Method for producing chemical product and apparatus for producing chemical product

Abstract

A method for producing a chemical product according to the present disclosure comprises: supplying an inert gas to a reactor that has a longitudinal direction as a height direction and accommodates a fluidizing material therein to fluidize the fluidizing material; heating the fluidizing material to 780°C or higher; supplying a raw material containing a plastic to the fluidizing material heated to 780°C or higher; and recovering the chemical product generated from the raw material containing the plastic. A value X (cm3 / g / second) calculated by a formula 1 below satisfies X ≤ 500. [Formula 1] X = V / (Gm + Pm); in the formula 1, V represents the total volume (cm3) of the inside of the reactor, Gm represents the mass flow rate (g / second) of the inert gas, and Pm represents the mass flow rate (g / second) of the raw material containing the plastic.

Description

Chemical manufacturing method and chemical manufacturing apparatus

[0001] This disclosure relates to a method for producing chemicals and an apparatus for producing chemicals.

[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 a method for producing hydrocarbon products from plastic, comprising: supplying plastic raw materials and a driving gas to a first conical jet-bed reactor stage containing a catalyst to produce a first product vapor and a first residual plastic; separating at least a portion of the first product vapor from the driving gas and the first residual plastic to produce a first production flow including the first product vapor; supplying the first residual plastic from the first conical jet-bed reactor stage to a second conical jet-bed reactor stage containing a catalyst to produce a second product vapor and a second residual plastic; and separating at least a portion of the second product vapor from the driving gas and the second residual plastic to produce a second production flow including the second product vapor. In this proposed method, the first conical jet-bed reactor stage is at a temperature of approximately 300°C to approximately 650°C.

[0004] Special Publication No. 2024-537212

[0005] The present disclosure aims to provide a method for producing chemicals that can efficiently obtain at least one chemical selected from the group consisting of olefins having 2 to 4 carbon atoms and aromatic hydrocarbons in high yield.

[0006] The means for solving the aforementioned problem are as follows: <1> A method for producing a chemical product, comprising: supplying an inert gas to a reactor in which the longitudinal direction is the height direction and a fluid material is contained inside, causing the fluid material to flow; heating the fluid material to 780°C or higher; supplying a raw material containing plastic to the fluid material heated to 780°C or higher; and recovering the chemical product produced from the raw material containing plastic, wherein the value X (cm) is calculated by the following formula 1. ３ A method for producing a chemical product characterized in that the flow rate (g / second) satisfies X ≤ 500. [Equation 1] X = V / (Gm + Pm) where V is the volume (cm³) of the part of the reactor where the fluid material is contained and the volume above it. ３ ) indicates, where Gm is the mass flow rate (g / sec) of the inert gas, and Pm is the mass flow rate (g / sec) of the raw material containing the plastic. <2> The method for producing the chemical product described in <1> above, wherein the value Y (cm / sec) calculated by the following formula 2 satisfies Y ≥ 20. [Formula 2] Y = Gv / A However, in formula 2, Gv is the volume flow rate (Ncm) of the inert gas at 0°C and 1 atm ３ ( / second) is shown, and A is the cross-sectional area (cm²) inside the reactor in a cross-section perpendicular to the longitudinal direction at the lower end of the part of the reactor that houses the fluid material. ２ ) shows. <3> A method for producing a chemical product, comprising: supplying an inert gas to a reactor in which the longitudinal direction is the height direction and a fluid material is contained inside, causing the fluid material to flow; heating the fluid material to 780°C or higher; supplying a raw material containing plastic to the fluid material heated to 780°C or higher; and recovering the chemical product produced from the raw material containing plastic, wherein the numerical value Y (cm / sec) calculated by the following formula 2 satisfies Y ≥ 20. [Formula 2] Y = Gv / A However, in formula 2, Gv is the volumetric flow rate (Ncm) of the inert gas at 0°C and 1 atm ３( / second) is shown, and A is the cross-sectional area (cm²) inside the reactor in a cross-section perpendicular to the longitudinal direction at the lower end of the part of the reactor that houses the fluid material. ２ ) indicates. <4> A method for producing a chemical product according to any one of the above <1> to <3>, wherein the raw material containing the plastic contains waste plastic. <5> A method for producing a chemical product according to any one of the above <1> to <4>, wherein the raw material containing the plastic contains 50% by mass or more of polyolefin. <6> A method for producing a chemical product according to any one of the above <1> to <5>, wherein the fluid material mainly contains one selected from the group consisting of silicon dioxide, zirconium oxide, yttria-stabilized zirconium oxide, calcia-stabilized zirconium oxide, magnesium oxide, calcium oxide, silicon carbide, silicon nitride, silicon oxide, tantalum oxide, niobium oxide, beryllium oxide, lanthanum oxide, manganese(II) oxide, chromium(III) oxide, gallium oxide, forsterite, and cordierite. <7> A method for producing a chemical product according to any one of the above <1> to <6>, wherein the chemical product contains ethylene and propylene. <8> The method according to any one of the above <1> to <7>, wherein, in the process of fluidizing, the inert gas is supplied to the fluid material from a direction opposite to the direction of gravity in the longitudinal direction of the reactor. <9> A chemical manufacturing apparatus comprising: a reactor whose longitudinal direction is the height direction and which houses a fluid material inside; a raw material supply unit connected to the reactor and which supplies raw materials including plastic into the reactor; an inert gas supply unit connected to one end of the reactor in the longitudinal direction and which is arranged to supply an inert gas to the fluid material from a direction opposite to the direction of gravity; a heating unit for heating the fluid material; a recovery unit for recovering the chemical product produced from the raw materials including plastic; and a control unit for controlling the heating temperature by the heating unit and the amount of inert gas supplied by the inert gas supply unit, wherein the control unit controls a target temperature T of the fluid material of 780°C or higher, and the total volume V (cm) inside the reactor. ３ ), any number X (cm) less than or equal to 500 based on the following formula 1. ３ / (g / sec)), and an input / output unit that inputs and outputs the mass flow rate Pm (g / sec) of the raw material containing the plastic when the raw material containing the plastic is introduced into the reactor, a heating temperature controller that controls the heating temperature of the heating unit to be the target temperature T from the input value of the target temperature T by the input / output unit, and the total volume V (cm ３ ), the numerical value X (cm ３ / (g / sec)), and from the input values of the mass flow rate Pm (g / sec), a first calculation unit that calculates the mass flow rate Gm (g / sec) of the inert gas supplied to the reactor based on the following formula 1, and a first inert gas supply amount controller that controls the supply of the inert gas from the inert gas supply unit at the mass flow rate Gm (g / sec) calculated by the first calculation unit. A chemical production apparatus characterized by comprising: [Formula 1] X = V / (Gm + Pm) However, in Formula 1, V represents the total volume (cm ３ ) inside the reactor, Gm represents the mass flow rate (g / sec) of the inert gas, and Pm represents the mass flow rate (g / sec) of the raw material containing the plastic. <10> A chemical production apparatus, comprising: a reactor having a longitudinal direction as the height direction and accommodating a fluid material inside; a raw material supply unit connected to the reactor and supplying a raw material containing plastic to the inside of the reactor; an inert gas supply unit connected to one end of the reactor in the longitudinal direction and arranged to supply an inert gas to the fluid material from a direction opposite to the gravitational direction; a heating unit that heats the fluid material; a recovery unit that recovers the chemical produced from the raw material containing the plastic; and a control unit that controls the heating temperature by the heating unit and the supply amount of the inert gas by the inert gas supply unit. The control unit includes: a target temperature T of the fluid material of 780 ° C or higher, and a cross-sectional area A (cm ２An input / output unit that inputs and outputs the cross-sectional area A (cm / sec) and 20 or more arbitrary numerical values ​​Y (cm / sec) based on the following formula 2; a heating temperature control controller that controls the heating temperature of the heating unit to reach the target temperature T based on the input value of the target temperature T from the input / output unit; and the input / output unit that inputs the cross-sectional area A (cm / sec) ２ ) and the input value of the above numerical value Y (cm / sec) are used to calculate the volumetric flow rate (Ncm) of the inert gas at 0°C and 1 atmosphere based on the following formula 2. ３ A second calculation unit calculates the volume flow rate Gv (Ncm²) calculated by the second calculation unit at 0°C and 1 atmosphere. ３ A chemical manufacturing apparatus comprising: a second inert gas supply rate controller that controls the supply of the inert gas from the inert gas supply unit at a rate of ( / second); and Y = Gv / A, where Gv is the volume flow rate of the inert gas at 0°C and 1 atm (Ncm² / second). ３ The value is the length of the reactor (cm²), and A is the cross-sectional area (cm²) inside the reactor in a cross-section perpendicular to the longitudinal direction of the reactor. ２ ) indicates.

[0007] According to embodiments of this disclosure, it is possible to provide a method for producing chemicals that can efficiently obtain at least one chemical selected from the group consisting of olefins having 2 to 4 carbon atoms and aromatic hydrocarbons in high yield.

[0008] Figure 1A is a schematic diagram along the line IA-IA in Figure 1B, showing an example of a cross-section parallel to the longitudinal direction of the reactor. Figure 1B is a schematic diagram along the line IB-IB in Figure 1A, showing an example of a cross-section perpendicular to the longitudinal direction of the reactor. Figure 2 is a diagram showing an example of a flowchart of a chemical manufacturing method according to the first embodiment of this disclosure. Figure 3 is a diagram showing another example of a flowchart of a chemical manufacturing method according to the first embodiment of this disclosure. Figure 4 is a schematic cross-sectional view showing an example of a chemical manufacturing apparatus according to the first embodiment of this disclosure. Figure 5A is a partially enlarged view of the reactor in Figure 4, and is a schematic diagram along the line VA-VA in Figure 5B, showing an example of a cross-section parallel to the longitudinal direction of the reactor. Figure 5B is a schematic diagram along the line VB-VB in Figure 5A, showing an example of a cross-section perpendicular to the longitudinal direction of the reactor. Figure 6 is a functional block diagram showing an example of a control unit of a chemical manufacturing apparatus according to the first embodiment of this disclosure. Figure 7 is a functional block diagram showing an example of a control unit of a chemical manufacturing apparatus according to the second embodiment of this disclosure. Figure 8 is a functional block diagram showing an example of a control unit for a chemical manufacturing apparatus according to the third embodiment of this disclosure. Figure 9A is a schematic cross-sectional view showing an example of a chemical manufacturing apparatus according to the fourth embodiment of this disclosure. Figure 9B is a partially enlarged view of the reactor in Figure 9A.

[0009] The method disclosed in Patent Document 1 primarily uses a catalyst for plastic decomposition. In a fluidized bed or jet bed reactor, the catalyst flow is highly back-mixed, resulting in a non-uniform catalyst residence time distribution. This invention addresses this problem by having two or more fluidized beds or jet beds in series, thereby significantly narrowing the residence time distribution of the catalyst and plastic, and reducing the proportion of unconverted plastic entrained by the catalyst circulating from the reactor to the regenerator. Therefore, this invention does not optimize the conditions of the fluidized bed in the thermal decomposition of plastic.

[0010] In response, the inventors have conducted diligent studies and found that when thermally decomposing a raw material containing plastic while flowing a fluidizing agent, the fluidizing agent should be heated to 780°C or higher, and that in the method for producing a chemical product according to the first embodiment below, the value X (cm) calculated by the following formula 1 is ３We have found that even without using a catalyst in the reaction, if X ≤ 500 (g / sec), or if the value Y (cm / sec) calculated by the following formula 2 satisfies Y ≥ 20, then at least one chemical selected from the group consisting of olefins having 2 to 4 carbon atoms and aromatic hydrocarbons can be efficiently obtained in high yield. However, a catalyst can also be used in the chemical manufacturing method of this disclosure.

[0011] Embodiments of this disclosure will be described below with reference to the drawings. However, the embodiments of this disclosure are not limited to the following description, but are illustrative examples of chemical manufacturing methods and chemical manufacturing apparatus for embodying the technical concept of the present invention, and can be modified as appropriate without departing from the gist of this disclosure. Furthermore, in this disclosure, the "~" indicating a numerical range means that the numerical values ​​described before and after it are included as the lower and upper limits, respectively, unless otherwise specified. In numerical ranges described in stages within this disclosure, the upper or lower limit described in one numerical range may be replaced with the upper or lower limit of another numerical range described in stages.

[0012] In the following explanation, terms indicating specific directions or positions (e.g., "up," "down," "X," "Y," "Z," and other terms including these) will be used as needed. However, the use of these terms is solely to facilitate understanding the invention by referring to the drawings, and the technical scope of the invention is not excessively limited by the meaning of these terms. For example, if "top surface" is mentioned, the invention must not always be used in a way that it faces upwards. Also, parts with the same reference numerals appearing in multiple drawings indicate the same or equivalent parts or components.

[0013] Furthermore, in this disclosure, the term "polygon" refers to polygons such as triangles and quadrilaterals, including shapes where the corners of the polygon have been rounded, chamfered, or otherwise modified. Similarly, shapes where modifications have been made not only to the corners (ends of the sides) but also to the middle parts of the sides will also be referred to as polygons. In other words, shapes that retain the shape of a polygon but have been partially modified are included in the interpretation of "polygon" as described in this disclosure.

[0014] Furthermore, the same applies not only to polygons, but also to words describing specific shapes such as trapezoids, circles, and concave shapes. The same also applies when dealing with each side that forms such a shape. In other words, even if a side has been processed at a corner or in the middle, the interpretation of "side" includes the processed part. When distinguishing a "polygon" or "side" without partial processing from a processed shape, the term "strictly" should be added, for example, "strictly quadrilateral."

[0015] Furthermore, unless otherwise specified, the sizes, materials, shapes, and relative arrangements of the components described below are intended to be illustrative examples of the embodiments of this disclosure, and are not intended to limit the scope to those embodiments. Also, the content described in one embodiment may be applicable to other embodiments and modifications. Additionally, the sizes and positional relationships of the members shown in the drawings may be exaggerated for clarity. Moreover, to avoid overly complex drawings, schematic diagrams may be used with some elements omitted, or end views showing only the cross-section may be used as cross-sectional views.

[0016] (Method for manufacturing chemical products) The method for manufacturing chemical products described herein includes the following first, second, and third embodiments.

[0017] [First Embodiment] The method for producing a chemical product according to the first embodiment of the present disclosure includes supplying an inert gas to a reactor whose longitudinal direction is the height direction and which contains a fluid material inside, causing the fluid material to flow, heating the fluid material to 780°C or higher, supplying a raw material containing plastic to the fluid material heated to 780°C or higher, and recovering the chemical product produced from the raw material containing plastic, wherein the value X (cm) is calculated by the following formula 1. ３ The ratio (g / second) satisfies X ≤ 500. [Equation 1] X = V / (Gm + Pm) where V is the volume (cm³) of the part of the reactor's interior where the fluid material is contained and the volume above it. ３ The values ​​shown are Gm, where Gm represents the mass flow rate (g / second) of the inert gas, and Pm represents the mass flow rate (g / second) of the raw material containing the plastic.

[0018] With respect to the reactor, if the inner diameter of the portion containing the fluid material and the upper part thereof is constant, then in formula 1, the volume V (cm³) of the portion containing the fluid material and the upper part thereof within the reactor. ３ V can be calculated by the following formula 1-1. [Formula 1-1] V = A × L However, in formula 1-1, A is the cross-sectional area (cm²) inside the reactor in a cross section perpendicular to the longitudinal direction at the lower end of the part of the reactor that houses the fluid material. ２ ) indicates the distance (cm) from the lower end of the portion containing the fluid material to the height that coincides with the upper end of the heating portion.

[0019] If the reactor is cylindrical, in formula 1-1, the cross-sectional area A (cm²) inside the reactor in a cross-section perpendicular to the longitudinal direction at the lower end of the portion of the reactor that houses the fluid material. ２ ) can be calculated by the following formula 1-2. [Formula 1-2] A = r ２ π However, in equation 1-2 above, r represents the radius in the cross-section of the reactor in a direction perpendicular to the longitudinal direction, and π represents pi.

[0020] In the above formula 1, the mass flow rate Gm (g / sec) of the inert gas can be calculated by the following formula 1-3. [Formula 1-3] Gm = Gv / 1,000 / 22.4 × M where Gv is the volumetric flow rate (Ncm²) of the inert gas. ３ The value ( / second) is 22.4, which represents standard conditions (0°C, 1.013 × 10⁻¹⁰). ５ The molar volume (L / mol) of the gas at Pa is shown, and M represents the molar mass (g / mol) of the inert gas. However, if a mixed gas containing two or more inert gases is used as the inert gas, "M" represents the weighted average of the molar masses of each gas in the mixed gas, based on volume.

[0021] In this disclosure, unless otherwise specified, the volumetric flow rate of the gas is calculated at 0°C and 1 atmosphere.

[0022] Formulas 1, 1-1, 1-2, and 1-3 will be described in detail with reference to Figures 1A and 1B. Figure 1A is a schematic diagram along the line IA-IA in Figure 1B, showing an example of a cross-section parallel to the longitudinal direction of the reactor. Figure 1B is a schematic diagram along the line IB-IB in Figure 1A, showing an example of a cross-section perpendicular to the longitudinal direction of the reactor. The reactors shown in Figures 1A and 1B are cylindrical reactors with a perfectly circular cross-section perpendicular to the longitudinal direction of the reactor. Note that in Figure 1B, the fluid material 2 contained inside the reactor is omitted.

[0023] When the chemical manufacturing apparatus is not in operation, the direction of gravity in which the fluid material 2 accumulates by its own weight in the internal space of the reactor 1 is defined as the Y-axis direction, the direction approximately perpendicular to the Y-axis direction is defined as the X-axis direction, and the direction approximately perpendicular to both the X-axis and Y-axis directions is defined as the Z-axis direction. The X-axis, Y-axis, and Z-axis are mutually orthogonal. The longitudinal direction of the reactor 1 is preferably the Y-axis direction, but is not limited to this.

[0024] In this disclosure, "approximately orthogonal" is not limited to 90°, but allows for a difference of 90° ± 5°.

[0025] In the method for producing chemicals according to the first embodiment of this disclosure, the raw material containing plastic is rapidly heated and thermally decomposed by contact with a fluidizing agent. That is, the location where the chemicals produced by the thermal decomposition of the plastic are generated coincides with the part of the reactor 1 that contains the fluidizing agent 2. Furthermore, it is assumed that the volume of the fluidizing agent 2 is generally very small compared to the volume of the reactor 1 and can therefore be ignored. Based on these assumptions, the parameter for the thermal decomposition of the raw material containing plastic is the numerical value X (cm) calculated by Equation 1. ３ A rate of ( / g / sec) is effective, and the method for producing a chemical product according to the first embodiment of this disclosure can efficiently produce at least one chemical product selected from the group consisting of olefins having 2 to 4 carbon atoms and aromatic hydrocarbons in high yield, provided that X ≤ 500 is satisfied.

[0026] Furthermore, the ratio [Pm / Gm] of the mass flow rate Pm (g / sec) of the raw material containing the plastic to the mass flow rate Gm (g / sec) of the inert gas is preferably 1 or less, and more preferably 0.5 or less. When the ratio [Pm / Gm] is 1 or less, the chemicals produced by the thermal decomposition of the plastic in the reactor 1 are sufficiently diluted, and unwanted side reactions such as the recombination of the chemicals and polycyclization of aromatic chemicals can be suppressed. There is no particular lower limit to the ratio [Pm / Gm], but from the viewpoint of suppressing the energy consumption required to heat the reactor 1, it is preferably 0.005 or more, more preferably 0.007 or more, and even more preferably 0.01 or more.

[0027] The distance L (cm) from the lower end of the portion containing the fluid material 2 (the position where the fluid material 2 contacts the stopper 10 in a cross-sectional view) to the height that coincides with the upper end 5a of the heating section 5 may vary depending on the shape, structure, and size of the heating section 5 and the reactor 1. However, L is defined as the maximum length (cm) in the longitudinal direction of the reactor within the range from the portion containing the fluid material 2 to the upper end of the area of ​​the reactor 1 that the heating section 5 can heat.

[0028] Next, a method for manufacturing a chemical product according to one embodiment of this disclosure will be described. Figure 2 is a diagram showing an example of a flowchart for manufacturing a chemical product according to the first embodiment of this disclosure.

[0029] A method for producing a chemical product according to the first embodiment of this disclosure includes S1 of making a fluid material fluid, S2 of heating, S3 of supplying raw materials, and S4 of recovering the chemical product. The method for producing a chemical product according to the first embodiment of this disclosure may further include other processes as necessary.

[0030] -Chemicals- The chemicals produced by the method for producing chemicals according to the first embodiment of this disclosure are not particularly limited as long as they are chemicals obtained by decomposing raw materials including plastics, and can be appropriately selected depending on the purpose. However, it is preferable that the chemicals include at least one selected from the group consisting of olefins having 2 to 4 carbon atoms and aromatic hydrocarbons, and it is more preferable that the chemicals include ethylene and propylene.

[0031] In addition, the chemical product produced by the method for producing a chemical product according to the first embodiment of this disclosure may include by-products in addition to the chemical product containing at least one selected from the group consisting of olefins having 2 to 4 carbon atoms and aromatic hydrocarbons. In such cases, the chemical product in this disclosure shall include both the chemical product containing at least one selected from the group consisting of olefins having 2 to 4 carbon atoms and aromatic hydrocarbons and the by-products.

[0032] In this disclosure, "useful component" means at least one chemical selected from the group consisting of olefins having 2 to 4 carbon atoms and aromatic hydrocarbons.

[0033] In this disclosure, “auxiliary component” means a component other than at least one chemical selected from the group consisting of olefins having 2 to 4 carbon atoms and aromatic hydrocarbons, contained in a chemical product.

[0034] --Olefins having 2 to 4 carbon atoms-- In the method for producing chemicals according to the first embodiment of this disclosure, olefins having 2 to 4 carbon atoms may be referred to as "lower olefins". The olefins having 2 to 4 carbon atoms are preferably at least one selected from the group consisting of alkenes having 2 to 4 carbon atoms and dienes having 2 to 4 carbon atoms, and alkenes having 2 to 4 carbon atoms are more preferred.

[0035] Examples of olefins with two carbon atoms include ethylene and acetylene.

[0036] An example of an olefin with three carbon atoms is propylene.

[0037] Examples of olefins with four carbon atoms include trans-2-butene, 1-butene, cis-2-butene, 1,3-butadiene, and isobutene.

[0038] There are no particular restrictions on the total yield (mass%) of olefins having 2 to 4 carbon atoms, and it can be appropriately selected depending on the purpose. However, relative to the raw materials containing plastic, it is preferably 30% by mass or more, more preferably 35% by mass or more, even more preferably 46% by mass or more, and particularly preferably 52% by mass or more. A higher total yield (mass%) of olefins having 2 to 4 carbon atoms is preferable, and there are no particular restrictions on its upper limit, but for example, it may be 90% by mass or less, or 80% by mass or less.

[0039] In this disclosure, the yield of each component or the total yield represents the mass percentage (mass%) of each component relative to the raw material containing the plastic.

[0040] Among these, the method for producing chemicals according to the first embodiment of this disclosure has the advantage of high yields of ethylene and propylene. The total yield (mass%) of ethylene and propylene is not particularly limited and can be appropriately selected depending on the purpose, but is preferably 30% by mass or more, more preferably 33% by mass or more, and even more preferably 40% by mass or more relative to the raw materials including plastic. The higher the total yield (mass%) of ethylene and propylene, the better, and there is no particular upper limit, for example it may be 70% by mass or less, 60% by mass or less, or 50% by mass or less.

[0041] Olefins with 2 to 4 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 fibers.

[0042] --Aromatic Hydrocarbons-- In this disclosure, aromatic hydrocarbons that are suitable for use as chemical products may be referred to as "useful aromatic hydrocarbons." There are no particular limitations on useful aromatic hydrocarbons, but benzene, toluene, ethylbenzene, three positional isomers of xylene (p-xylene, m-xylene, and o-xylene), styrene, and the like are preferred.

[0043] 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, relative to the raw materials containing plastic, it is preferably 10% by mass or more, more preferably 12% by mass or more, and even more preferably 15% by mass or more. A higher total yield (mass%) of useful aromatic hydrocarbons is preferable, and there are no particular restrictions on its upper limit. For example, it may be 50% by mass or less, 30% by mass or less, or 25% by mass or less.

[0044] --By-products-- The chemicals obtained by the method for producing chemicals according to the first embodiment of this disclosure may contain by-products. Examples of by-products include paraffin, carbon, and hydrogen gas. The carbon as a by-product refers to a composition consisting only of carbon atoms, and examples include soot, graphite, and diamond.

[0045] There are no particular restrictions on the paraffin, but examples include aliphatic saturated hydrocarbons having 1 to 4 carbon atoms, with aliphatic saturated hydrocarbons having 2 to 4 carbon atoms being preferred. Examples of aliphatic saturated hydrocarbons having 1 to 4 carbon atoms include chain-like aliphatic saturated hydrocarbons having 1 to 4 carbon atoms.

[0046] Specific examples of paraffins include methane, ethane, propane, isobutane, and n-butane. Among these, the method for producing the chemicals described herein has a low selectivity for methane.

[0047] There are no particular restrictions on the total yield (mass%) of paraffins having 1 to 4 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 raw materials containing plastic. The lower limit of the total yield (mass%) of paraffins having 1 to 4 carbon atoms is preferable as low as possible, for example, 0.1% by mass or more relative to the raw materials containing plastic.

[0048] The yield of useful components and by-products contained in the chemical can be determined by analyzing the gaseous product, liquid substance, and residue obtained as the chemical by the chemical manufacturing method according to the first embodiment of this disclosure using gas chromatography (GC) equipped with a flame ionization detector.

[0049] When analyzing gaseous chemical products, 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.

[0050] Furthermore, when analyzing liquid substances as chemicals, the analysis can be performed using gas chromatography (GC) equipped with a flame ionization detector under the analytical conditions described in the examples, and each component can 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.

[0051] Furthermore, the content of by-products such as coking residues contained in chemical products can be calculated by burning the fluid material with air inside the reactor and measuring the weight change before and after air calcination.

[0052] <Flowing the fluid material S1> In flowing the fluid material S1, an inert gas is supplied to a reactor that has the longitudinal direction as the height direction and contains the fluid material inside, causing the fluid material to flow.

[0053] In the process of fluidizing the fluid material S1, it is preferable to supply the fluid material with an inert gas from a direction opposite to the direction of gravity in the longitudinal direction of the reactor.

[0054] The reactor is a reactor capable of accommodating a fluidized material and having a certain internal space to ensure a flow path for raw materials including plastics and inert gases, and is preferably a fluidized bed.

[0055] As for the shape, structure, and size of the reactor, there are no particular restrictions as long as the longitudinal direction is the height direction, and they can be appropriately selected according to the purpose. However, from the viewpoint of allowing smooth flow of raw materials containing plastics and chemicals, and ensuring sufficient contact time between the raw materials containing plastics and the fluid, it is preferable that the flow direction of the raw materials containing plastics is in the longitudinal direction.

[0056] The fluid material is placed in the internal space of the reactor. In this disclosure, "to make the fluid material flow" means to suspend the fluid material by passing an inert gas through it at a sufficient rate, thereby causing the fluid material to behave like a fluid. In such a reaction system, the fluid material may be referred to as "fluidized sand."

[0057] <<Flowing Material>> There are no particular restrictions on the flowing material as long as it can be made to flow with an inert gas, and it can be appropriately selected according to the purpose, but it is preferable that it does not react with the inert gas, and it is more preferable that it contains as a main component one selected from the group consisting of silicon dioxide, zirconium oxide, yttria-stabilized zirconium oxide, calcia-stabilized zirconium oxide, magnesium oxide, calcium oxide, silicon carbide, silicon nitride, silicon oxide, tantalum oxide, niobium oxide, beryllium oxide, lanthanum oxide, manganese(II) oxide, chromium(III) oxide, gallium oxide, forsterite, and cordierite.

[0058] In this disclosure, the “main component” of the fluid material means the component that accounts for the largest mass ratio of the total mass of the fluid material.

[0059] Furthermore, the fluid material 2 may be one in which the surface of the material is coated with ceramics such as tungsten oxide, molybdenum(VI) oxide, molybdenum disilicide, lanthanum chromium, triiron tetroxide, copper(I) oxide, tin dioxide, or indium oxide, so as to stabilize in the atmosphere when heating raw materials including plastic.

[0060] From the viewpoint of not hindering heat conduction between particles of the fluid material 2, the film thickness of the coating on the fluid material 2 is preferably 0.001 μm to 5 μm.

[0061] There are no particular limitations on the method for coating the surface of the fluid material 2. A known method can be appropriately selected depending on the material, shape, structure, and size of the fluid material 2. For example, a method of coating with a ceramic raw material such as tungsten oxide using a spray coating method, printing method, immersion method, dispenser coating method, etc. The fluid material 2 coated with the ceramic raw material can be fired using a known method to form a ceramic coating on its surface.

[0062] Furthermore, the fluid material 2 may be coated by a dry method such as physical vapor deposition, chemical vapor deposition, or sputtering, or the surface of the fluid material 2 itself may be oxidized to form an oxide film of the aforementioned thickness.

[0063] Furthermore, a catalyst suitable for the purpose of heat treatment may be supported on the surface of the fluid material 2. There are no particular restrictions on the type of catalyst, and examples include various zeolites and FCC (Fluid Catalytic Cracking) catalysts. The catalyst supported on the surface of the fluid material 2 may be an unused catalyst or a catalyst that has been used in heat treatment one or more times.

[0064] The structure of surface-treated fluid materials 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.

[0065] Among these, the fluidizing agent is preferably one that mainly contains silicon dioxide or a surface-treated version thereof. Examples of fluidizing agents that mainly contain silicon dioxide include silica sand. The fluidizing agent may be unused, or it may be a fluidizing agent that has been used in heat treatment once or more, or a fluidizing agent that has been regenerated by firing in air.

[0066] From the viewpoint of use in fluidized sand, the fluid material is preferably granular. The granular fluid material may be of a fixed shape or an irregular shape.

[0067] There are no particular restrictions on the particle size of the granular fluid material, and it can be appropriately selected according to the purpose. Examples include 1.7 mm to 0.2 mm, 1 mm to 0.1 mm, and 0.6 mm to 0.07 mm. These may be used individually or in combination of two or more. Among these, a particle size of 0.6 mm to 0.07 mm is preferred for the granular fluid material from the viewpoint of yielding the active ingredient. The particle size of the fluid material is measured by a sieving test (ISO 2591-1:1988).

[0068] There are no particular restrictions on the pore volume of the fluid material, and it can be appropriately selected depending on the purpose, but 0.0001 cm³ is a reasonable value. ３ / g or more 10cm ３ Preferably less than or equal to 0.0005 cm². ３ / g or more 9cm ３ It is more preferable to have less than or equal to 0.01 cm / g. ３ / g or more 8cm ３ A value of less than or equal to / g is even more preferable. The pore volume of the fluid material is 0.0001 cm³. ３ / g or more 8cm ３ A value of less than / g is preferable because it allows for the use of readily available materials and makes it easier to maintain a suitable flow state even during long-term operation. The pore volume of the fluid material is measured in accordance with ISO 15901-2:2006 and analyzed by the BET method.

[0069] There are no particular restrictions on the specific surface area of ​​the fluid material, and it can be appropriately selected depending on the purpose, but 0.1 m ２ / g or more 3,000m ２ Preferably less than 0.2 m ２ / g or more 2,000m ２ More preferably less than or equal to 0.3 m ２ / g or more 1,000m ２ A value of less than or equal to / g is even more preferable. The specific surface area of ​​the fluid material is 0.1 m². ２ / g or more 1,000m ２A value of less than / g is preferable because it allows for the use of readily available materials and makes it easier to maintain a suitable flow state even during long-term operation. The specific surface area of ​​the fluid material is measured in accordance with ISO 9277:2010 using a specific surface area measuring device (e.g., BELSORP® MAX II, manufactured by Microtrac-Bell Co., Ltd.) at liquid nitrogen temperature, with nitrogen molecules as the probe.

[0070] The fluid material may contain components other than the main component. There are no particular restrictions on the other components in the fluid material, and they can be appropriately selected depending on the purpose. However, it is preferable that they are materials that are stable in the temperature range of thermal decomposition when heated, are not reduced by by-products such as carbon and hydrogen produced by the thermal decomposition of plastics, and do not react with inert gases.

[0071] There are no particular restrictions on the content of other components in the fluid material; they can be appropriately selected depending on the purpose.

[0072] <<Inert Gas>> There are no particular restrictions on the inert gas, but a gas that is stable in the heating temperature range is preferred.

[0073] Specific examples of inert gases include nitrogen gas, water vapor, carbon dioxide, and noble gases. These may be used individually or in combination of two or more. Among these, at least one of nitrogen gas and water vapor is preferred as the inert gas due to its industrial availability and low cost, with nitrogen gas being more preferred.

[0074] Furthermore, from the viewpoint of preventing the generation of reaction residue, it is preferable that the inert gas contains water vapor. There are no particular restrictions on the water vapor content of the inert gas, but it is preferable that it contains 5% by volume or more, more preferably 7% by volume or more, and even more preferably 10% by volume or more. There are also no particular restrictions on the upper limit of the water vapor content of the inert gas; it may contain only water vapor, i.e., 100% by volume. However, from the viewpoint of preventing blockage of pipes due to condensation, it is preferable that it be 50% by volume or less, more preferably 40% by volume or less, and even more preferably 35% by volume or less.

[0075] The mass flow rate of the inert gas introduced into the reactor is not particularly limited as long as it satisfies the above equation 1, and can be appropriately selected according to the purpose.

[0076] <Heating S2> In heating S2, the fluid material is heated to 780°C or higher. Heating S2 may be performed separately from the fluidization of the fluid material S1, or it may be performed simultaneously with the fluidization of the fluid material S1.

[0077] There are no particular restrictions on the method of heating the fluid material, and it can be appropriately selected according to the purpose. It may be an external heating method in which the fluid material is heated by heat transfer from the outside, or an internal heating method in which the fluid material is heated by resistance heating using heat transfer wires or the like inside the reactor.

[0078] The heating temperature for the fluid material is 780°C or higher, preferably 800°C or higher, and more preferably 900°C or higher. If the heating temperature for the fluid material is below 780°C, the yield of useful components will be poor. There is no particular upper limit to the heating temperature for the fluid material, but it is preferably 1,200°C or lower, more preferably 1,000°C or lower, and even more preferably 980°C or lower. If the heating temperature for the fluid material is 1,200°C or lower, the generation of methane, a by-product of plastic decomposition that is difficult to utilize as a basic chemical, can be suppressed.

[0079] The upper and lower limits of the heating temperature for heating the fluid material can be combined as appropriate, but 780°C to 1,200°C is preferred, 800°C to 1,000°C is more preferred, and 900°C to 980°C is even more preferred.

[0080] <Supplying raw materials S3> In supplying raw materials S3, raw materials containing plastic are supplied to the fluid material which has been heated to 780°C or higher. As a result, the raw materials containing plastic are thermally decomposed, and at least one chemical product selected from the group consisting of olefins having 2 to 4 carbon atoms and aromatic hydrocarbons can be produced.

[0081] The supply of raw materials S3 may be performed separately from the fluidization of the fluid material S1 and the heating of the fluid, or it may be performed simultaneously with at least one of the fluidization of the fluid material S1 and the heating of the fluid. If the supply of raw materials S2 is performed separately from the fluidization of the fluid material S1 and the heating of the fluid, the supply of raw materials S2 is performed after the fluidization of the fluid material S1 and the heating of the fluid.

[0082] There are no particular restrictions on the method of supplying the raw material containing plastic to the fluid material; it may be supplied intermittently or continuously. Among these methods, continuous supply is preferred because it minimizes temperature changes in the heated fluid material.

[0083] When raw materials containing plastic are intermittently supplied to a fluid material, there are no particular restrictions on the supply time, non-supply time, or intervals between these.

[0084] When supplying raw materials containing plastic to a fluid material intermittently, there is no particular limit on the amount of raw materials containing plastic supplied at one time. However, when supplying raw materials containing plastic to a fluid material intermittently, from the viewpoint of preventing the temperature of the fluid material from dropping too low, it is preferable to wait until the temperature of the fluid material, which dropped during the previous supply, has recovered to the desired temperature before adding the raw materials containing plastic for the second time and beyond.

[0085] When supplying raw materials containing plastic to a fluid material continuously, there are no particular restrictions on the amount of raw materials containing plastic that can be supplied.

[0086] -Raw materials containing plastic- There are no particular restrictions on the type of plastic used in raw materials containing plastic, and they can be appropriately selected according to the purpose. Examples include mixed plastics containing polyolefins, aromatic plastics, and chlorine-containing plastics. These may be used individually or in combination of two or more types. Furthermore, raw materials containing plastic may also contain other components other than plastic as needed.

[0087] --Mixed Plastics-- There are no particular restrictions on the polyolefins included in the mixed plastics, and they can be appropriately selected depending on the purpose, but it is preferable that they include polyethylene (PE) and polypropylene (PP), which are commonly used in beverage and food containers, packaging materials, molded products, films, etc.

[0088] There are no particular restrictions on the polyolefin content in the raw materials containing plastics, and it can be appropriately selected depending on the purpose. However, it is preferably 50% to 90% by mass, more preferably 55% to 87% by mass, and even more preferably 60% to 85% by mass, relative to the total mass of the raw materials containing plastics.

[0089] --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.

[0090] --Chlorine-containing plastics-- There are no particular restrictions on chlorine-containing plastics, and they can be appropriately selected depending on the purpose, but it is preferable that they contain 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.

[0091] 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 50% by mass or less, more preferably 45% by mass or less, and even more preferably 40% by mass or less, relative to the total mass of the raw material containing the plastic. When the content of at least one selected from the group consisting of aromatic plastics and chlorine-containing plastics in the raw material containing the plastic is 50% by mass or less, useful components can be obtained efficiently in high yield. Furthermore, the lower the content of at least one selected from the group consisting of aromatic plastics and chlorine-containing plastics, the better. The lower limit may be, for example, 0.1% by mass or more, 0.5% by mass or more, 5% by mass or more, or 10% by mass or more.

[0092] --Other Components-- There are no particular restrictions on other components contained in raw materials containing plastics, and they can be appropriately selected depending on the purpose. Examples include other plastics other than polyolefins, aromatic plastics, and chlorine-containing plastics; and materials that are normally found in waste plastics such as paper and metal. These may be contained individually or in combination of two or more types.

[0093] Other plastics are not particularly limited and can be selected as appropriate depending on the purpose, and examples include polyamide, polyurethane, and polymethyl methacrylate.

[0094] There are no particular restrictions on the content of other components in the raw material containing plastic, and they can be appropriately selected depending on the type of raw material containing plastic used. However, from the viewpoint of the yield of the active ingredient, 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 the raw material containing plastic.

[0095] From the viewpoint of reducing environmental impact, it is preferable that the raw materials containing plastic include waste plastic. When the raw materials containing plastic are waste plastic, there are no particular restrictions on the composition and composition ratio, and they can be appropriately selected according to the purpose, but it is preferable that PE is 20% to 40% by mass, PP is 20% to 40% by mass, and PS is 10% to 30% by mass.

[0096] As waste plastics, for example, Refuse-derived paper and plastics-densified fuel (RPF) can be used.

[0097] The structure and content of each component in raw materials containing plastics can be determined by analysis using methods such as gel permeation chromatography (GPC), nuclear magnetic resonance (NMR), liquid chromatography-mass spectrometry (LC-MS), pyrolysis gas chromatography-mass spectrometry (PyGC-MS), and matrix-assisted laser desorption / ionization time-of-flight mass spectrometry (MALDI-TOFMS).

[0098] In supplying the raw materials (S3), there are no particular restrictions on the state of the plastic in the raw materials supplied to the fluid material, including crystalline, glassy, ​​rubbery, or liquid plastics. The plastic may also be in a decomposed state. Among these, rubbery or liquid plastics are preferred because they are easier to control the supply amount.

[0099] When the plastic is crystalline or glassy, ​​there are no particular restrictions on its form, and examples include crushed plastic, pellets of crushed plastic, and chips of crushed plastic.

[0100] There are no particular restrictions on the type of plastic used for the pulverized material; it can be appropriately selected depending on the purpose, for example, in powder or flake form.

[0101] 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."

[0102] 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.

[0103] 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 also decreases, so in practice, this can be determined by the melting temperature. The melting temperature is measured by the method specified in JIS K7121-2012.

[0104] 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, 85°C to 195°C is more preferred, and 90°C to 190°C is even more preferred.

[0105] These raw materials, including various forms of plastic, may be used after being processed separately from the chemical manufacturing method according to the first embodiment of this disclosure, or after being subjected to other processing described later.

[0106] <Recovering chemicals S4> In recovering chemicals S4, chemicals generated from the raw materials containing the plastic are recovered. There are no particular restrictions on the recovery method, and a method can be appropriately selected from known methods depending on the type of chemical obtained. For example, gaseous products may be separated by atmospheric pressure or pressurized distillation, and liquid hydrocarbons may be separated by atmospheric pressure or reduced pressure distillation.

[0107] <Other Processing> The method for producing the chemical product of this disclosure may further include, as necessary, other processing steps besides flowing the fluidizing agent S1, heating S2, supplying raw materials S3, and recovering the chemical product S4.

[0108] Figure 3 shows another example of a flowchart of a method for producing a chemical product according to the first embodiment of this disclosure.

[0109] Other processing methods are not particularly limited and can be selected as appropriate depending on the purpose. Examples include pre-treatment of raw materials containing plastics (S11), post-treatment of chemicals (S12), and separation of useful components (S13).

[0110] <<Pre-treatment S11>> In pre-treatment S11, the raw materials containing plastic are pre-treated before being supplied in S3. By pre-treating the raw materials containing plastic to make them easier to decompose, the plastic can be decomposed more efficiently.

[0111] Examples of pretreatment include crushing of raw materials containing plastic, pelletizing (chipping) of crushed raw materials containing plastic, melting of raw materials containing plastic, and pre-decomposition of raw materials containing plastic.

[0112] There are no particular restrictions on the pulverization process of raw materials containing plastic, and one method is to pulverize the raw materials containing plastic using a known pulverizer. There are no particular restrictions on the pulverized material of the raw materials containing plastic, and can be appropriately selected depending on the purpose, for example, in the form of powder or flakes.

[0113] There are no particular restrictions on the method for pelletizing (chipping) pulverized raw materials, including plastics. A suitable method can be selected from conventionally known methods. For example, one method involves melting and extruding the pulverized material, and then cutting the strand-shaped melted extruded material to obtain chipped raw materials.

[0114] There are no particular restrictions on the melting treatment of raw materials containing plastics, and any conventionally known method can be appropriately selected. For example, a method of continuously supplying the material to the decomposition process using a melt extruder can be used. It is preferable to perform the melting treatment of raw materials containing plastics at a temperature of less than 300°C.

[0115] There are no particular limitations on the pre-decomposition treatment of the plastic-containing raw material, but one example is treatment at a temperature above the decomposition temperature of the plastic (for example, above 200°C) but below 300°C. By pre-decomposing the plastic-containing raw material, it is possible to obtain partially decomposed plastic products from the plastic-containing raw material, although their molecular weight is higher than that of the chemicals described herein.

[0116] <<Post-treatment of chemicals S12>> Post-treatment of chemicals S12 is a process to decompose by-products in the chemicals generated by thermal decomposition of the raw materials containing plastic by heating S2. It is preferable to perform post-treatment of chemicals S12 after recovering the chemicals S4.

[0117] Post-treatment methods performed in S12, which involves post-treatment of chemical products, 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.

[0118] <<Separation of useful components S13>> In separation of useful components S13, only the useful components are separated from the chemicals recovered in chemical recovery S4. Separation of useful components S13 may be performed after chemical recovery S4, or after chemical recovery S4 and after chemical post-treatment S12.

[0119] In separating the useful components (S13), there are no particular restrictions on the method for separating the useful components from the by-products, and a method can be appropriately selected from known methods depending on the type of useful component or by-product obtained.

[0120] The chemical manufacturing method according to the first embodiment described above makes it possible to efficiently obtain at least one chemical selected from the group consisting of olefins having 2 to 4 carbon atoms and aromatic hydrocarbons in high yield. In particular, the chemical manufacturing method according to the first embodiment makes it possible to efficiently obtain chemicals containing ethylene and propylene in high yield. The manufactured chemicals can be used as basic chemicals suitable for chemical recycling.

[0121] [Second Embodiment] The method for producing a chemical product according to the second embodiment of the present disclosure includes supplying an inert gas to a reactor whose longitudinal direction is the height direction and which contains a fluid material inside, causing the fluid material to flow, heating the fluid material to 780°C or higher, supplying a raw material containing plastic to the fluid material heated to 780°C or higher, and recovering the chemical product produced from the raw material containing plastic, wherein the value Y (cm / sec) calculated by the following formula 2 satisfies Y ≥ 20. [Formula 2] Y = Gv / A However, in formula 2, Gv is the volumetric flow rate (Ncm) of the inert gas at 0°C and 1 atm ３ ( / second) is shown, and A is the cross-sectional area (cm²) inside the reactor in a cross-section perpendicular to the longitudinal direction at the lower end of the part of the reactor that houses the fluid material. ２ ) indicates.

[0122] If the reactor is cylindrical, then in formula 2, A can be calculated by formula 1-2 in the method for producing a chemical product according to the first embodiment of this disclosure.

[0123] In the method for producing chemicals according to the second embodiment of this disclosure, the yield of at least one chemical selected from the group consisting of olefins having 2 to 4 carbon atoms and aromatic hydrocarbons may vary depending on the flow state of the fluid material 2. The factor that most influences the flow state of the fluid material 2 is the inert gas that keeps the fluid material 2 in a flow state. Therefore, the numerical value Y (cm / second) calculated by the above formula 2 is effective as a parameter for the thermal decomposition of raw materials including plastics, and the method for producing chemicals according to the second embodiment of this disclosure can efficiently produce at least one chemical selected from the group consisting of olefins having 2 to 4 carbon atoms and aromatic hydrocarbons in high yield by satisfying Y ≥ 20.

[0124] In the method for producing chemicals according to the second embodiment of this disclosure, the difference from the method for producing chemicals according to the first embodiment of this disclosure is that the parameter for the thermal decomposition of raw materials including plastic is a numerical value X (cm) calculated by formula 1. ３ The only difference is that the value has been changed from (g / sec) to the numerical value Y (cm / sec) calculated by formula 2 above; all other aspects can be carried out in the same manner as the method for producing a chemical product according to the first embodiment of this disclosure.

[0125] The chemical manufacturing method according to the second embodiment described above allows for the efficient and high-yield production of at least one chemical selected from the group consisting of olefins having 2 to 4 carbon atoms and aromatic hydrocarbons. In particular, the chemical manufacturing method according to the second embodiment allows for the efficient and high-yield production of chemicals containing ethylene and propylene. The produced chemicals can be used as basic chemicals suitable for chemical recycling.

[0126] [Third Embodiment] The method for producing a chemical product according to the third embodiment of the present disclosure includes supplying an inert gas to a reactor whose longitudinal direction is the height direction and which contains a fluid material inside, causing the fluid material to flow, heating the fluid material to 780°C or higher, supplying a raw material containing plastic to the fluid material heated to 780°C or higher, and recovering the chemical product produced from the raw material containing plastic, wherein the value X (cm) is calculated by the following formula 1. ３The volume (cm / sec) satisfies X ≤ 500, and the value Y (cm / sec) calculated by the following formula 2 satisfies Y ≥ 20. [Formula 1] X = V / (Gm + Pm) where V is the volume (cm) of the part of the reactor's interior where the fluid material is contained and the volume above it. ３ The formula is given by: [Equation 2] Y = Gv / A where Gm is the mass flow rate (g / sec) of the inert gas and Pm is the mass flow rate (g / sec) of the raw material containing the plastic. ３ ( / second) is shown, and A is the cross-sectional area (cm²) inside the reactor in a cross-section perpendicular to the longitudinal direction at the lower end of the part of the reactor that houses the fluid material. ２ ) indicates.

[0127] Formula 1 is as described in the method for manufacturing a chemical product according to the first embodiment, and Formula 2 is as described in the method for manufacturing a chemical product according to the second embodiment.

[0128] The chemical manufacturing method according to the third embodiment described above makes it possible to efficiently obtain at least one chemical selected from the group consisting of olefins having 2 to 4 carbon atoms and aromatic hydrocarbons in high yield. In particular, the chemical manufacturing method according to the third embodiment makes it possible to efficiently obtain chemicals containing ethylene and propylene in high yield. The manufactured chemicals can be used as basic chemicals suitable for chemical recycling.

[0129] (Chemical Manufacturing Apparatus) The chemical manufacturing apparatus of this disclosure includes the following first, second, third, and fourth embodiments.

[0130] [First Embodiment] The chemical manufacturing apparatus according to the first embodiment of the present disclosure comprises: a reactor whose longitudinal direction is the height direction and which houses a fluid material inside; a raw material supply unit connected to the reactor and which supplies raw materials including plastic into the reactor; an inert gas supply unit connected to one end of the reactor in the longitudinal direction and which is arranged to supply inert gas to the fluid material from the direction opposite to the direction of gravity; a heating unit for heating the fluid material; a recovery unit for recovering the chemical product generated from the raw materials including plastic; and a control unit that controls the heating temperature by the heating unit and the amount of inert gas supplied by the inert gas supply unit, wherein the control unit controls the target temperature T of the fluid material to 780°C or higher, and the total volume V (cm³) inside the reactor. ３ ), any number X (cm) less than or equal to 500 based on the following formula 1. ３ An input / output unit that inputs and outputs the mass flow rate Pm (g / sec) of the raw material containing the plastic when the raw material containing the plastic is introduced into the reactor; a heating temperature control controller that controls the heating temperature of the heating unit to reach the target temperature T based on the input value of the target temperature T from the input / output unit; and the total volume V (cm³) from the input / output unit. ３ ), the aforementioned numerical value X (cm ３ The apparatus comprises a first calculation unit that calculates the mass flow rate Gm (g / sec) of the inert gas to be supplied to the reactor based on the following formula 1 from the input values ​​of the mass flow rate Pm (g / sec) and the mass flow rate Pm (g / sec), and a first inert gas supply amount controller that controls the supply of the inert gas from the inert gas supply unit at the mass flow rate Gm (g / sec) calculated by the first calculation unit. The chemical manufacturing apparatus according to the first embodiment of the present disclosure may further have other components as needed. [Formula 1] X = V / (Gm + Pm) However, in formula 1, V is the total volume inside the reactor (cm³) ３ The values ​​shown are Gm, where Gm represents the mass flow rate (g / second) of the inert gas, and Pm represents the mass flow rate (g / second) of the raw material containing the plastic.

[0131] The chemical manufacturing apparatus according to the first embodiment of this disclosure can suitably carry out the chemical manufacturing method according to the first embodiment of this disclosure. Accordingly, Formula 1 is as described in the section [First Embodiment] of (Chemical Manufacturing Method) of this disclosure.

[0132] Figure 4 is a schematic cross-sectional view showing an example of a chemical manufacturing apparatus according to the first embodiment of the present disclosure. Figure 5A is a partially enlarged view of the reactor in Figure 4, and is a schematic diagram along the line VA-VA in Figure 5B, showing an example of a cross-section parallel to the longitudinal direction of the reactor. Figure 5B is a schematic diagram along the line VB-VB in Figure 5A, showing an example of a cross-section perpendicular to the longitudinal direction of the reactor.

[0133] The chemical manufacturing apparatus (hereinafter sometimes abbreviated as "manufacturing apparatus 100") comprises a reactor 1, a fluidizing agent 2, a raw material supply unit 3, an inert gas supply unit 4, a heating unit 5, a control unit 6, and a recovery unit 7.

[0134] <Reactor 1> Reactor 1 is a component whose length is the height direction and which houses a fluid material 2 inside. In reactor 1, the fluid material 2 placed inside reactor 1 is heated by the heating unit 5, thereby heating the raw material M (hereinafter sometimes abbreviated as "raw material M") containing plastic that is supplied inside reactor 1.

[0135] The material of reactor 1 is not particularly limited as long as it is stable in terms of surface temperature and atmosphere on the inside of reactor 1, that is, on the side of reactor 1 where the raw materials M are contained. For example, alumina (Al ２ O ３ ), Zirconia (ZrO ２ ), silicon carbide (SiC), silicon nitride (Si ３ N ４ ), mullite (3Al ２ O ３ ・2SiO ２ Inorganic compounds such as SUS310S, Inconel (registered trademark), Hastelloy (registered trademark), and other alloys can be used.

[0136] The shape, structure, and size of the reactor 1 are not particularly limited as long as it can accommodate the fluid material 2 and allow the raw material M to flow through it, and can be appropriately selected according to the purpose.

[0137] Examples of the reactor 1's shape include cylindrical, rectangular parallelepiped, conical, frustoconical, and columnar, where the cross-sectional shape perpendicular to the longitudinal direction of the reactor 1 is polygonal.

[0138] In order to retain the fluid material 2 inside the reactor 1, it is preferable to install a stopper 10 through which an inert gas G such as quartz wool can be circulated, thereby sealing the inside of the reactor 1.

[0139] The structure, shape, material, and size of the stopper 10 are not particularly limited, as long as it does not allow the filler to pass through, but does allow the inert gas G, raw material M, or chemical product R to pass through. They can be appropriately selected according to the purpose, and examples include quartz wool, a mesh, a screen, and a dispersion plate. These may be used individually or in combination of two or more types.

[0140] <Fluidized Material 2> Fluidized material 2 is placed in the internal space of reactor 1. When the manufacturing apparatus 100 is in operation, inert gas G is supplied to the fluidized material 2 from an inert gas supply unit 4, which is connected to one end of the reactor 1 in the longitudinal direction and is positioned to supply inert gas G to the fluidized material 2 from the direction opposite to the direction of gravity. As a result, the inert gas G passes through the fluidized material 2 at a sufficient speed, causing the fluidized material 2 to be suspended and function as fluidized sand.

[0141] The fluid material 2 can be the one described in the section (Method of Manufacturing Chemical Products) of this disclosure.

[0142] <Raw Material Supply Unit 3> The raw material supply unit 3 is connected to the reactor 1 and is a component that supplies raw material M containing plastic into the reactor 1. Examples of the raw material supply unit 3 include a raw material distribution unit 3a through which the raw material M containing plastic flows, and a raw material input unit 3b that puts the raw material M containing plastic into the reactor 1.

[0143] In this disclosure, "connection" of the raw material supply unit 3 to the reactor 1 means that the inside of the raw material flow section 3a of the raw material supply unit 3 and the inside of the reactor 1 are in communication so that the raw material M can pass through them.

[0144] 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 reactor 1, depending on the purpose.

[0145] 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.

[0146] The location of the raw material supply unit 3 is not particularly limited as long as it can be connected to the reactor 1 and supply raw material M to the fluid material 2. It can be appropriately selected depending on the type of raw material M, but it is preferable that it be located in a position where the raw material M is supplied from above the fluid material 2. Figure 4 shows the raw material supply unit 3 being located on the upper surface in the longitudinal direction of the reactor 1, but it may also be located on the side of the reactor 1.

[0147] The raw materials M, including plastic, used in the manufacturing apparatus 100 are as described in the section (Method of Manufacturing Chemicals) of this disclosure.

[0148] <Inert Gas Supply Unit 4> The inert gas supply unit 4 is connected to one end of the reactor 1 in the longitudinal direction and is positioned to supply inert gas to the fluid material 2 from the direction opposite to the direction of gravity. Examples of the inert gas supply unit 4 include an inert gas flow unit 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.

[0149] In this disclosure, "connecting" the inert gas supply unit 4 to one end of the reactor 1 in the longitudinal direction means that the inside of the inert gas flow section 4a of the inert gas supply unit 4 and the inside of the reactor 1 are in communication with each other at one end of the reactor 1 in the longitudinal direction, allowing the inert gas G to pass through.

[0150] 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 the reactor 1, depending on the purpose.

[0151] 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.

[0152] When the chemical manufacturing equipment is not in operation, the fluid material 2 usually accumulates in the internal space of the reactor 1 due to its own weight. That is, the direction of accumulation of the fluid material 2 is in the direction of gravity. In order to position the inert gas supply unit 4 to supply inert gas to the fluid material 2 from the direction opposite to the direction of gravity in the internal space of the reactor 1, it is preferable to position the inert gas supply unit 4 below the position where the fluid material 2 is placed in the reactor 1, in the direction of gravity. Figure 4 shows the inert gas supply unit 4 being placed on the lower surface in the longitudinal direction of the reactor 1, but it may also be placed on the side of the reactor 1.

[0153] As for the type of inert gas G, those described in the section (Method of Manufacturing Chemical Products) of this disclosure can be used.

[0154] <Heating Unit 5> The heating unit 5 is a component that heats the fluidized material 2. There are no particular restrictions on the heating unit 5, and it is an external heating method that heats the fluidized bed by heat transfer from the outside. As the heating unit 5 of the external heating method, for example, a known electric furnace can be used.

[0155] The temperature of reactor 1 can be measured by inserting a thermocouple into the center of the fluid material 2.

[0156] <Control Unit 6> The control unit 6 controls the heating temperature by the heating unit 5 and the amount of inert gas G supplied by the inert gas supply unit 4. The control unit 6 may also control other processes of the manufacturing apparatus 100.

[0157] Figure 6 is a functional block diagram showing an example of a control unit for a chemical manufacturing apparatus according to the first embodiment of this disclosure.

[0158] The control unit 6 comprises an input / output unit 61, a heating temperature control controller 62a, a first calculation unit 63, and a first inert gas supply amount controller 62b. The heating temperature control controller 62a and the first inert gas supply amount controller 62b are included in the controller 62. The controller 62 may also have controllers for controlling other components.

[0159] Furthermore, the control unit 6 may have other components. Examples of other components in the control unit 6 include a CPU (central processing unit) 64, memory 65, display unit 66, communication unit 67, and storage unit 68.

[0160] <<Input / Output Unit 61>> The input / output unit 61 consists of an operation panel, keyboard, etc., for the operator to perform various operations such as inputting various data and outputting various data to a predetermined storage medium.

[0161] The input / output unit 61 is a target temperature T input / output unit 61a that inputs and outputs a target temperature T of 780°C or higher for the fluid material 2, and the total internal volume V (cm³) of the reactor 1 is also included. ３ The total volume V input / output section 61b inputs and outputs ) and any numerical value X (cm) less than or equal to 500 based on the above formula 1. ３ The system preferably includes a numerical X input / output unit 61c that inputs and outputs (g / second), and a mass flow rate Pm input / output unit 61d that inputs and outputs the mass flow rate Pm (g / second) of the raw material M containing plastic when the raw material M containing plastic is introduced into the reactor 1.

[0162] The target temperature T information in the target temperature T input / output unit 61a, the total volume V information in the total volume V input / output unit 61b, the numerical value X information in the numerical value X input / output unit 61c, and the mass flow rate Pm information in the mass flow rate Pm input / output unit 61d are input by the operator.

[0163] <<Controller 62>> The controller 62 controls the operation of various components. The controller 62 includes a heating temperature control controller 62a and a first inert gas supply amount controller 62b.

[0164] - Heating Temperature Control Controller 62a - The heating temperature control controller 62a is a component that controls the heating temperature of the heating unit 5 to reach the target temperature T, based on the input value of the target temperature T at the input / output unit 61a.

[0165] Preferably, the heating temperature control controller 62a receives a signal based on the input value of the target temperature T in the target temperature T input / output unit 61a and a signal based on the temperature of the fluid material 2 in the reactor 1 actually measured by a temperature measuring unit such as a thermocouple, and feedback controls the heating temperature of the heating unit 5 using PID (Proportional-Integral-Differental) control or on-off control so as to heat the fluid material 2 to a constant temperature of the target temperature T.

[0166] -First inert gas supply amount controller 62b- The first inert gas supply amount controller 62b is a component that controls the supply of inert gas G from the inert gas supply unit 4 at a mass flow rate Gm (g / second) calculated by the first calculation unit 63, which will be described later.

[0167] The first inert gas supply controller 62b preferably receives a signal based on the input value of the mass flow rate Gm (g / sec) calculated by the first calculation unit 63 and a signal based on the amount of inert gas G supplied into the reactor 1, which is actually measured by an inert gas supply rate measuring unit such as a gas flow meter, and feedback controls the amount of inert gas G supplied by the inert gas supply unit 4 using PID (Proportional-Integral-Differental) control or on-off control so as to keep the mass flow rate Gm calculated by the first calculation unit 63 constant.

[0168] <<First Calculation Unit 63>> The first calculation unit 63 calculates the total volume V (cm) from the input / output unit 61. ３ ), numerical value X (cm ３ This component calculates the mass flow rate Gm (g / second) of the inert gas G supplied to the reactor 1 based on the input values ​​of the gas flow rate (g / second) and the mass flow rate Pm (g / second), according to the above formula 1.

[0169] More specifically, the first calculation unit 63 calculates the total volume V of the input / output unit 61 and the total volume V (cm) of the input / output unit 61b. ３ The input value of ) and the numerical value X (cm) from the numerical X input / output unit 61c. ３ Based on the input value of mass flow rate Pm (g / sec) and the input value of mass flow rate Pm (g / sec) from the mass flow rate Pm input / output unit 61d, the mass flow rate Gm (g / sec) of the inert gas G supplied to the reactor 1 is calculated according to formula 1.

[0170] The signal based on the mass flow rate Gm calculated by the first calculation unit 63 is sent to the first inert gas supply controller 62b.

[0171] <<CPU 64>> The CPU 64 reads various programs and data necessary for program execution from the storage unit 68 as needed and uses them.

[0172] <<Memory 65>> Memory 65 is used for various processes performed by the CPU 64.

[0173] <<Display Unit 66>> The display unit 66 is a liquid crystal display that displays the operation screen, selection screen, etc. of the manufacturing device 100.

[0174] <<Communication Unit 67>> The communication unit 67 handles data exchange via networks, etc.

[0175] <<Storage Unit 68>> The storage unit 68 consists of a hard disk (HDD) and the like that stores various programs executed by the CPU 64 and processing recipe data 68a necessary for the execution of those programs.

[0176] <Recovery Unit 7> The recovery unit 7 is a component that recovers chemical products R generated from raw materials M, including plastic. The recovery unit 7 may consist of only one unit or two or more units.

[0177] There are no particular restrictions on the structure, shape, material, and size of the recovery unit 7, and they can be appropriately selected according to the purpose and type of product, including known containers.

[0178] Furthermore, the recovery unit 7 may contain a solvent capable of separating the 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 liquid products.

[0179] The useful components in the gaseous product can be suitably separated by further pressurized distillation.

[0180] <Other Components> Other components are not particularly limited as long as they do not impair the effectiveness of the chemical manufacturing apparatus according to the first embodiment of this disclosure. Examples include a chemical product R extraction unit 8, a cooling unit 9, a storage unit 11, a measuring unit for measuring the yield of useful components, a pre-processing unit, a post-processing unit, a separation unit, and so on.

[0181] <<Removal Section 8>> The removal section 8 is connected to the reactor 1 and is a component that removes the chemical product R produced from the raw material M containing plastic from the reactor 1.

[0182] In this disclosure, "connection" of the extraction unit 8 to the reactor 1 means that the inside of the extraction unit 8 and the inside of the reactor 1 are in communication so that the chemical product R can pass through them.

[0183] There are no particular restrictions on the material of the extraction section 8; for example, it can be appropriately selected from the same materials as those used for the reactor 1, depending on the purpose.

[0184] The shape, structure, and size of the extraction section 8 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 8.

[0185] The location of the extraction unit 8 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 4 shows the extraction unit 8 positioned on the upper side of the reactor 1 in the Y-axis direction, but the extraction unit 8 may be positioned anywhere on the side of the reactor 1 as long as the chemical R can be extracted from the reactor 1, or it may be positioned on the top surface of the reactor 1.

[0186] <<Cooling Section 9>> The cooling section 9 is a component that cools the chemical product R obtained after passing through the reactor 1. By cooling the chemical product R, the liquid components in the product can be recovered within the cooling section.

[0187] The cooling unit 9 is preferably positioned between the extraction unit 8 and the recovery unit 7. That is, the cooling unit 9 is preferably connected to the extraction unit 8 in one part and to the recovery unit 7 in another part.

[0188] In this disclosure, "connection" of the cooling unit 9 to the extraction unit 8 means that the interior of the cooling unit 9 and the interior of the extraction unit 8 are in communication so that the chemical product R can pass through them. Furthermore, "connection" of the cooling unit 9 to the recovery unit 7 means that the interior of the cooling unit 9 and the interior of the recovery unit 7 are in communication so that the chemical product R can pass through them.

[0189] Examples of the cooling section 9 include a cooling trap 9a for cooling the chemical product 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 product R, and can be appropriately selected according to the purpose.

[0190] 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 8 is placed in the organic solvent 9c so that the chemical R (e.g., the generated gas) bubbles in the organic solvent 9c.

[0191] The useful components dissolved in a non-aqueous solvent can be suitably separated by further distillation at atmospheric pressure.

[0192] 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.

[0193] <<Storage section 11>> The storage section 11 is a component for storing raw materials M, including plastic.

[0194] The structure, shape, material, and size of the storage section 11 are not particularly limited as long as it can store raw materials M including plastic, and can be appropriately selected according to the purpose.

[0195] There are no particular restrictions on the number of storage units 11; there may be one or more. If the manufacturing apparatus 100 has multiple storage units 11, for example, it can be used to store plastics containing polyolefin and at least one selected from the group consisting of aromatic plastics and chlorine-containing plastics, where the composition and content of each component differ.

[0196] <<Measurement Unit>> The measurement unit is a component that measures the yield of useful components contained in the chemical product R manufactured by the manufacturing apparatus 100.

[0197] The measuring unit may be located inside the manufacturing apparatus 100, or it may be connected to and provided outside the manufacturing apparatus 100.

[0198] The measuring unit is not particularly limited as long as it can measure the yield of useful components contained in the chemical product R, and any known measuring device may be used. Examples of known measuring devices include flame ionization detectors (FIDs) and gas chromatography equipped with thermal conduction detectors (TCDs).

[0199] 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.

[0200] <<Pre-processing section>> The pre-processing section is a component that pre-processes the raw material M, which includes plastic. It is preferable that the pre-processing section is connected to the raw material supply section 3.

[0201] In this disclosure, "connecting" the pre-processing unit to the raw material supply unit 3 means that the inside of the pre-processing unit and the inside of the raw material supply unit 3 are in communication so that the raw material M can pass through them.

[0202] The pre-processing unit performs, for example, the task of transforming the plastic contained in the raw material M into a form or state that is easily decomposed.

[0203] There are no particular restrictions on the material of the pre-treatment section; for example, it can be appropriately selected from the same materials as those used for reactor 1, depending on the purpose.

[0204] The shape, structure, and size of the pre-processing unit are not particularly limited as long as it can be connected to the raw material supply unit 3 and perform pre-processing on the raw material M. They can be appropriately selected according to the purpose, and examples include cylindrical and rectangular parallelepiped shapes.

[0205] <<Post-processing section>> The post-processing section is a component that decomposes unwanted components such as by-products from the chemical product R. It is preferable that the post-processing section is connected to the recovery section 7.

[0206] In this disclosure, "connection" of the post-processing unit to the recovery unit 7 means that the inside of the post-processing unit and the inside of the recovery unit 7 are in communication with each other in a manner that allows the chemical product R to pass through.

[0207] The post-processing unit performs tasks such as removing paraffin, halogens, etc., generated from the plastic contained in the raw material M.

[0208] There are no particular restrictions on the material of the post-processing section; for example, it can be appropriately selected from the same materials as those used for reactor 1, depending on the purpose.

[0209] The shape, structure, and size of the post-processing unit are not particularly limited as long as it can be connected to the recovery unit 7 and decompose unwanted components in the chemical product R. They can be appropriately selected according to the purpose, for example, cylindrical or rectangular.

[0210] <<Separation Processing Unit>> The separation processing unit is a component that separates useful components from the chemical product R recovered in the recovery unit 7. It is preferable that the separation processing unit is connected to the recovery unit 7 or the post-processing unit.

[0211] In this disclosure, "connection" of the separation processing unit to the recovery unit 7 or post-processing unit means that the interior of the post-separation processing unit and the interior of the recovery unit 7 or post-processing unit are in communication with each other in a manner that allows the chemical product R to pass through.

[0212] There are no particular restrictions on the material of the separation processing unit; for example, it can be appropriately selected from the same materials as those used for reactor 1, depending on the purpose.

[0213] The shape, structure, and size of the separation processing unit are not particularly limited as long as it can be connected to the recovery unit 7 or the post-processing unit and separate useful components from the chemical product R. They can be appropriately selected according to the purpose, for example, a cylindrical shape or a rectangular parallelepiped.

[0214] The separation unit includes, for example, a pressurized distillation apparatus. This separates the useful components from the chemical product R. For example, if the chemical product R contains at least one chemical selected from the group consisting of olefins having 2 to 4 carbon atoms and aromatic hydrocarbons, these useful components can be suitably separated from the chemical product R by pressurized distillation.

[0215] Next, a specific example of the operation of the chemical manufacturing apparatus 100 according to the first embodiment will be described.

[0216] Next, an example of the operation of the manufacturing apparatus 100 will be described. The manufacturing apparatus 100, for example, introduces an inert gas G from the inert gas supply unit 4 into the fluidized material 2 in the reactor 1, thereby converting the fluidized material in the chemical manufacturing method of this disclosure into a fluidized bed. Then, the heating unit 5 heats the reactor 1 to a desired temperature, thereby performing the heating in the chemical manufacturing method of this disclosure. While the reactor 1 is being heated by the heating unit 5, the raw material M, which includes plastic and is stored in the storage unit 11, is supplied to the reactor 1 by the raw material supply unit 3, thereby performing the supply in the chemical manufacturing method of this disclosure. The reactor 1 is a fluidized bed reactor in the chemical manufacturing method of this disclosure.

[0217] 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 recovery unit 7 in the chemical product manufacturing method of this disclosure.

[0218] The chemicals produced by the manufacturing apparatus 100 of this disclosure are as described in the section (Method of Manufacturing Chemicals) of this disclosure.

[0219] Next, an example of the operation of the chemical manufacturing apparatus 100 according to the first embodiment of this disclosure will be described. The manufacturing apparatus 100 performs the fluidization of the fluidized material in the chemical manufacturing method of this disclosure, S1, by supplying inert gas G from the inert gas supply unit 4 to the fluidized material 2 inside the reactor 1. At this time, the amount of inert gas G supplied to the fluidized material 2 inside the reactor 1 is the mass flow rate Gm (g / second) calculated by the first calculation unit 63 based on the information input to the operator at the input / output unit 61.

[0220] Then, the heating unit 5 heats the fluid material 2 inside the reactor 1 to a desired temperature, thereby performing heating S2 in the chemical manufacturing method of this disclosure. At this time, the heating temperature by the heating unit 5 is the target temperature T input to the operator at the input / output unit 61. Based on the input value of the target temperature T at the input / output unit 61a, the heating temperature control controller 62a controls the heating temperature of the heating unit 5 to reach the target temperature T. The target temperature T is set to 780°C or higher.

[0221] Next, while heating the reactor 1 to a target temperature T by the heating unit 5, the raw material M containing plastic stored in the storage unit 11 is supplied to the reactor 1 by the raw material supply unit 3, thereby performing the supply of raw materials S3 in the chemical manufacturing method of this disclosure. At this time, the amount of raw material M supplied is supplied to the fluid material 2 inside the reactor 1 at a mass flow rate Pm (g / second) of raw material M based on information input to the operator by the input / output unit 61.

[0222] The chemical product R containing the useful components obtained by heating is recovered in the recovery unit 7. Preferably, the chemical product R containing the useful components obtained by heating is removed from the reactor 1 by the removal unit 8, and recovered in the recovery unit 7 via the cooling unit 9. In the recovery unit 7, preferably the removal unit 8, the cooling unit 9, and the recovery unit 7, the chemical product S4 in the chemical product manufacturing method of this disclosure can be recovered.

[0223] When chemical product R is transferred to the cooling trap 9a of the cooling unit 9, first, chemical product R is cooled in the cooling unit 9, which contains organic solvent 9c cooled by the refrigerant 9d in the insulation unit 9b. As a result, components in chemical product R that can dissolve in the organic solvent 9c are condensed in the organic solvent 9c. On the other hand, components in chemical product R that do not dissolve in the organic solvent 9c are transferred directly to the recovery unit 7. This allows the target components to be recovered in the organic solvent 9c and in the recovery unit 7.

[0224] If necessary, the raw material M is subjected to a pre-treatment process S11 in the method for producing chemicals according to the present disclosure before being supplied to the reactor 1. The chemical product R recovered in the recovery unit 7 is subjected to a post-treatment process S12 in the method for producing chemicals according to the present disclosure. The chemical product R recovered in the recovery unit 7 or the chemical product R from which unwanted components have been decomposed in the post-treatment process is subjected to a separation process S13 in the method for producing chemicals according to the present disclosure to separate the useful components.

[0225] The chemical production apparatus according to the first embodiment described above can efficiently produce at least one chemical selected from the group consisting of olefins having 2 to 4 carbon atoms and aromatic hydrocarbons in high yield. In particular, the chemical production apparatus according to the first embodiment can efficiently produce chemicals containing ethylene and propylene in high yield.

[0226] [Second Embodiment] The chemical manufacturing apparatus according to the second embodiment of the present disclosure comprises: a reactor whose longitudinal direction is the height direction and which houses a fluid material inside; a raw material supply unit connected to the reactor and which supplies raw materials including plastic into the reactor; an inert gas supply unit connected to one end of the reactor in the longitudinal direction and which is arranged to supply inert gas to the fluid material from the direction opposite to the direction of gravity; a heating unit for heating the fluid material; a recovery unit for recovering the chemical product generated from the raw materials including plastic; and a control unit that controls the heating temperature by the heating unit and the amount of inert gas supplied by the inert gas supply unit, wherein the control unit controls the target temperature T of the fluid material to 780°C or higher, and the cross-sectional area A (cm²) of the inside of the reactor in a cross section perpendicular to the longitudinal direction of the reactor. ２ An input / output unit that inputs and outputs the cross-sectional area A (cm / sec) and 20 or more arbitrary numerical values ​​Y (cm / sec) based on the following formula 2; a heating temperature control controller that controls the heating temperature of the heating unit to reach the target temperature T based on the input value of the target temperature T from the input / output unit; and the input / output unit that inputs the cross-sectional area A (cm / sec) ２ ) and the input value of the above numerical value Y (cm / sec) are used to calculate the volumetric flow rate of the inert gas (Ncm) based on the following formula 2. ３ A second calculation unit calculates the volume flow rate Gv (Ncm² / second) calculated by the second calculation unit, and the volume flow rate Gv (Ncm² / second) ３ The apparatus comprises a second inert gas supply rate controller that controls the supply of the inert gas from the inert gas supply unit at a rate of ( / second). The chemical manufacturing apparatus according to the second embodiment of the present disclosure may further have other components as needed. [Equation 2] Y = Gv / A However, in Equation 2, Gv is the volume flow rate of the inert gas at 0°C and 1 atm (Ncm² / second) ３ ( / second) is shown, and A is the cross-sectional area (cm²) inside the reactor in a cross-section perpendicular to the longitudinal direction at the lower end of the part of the reactor that houses the fluid material. ２ ) indicates.

[0227] The chemical manufacturing apparatus according to the second embodiment of this disclosure can suitably carry out the chemical manufacturing method according to the second embodiment of this disclosure.

[0228] The chemical manufacturing apparatus according to the second embodiment of this disclosure has the same configuration as the chemical manufacturing apparatus according to the first embodiment of this disclosure, except for the control unit 6. The following describes the differences between the chemical manufacturing apparatus according to the second embodiment of this disclosure and the chemical manufacturing apparatus according to the first embodiment of this disclosure.

[0229] <Control Unit 6> The control unit 6 controls the heating temperature by the heating unit 5 and the amount of inert gas G supplied by the inert gas supply unit 4. The control unit 6 may also control other processes of the manufacturing apparatus 100.

[0230] Figure 7 is a functional block diagram showing an example of a control unit for a chemical manufacturing apparatus according to the second embodiment of this disclosure.

[0231] The control unit 6 comprises an input / output unit 61, a heating temperature control controller 62a, a second calculation unit 70, and a second inert gas supply amount controller 72b. The heating temperature control controller 62a and the second inert gas supply amount controller 72b are included in the controller 62. The controller 62 may also have controllers for controlling other components.

[0232] Furthermore, the control unit 6 may have other components. Examples of other components in the control unit 6 include a CPU (central processing unit) 64, memory 65, display unit 66, communication unit 67, and storage unit 68. These other components in the control unit 6 are the same as those in the chemical manufacturing apparatus according to the first embodiment of this disclosure.

[0233] <<Input / Output Unit 61>> The input / output unit 61 consists of an operation panel, keyboard, etc., for the operator to perform various operations such as inputting various data and outputting various data to a predetermined storage medium.

[0234] The input / output unit 61 is a target temperature T input / output unit 61a that inputs and outputs a target temperature T of 780°C or higher for the fluid material 2, and the cross-sectional area A (cm²) inside the reactor 1 in a cross section perpendicular to the longitudinal direction of the reactor 1. ２ The system preferably includes a cross-sectional area A input / output unit 71b that inputs and outputs ) and a numerical value Y input / output unit 71c that inputs and outputs 20 or more arbitrary numerical values ​​Y (cm / second) based on the above formula 2.

[0235] The target temperature T information in the target temperature T input / output unit 61a, the cross-sectional area A information in the cross-sectional area A input / output unit 71b, and the numerical value Y (cm / sec) information in the numerical value Y input / output unit 71c are input by the operator.

[0236] <<Controller 62>> The controller 62 controls the operation of various components. The controller 62 includes a heating temperature control controller 62a and a second inert gas supply amount controller 72b. The heating temperature control controller 62a is the same as that of the chemical manufacturing apparatus according to the first embodiment of this disclosure.

[0237] - Second inert gas supply controller 72b - The second inert gas supply controller 72b controls the volume flow rate Gv (Ncm) calculated by the second calculation unit 70, which will be described later. ３ This component controls the supply of inert gas G from the inert gas supply unit 4 at a rate of ( / second).

[0238] The second inert gas supply controller 72b controls the volumetric flow rate Gv (Ncm²) calculated by the second calculation unit 70. ３ Preferably, the system takes in a signal based on the input value ( / second) and a signal based on the amount of inert gas G supplied into the reactor 1, which is actually measured by an inert gas supply rate measuring unit such as a gas flow meter, and uses PID (Proportional-Integral-Differental) control or on-off control to feedback control the amount of inert gas G supplied by the inert gas supply unit 4 so as to keep the volumetric flow rate Gv calculated by the second calculation unit 70 constant.

[0239] <<Second Calculation Unit 70>> The second calculation unit 70 calculates the cross-sectional area A (cm²) by the input / output unit 61. ２ Based on the input values ​​of ) and the numerical value Y (cm / sec), the volumetric flow rate Gv (Ncm) of the inert gas G supplied to the reactor 1 is calculated according to Equation 2. ３ This is a component that calculates (per second).

[0240] More specifically, the second calculation unit 70 calculates the cross-sectional area A of the input / output unit 61 and the cross-sectional area A (cm²) of the input / output unit 71b. ２Based on the input value of ) and the input value of numerical Y (cm / sec) from the numerical Y input / output unit 71c, the volumetric flow rate Gv (Ncm) of the inert gas G supplied to the reactor 1 is calculated according to formula 2. ３ Calculate (per second).

[0241] The signal based on the volumetric flow rate Gv calculated by the second calculation unit 70 is sent to the second inert gas supply controller 72b.

[0242] Next, an example of the operation of the chemical manufacturing apparatus 100 according to the second embodiment of this disclosure will be described. The manufacturing apparatus 100 performs the fluidization of the fluidized material in the chemical manufacturing method of this disclosure, S1, by supplying inert gas G from the inert gas supply unit 4 to the fluidized material 2 inside the reactor 1. At this time, the amount of inert gas G supplied is calculated by the second calculation unit 70 based on the information input to the operator in the input / output unit 61, and the volume flow rate Gv (Ncm) ３ It is supplied to the fluid material 2 inside reactor 1 at a rate of ( / second).

[0243] Then, the heating unit 5 heats the fluid material 2 inside the reactor 1 to a desired temperature, thereby performing heating S2 in the chemical manufacturing method of this disclosure. At this time, the heating temperature by the heating unit 5 is the target temperature T input to the operator at the input / output unit 61. Based on the input value of the target temperature T at the input / output unit 61a, the heating temperature control controller 62a controls the heating temperature of the heating unit 5 to reach the target temperature T. The target temperature T is set to 780°C or higher.

[0244] Next, while heating the reactor 1 to a target temperature T using the heating unit 5, the raw material M containing plastic stored in the storage unit 11 is supplied to the reactor 1 by the raw material supply unit 3, thereby performing the supply of raw materials in the method for producing chemicals according to this disclosure S3.

[0245] [Third Embodiment] The manufacturing apparatus for chemicals according to the third embodiment of the present disclosure has a reactor with its longitudinal direction as the height direction and accommodating a fluid material therein, a raw material supply unit connected to the reactor for supplying a raw material containing plastic into the interior of the reactor, an inert gas supply unit connected to one end of the reactor in the longitudinal direction and arranged to supply an inert gas to the fluid material from a direction opposite to the gravitational direction, a heating unit for heating the fluid material, a recovery unit for recovering the chemicals generated from the raw material containing plastic, and a control unit for controlling the heating temperature by the heating unit and the supply amount of the inert gas by the inert gas supply unit. The control unit has an input / output unit for performing input / output of a target temperature T of 780 °C or higher of the fluid material, the total volume V (cm ３ ), an arbitrary numerical value X (cm ３ / g / sec) of 500 or less based on the following formula 1, the mass flow rate Pm (g / sec) of the raw material containing plastic when the raw material containing plastic is introduced into the reactor, the cross-sectional area A (cm ２ ) of the interior of the reactor in a cross-section perpendicular to the longitudinal direction of the reactor, and an arbitrary numerical value Y (cm / sec) of 20 or more based on the following formula 2; a heating temperature adjustment controller for controlling the heating temperature of the heating unit to be the target temperature T from the input value of the target temperature T by the input / output unit; a first calculation unit for calculating the mass flow rate Gm (g / sec) of the inert gas to be supplied to the reactor based on the following formula 1 from the input values of the total volume V (cm ３ ), the numerical value X (cm ３ / g / sec), and the mass flow rate Pm (g / sec) by the input / output unit; a second calculation unit for calculating the volume flow rate (Ncm ２ / sec) of the inert gas based on the following formula 2 from the input values of the cross-sectional area A (cm ３ ) and the numerical value Y (cm / sec) by the input / output unit; a first inert gas supply amount controller for controlling the supply of the inert gas from the inert gas supply unit at the mass flow rate Gm (g / sec) calculated by the first calculation unit; the volume flow rate Gv (Ncm ３The apparatus comprises a second inert gas supply rate controller that controls the supply of the inert gas from the inert gas supply unit at a rate of (cm³ / second). The chemical manufacturing apparatus according to the third embodiment of the present disclosure may further have other components as needed. [Formula 1] X = V / (Gm + Pm) where V is the total volume (cm³) inside the reactor ３ The formula is given by: [Equation 2] Y = Gv / A where Gm is the mass flow rate (g / sec) of the inert gas and Pm is the mass flow rate (g / sec) of the raw material containing the plastic. ３ ( / second) is shown, and A is the cross-sectional area (cm²) inside the reactor in a cross-section perpendicular to the longitudinal direction at the lower end of the part of the reactor that houses the fluid material. ２ ) indicates.

[0246] The chemical manufacturing apparatus according to the third embodiment of this disclosure can suitably carry out the chemical manufacturing method according to the third embodiment of this disclosure. Accordingly, formulas 1 and 2 are as described in the section on the [Third Embodiment] of the (Chemical Manufacturing Method) of this disclosure.

[0247] Figure 8 is a functional block diagram showing an example of a control unit for a chemical manufacturing apparatus according to the third embodiment of this disclosure.

[0248] The chemical manufacturing apparatus according to the third embodiment of this disclosure differs from the chemical manufacturing apparatus according to the first embodiment and the chemical manufacturing apparatus according to the second embodiment in that the control unit 6 comprises an input / output unit 61, a heating temperature control controller 62a, a first calculation unit 63, a second calculation unit 70, a first inert gas supply amount controller 62b, and a second inert gas supply amount controller 72b.

[0249] [Fourth Embodiment] The chemical manufacturing apparatus according to the fourth embodiment differs from the chemical manufacturing apparatus according to the first embodiment, the chemical manufacturing apparatus according to the second embodiment, or the chemical manufacturing apparatus according to the third embodiment in that the heating unit 5 uses an internal heating method.

[0250] FIG. 9A is a schematic cross-sectional view showing an example of a chemical production apparatus according to the fourth embodiment. FIG. 9B is a partially enlarged view of the reactor in FIG. 9A.

[0251] By energizing a resistor as the heating unit 5 such as a heating wire, the resistor can be heated, and the fluid material around it can be heated.

[0252] In the chemical production apparatus according to the fourth embodiment, the upper end of the resistor becomes the upper end of the heating unit 5. Therefore, the distance L (cm) is defined from the lower end of the portion where the fluid material 2 is accommodated to the height that coincides with the upper end of the heating unit 5.

[0253] Hereinafter, the embodiments will be described more specifically with reference to examples and comparative examples, but the embodiments are not limited to these examples and comparative examples.

[0254] (Example 1) <Preparation of Apparatus> The production apparatus 100 shown in FIGS. 4, 5A, and 5B was prepared. Specifically, a sieve was installed in a cylindrical quartz tube with an inner diameter of 15 mm and a height of 550 mm as the reactor 1, quartz wool was laid, and the stopper 10 was arranged. Then, silica sand No. 6 (trade name: Ube silica sand No. 6, particle size: 0.6 mm to 0.07 mm, specific surface area: 1.3 m ２ / g, pore volume: 3.5×10 －３ cm ３5 g of (manufactured by Ube Sand Industries Co., Ltd.) was added. A quartz tube was placed inside a cylindrical electric furnace (product name: ARF-30MC, manufactured by Asahi Rika Seisakusho Co., Ltd.) which was installed vertically. The quartz tube was positioned so that the distance L from the upper end of the stopper 10, i.e., the lower end of the fluid material 2, to the upper end of the area in which the reactor 1 of the electric furnace can be heated was 16.1 cm. The electric furnace is an external heating type heating section 5. A manual powder feeding device (airless feed cock, manufactured by Asahi Seisakusho Co., Ltd.) as the raw material input section 3b of the raw material supply section 3 and one end of a gas extraction pipe as the extraction section 8 for extracting gas as chemical product R were connected to the upper part of the quartz tube. In addition, a gas inlet as the inert gas supply section 4 was connected to the lower part of the quartz tube. 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 installed in the cooling section 9b, which contained 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) which served as the recovery section 7. A thermocouple for controlling the electric furnace was brought into contact with the outer surface of the quartz tube. Since the diameter of the quartz tube is very small, the temperature of the outer surface of the quartz tube and the temperature of the fluid material 2 can be considered to be equal.

[0255] <Heating S2> The electric furnace temperature was set to 800°C and the heating was started, and the fluid material 2 inside the electric furnace was heated to 800°C.

[0256] <S1 Fluidizing the fluid material and S3 supplying the raw materials> After the electric furnace reaches the set temperature of 800°C and the temperature stabilizes, the volumetric flow rate of nitrogen gas from the gas inlet is set to 3,200 Ncm². ３While introducing the material at a rate of one minute, RPF1, with the following composition, was supplied into a quartz tube from a manual powder dispenser as raw material M containing plastic, over a period of 5.0 minutes. The total amount of RPF1 supplied to the fluid material 2 was 0.8 g. [Composition of RPF1] ・ PE ... 28 mass% ・ PP ... 29 mass% ・ PS ... 15 mass% ・ PET ... 13 mass% ・ PVC ... 1 mass% ・ PVDC ... 1 mass% ・ Other organic polymers ... 7 mass% ・ Organic low molecular weight components ... 4 mass% ・ Inorganic substances ... 2 mass% (Total: 100 mass%)

[0257] The mass flow rate (Pm) of the RPF at this time is 2.67 × 10⁻⁶. －３ The flow rate was set to g / second (0.16 g / min). The mass flow rate (Gm) of nitrogen gas was 6.67 × 10⁻⁶ －２ Assuming a flow rate of g / second, the volumetric flow rate (Gv) of nitrogen gas is 53.33 Ncm². ３ It was set to per second.

[0258] <Recovering chemicals S4> Subsequently, the liquid component of chemical R was recovered in the cooling trap 9a, and the gaseous component of chemical R was collected in the gas bag, which is the recovery unit 7. Five minutes after the RPF supply ended, the gas bag was disconnected from the manufacturing apparatus 100. The cooling trap 9a was also returned to room temperature (25°C ± 5°C) and left for approximately three minutes before being disconnected from the manufacturing apparatus 100.

[0259] In Example 1, the value X calculated by formula 1 is 379.4 cm. ３ The value was / g / second. In addition, in Example 1, the value Y calculated by formula 2 was 30.2 cm / second.

[0260] (Example 2 and Comparative Examples 1-4) Except for changing the decomposition conditions of RPF1 in Example 1 to the conditions shown in Table 1, RPF1 was decomposed in the same manner as in Example 1, and the liquid and gaseous components as chemical product R were recovered.

[0261] (Examples 3-6 and Comparative Examples 5-6) In Example 1, the raw material M was changed from RPF1 to RPF2 with the following composition, and silica sand No. 6 was used as the fluidizing agent 2. ２ / g, pore volume: 3.6 × 10 －３ cm ３ Except for changing the amount of 7g of (manufactured by Ube Sand Industries Co., Ltd.) used and further changing the RPF2 decomposition conditions to those shown in Table 2, RPF2 was decomposed in the same manner as in Example 1, and the liquid and gaseous components as chemical product R were recovered. [Composition of RPF2] ・PE ... 27% by mass ・PP ... 27% by mass ・PS ... 19% by mass ・PET ... 14% by mass ・PVC ... 2% by mass ・Cellulose ... 5% by mass ・Aluminum foil ... 2% by mass ・Calcium carbonate ... 2% by mass ・Polyamide ... 2% by mass (Total: 100% by mass)

[0262] (Example 7) In Example 4, the gas introduced was changed from nitrogen gas to a mixture of water vapor and nitrogen, and the decomposition conditions for RPF2 were changed to the conditions shown in Table 3. Except for these changes, RPF2 was decomposed in the same manner as in Example 4, and the liquid and gaseous components as chemical product R were recovered. The volume ratio of the water vapor and nitrogen mixture was set to water vapor:nitrogen = 17:83 (v / v).

[0263] (Example 8) Except for changing the decomposition conditions of RPF2 in Example 4 to the conditions shown in Table 3, RPF2 was decomposed in the same manner as in Example 4, and the liquid and gaseous components as chemical product R were recovered.

[0264] <<Analysis of Fluidized Materials>> The BET specific surface area of ​​silica sand No. 6 and silica sand No. 5 was measured in accordance with ISO 9277:2010 using a specific surface area analyzer (BELSORP® MAX II, manufactured by Microtrac-Bell Co., Ltd.) at liquid nitrogen temperature, with nitrogen molecules as the probe.

[0265] Furthermore, the pore volumes of silica sand No. 6 and silica sand No. 5 were measured in accordance with ISO 15901-2:2006 and analyzed using the BET method.

[0266] The particle size values ​​for silica sand No. 6 and silica sand No. 5 are those disclosed by the manufacturer.

[0267] <<Analysis of Gas Bag Contents>> In Examples 1-7 and Comparative Examples 1-6, the yield (mass%) of useful components and by-products in the pyrolysis gas recovered in the gas bag was determined by the following method.

[0268] In the gas bag, cyclopentane (>98.0%, density 0.75 g / cm³) was used 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 ratio of the peak area of ​​cyclopentane to the peak area of ​​each component was used to determine the proportion of each component (Cmol%) relative to carbon atoms in the pyrolysis gas in the gas bag. The mass of each component in 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 raw material M was determined. The results are shown in Tables 1 and 2. [GC Analysis Conditions] • Instrument: Nexus GC-2030 (Shimadzu Corporation) • Column: Rt-Alumina BOND (Diameter: 0.32 mm, Length: 30 m, Restek) • Carrier gas type: Ar • Carrier gas flow rate: 360 mL / min • Injection temperature: 200°C • Sample injection volume: 1 mL • Split ratio: 1 / 200 • Column temperature: Held at 120°C for 9 minutes, then increased to 200°C at 10°C / min, and held at 200°C for 30 minutes. • Detector: Flame ionization detector (FID) • Detector temperature: 200°C

[0269] <<Analysis of Cooling Trap Contents>> In Examples 1 to 8 and Comparative Examples 1 to 6, the yield (mass%) of useful components and by-products in the pyrolysis components recovered in the cooling trap 9a was determined by the following method.

[0270] The contents of cooling trap 9a 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 ratio of the peak area of ​​cyclopentane to the peak area of ​​each component was used to determine the carbon-carbon-based percentage (Cmol%) of each component in the pyrolysis components in cooling trap 9a. The mass of each component in the pyrolysis components in cooling trap 9a was calculated from this value and the amount of cyclopentane (0.3 g) added to the sample vial, and the yield (mass%) relative to the raw material M was determined. The results are shown in Tables 1 and 2. [GC Analysis Conditions] • Instrument: Nexus GC-2030 (Shimadzu Corporation) • Column: DB-1 (Diameter: 0.25 mm, Length: 30 m, Agilent Technology) • Carrier Gas Type: He • Carrier Gas Flow Rate: 97 mL / min • Injection Temperature: 350°C • Sample Injection Volume: 1 μL • Split Ratio: 1 / 50 • Column Temperature: Temperature increase program set in the following order: 35°C (10 mins) → Increase (5°C / min) → 350°C (10 mins) • Detector: Flame Ionization Detector (FID) • Detector Temperature: 350°C

[0271] In Tables 1 to 3, "Yield of useful components" and "Yield of by-products" refer to the ratio of the total number of moles of carbon atoms in each product listed in Tables 1 and 2 to the number of moles (Cmol) of carbon atoms contained in RPF1 or RPF2 as raw material M.

[0272] Furthermore, in Tables 1 to 3, "total yield of useful components" is the ratio of the total mass of carbon-2 to carbon-4 olefins and useful aromatic hydrocarbons in the product to the mass of RPF1 or RPF2 added. "Useful components" refers to carbon-4 olefins (ethylene and acetylene), carbon-3 olefins (propylene), carbon-4 olefins (trans-2-butene, 1-butene, 2-methylpropene, cis-2-butene, 1,3-butadiene, and isobutene), and useful aromatic hydrocarbons (benzene, toluene, ethylbenzene, three positional isomers of xylene (p-xylene, m-xylene, and o-xylene), and styrene).

[0273] In Table 3, "Molar mass of inert gas (M)" indicates the volume-weighted average of the molar masses of each gas in the mixed gas when a mixture of two inert gases is used.

[0274]

[0275]

[0276]

[0277] From the comparison between Examples 1 and 2 and Comparative Examples 1 to 4, or from the comparison between Examples 3 to 6 and Comparative Examples 5 to 6, the numerical value X (cm) calculated by formula 1 above is obtained. ３ It was found that when the yield (g / sec) satisfies X ≤ 500, and / or when the value Y (cm / sec) calculated by formula 2 satisfies Y ≥ 20, the yield of at least one chemical selected from the group consisting of olefins and aromatic hydrocarbons having 2 to 4 carbon atoms is improved, and in particular, the yields of ethylene and propylene are improved.

[0278] <<Measurement of Reaction Residue Amount>> RPF2 was decomposed using the same apparatus, raw materials, and decomposition conditions as in Examples 4, 7, and 8, and the liquid and gaseous components as chemical product R were recovered. However, before preparing the apparatus, the quartz tube as reactor 1, the strainer and quartz wool as stopper 10, silica sand No. 6 as fluidizing agent 2, and the gas extraction piping as extraction unit 8 in the manufacturing apparatus 100 were weighed in advance, and then the manufacturing apparatus 100 was assembled. The masses of each component of the manufacturing apparatus 100 before the decomposition of RPF2 were totaled to obtain the pre-decomposition mass "M1" (g). Next, after decomposing RPF2 using the same method as in Examples 4, 7, and 8, the quartz tube, strainer, quartz wool, silica sand No. 6, and gas extraction piping were removed. Each of the removed components of the manufacturing apparatus 100 was heated in an oven at 80°C for 1 hour to evaporate the water adhering to each component. Next, each component of the drying manufacturing apparatus 100 was cooled to 25°C and weighed. At this time, the masses of each component of the manufacturing apparatus 100 after the disassembly of RPF2 were totaled and defined as the disassembly mass "M2" (g). The mass of the raw materials introduced into the apparatus was defined as "M3" (g). Next, the reaction residue (mass%) was calculated based on the following formula 3. The results are shown in Table 4 below. [Formula 3] Reaction residue (mass%) = (M2 - M1) / M3 × 100

[0279]

[0280] 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.

[0281] This international application claims priority under Japanese Patent Application No. 2024-226818, filed on 23 December 2024, which is incorporated herein by reference to the entire contents of Japanese Patent Application No. 2024-226818.

[0282] 1...Reactor 2...Fluiding material 3...Raw material supply unit 3a...Raw material distribution unit 3b...Raw material input unit 4...Inert gas supply unit 4a...Inert gas distribution unit 4b...Pump 5...Heating unit 6...Control unit 7...Recovery unit 8...Delivery unit 9...Cooling unit 9a...Cooling trap 9b...Insulation unit 9c...Organic solvent 9d...Refrigerant 10...Stopper 11...Storage unit 61...Input / Output unit 61a...Target temperature T input / output unit 61b...Total volume V input / output unit 61c...Numerical value X input / output unit 61d...Mass flow rate Pm input / output unit 62...Controller 62a...Heating temperature control controller 62b...First inert gas supply amount controller 63...First calculation unit 64...CPU 65...Memory 66...Display unit 67...Communication unit 68...Storage unit 68a...Processing recipe data 70...Second calculation unit 71b...Cross-sectional area A input / output unit 72b...Second inert gas supply controller 100...Manufacturing equipment

Claims

1. A method for producing a chemical product, comprising: supplying an inert gas to a reactor whose longitudinal direction is the height direction and which contains a fluid material inside, causing the fluid material to flow; heating the fluid material to 780°C or higher; supplying a raw material containing plastic to the fluid material heated to 780°C or higher; and recovering the chemical product produced from the raw material containing plastic, wherein the value X (cm) is calculated by the following formula 1. ３ A method for producing a chemical product, characterized in that the flow rate (g / second) satisfies X ≤ 500. [Formula 1] X = V / (Gm + Pm) where V is the volume (cm³) of the part of the reactor where the fluid material is contained and the volume above it. ３ The values ​​shown are Gm, where Gm represents the mass flow rate (g / second) of the inert gas, and Pm represents the mass flow rate (g / second) of the raw material containing the plastic.

2. A method for producing a chemical product according to claim 1, wherein the value Y (cm / sec) calculated by the following formula 2 satisfies Y ≥ 20. [Formula 2] Y = Gv / A However, in formula 2, Gv is the volumetric flow rate (Ncm) of the inert gas at 0°C and 1 atm. ３ ( / second) is shown, and A is the cross-sectional area (cm²) inside the reactor in a cross-section perpendicular to the longitudinal direction at the lower end of the part of the reactor that houses the fluid material. ２ ) indicates.

3. A method for producing a chemical product, comprising: supplying an inert gas to a reactor whose longitudinal direction is the height direction and which contains a fluid material inside, causing the fluid material to flow; heating the fluid material to 780°C or higher; supplying a raw material containing plastic to the fluid material heated to 780°C or higher; and recovering the chemical product produced from the raw material containing plastic, wherein the value Y (cm / sec) calculated by the following formula 2 satisfies Y ≥ 20. [Formula 2] Y = Gv / A However, in formula 2, Gv is the volumetric flow rate (Ncm) of the inert gas at 0°C and 1 atm ３ ( / second) is shown, and A is the cross-sectional area (cm²) inside the reactor in a cross-section perpendicular to the longitudinal direction at the lower end of the part of the reactor that houses the fluid material. ２ ) indicates.

4. A method for producing a chemical product according to any one of claims 1 to 3, wherein the raw material containing the plastic includes waste plastic.

5. A method for producing a chemical product according to any one of claims 1 to 4, wherein the raw material containing the plastic contains 50% by mass or more of polyolefin.

6. A method for producing a chemical product according to any one of claims 1 to 5, wherein the fluid material mainly comprises one selected from the group consisting of silicon dioxide, zirconium oxide, yttria-stabilized zirconium oxide, calcia-stabilized zirconium oxide, magnesium oxide, calcium oxide, silicon carbide, silicon nitride, silicon oxide, tantalum oxide, niobium oxide, beryllium oxide, lanthanum oxide, manganese(II) oxide, chromium(III) oxide, gallium oxide, forsterite, and cordierite.

7. A method for producing a chemical product according to any one of claims 1 to 6, wherein the chemical product comprises ethylene and propylene.

8. The method according to any one of claims 1 to 7, wherein, in the process of fluidizing, the inert gas is supplied to the fluid material from a direction opposite to the direction of gravity in the longitudinal direction of the reactor.

9. A chemical manufacturing apparatus, comprising: a reactor having a longitudinal direction as a height direction and accommodating a fluid material therein; a raw material supply unit connected to the reactor and supplying a raw material containing plastic into the reactor; an inert gas supply unit connected to one end of the reactor in the longitudinal direction and arranged to supply an inert gas to the fluid material from a direction opposite to the gravitational direction; a heating unit for heating the fluid material; a recovery unit for recovering the chemical produced from the raw material containing plastic; and a control unit for controlling the heating temperature by the heating unit and the supply amount of the inert gas by the inert gas supply unit. The control unit includes: an input / output unit that inputs and outputs a target temperature T of 780 °C or higher of the fluid material, the total internal volume V (cm ３ ), any value X of 500 or less based on the following formula 1 (cm ３ / g / sec), and the mass flow rate Pm (g / sec) of the raw material containing plastic when the raw material containing plastic is introduced into the reactor; a heating temperature adjustment controller that controls the heating temperature of the heating unit to be the target temperature T from the input value of the target temperature T by the input / output unit; a first calculation unit that calculates the mass flow rate Gm (g / sec) of the inert gas to be supplied to the reactor based on the following formula 1 from the input values of the total internal volume V (cm ３ ), the value X (cm ３ / g / sec), and the mass flow rate Pm (g / sec) by the input / output unit; and a first inert gas supply amount controller that controls the supply of the inert gas from the inert gas supply unit at the mass flow rate Gm (g / sec) calculated by the first calculation unit. A chemical manufacturing apparatus characterized by comprising the above. [Formula 1] X = V / (Gm + Pm) However, in the above formula 1, V represents the total internal volume (cm ３ ) of the reactor, Gm represents the mass flow rate (g / sec) of the inert gas, and Pm represents the mass flow rate (g / sec) of the raw material containing plastic.

10. A chemical manufacturing apparatus comprising: a reactor whose longitudinal direction is the height direction and which contains a fluid material inside; a raw material supply unit connected to the reactor and which supplies raw materials including plastic into the reactor; an inert gas supply unit connected to one end of the reactor in the longitudinal direction and which is arranged to supply inert gas to the fluid material from the direction opposite to the direction of gravity; a heating unit for heating the fluid material; a recovery unit for recovering the chemical product produced from the raw materials including plastic; and a control unit for controlling the heating temperature by the heating unit and the amount of inert gas supplied by the inert gas supply unit, wherein the control unit controls the target temperature T of the fluid material of 780°C or higher, and the cross-sectional area A (cm²) of the inside of the reactor in a cross section perpendicular to the longitudinal direction of the reactor. ２ An input / output unit that inputs and outputs the cross-sectional area A (cm / sec) and 20 or more arbitrary numerical values ​​Y (cm / sec) based on the following formula 2; a heating temperature control controller that controls the heating temperature of the heating unit to reach the target temperature T based on the input value of the target temperature T from the input / output unit; and the input / output unit that inputs the cross-sectional area A (cm / sec) ２ ) and the input value of the above numerical value Y (cm / sec) are used to calculate the volumetric flow rate (Ncm) of the inert gas at 0°C and 1 atmosphere based on the following formula 2. ３ A second calculation unit calculates the volume flow rate Gv (Ncm²) calculated by the second calculation unit at 0°C and 1 atmosphere. ３ A chemical manufacturing apparatus comprising: a second inert gas supply rate controller that controls the supply of the inert gas from the inert gas supply unit at a rate of ( / second); and [Equation 2] Y = Gv / A where Gv is the volume flow rate of the inert gas at 0°C and 1 atm (Ncm² / second). ３ The value is the length of the reactor (cm²), and A is the cross-sectional area (cm²) inside the reactor in a cross-section perpendicular to the longitudinal direction of the reactor. ２ ) indicates.

Images