006 and analyzed by the BET method.

[0036] There is no particular limitation on the specific surface area of Filler 2, and it can be appropriately selected according to the purpose. However, 0.1 m 2 / g or more and 3,000 m 2 / g or less is preferable, and 0.3 m 2 / g or more and 1,000 m 2 / g or less is more preferable. When the specific surface area of Filler 2 is 0.1 m 2 / g or more and 1,000 m 2 / g or less, it is preferable in that it is easy to maintain a suitable flow state even during long-term operation using easily available materials. The specific surface area of Filler 2 is measured in accordance with ISO 9277:2010 using a specific surface area measuring device (for example, BELSORP (registered trademark) MAX II, manufactured by MicrotracBEL Corporation) at liquid nitrogen temperature with nitrogen molecules as probes.

[0037] There is no particular limitation on the shape and structure of Filler 2, and it can be appropriately selected according to the purpose. The shape of Filler 2 may be regular or irregular. A shape in which the melt of the raw material hardly stays on Filler 2 is preferable, a spherical shape is preferable, and a true spherical shape is more preferable.

[0038] Filler 2 may be used with an additive added. There is no particular limitation on the additive added to Filler 2, and it can be appropriately selected according to the purpose. For example, SiO 2、Examples of catalysts include silica or silica-containing compounds such as SiO2-MgO, SiO2-Al2O3, SiO2-TiO2, SiO2-V2O5, SiO2-Cr2O2, and SiO2-TiO2-MgO, as well as zeolites, FCC catalysts, and alkali metal compounds. These may be used individually or in combination of two or more. The catalyst may be an unused catalyst or a catalyst that has been used in heat treatment one or more times.

[0039] If filler 2 contains additives, there are no particular restrictions on the amount of additives, and they can be appropriately selected depending on the purpose.

[0040] <<Raw material supply section 3>> The raw material supply unit 3 is a component that supplies raw materials M into the reactor 1. The raw material supply unit 3 includes a raw material distribution unit 3a for circulating the raw materials M, a raw material input unit 3b for introducing the raw materials M into the reactor 1, and so on. The raw material supply unit 3 may supply the raw materials M to the reactor 1 using a known pump or the like.

[0041] The raw material distribution section 3a is connected to the reactor 1. In this disclosure, "connection" of the raw material distribution section 3a to the reactor 1 means that the inside of the raw material distribution section 3a and the inside of the reactor 1 are in communication, allowing the raw material M to pass through.

[0042] The location of the raw material supply unit 3 is not particularly restricted as long as it can be connected to the reactor 1, and can be appropriately selected according to the type of raw material M. Figure 1 shows the extraction unit 6 positioned on the upper surface in the Y-axis direction of the reactor 1, but the extraction unit 6 may also be positioned on the lower surface in the Y-axis direction of the reactor 1, or on the side surface in the X-axis direction of the reactor 1.

[0043] Furthermore, the raw material supply unit 3 may have a raw material supply stopper, such as a stopper, that can stop the supply of raw material M. If a raw material supply stopper is provided, raw material M can be supplied to the reactor 1 intermittently. The raw material supply stopper can be located, for example, at the inlet of the raw material input unit 3b.

[0044] There are no particular restrictions on the material of the raw material supply unit 3; for example, it can be appropriately selected from the same materials as those used for the reactor 1, depending on the purpose.

[0045] The shape, structure, and size of the raw material supply unit 3 are not particularly limited as long as it can be connected to the reactor 1 and supply raw materials M to the reactor 1. They can be appropriately selected according to the purpose, for example, a cylindrical shape or a rectangular parallelepiped. Also, if a part of the reactor 1 has an opening, this opening can be used as the raw material supply unit 3.

[0046] <<Inert gas supply unit 4>> The inert gas supply unit 4 is a component that supplies inert gas G into the reactor 1. Examples of the inert gas supply unit 4 include an inert gas flow section 4a through which the inert gas G flows, and a pump 4b that flows the inert gas G in a fixed amount for a fixed period of time.

[0047] The inert gas flow section 4a is connected to the reactor 1. In this disclosure, "connection" of the inert gas flow section 4a to the reactor 1 means that the inside of the inert gas flow section 4a and the inside of the reactor 1 are in communication so that the inert gas G can pass through them.

[0048] The location of the inert gas supply unit 4 is not particularly limited as long as it can be connected to the reactor 1 and the filler 2 can be made into a fluidized bed. The location can be appropriately selected depending on the type of inert gas G. However, from the viewpoint of making the filler 2 into a fluidized bed, it is preferable to place it in a position where the inert gas G can be supplied to the filler 2 from a direction opposite to the vertical direction. For example, as shown in Figure 1, the inert gas supply unit 4 can be placed on the lower surface of the reactor 1 in the Y-axis direction. However, the location of the inert gas supply unit 4 is not limited to this. As long as it can be connected to the reactor 1 and the filler 2 can be made into a fluidized bed, the inert gas supply unit 4 may also be placed on the upper surface of the reactor 1 in the Y-axis direction, or on the side surface of the reactor 1 in the X-axis direction.

[0049] There are no particular restrictions on the material of the inert gas supply unit 4; for example, it can be appropriately selected from the same materials as those used for the reactor 1, depending on the purpose.

[0050] The shape, structure, and size of the inert gas supply unit 4 are not particularly limited as long as it can be connected to the reactor 1 and supply inert gas G to the reactor 1. They can be appropriately selected according to the purpose, for example, a cylindrical shape or a rectangular parallelepiped. Also, if a part of the reactor 1 has an opening, this opening can be used as the inert gas supply unit 4.

[0051] <<First heating section 5>> The first heating section 5 is a component that heats the reactor 1. The structure, shape, material, and size of the first heating section 5 are not particularly limited as long as they can heat the reactor 1, and can be appropriately selected according to the purpose.

[0052] There are no particular restrictions on the heating method of the first heating section 5. It may be an external heating method in which the reactor 1 is heated by heat transfer from the outside, or an internal heating method in which the reactor 1 is heated from inside. For the first heating section 5 using the external heating method, for example, a known electric furnace can be used. For the first heating section 5 using the internal heating method, for example, a method in which the filler itself is heated by a method such as resistance heating, or a resistance heating method in which a resistor such as an electric heating wire is placed inside the reactor 1 and heat is generated by applying a voltage to the resistor.

[0053] The temperature of filler 2 can be measured by inserting a thermocouple into the center of filler 2.

[0054] <<Removal section 6>> The extraction section 6 is a component that extracts the chemical product R from the reactor 1. Examples of the extraction section 6 include a chemical distribution section 6a through which the chemical product R flows, and a pump 6b that distributes the chemical product R in a fixed amount for a fixed period of time.

[0055] The extraction unit 6 is connected to the reactor 1. In this disclosure, "connection" of the extraction unit 6 to the reactor 1 means that the inside of the extraction unit 6 and the inside of the reactor 1 are in communication and can be passed through by the chemical R.

[0056] The structure, shape, material, and size of the extraction section 6 are not particularly limited as long as they can extract the chemical product R processed in the reactor 1, and can be appropriately selected according to the purpose. Examples include cylindrical shapes and rectangular parallelepipeds. Furthermore, if a part of the reactor 1 has an opening, this opening can also be used as the extraction section 6.

[0057] The location of the extraction section 6 is not particularly restricted as long as it can be connected to the reactor 1, and can be appropriately selected depending on the type of chemical R. Figure 1 shows the extraction section 6 positioned on the lower surface in the Y-axis direction of the reactor 1, but the extraction section 6 may also be positioned on the upper surface in the Y-axis direction of the reactor 1, or on the side surface in the X-axis direction of the reactor 1.

[0058] In reactor 1, chemical product R is produced from raw material M, so raw material M and chemical product R may be mixed inside reactor 1. Therefore, the extraction unit 6 may extract not only chemical product R, but also a mixture of raw material M and chemical product R. In addition, if by-products are produced in reactor 1, the extraction unit 6 may also extract the by-products.

[0059] <<First Oxygen-Containing Gas Supply Unit 7>> The first oxygen-containing gas supply unit 7 is a component that supplies oxygen-containing gas O into the reactor 1. Examples of the first oxygen-containing gas supply unit 7 include an oxygen-containing gas flow section 7a through which oxygen-containing gas O flows, and a pump 7b that flows oxygen-containing gas O in a fixed amount for a fixed period of time.

[0060] The oxygen-containing gas flow section 7a is connected to the reactor 1. In this disclosure, "connection" of the oxygen-containing gas flow section 7a to the reactor 1 means that the inside of the oxygen-containing gas flow section 7a and the inside of the reactor 1 are in communication so that oxygen-containing gas O can pass through them.

[0061] The position of the first oxygen-containing gas supply unit 7 is not particularly limited as long as it is connected to the reactor 1 and can supply oxygen-containing gas O to the reactor 1, and can be appropriately selected according to the purpose. However, it is preferable to position it in a location that can supply oxygen-containing gas O to the filler 2 from a direction opposite to the vertical direction. For example, as shown in Figure 1, the first oxygen-containing gas supply unit 7 can be positioned on the lower surface of the reactor 1 in the Y-axis direction. However, the position of the first oxygen-containing gas supply unit 7 is not limited to this, and as long as it is connected to the reactor 1 and can supply oxygen-containing gas O to the reactor 1, the first oxygen-containing gas supply unit 7 may be positioned on the upper surface of the reactor 1 in the Y-axis direction, or on the side surface of the reactor 1 in the X-axis direction.

[0062] There are no particular restrictions on the material of the first oxygen-containing gas supply unit 7; for example, it can be appropriately selected from the same materials as those used for the reactor 1, depending on the purpose.

[0063] The shape, structure, and size of the first oxygen-containing gas supply unit 7 are not particularly limited as long as it can be connected to the reactor 1 and supply oxygen-containing gas O to the reactor 1. They can be appropriately selected according to the purpose, for example, a cylindrical shape or a rectangular parallelepiped. Furthermore, if a part of the reactor 1 has an opening, this opening can also be used as the first oxygen-containing gas supply unit 7.

[0064] Furthermore, if the flow path of the inert gas G in the inert gas supply unit 4 is branched and the type of gas supplied from the inert gas supply unit 4 can be switched, then oxygen-containing gas O may be supplied from the inert gas supply unit 4. In this case, it is not necessary to provide a separate first oxygen-containing gas supply unit 7 from the inert gas supply unit 4.

[0065] <<Other components>> Other components of the chemical manufacturing apparatus 100 are not particularly limited and can be appropriately selected according to the purpose. Examples include a storage unit 8, a cooling unit 9, a gaseous product recovery unit 10, a mist trap 14, a hydrogen chloride trap 15a, and a measuring unit for measuring the yield of useful components.

[0066] -Storage section 8- The storage section 8 is a component for storing the raw material M.

[0067] The structure, shape, material, and size of the storage section 8 are not particularly limited as long as they can store the raw material M, and can be appropriately selected according to the purpose.

[0068] There are no particular restrictions on the number of storage units 8; there may be one or multiple units. If the manufacturing apparatus 100 has multiple storage units 8, for example, multiple types of raw materials M can be stored separately. For example, if the raw material M is a plastic containing polyolefin and at least one selected from the group consisting of aromatic plastics and chlorine-containing plastics, it can be used to store plastics with different compositions and content rates of each component.

[0069] -Cooling section 9- The cooling section 9 is a component that cools the chemical product R obtained by passing through the reactor 1. By cooling the chemical product R, the liquid component of the chemical product R can be recovered within the cooling section.

[0070] Examples of the cooling section 9 include a cooling trap 9a for cooling the chemical R and a cooling section 9b for cooling the cooling trap 9a. The structure, shape, material, and size of the cooling trap 9a and the cooling section 9b are not particularly limited as long as they can cool the chemical R, and can be appropriately selected according to the purpose.

[0071] The cooling trap 9a may contain an organic solvent 9c for dissolving the chemical R. The organic solvent 9c can condense the useful components in the chemical R, especially the liquid useful components. A non-aqueous solvent is preferred as the organic solvent for dissolving the chemical R. Examples of non-aqueous solvents include aromatic organic solvents such as monochlorobenzene, o-dichlorobenzene, and mesitylene. It is preferable that the outlet of the outlet 6 is placed in the organic solvent 9c so that the chemical R (e.g., the generated gas) bubbles in the organic solvent 9c.

[0072] The useful components dissolved in a non-aqueous solvent can be suitably separated by further distillation at atmospheric pressure.

[0073] The cooling section 9b is not particularly limited as long as it can cool the cooling trap 9a, and may, for example, contain a refrigerant 9d. Examples of refrigerant 9d include ice water and antifreeze.

[0074] -Gaseous product recovery unit 10- The gaseous product recovery unit 10 is a component that recovers gaseous products from the chemical product R containing useful components produced by the manufacturing apparatus 100. The gaseous product recovery unit 10 may consist of only one unit or two or more units.

[0075] There are no particular restrictions on the structure, shape, material, and size of the gaseous product recovery unit 10, and they can be appropriately selected according to the purpose and the type of chemical R, including known containers.

[0076] Furthermore, the gaseous product recovery unit 10 may contain a solvent capable of separating useful components. There are no particular restrictions on the solvent, and it can be appropriately selected depending on the type of useful component to be recovered. For example, ethanol, hexane, dimethylformamide, cyclopentane, and water can be used as solvents for extracting useful components from the chemical product R as a liquid product.

[0077] The useful components in the gaseous product can be suitably separated by further pressurized distillation.

[0078] -Mist Trap 14- The mist trap 14 is a component that recovers liquid components that could not be collected by the cooling trap 9a. The mist trap 14 is preferably placed between the cooling section 9 and the gaseous product recovery section 10. If the manufacturing apparatus 100 has a hydrogen chloride trap 15a, the mist trap 14 is preferably placed between the cooling section 9 and the hydrogen chloride trap 15a.

[0079] The structure, shape, material, and size of the mist trap 14 are not particularly limited as long as they can capture liquid components, and can be appropriately selected according to the purpose. It is preferable to use glass wool or other adsorbent inside the mist trap 14 for the purpose of capturing liquid components.

[0080] -Hydrogen chloride trap 15a- The hydrogen chloride trap 15a is a component that separates and recovers hydrogen chloride generated from chlorine-containing plastics, and is preferably installed when the raw material M contains chlorine-containing plastics such as PVC. The hydrogen chloride trap 15a is preferably placed between the cooling unit 9 and the gas product recovery unit 10. If the manufacturing apparatus 100 has a mist trap 14, the hydrogen chloride trap 15a is preferably placed between the mist trap 14 and the gas product recovery unit 10. The hydrogen chloride trap 15a is a component that separates and recovers hydrogen chloride generated from chlorine-containing plastics, and it is preferable to install it when the raw material M contains chlorine-containing plastics such as PVC.

[0081] The hydrogen chloride trap 15a contains the chemical agent 15b. The chemical agent 15b allows for the separation and recovery of hydrogen chloride encompassed in the chemical product R. Examples of chemical agent 15b include alkaline aqueous solutions such as sodium hydroxide aqueous solution, alkali metal carbonates such as potassium carbonate, and alkaline earth metal carbonates such as calcium carbonate. If there is an outlet for the flow path 16c connecting the mist trap 14 to the hydrogen chloride trap 15a, it is preferable to place the outlet within the chemical agent 15b so that the chemical product R (e.g., the generated gas) bubbles within the chemical agent 15b.

[0082] -Measurement part- The measuring unit is a component that measures the yield of useful components in chemical product R, which contains useful components manufactured by the manufacturing apparatus 100.

[0083] The measuring unit may be located inside the manufacturing apparatus 100, or it may be connected to and provided outside the manufacturing apparatus 100.

[0084] The measurement unit is not particularly limited as long as it can measure the yield of useful components in the chemical product R, and known measuring devices may be used. Examples of known measuring devices include gas chromatographs and liquid chromatographs equipped with a flame ionization detector (FID), a thermal conduction detector (TCD), or a mass spectrometer (MS), and a Fourier transform infrared spectrometer (FT-IR).

[0085] There are no particular restrictions on the structure, shape, material, and size of the measuring section; they can be appropriately selected according to the purpose and type of product.

[0086] <Operation method of a chemical manufacturing apparatus according to the first embodiment> Next, a method for operating a chemical manufacturing apparatus according to the first embodiment of this disclosure will be described. Figure 2 is a flowchart showing an example of a method for operating a chemical manufacturing apparatus according to the first embodiment of this disclosure.

[0087] The method of operating the chemical manufacturing apparatus according to the first embodiment of this disclosure includes: (Sa1) supplying inert gas G into the reactor 1 by an inert gas supply unit 4 (hereinafter sometimes abbreviated as "(Sa1) supplying inert gas" or simply "Sa1"); (Sa2) supplying raw material M by a raw material supply unit 3 while heating the reactor 1 by a first heating unit 5 (hereinafter sometimes abbreviated as "(Sa2) supplying raw material" or simply "Sa2"); (Sa3) removing the chemical product R generated from the raw material M from the reactor 1 by an extraction unit 6 (hereinafter sometimes abbreviated as "(Sa3) removing the chemical product" or simply "Sa3"); and (Sa4) after (Sa3), heating the filler 2 to 400°C to 720°C by the first heating unit 5 while supplying oxygen-containing gas O from a first oxygen-containing gas supply unit 7 (hereinafter sometimes abbreviated as "(Sa4) heating the filler" or simply "Sa4"). In the operation method of the chemical manufacturing apparatus according to the first embodiment, in (Sa1) or (Sb1), inert gas G is supplied to the inside of the reactor 1 from the inert gas supply unit 4 to cause the filler 2 to flow. The operation method of the chemical manufacturing apparatus according to the first embodiment is preferably carried out by the chemical manufacturing apparatus 100 according to the first embodiment.

[0088] <<(Sa1) Supply an inert gas>> (Sa1) By supplying an inert gas, an inert gas G is supplied into the reactor 1 by the inert gas supply unit 4. This converts the reactor 1, which has filler 2, into a fluidized bed.

[0089] The fluidized bed is placed inside the reactor. The fluidized bed is a reaction vessel that suspends the filler 2 by passing an inert gas G through it at a sufficient speed, causing the filler 2 to behave like a fluid.

[0090] -Inert Gas G- There are no particular restrictions on the inert gas G, but (Sa2) when supplying the raw material, a gas that is stable in the heating temperature range in which the raw material M is heated is preferred.

[0091] Specific examples of inert gas G include nitrogen gas, water vapor, carbon dioxide, and noble gases. These may be used individually or in combination of two or more. Among these, nitrogen gas and water vapor are preferred as inert gas G because they are inexpensive, and nitrogen gas is more preferred.

[0092] There are no particular restrictions on the volumetric flow rate of the inert gas G supplied to the reactor 1, and it can be appropriately selected according to the purpose, but the cross-sectional area of ​​the reactor 1 is 1 cm². 2 At 0°C and 1 atmosphere, the result is 5 cm. 3 / second or more 1,000cm 3 Preferably less than / second, and 10cm 3 / second or more 500cm 3 Less than / second is more preferable. The flow rate of inert gas G is less than the cross-sectional area of ​​the reaction tube 1 cm². 2 That's 5cm when calculated at 0°C and 1 atmosphere. 3 / second or more 1,000cm 3 If the contact time is less than / second, sufficient contact time between the raw material M and the filler 2 can be ensured, and side reactions can be suppressed, so that the chemical product R, preferably the useful component, can be obtained efficiently in high yield.

[0093] Volumetric flow rate of inert gas G Gv(cm 3 The value per second ( / second) can be calculated using the following formula 1. [Formula 1] Gv=Y / A However, in Equation 1, Y is the flow velocity of the inert gas G (cm²). 3 The value is (cm² / second), where A is the lower end of the part of the reactor 1 that houses the filler, and the cross-sectional area (cm²) of the inside of the reactor 1 in a cross-section perpendicular to the longitudinal direction of the reactor (the direction in which raw material M is supplied). 2 ) indicates.

[0094] <<(Sa2) Supplying raw materials>> (Sa2) In supplying raw materials, the reactor 1 is heated by the first heating unit 5, while the raw material supply unit 3 supplies the raw material M. As a result, the raw material M is thermally decomposed to produce the chemical product R.

[0095] (Sa2) The supply of raw materials is carried out simultaneously with the supply of (Sa1) the inert gas. However, the timing of starting to supply the (Sa1) inert gas may be to start at the same time as supplying the (Sa2) raw materials, or to start before supplying the (Sa2) raw materials, but it is more preferable to start supplying the (Sa1) inert gas before supplying the (Sa2) raw materials, and then start supplying the (Sa2) raw materials after the inside of the reactor 1 has been filled with the inert gas.

[0096] (Sa2) In supplying raw materials, there are no particular restrictions on the method of supplying raw materials M to the reactor 1; they may be supplied intermittently or continuously. Among these, supplying raw materials M intermittently is preferable because it can minimize temperature changes in the reactor 1, preferably the fluidized bed.

[0097] When raw material M is supplied intermittently to reactor 1, there are no particular restrictions on the supply time, non-supply time, or intervals between these.

[0098] When raw material M is supplied to reactor 1 intermittently, there are no particular restrictions on the amount of raw material M supplied each time. When raw material M is supplied to reactor 1 intermittently, from the viewpoint of preventing the temperature of reactor 1 from dropping too low, it is preferable to add raw material M for the second and subsequent times only after the temperature of reactor 1, which dropped after the previous addition, has recovered to the desired temperature.

[0099] When raw material M is continuously supplied to reactor 1, there are no particular restrictions on the amount of raw material M supplied.

[0100] (Sa2) In supplying raw materials, there are no particular restrictions on the method of heating the reactor 1, and it can be appropriately selected according to the purpose. It may be an external heating method in which the reactor 1 is heated by heat transfer from the outside, or an internal heating method in which the reactor 1 is heated from the inside. Among these, the external heating method is preferred as the method of heating the reactor 1.

[0101] There are no particular restrictions on the heating temperature for heating reactor 1, and it can be appropriately selected depending on the type of raw material M.

[0102] -Raw material M- The raw materials M applicable to the operating method of the chemical manufacturing apparatus of this disclosure are not particularly limited, as long as they are materials to be subjected to a thermal decomposition reaction. An example of raw materials M is a raw material containing one or more selected from the group consisting of naphtha, hydrocarbons, plastics, and biomass. Among these, raw materials M containing plastics can be suitably used. Plastics will be described in detail in the (Method of Manufacturing Chemicals) section of this disclosure, but plastics of the same nature can also be used in the operating method of the chemical manufacturing apparatus of this disclosure.

[0103] When the raw material M is a raw material that includes one or more selected from the group consisting of naphtha, hydrocarbons, plastics, and biomass, the heating temperature for heating the reactor 1 is preferably 400°C or higher, and when carried out without a catalyst, from the viewpoint of yielding chemical product R, preferably useful components in chemical product R, a temperature of 650°C to 1,000°C is preferred, and 700°C to 980°C is more preferred.

[0104] <<(Sa3) Extracting chemicals>> (Sa3) In extracting the chemical product, the chemical product R generated from the raw material M is extracted from the inside of the reactor 1 by the extraction unit 6.

[0105] -Chemicals R- (Sa3) The chemical product extracted by the extraction of the chemical product is not particularly limited as long as it is a chemical product R obtained by decomposing the raw material M, and can be appropriately selected according to the purpose.

[0106] If the raw material M is a raw material that includes one or more selected from the group consisting of naphtha, hydrocarbons, plastics, and biomass, then it is preferable that the chemical product R includes at least one selected from the group consisting of olefins having 2 to 5 carbon atoms and aromatic hydrocarbons. The at least one selected from the group consisting of olefins having 2 to 5 carbon atoms and aromatic hydrocarbons will be described in detail in the (Method of Manufacturing Chemical Products) section of this disclosure, but components of the same nature can also be obtained by the operating method of the chemical product manufacturing apparatus of this disclosure.

[0107] In addition to the target product, chemical product R may contain by-products generated by the thermal decomposition of raw material M. In such cases, the target product and by-products are included in the chemical product R.

[0108] <<(Sa4) Heat the filler>> (Sa4) Heating the filler involves heating the filler 2 to 400°C to 720°C by the first heating unit 5 while supplying oxygen-containing gas O from the first oxygen-containing gas supply unit 7 after (Sa3) extracting the chemicals. As a result, when the filler 2 is used in the thermal decomposition of raw material M once or more, for reasons that are not clear, the decomposition efficiency of raw material M decreases and the yield of chemical product R deteriorates. In contrast, by heating the filler (Sa4), even if the filler 2 is used in the thermal decomposition of raw material M once or more, it is possible to achieve thermal decomposition efficiency equivalent to or better than when the filler 2 has not been used in the thermal decomposition of raw material M (i.e., when the filler 2 is unused or new).

[0109] In this disclosure, when filler 2 is said to have a thermal decomposition efficiency equivalent to or better than that of filler 2 that has never been used in the thermal decomposition of raw material M, it means that the ratio P of the yield when the comparative filler 2 is used in the thermal decomposition of raw material M is 90% or more, preferably 96% or more, more preferably 97% or more, even more preferably 98% or more, and particularly preferably 99% or more. Note that when filler 2 has a thermal decomposition efficiency equivalent to that of unused filler, it means that the ratio P is 100%. Furthermore, when filler 2 has a thermal decomposition efficiency greater than or equal to that of filler 2 that has never been used in the thermal decomposition of raw material M, it means that the ratio P exceeds 100%.

[0110] (Sa4) In heating the filler, there are no particular restrictions on the method of heating the filler 2, and it can be appropriately selected according to the purpose. It may be an external heating method in which the filler 2 is heated by heat transfer from the outside, or an internal heating method in which it is heated from inside the reactor 1. Among these, the external heating method is preferred as the method of heating the filler 2. Furthermore, in heating the filler, (Sa4) it is preferable to use the same method as the method used to heat the reactor 1 in supplying the raw materials (Sa2), as this does not require changing the configuration of the manufacturing apparatus 100 and is therefore efficient.

[0111] The heating temperature for heating filler 2 is 400°C to 720°C, but 450°C to 700°C is preferred, 480°C to 680°C is more preferred, 500°C to 650°C is even more preferred, and 550°C to 620°C is particularly preferred. If the heating temperature for heating filler 2 is less than 400°C or more than 720°C, the thermal decomposition efficiency of raw material M will decrease, and the rate of increase in the yield of chemical product R will decrease.

[0112] (Sa4) When heating the filler, the heated filler 2 can achieve a thermal decomposition efficiency equivalent to or better than that of unused filler, as described above, and can be reused in the production of chemical product R by thermal decomposing the raw material M. Therefore, the operating method of the chemical product production apparatus according to the first embodiment of this disclosure can repeat (Sa1), (Sa2), and (Sa3) after (Sa4). And while repeating this series of processes, the filler 2 can achieve a thermal decomposition efficiency equivalent to or better than that of filler 2 that has not been used even once in the thermal decomposition of raw material M, so it can operate stably for a long time and the raw material can be thermally decomposed efficiently.

[0113] -Oxygen-containing gas O- There are no particular restrictions on the oxygen content in the oxygen-containing gas O; it can be appropriately selected depending on the purpose, and may even be a gas consisting solely of oxygen.

[0114] If the oxygen-containing gas O contains gases other than oxygen, examples of these gases include nitrogen gas, water vapor, and carbon dioxide gas, with nitrogen gas being preferred. These gases may be present individually or in combination of two or more.

[0115] There are no particular restrictions on the content of gases other than oxygen in oxygen-containing gas O, and can be appropriately selected depending on the purpose, but it is preferably 95% or less, and more preferably 85% or less. Air is an example of an oxygen-containing gas that also contains substances other than oxygen.

[0116] <Other processing> The method of operating the chemical manufacturing apparatus according to the first embodiment of this disclosure may further include, if necessary, other processes other than those described in (Sa1) to (Sa4).

[0117] Other processing methods are not particularly limited and can be selected as appropriate depending on the purpose. Examples include (Sa2) pre-treating the raw material M, (Sa3) recovering the chemical product R generated by supplying the raw material, (Sa3) post-treating the extracted chemical product after extraction, and (Sa3) separating useful components from the extracted chemical product R.

[0118] If the operating method of the chemical manufacturing apparatus of this disclosure involves repeatedly (Sa4) heating the filler, then (Sa1) supplying an inert gas, (Sa2) supplying raw materials, and (Sa3) removing the chemical, other processes may be repeated in the same manner. There are no particular restrictions on the frequency of repeating the other processes.

[0119] <<Pre-treatment required>> Pretreatment involves pre-treating the raw material M before supplying it. By pre-treating the raw material M to make it easier to decompose, the thermal decomposition of the raw material M can be performed more efficiently.

[0120] There are no particular restrictions on pretreatment, and it can be appropriately selected depending on the type of raw material M. For example, if the raw material M contains plastic, pretreatment may include crushing the raw material M, pelletizing (chipping) the crushed raw material M, or melting the raw material M.

[0121] If the raw material M contains plastic, it is preferable to melt the raw material M at a temperature of less than 300°C.

[0122] There are no particular restrictions on the pulverized form of raw material M, and it can be appropriately selected according to the purpose, for example, in powder or flake form.

[0123] There are no particular restrictions on the method for obtaining the pulverized raw material M, and any conventionally known method can be appropriately selected. For example, a method of pulverizing the raw material M with a pulverizer to obtain powder or flakes can be used.

[0124] Furthermore, there are no particular restrictions on the method of pelletizing (chipping) the pulverized material, and any conventionally known method can be appropriately selected. For example, one method is to melt-extrude the pulverized material and then cut the strand-shaped melt-extruded material to obtain chipped raw material.

[0125] The raw material M can also be supplied in a molten state. There are no particular restrictions on the method of melting the raw material M, and any conventionally known method can be appropriately selected. For example, a method of continuously supplying it to the reactor 1 using a molten extruder can be used.

[0126] <<To be collected>> Recovery involves recovering the chemical product R generated by supplying (Sa2) raw materials. There are no particular restrictions on the method of recovering the chemical product R, and a method can be appropriately selected from known methods depending on the type and physical properties of the obtained chemical product R. For example, gaseous chemical product R can be separated by atmospheric pressure or pressurized distillation, and liquid chemical product R can be separated by atmospheric pressure or reduced pressure distillation.

[0127] <<Post-processing of chemicals>> Post-treatment of chemicals involves (Sa2) the decomposition of by-products in the chemical R generated by supplying raw materials. It is preferable to perform post-treatment of chemicals after recovery.

[0128] Post-treatment methods for chemicals include, for example, the removal of halogen compounds. Methods for removing halogen compounds include a fixed bed filled with an oxide or hydroxide of one metal selected from alkali metals and alkaline earth metals, or a method of passing an aqueous solution of the oxide or hydroxide of the said metal through the bed.

[0129] <<Separation>> Separation involves separating only the useful components from the recovered liquid and gaseous chemicals R, and removing unwanted components. Alternatively, the separation process may involve separating multiple useful components within the chemical R individually.

[0130] For example, if the raw material M is a raw material containing plastic, and at least one selected from the group consisting of olefins having 2 to 5 carbon atoms and aromatic hydrocarbons is used as a useful component, paraffins having 2 to 5 carbon atoms may be included as by-products. In this case, separation may involve separating the useful component from the by-products, or separating the olefins having 2 to 5 carbon atoms and aromatic hydrocarbons according to their respective compounds.

[0131] In terms of separation, there are no particular restrictions on the method for separating the useful components from the minor components, and on the method for separating olefins having 2 to 5 carbon atoms and aromatic hydrocarbons, each compound separately. A method can be appropriately selected from known methods depending on the composition of the chemical product R, the type of useful component obtained, or the type of minor component.

[0132] Next, a specific example of the operation method of the chemical manufacturing apparatus according to the first embodiment of this disclosure will be described. The manufacturing apparatus 100 performs (Sa1) supply of inert gas by supplying inert gas G from the inert gas supply unit 4 to the filler 2 inside the reactor 1. Then, while heating the fluidized bed with the first heating unit 5 to a desired temperature according to the type of raw material M, the raw material supply unit 3 supplies the raw material M, thereby performing (Sa2) supply of raw material. As a result, the raw material M is heated in the reactor 1 in the presence of the fluidized bed, thermally decomposed, and produces chemical product R. Next, the chemical product R produced from the raw material M is removed from inside the reactor 1 with the removal unit 6, thereby performing (Sa3) extraction of the chemical product. The chemical product R, which is a product containing useful components obtained by heating, can be recovered and separated in the cooling unit 9 and the gaseous product recovery unit 10.

[0133] The timing and speed of supplying raw material M by the raw material supply unit 3, the timing and speed of supplying inert gas G by the inert gas supply unit 4, the timing of heating raw material M and filler 2 by the first heating unit 5, the heating temperature, and the heating time are all determined by the signal processing unit processing signals to each unit. The signal processing unit is an electronic circuit such as a CPU, FPGA, or ASIC, and performs the various processes described in the operating method of the chemical manufacturing apparatus of this disclosure by executing instruction codes stored in memory or by designing the circuit for special applications.

[0134] [Operation method of the chemical manufacturing apparatus according to the second embodiment] <Chemical manufacturing apparatus according to the second embodiment> Next, a second embodiment of the chemical manufacturing apparatus used in the operating method of the chemical manufacturing apparatus of this disclosure will be described with reference to Figure 3. Figure 3 is a schematic cross-sectional view showing an example of the chemical manufacturing apparatus according to the second embodiment of this disclosure.

[0135] The chemical manufacturing apparatus 200 (hereinafter sometimes abbreviated as "manufacturing apparatus 200"), in the manufacturing apparatus 100 according to the first embodiment, further comprises a regenerating furnace 20 provided separately from the reactor, a spent filler transfer unit 21 for transferring filler 2 from the reactor 1 to the inside of the regenerating furnace 20, a second oxygen-containing gas supply unit 22 for supplying oxygen-containing gas O to the inside of the regenerating furnace 20, a second heating unit 23 for heating the regenerating furnace 20, and a regenerated filler transfer unit 24 for transferring filler 2 from the regenerating furnace 20 to the inside of the reactor 1.

[0136] According to the chemical manufacturing apparatus of the second embodiment, in addition to heating the filler 2 by the first heating unit 5 inside the reactor 1, the filler 2 is further heated by the second heating unit 23 inside the regeneration furnace 20, thereby enabling more efficient regeneration of the filler 2.

[0137] <<Regeneration furnace 20>> The regeneration furnace 20 is provided separately from the reactor 1. The regeneration furnace 20 is a component for regenerating the filler 2 used in the decomposition of the raw material M.

[0138] The regeneration furnace 20 is a component that can accommodate the filler 2 and has a certain internal space to ensure a flow path for oxygen-containing gas O, and is preferably a fluidized bed. In the regeneration furnace 20, the filler 2 placed inside the regeneration furnace 20 is heated by the second heating unit 23 to regenerate the filler 2.

[0139] There are no particular restrictions on the material of the regeneration furnace 20; for example, it can be appropriately selected from the same materials as those used for the reactor 1, depending on the purpose.

[0140] The shape, structure, and size of the regenerating furnace 20 are not particularly limited as long as they can accommodate the filler 2 and are chemically and mechanically stable under reaction conditions. They can be appropriately selected according to the purpose. Examples include cylindrical, rectangular parallelepiped, conical, frustoconical, and columnar shapes with a polygonal cross-sectional shape perpendicular to the longitudinal direction of the reactor 1.

[0141] <<Used filler transfer section 21>> The spent filler transfer section 21 is a component that transfers the filler 2 from the reactor 1 to the inside of the regeneration furnace 20. Preferably, the spent filler transfer section 21 has a first filler transfer section 21a provided around the reactor 1 and a second filler transfer section 21b connecting the first filler transfer section 21a and the regeneration furnace 20.

[0142] The spent filler transfer section 21 connects the reactor 1 and the regeneration reactor 20. In this disclosure, "connecting" the spent filler transfer section 21 to the reactor 1 and the regeneration reactor 20 means that the inside of the spent filler transfer section 21 and the inside of the reactor 1 and the regeneration reactor 20 are in communication so that the filler 2 can pass through. It is preferable that the reactor 1 and the first filler transfer section 21a are connected, and it is more preferable that the regeneration reactor 20 and the second filler transfer section 21b are connected. In this case, the first filler transfer section 21a and the second filler transfer section 21b are connected so that the filler 2 can pass through them.

[0143] The location of the used filler transfer section 21 is not particularly restricted, as long as it can connect the reactor 1 and the regeneration reactor 20, and can be selected as appropriate.

[0144] Figure 3 illustrates one configuration in which the inert gas G is supplied from a direction opposite to the vertical direction. In this case, the filler 2 rises together with the inert gas G within the reactor 1, floats up to the top of the reactor 1, and can be taken out from the top of the reactor 1 to the first filler transfer section 21a. The first filler transfer section 21a is configured so that the inert gas G does not flow into it, so the filler 2 is transported vertically downward by its own weight to the first filler transfer section 21a. Next, the second filler transfer section 21b is provided vertically below the first filler transfer section 21a, and the regeneration furnace 20 is provided vertically below the second filler transfer section 21b, so that the filler 2 is transported vertically downward by its own weight to the second filler transfer section 21b and supplied to the regeneration furnace 20 connected to the second filler transfer section 21b.

[0145] Furthermore, in the first filler transfer section 21a and the second filler transfer section 21b, a separate inert gas supply section is provided, different from the inert gas supply section 4 connected to the reactor 1. By flowing this inert gas towards the first filler transfer section 21a, the second filler transfer section 21b, and the regeneration furnace 20, the filler 2 can be transported from the reactor 1 to the regeneration furnace 20. In this configuration, the filler 2 can be transported from the reactor 1 to the regeneration furnace 20 more quickly.

[0146] <<Second oxygen-containing gas supply unit 22>> The second oxygen-containing gas supply unit 22 is a component that supplies oxygen-containing gas O to the inside of the regeneration furnace 20. The second oxygen-containing gas supply unit 22 may include an oxygen-containing gas flow section 22a through which oxygen-containing gas O flows, and a pump 22b that flows oxygen-containing gas O in a fixed amount for a fixed period of time.

[0147] The oxygen-containing gas flow section 22a is connected to the regeneration furnace 20. In this disclosure, "connection" of the oxygen-containing gas flow section 22a to the regeneration furnace 20 means that the inside of the oxygen-containing gas flow section 22a and the inside of the regeneration furnace 20 are in communication so that oxygen-containing gas O can pass through them.

[0148] The location of the second oxygen-containing gas supply unit 22 is not particularly limited as long as it is connected to the regeneration furnace 20 and can supply oxygen-containing gas O to the regeneration furnace 20, and can be appropriately selected according to the purpose. However, it is preferable to place it in a position where oxygen-containing gas O can be supplied to the filler 2 from a direction opposite to the vertical direction.

[0149] For example, as shown in Figure 3, when the second filler transfer unit 21b is connected to the lower part of the regeneration furnace 20 in the Y-axis direction, by arranging the second oxygen-containing gas supply unit 22 on the lower surface of the regeneration furnace 20 in the Y-axis direction, the filler 2 supplied into the regeneration furnace 20 from the second filler transfer unit 21b rises together with the oxygen-containing gas OG, floats up to the top of the regeneration furnace 20, and can be taken out from the top of the regeneration furnace 20 by the regeneration filler transfer unit 24.

[0150] However, the location of the second oxygen-containing gas supply unit 22 is not limited to this. As long as it is connected to the regenerating furnace 20 and can supply oxygen-containing gas O to the regenerating furnace 20, the second oxygen-containing gas supply unit 22 may be located on the upper surface of the regenerating furnace 20 in the Y-axis direction, or on the side surface of the regenerating furnace 20 in the X-axis direction. For example, if the second filler transfer unit 21b is connected to the upper part of the regenerating furnace 20 in the Y-axis direction, by locating the second oxygen-containing gas supply unit 22 on the upper surface of the regenerating furnace 20 in the Y-axis direction, the filler 2 supplied into the regenerating furnace 20 from the second filler transfer unit 21b can descend together with the oxygen-containing gas O and be taken out from the bottom of the regenerating furnace 20 by the regenerating filler transfer unit 24.

[0151] There are no particular restrictions on the material of the second oxygen-containing gas supply unit 22; for example, it can be appropriately selected from the same materials as those used for the reactor 1, depending on the purpose.

[0152] The shape, structure, and size of the second oxygen-containing gas supply unit 22 are not particularly limited as long as it can be connected to the regeneration furnace 20 and supply oxygen-containing gas O to the regeneration furnace 20. They can be appropriately selected according to the purpose, for example, a cylindrical shape or a rectangular parallelepiped. Furthermore, if a part of the regeneration furnace 20 has an opening, this opening can also be used as the second oxygen-containing gas supply unit 22.

[0153] The oxygen-containing gas O supplied by the second oxygen-containing gas supply unit 22 can be the same as the oxygen-containing gas O supplied by the first oxygen-containing gas supply unit 7.

[0154] <<Second heating section 23>> The second heating section 23 is a component that heats the regeneration furnace 20. Specifically, the second heating section 23 is The regeneration furnace 20 is heated to a temperature of 400°C to 720°C. This allows the filler 2 to be regenerated more efficiently inside the regeneration furnace 20.

[0155] The structure, shape, material, and size of the second heating section 23 are not particularly limited as long as they can heat the regeneration furnace 20, and can be appropriately selected according to the purpose.

[0156] There are no particular restrictions on the heating method of the second heating section 23. It may be an external heating method in which the regeneration furnace 20 is heated by heat transfer from the outside, or an internal heating method in which the regeneration furnace 20 is heated from inside. For the second heating section 23 using the external heating method, for example, a known electric furnace can be used. For the second heating section 23 using the internal heating method, for example, a resistance heating method can be used in which a low-resistance resistor such as a heat transfer wire is placed inside the regeneration furnace 20 and heat is generated by applying a voltage to the resistor.

[0157] <<Recycled filler transfer unit 24>> The regenerated filler transfer unit 24 is a component that transfers the filler 2 from the regenerated furnace 20 to the inside of the reactor 1.

[0158] The regenerated filler transfer unit 24 connects the regenerated furnace 20 and the reactor 1. In this disclosure, "connecting" the regenerated filler transfer unit 24 to the regenerated furnace 20 and the reactor 1 means that the inside of the regenerated filler transfer unit 24 and the inside of the regenerated furnace 20 and the reactor 1 are in communication so that the filler 2 can pass through them.

[0159] The location of the regenerated filler transfer section 24 is not particularly restricted, as long as it can connect the regenerated furnace 20 and the reactor 1, and can be selected as appropriate.

[0160] Figure 3 illustrates one embodiment in which the regenerated filler transfer unit 24 is positioned to connect the side of the regenerated furnace 20 in the Y-axis direction with the lower side of the reactor 1 in the Y-axis direction. In this case, the filler 2 is removed from the regenerated furnace 20 by oxygen-containing gas O to the regenerated filler transfer unit 24, then moves within the regenerated filler transfer unit 24 by its own weight and is supplied to the reactor 1. It is preferable that the connection between the regenerated filler transfer unit 24 and the reactor 1 be positioned downstream in the flow direction of the inert gas G supplied from the inert gas supply unit 4. As a result, the filler 2 supplied from the regenerated filler transfer unit 24 to the reactor 1 rises together with the inert gas G, floats up to the top of the reactor 1, and is suitably reused within the reactor 1.

[0161] However, the position of the regenerated filler transfer unit 24 is not limited to this, and as long as the filler 2 can be transferred from the regenerated furnace 20 to the reactor 1, the regenerated filler transfer unit 24 may be positioned on the upper or lower surface in the Y-axis direction of the regenerated furnace 20, or on the upper surface in the Y-axis direction of the reactor 1. For example, if the second filler transfer unit 21b is connected to the upper part of the regenerated furnace 20 in the Y-axis direction, it is preferable to position the regenerated filler transfer unit 24 on the lower surface in the Y-axis direction of the regenerated furnace 20.

[0162] <<Other components>> Other components in the chemical manufacturing apparatus 200 are not particularly limited and can be appropriately selected according to the purpose, for example, an exhaust unit 25 and a gas switching unit 26.

[0163] -Exhaust section 25- The exhaust section 25 is connected to the regeneration furnace 20 and is a component that exhausts the oxygen-containing gas O used in the regeneration furnace 20.

[0164] The exhaust section 25 is connected to the regenerating furnace 20. In this disclosure, "connected" to the regenerating furnace 20 means that the inside of the exhaust section 25 and the inside of the regenerating furnace 20 are in communication so that the oxygen-containing gas O used in the regenerating furnace 20 can pass through them.

[0165] The location of the exhaust unit 25 is not particularly limited as long as it is connected to the regenerating furnace 20 and can exhaust the oxygen-containing gas O used in the regenerating furnace 20 to the outside of the regenerating furnace 20. It can be appropriately selected according to the purpose, however, it is preferable to place it in the regenerating furnace 20 at a position opposite the second oxygen-containing gas supply unit 22.

[0166] There are no particular restrictions on the material of the exhaust section 25; for example, it can be appropriately selected from the same materials as those used for the reactor 1, depending on the purpose.

[0167] The shape, structure, and size of the exhaust section 25 are not particularly limited as long as it is connected to the regeneration furnace 20 and can exhaust the gas generated when the oxygen-containing gas O and (Sa4) filler used in the regeneration furnace 20 are heated to the outside of the regeneration furnace 20. They can be appropriately selected according to the purpose, for example, a cylindrical shape or a rectangular parallelepiped. Also, if a part of the regeneration furnace 20 has an opening, this opening can be used as the exhaust section 25.

[0168] -Gas switching section 26- The gas switching unit 26 is located at the branching point between the inert gas supply unit 4 and the first oxygen-containing gas supply unit 7, and is a component that switches the gas supplied into the reactor 1 so that it is either the inert gas G or the oxygen-containing gas O.

[0169] <Operation method of the chemical manufacturing apparatus according to the second embodiment> Next, a method for operating a chemical manufacturing apparatus according to the second embodiment of this disclosure will be described. Figure 4 is a flowchart showing an example of a method for operating a chemical manufacturing apparatus according to the second embodiment of this disclosure.

[0170] The method of operating the chemical manufacturing apparatus according to the second embodiment of this disclosure includes (Sa1) to (Sa4) in the method of operating the chemical manufacturing apparatus according to the first embodiment, and further includes (Sa5) transferring the filler from the reactor to the inside of the regenerating furnace through the used filler transfer unit simultaneously with (Sa4) or after (Sa4) (hereinafter, this may be abbreviated as "(Sa5) transferring the filler from the reactor to the inside of the regenerating furnace" or simply "Sa5"), and (Sa6) the second oxygen-containing The operation method of the chemical manufacturing apparatus according to the second embodiment is preferably carried out by the chemical manufacturing apparatus 200 according to the second embodiment.

[0171] <<(Sa5) Transferring filler from the reactor to the inside of the regenerating reactor>> (Sa5) Transferring the filler from the reactor to the inside of the regenerating reactor, simultaneously with (Sa4) or after (Sa4), the filler 2 is transferred from the reactor 1 to the inside of the regenerating reactor 20 through the used filler transfer unit 21.

[0172] (Sa5) When transferring the filler from the reactor to the inside of the regenerator, if it is done simultaneously with (Sa4), it may be done intermittently while (Sa4) is being performed, or it may be done continuously. Among these, (Sa5) transferring the filler from the reactor to the inside of the regenerator is preferable because it can minimize temperature changes in reactor 1 and regenerator 20.

[0173] When used filler is intermittently transferred from reactor 1 to the inside of regenerator 20, there are no particular restrictions on the timing of the transfer of used filler or the time interval between transfers.

[0174] When used filler is intermittently transferred from reactor 1 to the inside of regenerator 20, there are no particular restrictions on the amount of used filler transferred per transfer.

[0175] <<(Sa6) Heat the filler using the second heating element>> (Sa6) When heating the filler with the second heating unit, the filler 2 is heated to 400°C to 720°C by the second heating unit 23 while oxygen-containing gas O is supplied from the second oxygen-containing gas supply unit 22.

[0176] (Sa6) In heating the filler with the second heating section, there are no particular restrictions on the method of heating the filler 2, and it can be appropriately selected according to the purpose. It may be an external heating method in which the regeneration furnace 20 is heated by heat transfer from the outside, or an internal heating method in which the regeneration furnace 20 is heated from the inside.

[0177] The heating temperature for heating filler 2 is not particularly limited as long as it is within the range of 400°C to 720°C, and can be appropriately selected depending on the type of raw material M.

[0178] <<(Sa7) Transferring filler from the regenerator to the inside of the reactor>> (Sa7) In transferring the filler from the regenerating furnace to the inside of the reactor, the filler 2 is transferred from the regenerating furnace 20 to the inside of the reactor 1 via the regenerating filler transfer unit 24.

[0179] (Sa7) The transfer of filler from the regenerator to the inside of the reactor may be performed simultaneously with each process or separately. Among these, (Sa7) the transfer of filler from the regenerator to the inside of the reactor is preferable to perform simultaneously with (Sa5) the transfer of filler from the reactor to the inside of the regenerator, as this allows a certain amount of filler 2 to be used within the reactor 1.

[0180] Furthermore, the transfer of filler from the regenerator to the inside of the reactor (Sa7) may be performed intermittently or continuously during the execution of each process. Among these, the intermittent supply of filler from the regenerator to the inside of the reactor (Sa7) is preferable because it can minimize temperature changes in reactor 1 and regenerator 20.

[0181] When the regenerated filler is intermittently transferred from the regeneration reactor 20 to the reactor 1, there are no particular restrictions on the timing of the transfer of the regenerated filler or the time interval between transfers.

[0182] When the recycled filler is intermittently transferred from the regeneration reactor 20 to the reactor 1, there are no particular restrictions on the amount of recycled filler transferred per transfer.

[0183] [Operation method of the chemical manufacturing apparatus according to the third embodiment] <Chemical manufacturing apparatus according to the third embodiment> Next, a third embodiment of the chemical manufacturing apparatus used in the operating method of the chemical manufacturing apparatus of this disclosure will be described with reference to Figure 5. Figure 5 is a schematic cross-sectional view showing an example of the chemical manufacturing apparatus according to the third embodiment of this disclosure.

[0184] The chemical manufacturing apparatus 300 (hereinafter sometimes abbreviated as "manufacturing apparatus 300") comprises a reactor, filler 2 filled inside the reactor 1, a raw material supply unit 3 for supplying raw material M to the inside of the reactor 1, an inert gas supply unit 4 for supplying inert gas G to the inside of the reactor 1, a first heating unit 5 for heating the reactor 1, an extraction unit 6 for extracting chemical product R from the reactor 1, a regeneration furnace 20 provided separately from the reactor 1, a used filler transfer unit 21 for transferring filler 2 from the reactor 1 to the inside of the regeneration furnace 20, a second oxygen-containing gas supply unit 22 for supplying oxygen-containing gas O to the inside of the regeneration furnace 20, a second heating unit 23 for heating the regeneration furnace 20, and a regenerated filler transfer unit 24 for transferring filler from the regeneration furnace 20 to the inside of the reactor 1.

[0185] The chemical manufacturing apparatus 300 according to the third embodiment differs from the chemical manufacturing apparatus 200 according to the second embodiment in that it does not have a first oxygen-containing gas supply unit 7 that supplies oxygen-containing gas O into the reactor 1. Therefore, similar to the chemical manufacturing apparatus 200 according to the second embodiment, the chemical manufacturing apparatus 300 according to the third embodiment suspends the filler 2 by passing an inert gas G through the filler 2 at a sufficient speed, causing the filler 2 to behave like a fluid, and the reactor 1 of the manufacturing apparatus 300 functions as a fluidized bed.

[0186] In the chemical manufacturing apparatus 200 according to the second embodiment, (Sa4) is performed inside the reactor 1, so when (Sa4) is performed, (Sa1) to (Sa3) must be stopped. In contrast, the chemical manufacturing apparatus 300 according to the third embodiment is preferable because, since the filler 2 is regenerated by heating the filler 2 to 400°C to 720°C only inside the regeneration furnace 20, the chemical product R can be manufactured continuously without stopping the heating of the raw material M inside the reactor 1.

[0187] <Operation method of a chemical manufacturing apparatus according to the third embodiment> Next, a method for operating a chemical manufacturing apparatus according to the third embodiment of this disclosure will be described. Figure 6 is a flowchart showing an example of a method for operating a chemical manufacturing apparatus according to the third embodiment of this disclosure.

[0188] The method of operating the chemical manufacturing apparatus according to the third embodiment of this disclosure is as follows: (Sb1) supplying inert gas G into the reactor 1 by the inert gas supply unit 4 (hereinafter sometimes abbreviated as "(Sb1) supplying inert gas" or simply "Sb1"), (Sb2) supplying raw material M by the raw material supply unit 3 while heating the reactor 1 by the first heating unit 5 (hereinafter sometimes abbreviated as "(Sb2) supplying raw material" or simply "Sb2"), (Sb3) removing the chemical product R generated from the raw material M from the inside of the reactor 1 by the removal unit 6 (hereinafter sometimes abbreviated as "(Sb3) removing the chemical product" or simply "Sb3"), and (Sb4) transferring used filler simultaneously with (Sb2) or after (Sb2). The operation method of the chemical manufacturing apparatus according to the third embodiment may further include, if necessary, other processes other than those described above (Sb1) to (Sb6). The operation method of the chemical manufacturing apparatus according to the third embodiment is preferably carried out by the chemical manufacturing apparatus 300 according to the third embodiment.

[0189] The above (Sb1) to (Sb3) are the same as the above (Sa1) to (Sa3) in the operating method of the chemical manufacturing apparatus according to the second embodiment of this disclosure.

[0190] The above (Sb4) to (Sb6) are the same as the above (Sa5) to (Sa7) in the method of operating a chemical manufacturing apparatus according to the second embodiment of this disclosure.

[0191] (Sb5) When the filler is heated by the second heating section, the heated filler 2 can achieve a thermal decomposition efficiency equivalent to or better than that of unused filler, and can be reused in the production of chemical product R by thermal decomposing the raw material M. Therefore, the operating method of the chemical product production apparatus of this disclosure can be repeated after (Sb5), following (Sb1), (Sb2), (Sb3), and (Sb4). And while these series of processes are repeated, the filler 2 can achieve a thermal decomposition efficiency equivalent to or better than that of filler 2 that has not been used even once in the thermal decomposition of raw material M, so it can operate stably for a long time and the raw material can be thermally decomposed efficiently.

[0192] [Operation method of a chemical manufacturing apparatus according to the fourth embodiment] <Chemical manufacturing apparatus according to the fourth embodiment> Next, a fourth embodiment of the chemical manufacturing apparatus used in the operating method of the chemical manufacturing apparatus of this disclosure will be described with reference to Figure 7. Figure 7 is a schematic cross-sectional view showing an example of the chemical manufacturing apparatus according to the fourth embodiment of this disclosure.

[0193] The chemical manufacturing apparatus 400 (hereinafter sometimes abbreviated as "manufacturing apparatus 400") comprises a reactor 1, a filler 2 filled inside the reactor 1, a raw material supply unit 3 for supplying raw material M to the inside of the reactor 1, an inert gas supply unit 4 for supplying inert gas G to the inside of the reactor 1, a first heating unit 5 for heating the filler 2, a removal unit 6 for removing chemical product R from the reactor 1, and a first oxygen-containing gas supply unit 7 for supplying oxygen-containing gas to the reactor 1.

[0194] The chemical manufacturing apparatus 400 according to the fourth embodiment of this disclosure differs from the chemical manufacturing apparatus 100 according to the first embodiment of this disclosure in that the inert gas G is supplied to the filler 2 from a vertical direction in the Y-axis direction. In the manufacturing apparatus 400, even when the inert gas G is supplied into the reactor 1, the filler 2 does not flow and forms a filler layer 2A. Therefore, the reactor 1 functions as a fixed bed.

[0195] Figure 7 shows a configuration comprising a mist trap 14; a hydrogen chloride trap 15a and chemical agent 15b; an exhaust section 13 for exhausting the inert gas G that has passed through the reactor 1; a three-way cock 12 connecting the reactor 1, the outlet section 6, and the exhaust section 14; a flow path 16a connecting the three-way cock 12 to the cooling section 9; a flow path 16b connecting the cooling section 9 to the mist trap; a flow path 16c connecting the mist trap 14 to the hydrogen chloride trap 15a; and a flow path 16d connecting the hydrogen chloride trap 15a to the gaseous product recovery section 10. However, the chemical manufacturing apparatus 400 according to the fourth embodiment is not limited to this.

[0196] <Operation method of a chemical manufacturing apparatus according to the fourth embodiment> Next, a method for operating a chemical manufacturing apparatus according to the fourth embodiment of this disclosure will be described. The method for operating a chemical manufacturing apparatus according to the fourth embodiment is preferably carried out by the chemical manufacturing apparatus 400 according to the fourth embodiment.

[0197] As described above, the chemical manufacturing apparatus 400 according to the fourth embodiment of this disclosure differs from the chemical manufacturing apparatus 100 according to the first embodiment of this disclosure only in that it has a fixed bed consisting of a filler layer 2A instead of a fluidized bed with filler 2. Therefore, the operating method of the chemical manufacturing apparatus according to the fourth embodiment can be applied to the operating method of the chemical manufacturing apparatus according to the first embodiment, as described in (Sa1) to (Sa4).

[0198] However, in (Sa1) above, the gas space velocity (GHSV) of the inert gas G in the filler layer 2A, as determined by the following formula 2, is 5,000 h -1 It is preferable that the above conditions are met. [Formula 2] GHSV = Q / V However, in Equation 2, GHSV is the gas space velocity (h) of the inert gas G in the filler layer 2A. -1 ) indicates the flow rate (Nm³) of the inert gas G at 0°C and 1 atmosphere. 3 V represents the volume of filler 2 in filler layer 2A (m³ / h), where V is the volume of filler 2 in filler layer 2A. 3 ) indicates.

[0199] In the above equation 2, V can be calculated by the following equation 2-1. [Formula 2-1] V = A × H However, in equation 2-1 above, V is the volume of filler 2 in filler layer 2A (m³ 3 ) represents the cross-sectional area (m²) inside the reactor 1 in a cross-section perpendicular to the deposition direction of filler 2 in the filler layer 2A of the reactor 1. 2 ) indicates, and H indicates the height (m) of filler layer 2A.

[0200] If the reactor 1 is cylindrical, then in equation 2-1, A can be calculated using the following equation 2-2. [Formula 2-2] A=r 2 π However, in the above formula 2-2, A is the cross-sectional area (m²) inside the reactor 1 in a cross-section perpendicular to the deposition direction of filler 2 in the filler layer 2A of the reactor 1. 2 ) is shown, where r is the radius in the cross-section perpendicular to the deposition direction of filler 2 in the filler layer 2A of reactor 1, and π is the ratio of a circle's circumference to its diameter.

[0201] Formulas 2, 2-1, and 2-2 will be described in detail with reference to Figures 8A and 8B. Figure 8A is a schematic diagram showing an example of a cross-section parallel to the deposition direction of filler 2 in the filler layer 2A of reactor 1. Figure 8B is a schematic diagram along the line VIIIB-VIIIB in Figure 8A. The reactor 1 shown in Figures 8A and 8B is cylindrical, and the cross-section perpendicular to the longitudinal direction of reactor 1 is a perfect circle. Note that in Figure 8B, the plug 11 and filler layer 2A are omitted.

[0202] When filling a cylindrical reactor 11 with filler 2 to form a filler layer 2A, a stopper 11 is necessary to prevent it from falling due to its own weight. In this disclosure, the height H of the filler layer 2A is defined as the height from the top of the stopper 11 to the top of the layer where the filler 2 is deposited. The height H of the filler layer 2A can also be expressed as the depth of the filler layer 2A in the deposition direction or the length in the Y-axis direction.

[0203] Filler 2 is granular, and there may be voids between multiple fillers 2. According to equation 2-1, the volume V (m³) of filler 2 in the filler layer 2A is calculated. 3 When calculating the volume V of filler 2, the volume V of filler 2 includes the volume of filler 2 itself and the volume of the voids between multiple fillers 2.

[0204] In equation 2-2, when determining the internal cross-sectional area of ​​the reactor 1, in order to determine the volume V of filler 2 in the filler layer 2A in equation 2, the internal cross-sectional area of ​​the reactor 1 at the bottom surface of the filler layer 2A, i.e., at the point of contact between the filler layer 2A and the plug 11, as shown by the line VIIIB-VIIIB in Figure 8A, is determined.

[0205] [Operation method of the chemical manufacturing apparatus according to the fifth embodiment] <Chemical manufacturing apparatus according to the fifth embodiment> Next, a fifth embodiment of the chemical manufacturing apparatus used in the operating method of the chemical manufacturing apparatus of this disclosure will be described with reference to Figure 9. Figure 9 is a schematic cross-sectional view showing an example of the chemical manufacturing apparatus according to the fifth embodiment of this disclosure.

[0206] The chemical manufacturing apparatus 500 (hereinafter sometimes abbreviated as "manufacturing apparatus 500"), in the manufacturing apparatus 100 according to the fourth embodiment, further comprises a regenerating furnace 20 provided separately from the reactor, a spent filler transfer unit 21 for transferring filler 2 from the reactor 1 to the inside of the regenerating furnace 20, a second oxygen-containing gas supply unit 22 for supplying oxygen-containing gas O to the inside of the regenerating furnace 20, a second heating unit 23 for heating the regenerating furnace 20, and a regenerated filler transfer unit 24 for transferring filler 2 from the regenerating furnace 20 to the inside of the reactor 1.

[0207] According to the chemical manufacturing apparatus of the fifth embodiment, in addition to heating the filler 2 by the first heating unit 5 inside the reactor 1, the filler 2 is further heated by the second heating unit 23 inside the regeneration furnace 20, thereby enabling more efficient regeneration of the filler 2.

[0208] <Operation method of a chemical manufacturing apparatus according to the fifth embodiment> Next, a method for operating a chemical manufacturing apparatus according to the fifth embodiment of this disclosure will be described. The method for operating a chemical manufacturing apparatus according to the fifth embodiment is preferably carried out by the chemical manufacturing apparatus 500 according to the fifth embodiment.

[0209] As described above, the chemical manufacturing apparatus 500 according to the fifth embodiment of this disclosure differs from the chemical manufacturing apparatus 200 according to the second embodiment of this disclosure only in that it has a fixed bed consisting of a filler layer 2A instead of a fluidized bed with filler 2. Therefore, the operating method of the chemical manufacturing apparatus according to the fifth embodiment can be applied to the operating method of the chemical manufacturing apparatus according to the second embodiment, as described in (Sa1) to (Sa7).

[0210] However, in (Sa1) above, the gas space velocity (GHSV) of the inert gas G in the filler layer 2A, as determined by the following formula 2, is 5,000 h -1 It is preferable that the above conditions are met. [Formula 2] GHSV = Q / V However, in Equation 2, GHSV is the gas space velocity (h) of the inert gas G in the filler layer 2A. -1 ) indicates that Q is the flow rate of the inert gas G (Nm³). 3 V represents the volume of filler 2 in filler layer 2A (m³ / h), where V is the volume of filler 2 in filler layer 2A. 3 ) indicates.

[0211] In the above equation 2, V can be calculated by the following equation 2-1. [Formula 2-1] V = A × H However, in equation 2-1 above, V is the volume of filler 2 in filler layer 2A (m³ 3 ) represents the cross-sectional area (m²) inside the reactor 1 in a cross-section perpendicular to the deposition direction of filler 2 in the filler layer 2A of the reactor 1. 2 ) indicates, and H indicates the height (m) of filler layer 2A.

[0212] If the reactor 1 is cylindrical, then in equation 2-1, A can be calculated using the following equation 2-2. [Formula 2-2] A=r 2 π However, in the above formula 2-2, A is the cross-sectional area (m²) inside the reactor 1 in a cross-section perpendicular to the deposition direction of filler 2 in the filler layer 2A of the reactor 1. 2 ) is shown, where r is the radius in the cross-section perpendicular to the deposition direction of filler 2 in the filler layer 2A of reactor 1, and π is the ratio of a circle's circumference to its diameter.

[0213] [Operation method of the chemical manufacturing apparatus according to the sixth embodiment] <Chemical manufacturing apparatus according to the sixth embodiment> Next, a sixth embodiment of the chemical manufacturing apparatus used in the operating method of the chemical manufacturing apparatus of this disclosure will be described with reference to Figure 10. Figure 10 is a schematic cross-sectional view showing an example of the chemical manufacturing apparatus according to the sixth embodiment of this disclosure.

[0214] The chemical manufacturing apparatus 600 (hereinafter sometimes abbreviated as "manufacturing apparatus 600") includes a reactor, a filler 2 filled inside the reactor 1, a raw material supply unit 3 that supplies a raw material M inside the reactor 1, an inert gas supply unit 4 that supplies an inert gas G inside the reactor 1, a first heating unit 5 that heats the reactor 1, a take-out unit 6 that takes out the chemical R from the reactor 1, a regeneration furnace 20 provided separately from the reactor 1, a used filler transfer unit 21 that transfers the filler 2 from the reactor 1 to the inside of the regeneration furnace 20, a second oxygen-containing gas supply unit 22 that supplies an oxygen-containing gas O inside the regeneration furnace 20, a second heating unit 23 that heats the regeneration furnace 20, and a regenerated filler transfer unit 24 that transfers the filler from the regeneration furnace 20 to the inside of the reactor 1.

[0215] The chemical manufacturing apparatus 600 according to the sixth embodiment of the present disclosure is different from the chemical manufacturing apparatus 300 according to the third embodiment of the present disclosure in that the inert gas G is supplied to the filler 2 from the vertical direction in the Y-axis direction. In the manufacturing apparatus 600, even when the inert gas G is supplied inside the reactor 1, the filler 2 does not flow and forms a filler layer 2A. Therefore, the reactor 1 functions as a fixed bed.

[0216] In FIG. 10, a mist trap 14; a hydrogen chloride trap 15a and a chemical 15b; an exhaust unit 13 that exhausts the inert gas G that has passed through the reactor 1; a three-way cock 12 that connects the reactor 1, the take-out unit 6, and the exhaust unit 14; a flow path 16a that leads from the three-way cock 12 to the cooling unit 9; a flow path 16b that leads from the cooling unit 9 to the mist trap; a flow path 16c that leads from the mist trap 14 to the hydrogen chloride trap 15a; and a flow path 16d that leads from the hydrogen chloride trap 15a to the gas product recovery unit 10 are illustrated, but the chemical manufacturing apparatus 600 according to the fourth embodiment is not limited thereto.

[0217] <Operating Method of Chemical Manufacturing Apparatus According to the Sixth Embodiment> Next, the operating method of the chemical manufacturing apparatus according to the sixth embodiment of the present disclosure will be described. The operating method of the chemical manufacturing apparatus according to the sixth embodiment is preferably performed by the chemical manufacturing apparatus 600 according to the sixth embodiment.

[0218] As described above, the chemical manufacturing apparatus 600 according to the sixth embodiment of the present disclosure differs only in that it has a fixed bed composed of the filler 2A instead of the fluidized bed by the filler 2 of the chemical manufacturing apparatus 300 according to the third embodiment of the present disclosure. Therefore, the operation method of the chemical manufacturing apparatus according to the sixth embodiment can apply the above (Sb1) to (Sb6) in the operation method of the chemical manufacturing apparatus according to the third embodiment.

[0219] (Method for manufacturing chemical) The method for manufacturing a chemical according to the present disclosure includes: (Sc1) supplying an inert gas into a reactor containing a filler; (Sc2) supplying a raw material while heating the reactor; (Sc3) taking out the chemical produced from the raw material from the inside of the reactor by the taking-out part; and (Sc4) heating the filler to 400°C to 720°C while supplying an oxygen-containing gas after (Sc3) or simultaneously with (Sc3). The method for manufacturing a chemical according to the present disclosure may further include other processes as necessary.

[0220] FIG. 11 is a flowchart showing an example of the method for manufacturing a chemical according to the present disclosure.

[0221] The method for manufacturing a chemical according to the present disclosure can be preferably performed using the chemical manufacturing apparatus 100 described in the item of (Operation method of chemical manufacturing apparatus) of the present disclosure.

[0222] Therefore, (Sc1) supplying an inert gas, (Sc2) supplying a raw material, (Sc3) taking out a chemical, and (Sc4) heating a filler in the method for manufacturing a chemical according to the present disclosure can be performed in the same manner as (Sa1) supplying an inert gas, (Sa2) supplying a raw material, (Sa3) taking out a chemical, and (Sa4) heating a filler in the operation method of the chemical manufacturing apparatus according to the present disclosure, respectively. Therefore, detailed description is omitted. After (Sc4), (Sc1), (Sc2), and (Sc3) may be repeated.

[0223] Other processes in the method for producing the chemicals of this disclosure can be carried out in the same manner as other processes (such as pretreatment, recovery, and separation) in the operation method of the chemical production apparatus of this disclosure.

[0224] However, preferred embodiments of the raw material M and chemical product R in the method for producing the chemical product of this disclosure will be described below.

[0225] <Raw material M> (Sc2) The raw materials M that can be used by supplying raw materials are not particularly limited as long as they are materials that are the target of the thermal decomposition reaction, and examples include raw materials that include one or more selected from the group consisting of naphtha, hydrocarbons, plastics, and biomass. Among these, raw materials M that include plastics can be preferably used.

[0226] There are no particular restrictions on the plastic-containing raw materials, and they can be appropriately selected depending on the purpose. Examples include mixed plastics containing polyolefins, aromatic plastics, and chlorine-containing raw materials. These may be used individually or in combination of two or more. Furthermore, raw material M may contain other components as needed.

[0227] - Mixed Plastics - There are no particular restrictions on the polyolefins included in the mixed plastic, and they can be appropriately selected depending on the purpose. However, it is preferable that the mixture includes polyethylene (PE) and polypropylene (PP), which are commonly used in beverage and food containers, packaging materials, molded products, films, etc.

[0228] There are no particular restrictions on the polyolefin content in plastics, and it can be appropriately selected depending on the purpose. However, it is preferable that the polyolefin content be 50% to 90% by mass, and more preferably 60% to 85% by mass, relative to the total mass of the plastic. When the polyolefin content in plastics is 50% to 90% by mass, readily available plastics can be used without sorting, and chemicals containing ethylene and propylene can be obtained efficiently and in high yield.

[0229] -Aromatic plastics- Aromatic plastics are plastics that have an aromatic skeleton. There are no particular restrictions on aromatic plastics, and they can be appropriately selected from those commonly used for beverage and food containers, packaging materials, molded products, films, etc., depending on the purpose. Examples include polyethylene terephthalate (PET), polybutylene terephthalate (PBT), polyethylene naphthalate (PEN), acrylonitrile-butadiene-styrene copolymer, polycarbonate (PC), and polystyrene (PS). These may be contained individually or in combination of two or more. Among these, aromatic plastics that contain polyethylene terephthalate (PET) and polystyrene (PS) are preferred.

[0230] --Chlorine-containing plastic-- There are no particular restrictions on the chlorine-containing plastic, and it can be appropriately selected depending on the purpose. However, it is preferable that it contains at least one selected from the group consisting of polyvinyl chloride (PVC), polyvinylidene chloride (PVDC), and chlorinated polyethylene (CPE), which are commonly used in beverage and food containers, packaging materials, molded products, films, etc.

[0231] There are no particular restrictions on the content of at least one selected from the group consisting of aromatic plastics and chlorine-containing plastics in the plastic, and it can be appropriately selected depending on the purpose. However, it is preferably 10% by mass or more and 50% by mass or less, and more preferably 15% by mass or more and 40% by mass or less, relative to the total mass of the plastic. When the content of at least one selected from the group consisting of aromatic plastics and chlorine-containing plastics in the plastic is 10% by mass or more and 50% by mass or less, chemicals containing ethylene and propylene can be obtained efficiently in high yield.

[0232] -Other ingredients- Other components contained in raw material M are not particularly limited and can be appropriately selected depending on the purpose. Examples include other plastics other than polyolefins, aromatic plastics, and chlorine-containing plastics; and materials commonly found in waste plastics such as paper and metal. These may be contained individually or in combination of two or more.

[0233] Other plastics are not particularly limited and can be selected as appropriate depending on the purpose, and examples include polyamide, polyurethane, and polymethyl methacrylate.

[0234] There are no particular restrictions on the content of other components in raw material M, and they can be appropriately selected depending on the type of raw material M used. However, from the viewpoint of the yield of chemical products containing ethylene and propylene, it is preferable that the content be less than 30% by mass, more preferably 25% by mass or less, and even more preferably 20% by mass or less, based on the total mass of raw material M.

[0235] From the perspective of reducing environmental impact, raw material M preferably contains waste plastic. When raw material M is waste plastic, there are no particular restrictions on the composition and composition ratio, and it can be appropriately selected according to the purpose. However, it is preferable that PE is 10% to 40% by mass, PP is 20% to 40% by mass, PS is 10% to 30% by mass, and PET is 1% to 30% by mass.

[0236] As the waste plastic, for example, refuse derived paper and plastics densified fuel (RPF) can be used.

[0237] The structure and content ratio of each component contained in raw material M can be determined by analysis, for example, by Fourier transform infrared spectroscopy (FT-IR), gel permeation chromatography (GPC), ion chromatography (IC), nuclear magnetic resonance method (NMR), liquid chromatography-mass spectrometry (LC-MS), pyrolysis gas chromatography-mass spectrometry (PyGC-MS), matrix-assisted laser desorption ionization time-of-flight mass spectrometry (MALDI-TOFMS), etc.

[0238] (Sc2) When supplying the raw material, there are no particular restrictions on the state of the plastic in raw material M supplied to the fluidized bed. For example, it can be crystalline, glassy, rubbery, liquid, etc. Also, the plastic may be in the state of decomposition products. Among these, rubbery or liquid plastic is preferable from the viewpoint of easy control of the supply amount.

[0239] When the plastic is crystalline or glassy, there are no particular restrictions on its form. For example, it can be a pulverized product of plastic, pellets of the pulverized product of plastic, chips of the pulverized product of plastic, etc.

[0240] There are no particular restrictions on the pulverized product of plastic, and it can be appropriately selected according to the purpose. For example, it can be powdery or flaky.

[0241] Rubber-like or liquid plastic refers to plastic that is fluid at a temperature above its melting point but below its thermal decomposition temperature. Rubber-like or liquid plastic is also called "molten plastic."

[0242] Plastic decomposition products are materials that have been broken down from plastics into smaller molecules, but their molecular weight is still larger than that of the final chemical product.

[0243] The molecular weight of rubbery or liquid plastics does not change from the molecular weight of crystalline or glassy plastics of the same composition. Therefore, plastics and their decomposition products can be distinguished by their molecular weight. As the molecular weight decreases due to decomposition, the melting point decreases, so in practice, it can be determined by the melting temperature. The melting temperature is measured by the method specified in JIS K7121-2012.

[0244] There are no particular restrictions on the melting temperature of the plastic, and it can be appropriately selected depending on the raw materials used, but 80°C to 200°C is preferred, and 90°C to 190°C is more preferred.

[0245] These various forms of raw materials M may be used after being processed separately from the chemical manufacturing method of this disclosure, or after being pre-treated for the other processing.

[0246] <Chemicals R> (Sc3) The chemical product extracted by the extraction of the chemical product is not particularly limited as long as it is a chemical product R obtained by decomposing the raw material M, and can be appropriately selected according to the purpose. If the raw material M is a raw material that contains one or more selected from the group consisting of naphtha, hydrocarbons, plastics, and biomass, it is preferable that the chemical product R contains at least one selected from the group consisting of olefins having 2 to 5 carbon atoms and aromatic hydrocarbons. In addition, the chemical product R may contain by-products produced by the thermal decomposition of the raw material M in addition to the target product, but in that case, the chemical product R shall include both the target product and the by-products.

[0247] Therefore, in this disclosure, if the raw material M is a raw material containing plastic, “useful component” means at least one selected from the group consisting of olefins having 2 to 5 carbon atoms and aromatic hydrocarbons.

[0248] -Olefins with 2 to 5 carbon atoms- In this disclosure, olefins having 2 to 5 carbon atoms may be referred to as "lower olefins." The olefin having 2 to 5 carbon atoms is preferably at least one selected from the group consisting of alkenes having 2 to 4 carbon atoms and dienes having 2 to 5 carbon atoms, with alkenes having 2 to 5 carbon atoms being more preferred.

[0249] An example of an olefin with two carbon atoms is ethylene.

[0250] An example of an olefin with three carbon atoms is propylene.

[0251] Examples of olefins with four carbon atoms include trans-2-butene, 1-butene, 2-methylpropene, cis-2-butene, 1,3-butadiene, and isobutene.

[0252] Examples of olefins with 5 carbon atoms include 2-methyl-2-butene, 1-pentene, 2-methyl-1-butene, cis-2-pentene, trans-2-pentene, isoprene, and cyclopentadiene.

[0253] Among these, the method for producing the chemical product described herein has the advantage of high yields of ethylene and propylene. There are no particular restrictions on the total yield (mass%) of ethylene and propylene, and it can be appropriately selected depending on the purpose, but it is preferably 30% by mass or more, more preferably 32% by mass or more, and even more preferably 34% by mass or more, relative to the total mass of the raw materials including plastic. The higher the total yield (mass%) of ethylene and propylene in the chemical product, the better, and there are no particular restrictions on its upper limit, for example, it may be 70% by mass or less, or 55% by mass or less. The lower and upper limits of the total yield (mass%) of ethylene and propylene in the chemical product can be appropriately combined, for example, 30% by mass or more and 70% by mass or less, 32% by mass or more and 70% by mass or less, 34% by mass or more and 70% by mass or less, 30% by mass or more and 55% by mass or less, 32% by mass or more and 55% by mass or less, 34% by mass or more and 55% by mass or less, etc.

[0254] There are no particular restrictions on the total yield (mass%) of olefins having 2 to 5 carbon atoms in the chemical product, and it can be appropriately selected depending on the purpose. However, it is preferably 35% to 75% by mass, more preferably 40% to 70% by mass, and even more preferably 45% to 65% by mass, relative to the total mass of the raw materials including plastics.

[0255] Olefins with 2 to 5 carbon atoms can be used as basic chemicals suitable for chemical recycling and can serve as raw materials for polyolefins. Polyolefins can be suitably used in a variety of fields, such as shopping bags, plastic wrap, straws, medical devices, home appliance casings, erasers, hoses, tires, tubes, CD cases, food trays, food containers, plastic bottles, and textiles.

[0256] -Aromatic hydrocarbons- There are no particular restrictions on the aromatic hydrocarbon, but benzene, toluene, ethylbenzene, and the three positional isomers of xylene (p-xylene, m-xylene, and o-xylene), and styrene are preferred, and the three positional isomers of benzene, toluene, and xylene are more preferred.

[0257] In this disclosure, benzene, toluene, ethylbenzene, and the three positional isomers of xylene (p-xylene, m-xylene, and o-xylene), as well as styrene, may be referred to as "useful aromatic hydrocarbons."

[0258] There are no particular restrictions on the total yield (mass%) of useful aromatic hydrocarbons, and it can be appropriately selected depending on the purpose. However, it is preferably 3% to 50% by mass, and more preferably 5% to 30% by mass, relative to the total mass of the raw materials including plastic.

[0259] -By-products- The chemicals obtained by the chemical manufacturing methods of this disclosure may contain by-products. In this disclosure, if the raw material M is a raw material containing plastic, by-products may include, for example, paraffin, carbon, and hydrogen gas.

[0260] There are no particular restrictions on the paraffin, but examples include aliphatic saturated hydrocarbons having 1 to 5 carbon atoms, with aliphatic saturated hydrocarbons having 2 to 5 carbon atoms being preferred. Examples of aliphatic saturated hydrocarbons having 1 to 5 carbon atoms include chain-like aliphatic saturated hydrocarbons having 1 to 5 carbon atoms.

[0261] Specific examples of paraffins include methane, ethane, propane, iso-butane, n-butane, 2-methylbutane, and n-pentene.

[0262] There are no particular restrictions on the total yield (mass%) of paraffins having 1 to 5 carbon atoms, but it is preferably 35% by mass or less, more preferably 30% by mass or less, and even more preferably 10% by mass or less, relative to the total mass of the raw materials including plastic. The lower limit of the total yield (mass%) of paraffins having 1 to 5 carbon atoms is preferable as it is lower, for example, 0.1% by mass or more relative to the total mass of the raw materials including plastic.

[0263] The yields of useful components and by-products contained in the chemical can be determined by analyzing the gaseous and liquid products obtained as products of the chemical manufacturing method of this disclosure using a gas chromatograph (GC) equipped with a flame ionization detector.

[0264] When analyzing the gaseous products as byproducts, the analysis can be performed using gas chromatography (GC) equipped with a flame ionization detector under the analytical conditions described in the examples. Each component can then be quantified using the internal standard method, based on the ratio of the peak area of ​​each component to that of the internal standard. The internal standard is not particularly limited as long as it is stable under the analytical conditions and easily separated from the analyte; for example, cyclopentane can be used.

[0265] Furthermore, when analyzing the liquid substance as a product, it can be analyzed using gas chromatography (GC) equipped with a flame ionization detector under the analytical conditions described in the examples, and each component can be quantified by the internal standard method based on the ratio of the peak area of ​​each component to that of the internal standard. The internal standard is not particularly limited as long as it is stable under the analytical conditions and easily separated from the analyte; for example, cyclopentane can be used.

[0266] Furthermore, the yield of coking, a by-product of the chemical, can be calculated by burning the filler in air inside or after removing it from the reactor, and measuring the weight change before and after air calcination.

[0267] The above chemical manufacturing method allows for stable operation over long periods and efficient thermal decomposition of raw materials. The manufactured chemicals can be used as basic chemicals suitable for chemical recycling.

[0268] (How to regenerate fillers) The method for regenerating a filler according to the present disclosure includes (Sd1) introducing an inert gas into a reactor containing the filler and supplying the inert gas; (Sd2) supplying raw materials while heating the reactor; (Sd3) removing the chemical product generated from the raw materials from inside the reactor; and (Sd4) heating the filler to 400°C to 720°C while supplying an oxygen-containing gas after or simultaneously with (Sd3). The method for producing the chemical product according to the present disclosure may further include other processes as necessary.

[0269] Figure 12 is a flowchart showing an example of a method for producing the chemicals of this disclosure.

[0270] The filler regeneration method of this disclosure can be suitably carried out using the chemical manufacturing apparatus 100 described in the section (Operation method of chemical manufacturing apparatus) of this disclosure.

[0271] Therefore, the steps of (Sd1) supplying an inert gas, (Sd2) supplying raw materials, (Sd3) removing chemicals, and (Sd4) heating the filler in the filler regeneration method of this disclosure can be carried out in the same manner as the steps of (Sa1) supplying an inert gas, (Sa2) supplying raw materials, (Sa3) removing chemicals, and (Sa4) heating the filler in the operation method of the chemical manufacturing apparatus of this disclosure, so a detailed explanation is omitted. After (Sd4), steps (Sd1), (Sd2), and (Sd3) may be repeated.

[0272] Other processes in the filler regeneration method of this disclosure can be carried out in the same manner as other processes (such as pretreatment, recovery, and separation) in the operation method of the chemical manufacturing apparatus of this disclosure.

[0273] The raw materials M and chemicals R in the filler regeneration method of this disclosure may be those described in the section (Operation method of chemical manufacturing equipment) or the section (Method of manufacturing chemicals) of this disclosure. [Examples]

[0274] The present disclosure will be specifically described below by way of test examples, examples, and comparative examples, but the present disclosure is not limited to these test examples, examples, and comparative examples in any way.

[0275] (Preparation Example 1) <Preparation of RPF Powder (P1)> As the RPF powder, RPF produced from mixed plastics recovered from the market and having the following composition was cut with a hacksaw so that the maximum side was 5 mm or less and then powdered. The prepared RPF powder may be referred to as "P1" below. [[ID=Thirteen]] [Composition and Blending Amount] · Polyethylene... 28% by mass · Polypropylene... 28% by mass · Polystyrene... 15% by mass · Polyethylene terephthalate... 13% by mass · Polyamide... 2% by mass · PVC... 1% by mass · PVDC... 1% by mass · Organic low molecular weight components... 4% by mass · Inorganic filler... 2% by mass · Acrylic resin, cellulose, and polyurethane... 6% by mass in total (Total... 100% by mass)

[0276] (Preparation Example 2) <Preparation of Waste Plastic Simulated Pellets (P2)> As the waste plastic simulated pellets, pellets were prepared with the following composition and blending amount. Among the raw materials shown below, all raw materials other than cellulose were selected from waste plastic-derived plastics and impurities. The prepared waste plastic simulated pellets may be referred to as "P2" below. [Composition and Blending Amount] · Polyethylene... 27% by mass · Polypropylene... 27% by mass • Polystyrene… 19% by mass • Polyethylene terephthalate… 14% by mass • Polyvinyl chloride… 2% by mass • Cellulose… 5% by mass (Cellulose powder, manufactured by MP Biomedicals, LLC) • Metallic aluminum… 2% by mass • Calcium carbonate… 2% by mass • Polyamide… 2% by mass (Total…100% by mass)

[0277] (Test Example 1) <Preparing the equipment> A manufacturing apparatus 100, as shown in Figure 1, was prepared. Specifically, a quartz tube with an inner diameter of 15 mm and a height of 550 mm was placed in the center of the reactor 1. A sieve was placed in the center, quartz wool was laid down, and a stopper 11 was placed. Then, 5 g of silica sand (product name: Ube Silica Sand No. 6, particle size: 0.6 mm to 0.07 mm, manufactured by Ube Sand Industries Co., Ltd.) was added as filler 2. The quartz tube was placed inside a cylindrical electric furnace (product name: ARF-30MC, manufactured by Asahi Rika Seisakusho Co., Ltd.) which was installed vertically, and the quartz tube was positioned so that filler 2 was in the center of the cylindrical electric furnace. The electric furnace is the first heating section 5 with an external heating method. A manual powder feeding device (airless feed cock, manufactured by Asahi Seisakusho Co., Ltd.), which serves as the raw material input section 3b of the raw material supply section 3, and one end of the gas extraction piping, which serves as the extraction section 6 for extracting gas as chemical product R, were connected to the top of the electric furnace. In addition, a gas inlet, which serves as the inert gas supply section 4, was connected to the bottom of the electric furnace. The other end of the gas extraction pipe was connected to the inlet side of a cooling trap 9a containing 15 mL of o-dichlorobenzene (reagent grade, manufactured by Kanto Chemical Co., Ltd.) as the organic solvent 9c. The cooling trap 9a was placed in a cooling section 9b containing ice water as the refrigerant 9d. One end of another gas extraction pipe was connected to the outlet side of the cooling trap 9a, and the other end of the other gas extraction pipe was connected to a gas bag (volume 10 L) as the gas product recovery section 10. A thermocouple was attached to the outer surface of the reaction tube at a position corresponding to the center of the height of the filler 2 packed in the quartz tube, and connected to the electric furnace. Nitrogen gas as the inert gas G was blown in from the gas inlet at a flow rate of 1,600 mL / min, and the electric furnace temperature was set to 800°C to start heating.

[0278] Furthermore, to confirm the behavior of the filler, a blank test was conducted at room temperature (25°C ± 5°C) without adding raw material M, and only introducing 1,600 mL / min of nitrogen gas as the inert gas G. As a result, it was confirmed that filler 2 rose to a height of 7 cm from the sieve in the center of the quartz tube. In other words, it was confirmed that the manufacturing apparatus 100 functions as a fluidized bed.

[0279] (Test Example 2) <Test Example 2-1: Decomposition of Plastics Using Untreated Filler> Plastic decomposition was performed using the manufacturing apparatus 100 described in Test Example 1. Silica sand (product name: Ube Silica Sand No. 6, particle size: 0.6 mm to 0.07 mm, manufactured by Ube Sand Industries Co., Ltd.) used as filler 2 was new and untreated (hereinafter sometimes referred to as "untreated filler"). The plastic used as raw material M was RPF powder P1 obtained in Preparation Example 1. After the electric furnace reached the set temperature of 780°C and the temperature stabilized, nitrogen gas was introduced from the gas inlet at a flow rate of 800 mL / min while 0.4 g of P1 was supplied into the quartz tube from the manual powder feeder over 10 minutes. After that, the liquid component was collected in the cooling trap 9a in the ice bath, and the gas component was collected in the gas bag. Five minutes after the supply of P1 ended, the gas bag was detached from the apparatus. The cooling trap 9a was returned to room temperature (25°C ± 5°C) and left for approximately 3 minutes before being detached from the apparatus.

[0280] <Test Example 2-2: Decomposition of Plastic Using Post-Use Filler> After the completion of Test Example 2-1, the electric furnace was stopped and the temperature inside the electric furnace was lowered to room temperature (25°C ± 5°C). Then, the silica sand used as filler 2 for decomposing the plastic in Test Example 2-1 was used as is, and the plastic was decomposed in the same manner as in Test Example 2-1. Filler 2 used for decomposing the plastic in Test Example 2-1 may hereafter be referred to as "used filler". Specifically, after the electric furnace temperature reached the set temperature of 780°C again and stabilized, nitrogen gas was introduced from the gas inlet at a flow rate of 800 mL / min, while 0.4 g of P1 was supplied into the quartz tube from the manual powder feeder over 10 minutes. After that, the liquid component was collected in the cooling trap 9a in the ice bath, and the gas component was collected in the gas bag. Five minutes after the supply of P1 ended, the gas bag was detached from the apparatus. The cooling trap 9a was returned to room temperature (25°C ± 5°C) and left for approximately 3 minutes before being detached from the apparatus.

[0281] <Test Example 2-3: Decomposition of Plastics Using Filler After Atmospheric Calcination> After the completion of Test Example 2-1, the electric furnace was stopped and the temperature inside the furnace was lowered to room temperature (25°C ± 5°C). Then, the silica sand used as filler 2 for decomposing the plastic in Test Example 2-1 was fired in the electric furnace in air at 800°C for 1 hour (hereinafter sometimes referred to as "air-fired filler"). Using this air-fired filler, plastic decomposition was performed in the same manner as in Test Example 2-1. Specifically, after the electric furnace temperature reached the set temperature of 780°C again and stabilized, nitrogen gas was introduced from the gas inlet at a flow rate of 800 mL / min while 0.4 g of P1 was supplied into the quartz tube from the manual powder feeder over 10 minutes. Then, the liquid component was collected in the cooling trap 9a in the ice bath, and the gas component was collected in the gas bag. Five minutes after the supply of P1 ended, the gas bag was detached from the apparatus. Furthermore, the cooling trap 9a was allowed to return to room temperature (25°C ± 5°C) for approximately 3 minutes before being disconnected from the device.

[0282] <<Analysis of gas bag contents>> In Test Examples 2-1 to 2-3, the yield of useful components in the pyrolysis gas recovered in the gas bag was determined by the following method.

[0283] The gas bag contains cyclopentane (>98.0%, density 0.75 g / cm³) as an internal standard substance. 3 40 μL of (manufactured by Tokyo Chemical Industry Co., Ltd.) was added. The gas bag was heated to approximately 40°C to completely vaporize the contents, and then the contents were mixed by gently kneading the gas bag. The obtained contents were used as an analytical sample and analyzed by gas chromatography (GC) under the following GC analysis conditions. The molar ratio of each component to cyclopentane in the pyrolysis gas in the gas bag, based on carbon atoms, was determined from the ratio of the peak area of ​​cyclopentane to the peak area of ​​each component. The mass of the pyrolysis gas in the gas bag was calculated from this value and the amount of cyclopentane (40 μL) added to the gas bag, and the yield (mass %) relative to the mass of the raw material added was determined. The results are shown in Table 1. [GC analysis conditions] • Equipment: Nexus GC-2030 (manufactured by Shimadzu Corporation) • Column: Rt-Alumina BOND (Diameter: 0.32mm, Length: 30m, manufactured by Restek) • Carrier gas type: Ar • Carrier gas flow rate: 360 mL / min Injection temperature: 200℃ • Sample injection volume: 1 mL • Split ratio: 1 / 200 • Column temperature: After being held at 120°C for 9 minutes, the temperature was increased to 200°C at a rate of 10°C / min, and then held at 200°C for 30 minutes. • Detector: Flame ionization detector (FID) • Detector temperature: 200℃

[0284] <<Analysis of trap contents>> In Test Examples 2-1 to 2-3, the yield (mass %) of useful components in the pyrolysis components recovered in the cooling trap 9a in the ice bath, relative to the mass of the input raw material M(P1), was determined by the following method.

[0285] The contents of cooling trap 9a in the ice bath were transferred to a sample vial. 2 mL of o-dichlorobenzene (reagent grade, manufactured by Kanto Chemical Co., Ltd.) was added to the nearly empty cooling trap 9a to dissolve the remaining contents, which were then transferred to the sample vial. This process was repeated three times to thoroughly wash the cooling trap 9a. Approximately 0.3 g of cyclopentane (>98.0%, manufactured by Tokyo Chemical Industry Co., Ltd.) was weighed and added to the sample vial as an internal standard to prepare the analytical sample, which was then analyzed by gas chromatography (GC) under the following GC analysis conditions. The molar ratio of each component relative to cyclopentane in the thermal decomposition components of cooling trap 9a, based on carbon atoms, was determined from the ratio of the peak area of ​​cyclopentane to the peak area of ​​each component. The mass of each component in the thermal decomposition components of cooling trap 9a was calculated from this value and the amount of cyclopentane added to the sample vial (0.3 g), and the yield (mass %) relative to the raw material M was determined. The results are shown in Table 1. [GC analysis conditions] • Equipment: Nexus GC-2030 (manufactured by Shimadzu Corporation) • Column: DB-1 (Diameter: 0.25mm, Length: 30m, manufactured by Agilent Technology) • Carrier gas type: He • Carrier gas flow rate: 97 mL / min Injection temperature: 350℃ • Sample injection volume: 1 μL • Split ratio: 1 / 50 • Column temperature: Set the heating program in the following order: 35°C (10 minutes) → heating (5°C / minute) → 350°C (10 minutes). • Detector: Flame ionization detector (FID) • Detector temperature: 350℃

[0286] In Tables 1 to 5, "yield of useful components" refers to the ratio of the mass of each product listed in Tables 1 to 5 to the mass of the raw material.

[0287] Furthermore, in Tables 1 to 5, "total yield of useful components" refers to the ratio of the mass of carbon-2 to carbon-5 olefins and useful aromatic hydrocarbons in the product to the mass of the raw materials. "Useful components" refers to ethylene, propylene, carbon-4 olefins (trans-2-butene, 1-butene, 2-methylpropene, cis-2-butene, 1,3-butadiene, and isobutene), carbon-5 olefins (cis-2-butene, n-pentene, 2-methyl-2-butene, 3-methyl-2-butene, 1,3-pentadiene, isoprene, and cyclopentadiene), and useful aromatic hydrocarbons (benzene, toluene, ethylbenzene, three positional isomers of xylene (p-xylene, m-xylene, and o-xylene), and styrene).

[0288] Furthermore, in Table 1, the "increase rate of total yield of useful components" indicates the ratio of the total yield of useful components in Test Example 2-2 or Test Example 2-3 to the total yield of useful components in Test Example 2-1. If the increase rate of total yield of useful components is between 90% and 100%, the filler was judged to have the same plastic decomposition efficiency as the untreated filler.

[0289] Furthermore, in Tables 1 to 5, "(B) / (A)(cm 3 / cm 2 "· seconds)" is the internal cross-sectional area of ​​the reactor 1 at the lower end of the part that contains the filler 2, 1 cm² 2 This represents the flow rate of the inert gas per unit area. Since the unit of the inert gas flow velocity (B) has been converted, the actual calculation formula is (B) / 60 / (A).

[0290] [Table 1]

[0291] In Test Example 2-2, which used post-use filler that had been used once to decompose plastic, the yield of the active ingredient was lower compared to Test Example 2-1, which used untreated filler. In other words, it was found that post-use filler was less efficient at decomposing plastic compared to untreated filler. Furthermore, in Test Example 2-3, which used air-fired filler obtained by air-fired post-use filler that had been used once to decompose plastic, the yield of the active ingredient was even lower compared to Test Example 2-2, which used post-use filler.

[0292] (Test Example 3) <Test Example 3-1: Decomposition of Plastics Using Untreated Filler> In Test Example 2-1, the thermal decomposition of plastic was performed in the same manner as in Test Example 2-1, except that the electric furnace setting temperature was changed to 800°C and the nitrogen gas flow rate was changed from 800 mL / min to 1,600 mL / min, and the resulting liquid and gaseous components were recovered.

[0293] <Test Example 3-2: Decomposition of Plastics Using Pre-treatment Filler> -Pre-treatment of fillers- The filler was pre-treated using the apparatus described in Test Example 1. Silica sand (product name: Ube Silica Sand No. 6, particle size: 0.6 mm to 0.07 mm, manufactured by Ube Sand Industries Co., Ltd.) used as filler 2 was new and untreated (unpre-treated filler). The pre-treatment was performed by heating filler 2 for one hour after the electric furnace reached the set temperature of 800°C and the temperature stabilized. This pre-treated filler 2 may hereafter be referred to as "pre-treated filler."

[0294] - Decomposition of plastic - In Test Example 3-1, the plastic was thermally decomposed in the same manner as in Test Example 3-1, except that filler 2 was changed from an untreated filler to a pretreated filler, and the resulting liquid and gaseous components were recovered.

[0295] <<Analysis of gas bag contents and cooling trap contents>> In Test Examples 3-1 and 3-2, the yield of useful components in the pyrolysis gas recovered in the gas bag and the yield of useful components in the pyrolysis gas recovered in the cooling trap 9a in the ice bath were determined using the same method as in Test Example 2. The results are shown in Table 2.

[0296] In Table 2, the "Increase in Total Yield of Useful Components" represents the ratio of the total yield of useful components in Test Example 3-2 to the total yield of useful components in Test Example 3-1. If the increase in the total yield of useful components is between 90% and 100%, the filler was judged to have the same plastic decomposition efficiency as the untreated filler.

[0297] [Table 2]

[0298] In Test Example 3-2, which used pre-treated filler, there was no significant change in the yield of the active ingredient compared to Test Example 3-1, which used untreated filler. The increase in the total yield of useful ingredients in Test Example 3-2 was 98.00%. From these results, it was found that the decrease in the yield of the active ingredient in Test Example 2-3 was not due to the calcination of the filler itself at 800°C.

[0299] (Comparative Example 1) -Pre-treatment of fillers- Using the same method as in Test Example 3-2, pre-treatment was performed on silica sand (product name: Ube Silica Sand No. 6) as filler 2 to prepare a pre-treated filler.

[0300] - Decomposition of plastic (1st attempt) - Using a pre-treatment filler, the plastic was thermally decomposed in the same manner as in Test Example 3-2.

[0301] -Filler post-treatment- After the first decomposition of the plastic was completed, the electric furnace was stopped and the temperature inside the furnace was lowered to room temperature (25°C ± 5°C). Then, the silica sand used as filler 2 in the first decomposition of the plastic was calcined in the electric furnace in air at 800°C for 1 hour (hereinafter sometimes referred to as "post-processing filler IA").

[0302] - Decomposing plastic (second attempt) - In the first plastic decomposition, the thermal decomposition of the plastic was carried out in the same manner as in the first plastic decomposition, except that filler 2 was changed from a pre-treatment filler to a post-treatment filler IA, and the resulting liquid and gaseous components were recovered.

[0303] (Example 1) - Decomposition of plastic (1st attempt) - Using untreated filler, the plastic was thermally decomposed in the same manner as in Test Example 3-1.

[0304] -Filler post-treatment- After the first decomposition of the plastic was completed, the electric furnace was stopped and the temperature inside the furnace was lowered to room temperature (25°C ± 5°C). Then, the silica sand used as filler 2 in the first decomposition of the plastic was calcined in the electric furnace in air at 600°C for 1 hour (hereinafter sometimes referred to as "post-processing filler IIA").

[0305] - Decomposing plastic (second attempt) - In the first plastic decomposition, the thermal decomposition of the plastic was carried out in the same manner as in the first plastic decomposition, except that filler 2 was changed from a pre-treatment filler to a post-treatment filler IIA, and the resulting liquid and gaseous components were recovered.

[0306] (Example 2) - Decomposition of plastic (1st attempt) - Using untreated filler, the plastic was thermally decomposed in the same manner as in Test Example 3-1.

[0307] -Filler post-treatment- After the first decomposition of the plastic was completed, the electric furnace was stopped and the temperature inside the furnace was lowered to room temperature (25°C ± 5°C). Then, the silica sand used as filler 2 in the first decomposition of the plastic was calcined in the electric furnace in air at 500°C for 1 hour (hereinafter sometimes referred to as "post-processing filler IIIA").

[0308] - Decomposing plastic (second attempt) - In the first plastic decomposition, the thermal decomposition of the plastic was carried out in the same manner as in the first plastic decomposition, except that filler 2 was changed from a pre-treatment filler to a post-treatment filler IIIA, and the resulting liquid and gaseous components were recovered.

[0309] <<Analysis of gas bag contents and cooling trap contents>> In Comparative Example 1, Example 1, and Example 2, the yield of useful components in the pyrolysis gas recovered in the gas bag and the yield of useful components in the pyrolysis gas recovered in the cooling trap 9a in the ice bath were determined using the same method as in Test Example 2. The results are shown in Table 3. The results for Test Example 3-1 are also shown in Table 3.

[0310] In Table 3, the "Increase in Total Yield of Useful Components" indicates the ratio of the total yield of useful components in Comparative Example 1, Example 1, or Example 2 to the total yield of useful components in Test Example 3-1. If the increase in the total yield of useful components is between 90% and 100%, the filler was judged to have the same plastic decomposition efficiency as the untreated filler.

[0311] [Table 3]

[0312] In Comparative Example 1, which used post-treated filler I, which was post-treated at 800°C for 1 hour, the yield of the active ingredient was significantly lower compared to Test Example 3-1, which used unpre-treated filler, with an increase in the total yield of the useful ingredient in Comparative Example 1 of 67.88%. On the other hand, in Example 1, which used post-treated filler II, which was post-treated at 600°C for 1 hour, there was no significant change in the yield of the active ingredient compared to Test Example 3-1, which used unpre-treated filler, with an increase in the total yield of the useful ingredient in Example 1 of 99.66%. Similarly, in Example 2, which used post-treated filler III, which was post-treated at 500°C for 1 hour, there was no significant change in the yield of the active ingredient compared to Test Example 3-1, which used unpre-treated filler, with an increase in the total yield of the useful ingredient in Example 2 of 97.32%.

[0313] From the above results, it was found that fillers can be regenerated to a state similar to unused fillers by post-treatment within a specific temperature range after being used in the thermal decomposition of plastics. In Test Example 2-2, the total yield of useful components decreased after using fillers once in the thermal decomposition of plastics. Therefore, it was found that by post-treatment within the specific temperature range mentioned above, fillers can be reused for a longer period, and chemicals can be obtained efficiently with consistently high yields.

[0314] (Test Example 4-1) <Preparing the equipment> A manufacturing apparatus 400, as shown in Figures 7, 8A, and 8B, was prepared. Specifically, a cylindrical quartz tube with an inner diameter of 15 mm and a height of 550 mm was fitted with a strainer plate as reactor 1, quartz wool was laid on top, and a stopper 11 was placed. Then, silica gel particles (product name: CARiACT Q-10, particle size: 1.18 mm to 2.36 mm, manufactured by Fuji Silicia Chemical Co., Ltd.) as filler 2 were packed in so that the filler height H was 6 cm, creating reactor 1 with a filler layer 2A. 5 g of silica gel particles were used. The quartz tube was set in a cylindrical electric furnace (product name: ARF-30MC, manufactured by Asahi Rika Seisakusho Co., Ltd.) installed vertically. The electric furnace is the first heating section 5 with external heating. A manual powder feeding device (airless feed cock, manufactured by Asahi Seisakusho Co., Ltd.), which serves as the raw material input section 3b of the raw material supply section 3, and a gas inlet, which serves as the inert gas supply section 4, were connected to the top (inlet) of the quartz tube. Furthermore, one end of a gas extraction pipe (silicone tube), which serves as an extraction section 6a for extracting the chemical product R, was connected to the bottom of the quartz tube. The other end of the extraction section 6a was connected to a three-way cock 12 made of Teflon®, with one end of the three-way cock connected to the exhaust section 13 and the other end connected to a flow path 16a (silicone tube). The other end of the flow path 16 was connected to the inlet side of a cooling trap 9a containing 15 mL of o-dichlorobenzene (reagent grade, manufactured by Kanto Chemical Co., Ltd.) as the organic solvent 9c. The cooling trap 9a was installed in a cooling section 9b containing ice water as the refrigerant 9d. One end of the flow path 16b (silicone tube) was connected to the outlet side of the cooling trap 9a, and the other end of the flow path 16b was connected to the end of a mist trap 14 filled with quartz wool. One end of channel 16c (silicone tube) was connected to the other end of mist trap 14, and the other end of channel 16c was connected to the inlet side of hydrogen chloride trap 15a, which was filled with 15 mL of a 1 mol / L sodium hydroxide aqueous solution (prepared by diluting sodium hydroxide manufactured by Fujifilm Wako Co., Ltd. with pure water) as the agent 15b. One end of another channel 16d (silicone tube) was connected to the outlet side of hydrogen chloride trap 15a, and the other end of channel 16d was connected to a gas bag (volume 10 L) as the gas product recovery unit 10. A thermocouple was inserted into the center of the filler layer 2A packed in the quartz tube.

[0315] <Decomposition of plastics using untreated fillers> The plastic was decomposed using manufacturing equipment 200. Silica gel particles (product name: CARiACT Q-10) used as filler 2 were new and untreated (hereinafter sometimes referred to as "untreated filler"). The plastic used as raw material M was P1 obtained in preparation example 1.

[0316] After the electric furnace reached the set temperature of 800°C and the temperature stabilized, the three-way stopcock 12 was connected to the bottom of the reactor 1 and the outlet 6a, and the recovery of chemical product R as a product was started using the cooling trap 9a and the gas bag, which served as the gas product recovery unit 10. Immediately after the start of the recovery of chemical product R, P1, prepared in Preparation Example 1 as the raw material M containing plastic, was supplied into the reactor 1 from the manual powder input device, which served as the raw material input unit 3b, over a period of 3 minutes under a nitrogen gas flow rate of 1,600 mL / min. A total of 0.4 g of P1 was supplied. After the supply of P1 was completed, the recovery of chemical product R as a product was continued, and 2 minutes after the end of the raw material supply, the three-way stopcock 12 was connected to the reactor 1 and the exhaust unit 13, and the gas bag was disconnected from the manufacturing apparatus 200. The cooling trap 9a was left to stand until it reached room temperature (25°C ± 5°C) before being disconnected from the manufacturing apparatus 200. The liquid component of chemical R was recovered in the cooling trap 9a and the mist trap 14. The gaseous component of chemical R was recovered in the gas bag.

[0317] (Example 3) - Decomposition of plastic (1st attempt) - Using untreated fillers, the plastic was thermally decomposed in the same manner as in Test Example 4-1.

[0318] -Filler post-treatment- After the first decomposition of the plastic was completed, the electric furnace was stopped and the temperature inside the furnace was lowered to room temperature (25°C ± 5°C). Then, silica gel particles (product name: CARiACT Q-10), which were used as filler 2 in the first decomposition of the plastic, were fired in the electric furnace in air at 600°C for 1 hour (hereinafter sometimes referred to as "post-processing filler IB").

[0319] - Decomposing plastic (second attempt) - In the first plastic decomposition, the thermal decomposition of the plastic was carried out in the same manner as in the first plastic decomposition, except that filler 2 was changed from a pre-treatment filler to a post-treatment filler IB, and the resulting liquid and gaseous components were recovered.

[0320] (Comparative Example 2) - Decomposition of plastic (1st attempt) - Using untreated fillers, the plastic was thermally decomposed in the same manner as in Test Example 4-1.

[0321] -Filler post-treatment- After the first decomposition of the plastic was completed, the electric furnace was stopped and the temperature inside the furnace was lowered to room temperature (25°C ± 5°C). Then, silica gel particles (product name: CARiACT Q-10), which were used as filler 2 in the first decomposition of the plastic, were fired in the electric furnace in air at 800°C for 1 hour (hereinafter sometimes referred to as "post-processing filler IIB").

[0322] - Decomposing plastic (second attempt) - In the first plastic decomposition, the thermal decomposition of the plastic was carried out in the same manner as in the first plastic decomposition, except that filler 2 was changed from a pre-treatment filler to a post-treatment filler IIB, and the resulting liquid and gaseous components were recovered.

[0323] <<Analysis of gas bag contents and cooling trap contents>> In Test Example 4-1, as well as in Example 3 and Comparative Example 2, the yield of useful components in the pyrolysis gas recovered in the gas bag and the yield of useful components in the pyrolysis gas recovered in the cooling trap 9a in the ice bath were determined using the same method as in Test Example 2. The results are shown in Table 4.

[0324] In Table 4, the "increase rate of total yield of useful components" indicates the ratio of the total yield of useful components in Example 3 or Comparative Example 2 to the total yield of useful components in Test Example 4-1. If the increase rate of total yield of useful components is 90% or more and 100% or less, the filler was judged to have the same plastic decomposition efficiency as the untreated filler.

[0325] [Table 4]

[0326] (Test Example 4-2: Decomposition of plastics using untreated fillers) In the decomposition of plastic using untreated filler in Test Example 4-1, the plastic was decomposed in the same manner as in Test Example 4-1, except that the raw material M used was changed from P1 obtained in Preparation Example 1 to P2 obtained in Preparation Example 2.

[0327] (Example 4) - Decomposition of plastic (1st attempt) - Using untreated filler, the plastic was thermally decomposed in the same manner as in Test Example 4-2.

[0328] -Filler post-treatment- After the first decomposition of the plastic was completed, the electric furnace was stopped and the temperature inside the furnace was lowered to room temperature (25°C ± 5°C). Then, silica gel particles (product name: CARiACT Q-10), which were used as filler 2 in the first decomposition of the plastic, were fired in the electric furnace in air at 800°C for 1 hour (hereinafter sometimes referred to as "post-processing filler IIB").

[0329] - Decomposing plastic (second attempt) - In the first plastic decomposition, the thermal decomposition of the plastic was carried out in the same manner as in the first plastic decomposition, except that filler 2 was changed from a pre-treatment filler to a post-treatment filler IIB, and the resulting liquid and gaseous components were recovered.

[0330] <<Analysis of gas bag contents and cooling trap contents>> In Test Example 4-2 and Example 4, the yield of useful components in the pyrolysis gas recovered in the gas bag and the yield of useful components in the pyrolysis gas recovered in the cooling trap 9a in the ice bath were determined using the same method as in Test Example 2. The results are shown in Table 5.

[0331] In Table 5, the "Increase in Total Yield of Useful Components" represents the ratio of the total yield of useful components in Example 4 to the total yield of useful components in Test Example 4-2. If the increase in the total yield of useful components is between 90% and 100%, the filler was judged to have the same plastic decomposition efficiency as the untreated filler.

[0332] [Table 5]

[0333] The results in Tables 4 and 5 show that after using the filler for the thermal decomposition of plastics, post-treatment within a specific temperature range can regenerate the filler to a state similar to unused filler, demonstrating its effectiveness not only in fluidized bed reactions but also in fixed-bed reactions.

[0334] As described above, this disclosure has been explained based on specific embodiments and examples, but these embodiments and examples are merely presented as examples, and this disclosure is not limited to the above embodiments and examples. The above embodiments can be implemented in various other forms, and various combinations, omissions, substitutions, additions, modifications, etc., are possible without departing from the spirit of the invention. These embodiments and their variations are included in the scope and spirit of the invention, as well as in the claims of the invention and its equivalents. [Explanation of Symbols]

[0335] 100: Manufacturing equipment 200 : Manufacturing equipment 1: Reactor 2: Filler 2A: Filler layer 3: Raw material supply section 3a: Raw material distribution department 3b: Raw material input section 4: Inert gas supply unit 4a: Inert gas flow section 4b: Pump 5: 1st heating section 6, 6a, 6b, 6c, 6d, 6e: Removal section 7: First oxygen-containing gas supply unit 7a: Oxygen-containing gas flow section 7b: Pump 8: Storage section 9: Cooling section 9a: Cooling trap 9b: Cooling section 9c: Organic solvents 9d: Refrigerant 10: Gaseous product recovery section 11: Stopper 12: Three-way cooktop 13: Exhaust section 14: Mist Trap 15a: Hydrogen chloride trap 15b: Medications 16, 16a, 16b, 16c, 16d: Flow channel 20 : Regeneration furnace 21: Used filler transfer unit 22: Second oxygen-containing gas supply unit M: Raw material G: Inert gas O: Oxygen R: Chemicals

Claims

1. A method for operating a chemical manufacturing apparatus, The chemical manufacturing apparatus is, Reactor and The filler packed inside the reactor, A raw material supply unit that supplies raw materials to the inside of the reactor, An inert gas supply unit that supplies inert gas to the inside of the reactor, The reactor comprises a first heating section for heating the reactor, A removal section for removing the chemical from the reactor, A first oxygen-containing gas supply unit that supplies oxygen-containing gas to the reactor, Equipped with, (Sa1) The inert gas is supplied into the reactor by the inert gas supply unit, (Sa2) The first heating unit heats the reactor while the raw material supply unit supplies the raw material, (Sa3) The chemical product produced from the raw materials is removed from the inside of the reactor by the removal unit, (Sa4) After (Sa3), the filler is heated to 400°C to 720°C by the first heating unit while the oxygen-containing gas is supplied from the first oxygen-containing gas supply unit. A method for operating a chemical manufacturing apparatus, including the method described above.

2. A method for operating a chemical manufacturing apparatus according to claim 1, wherein (Sa4) is followed by (Sa1), (Sa2), and (Sa3) are repeated.

3. A method for operating a chemical manufacturing apparatus according to claim 1 or 2, wherein in (Sa1), the inert gas is supplied into the reactor from the inert gas supply unit to cause the filler to flow.

4. The aforementioned chemical manufacturing apparatus, A regenerating reactor is provided separately from the aforementioned reactor, A used filler transfer unit that transfers the filler from the reactor to the inside of the regenerating reactor, A second oxygen-containing gas supply unit supplies oxygen-containing gas to the inside of the regeneration furnace, A second heating section for heating the aforementioned regeneration furnace, The system further comprises a regenerated filler transfer unit for transferring the filler from the regenerated furnace to the inside of the reactor, (Sa5) Simultaneously with (Sa4), or after (Sa4), the filler is transferred from the reactor to the inside of the regenerating reactor through the used filler transfer section. (Sa6) Heating the filler to 400°C to 720°C by the second heating unit while supplying the oxygen-containing gas from the second oxygen-containing gas supply unit, (Sa7) Transferring the filler from the regenerating furnace to the inside of the reactor through the regenerating filler transfer unit, A method for operating a chemical manufacturing apparatus according to claim 1 or claim 2, further comprising:

5. A method for operating a chemical manufacturing apparatus, The chemical manufacturing apparatus is, Reactor and The filler packed inside the reactor, A raw material supply unit that supplies raw materials to the inside of the reactor, An inert gas supply unit that supplies inert gas to the inside of the reactor, The reactor comprises a first heating section for heating the reactor, A removal section for removing the chemical from the reactor, A regenerating reactor is provided separately from the aforementioned reactor, A used filler transfer unit that transfers the filler from the reactor to the inside of the regenerating reactor, A second oxygen-containing gas supply unit supplies oxygen-containing gas to the inside of the regeneration furnace, A second heating section for heating the aforementioned regeneration furnace, A regenerated filler transfer unit that transfers the filler from the reactor to the inside of the regenerated reactor, Equipped with, (Sb1) The inert gas is supplied into the reactor by the inert gas supply unit, (Sb2) The first heating unit heats the reactor while the raw material supply unit supplies the raw material, (Sb3) The chemical product produced from the raw materials is removed from the inside of the reactor by the removal unit, (Sb4) Simultaneously with (Sb2), or after (Sb2), the filler is transferred from the reactor to the inside of the regenerating reactor through the used filler transfer unit. (Sb5) The oxygen-containing gas is supplied to the inside of the regeneration furnace by the second oxygen-containing gas supply unit, while the filler is heated to 400°C to 720°C by the second heating unit, (Sb6) Transferring the filler from the regenerating furnace to the inside of the reactor through the regenerating filler transfer unit, A method for operating a chemical manufacturing apparatus, including the method described above.

6. A method for operating a chemical manufacturing apparatus according to claim 5, wherein (Sb5) is repeated, followed by (Sb1), (Sb2), (Sb3), and (Sb4).

7. A method for operating a chemical manufacturing apparatus according to claim 5 or 6, wherein in (Sb1), the inert gas is supplied into the reactor from the inert gas supply unit to cause the filler to flow.

8. A method for operating a chemical manufacturing apparatus according to claim 1 or claim 5, wherein the reactor is a fixed bed.

9. A method for operating a chemical manufacturing apparatus according to claim 1 or claim 5, wherein the filler comprises at least one of silica sand and silicon dioxide.

10. The aforementioned raw material is a raw material containing plastic, The chemical product comprises at least one selected from the group consisting of olefins having 2 to 5 carbon atoms and aromatic hydrocarbons. A method for operating a chemical manufacturing apparatus according to claim 1 or claim 5.

11. A method for manufacturing chemical products, (Sc1) Supplying an inert gas to the inside of the reactor containing the filler, (Sc2) Supplying raw materials including plastic while heating the reactor, (Sc3) Taking out the chemical product produced from the raw materials from inside the reactor, (Sc4) After (Sc3), or simultaneously with (Sc3), the filler is heated to 400°C to 720°C while supplying an oxygen-containing gas. Includes, A method for producing a chemical product, characterized in that the chemical product contains at least one selected from the group consisting of olefins having 2 to 5 carbon atoms and aromatic hydrocarbons.

12. A method for producing a chemical product according to claim 11, wherein (Sc4) is repeated, followed by (Sc1), (Sc2), and (Sc3).

13. The method for producing a chemical product according to claim 11 or claim 12, wherein the filler comprises at least one of silica sand and silicon dioxide.

14. A method for regenerating fillers, (Sd1) Supplying an inert gas to the inside of the reactor containing the filler, (Sd2) Supplying raw materials while heating the reactor, (Sd3) Taking out the chemical product produced from the raw materials from inside the reactor, (Sd4) After (Sd3), or simultaneously with (Sd3), the filler is heated to 400°C to 720°C while supplying an oxygen-containing gas. A method for regenerating fillers, characterized by including [a certain element].

15. The filler regeneration method according to claim 14, wherein (Sd4) is repeated, followed by (Sd1), (Sd2), and (Sd3).

16. The method for regenerating a filler according to claim 14 or claim 15, wherein the filler comprises at least one of silica sand and silicon dioxide.

17. The aforementioned raw material is a raw material containing plastic, The chemical product comprises at least one selected from the group consisting of olefins having 2 to 5 carbon atoms and aromatic hydrocarbons. A method for regenerating a filler according to claim 14 or claim 15.

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