Method for producing monocyclic aromatic hydrocarbon, terephthalic acid, and polyethylene terephthalate, and method for managing same

Abstract

Provided is a method with which it is possible to produce a monocyclic aromatic hydrocarbon such as benzene or xylene, which is effective as a base material, using a naphtha raw material containing renewable naphtha. A method for producing a monocyclic aromatic hydrocarbon, which uses a naphtha raw material containing renewable naphtha to produce at least one monocyclic aromatic hydrocarbon selected from benzene and xylene, said method comprising: a step (A-1) in which the naphtha raw material is thermally cracked in the presence of water vapor to produce toluene and separate the toluene; and a step (A-2) in which toluene is subjected to a disproportionation reaction or a transalkylation reaction to produce and separate at least one monocyclic aromatic hydrocarbon selected from benzene and xylene.

Description

Technical Field

[0001] The present invention relates to a method for producing monocyclic aromatic hydrocarbons, terephthalic acid (including high-purity terephthalic acid) and polyethylene terephthalate (hereinafter sometimes referred to as PET). In addition, the present invention relates to a method for producing monocyclic aromatic hydrocarbons and terephthalic acid and a method for managing polyethylene terephthalate. Background Art

[0002] Benzene is the basic raw material for styrene monomer, phenol, cyclohexane, etc., which are processed into chemical products such as plastics, synthetic rubber, nylon, etc., and are used in various occasions of daily necessities such as plastic products and clothing. In addition, paraxylene is also the basic raw material for terephthalic acid, which is processed into polyester fibers, etc., and is used in various occasions of daily necessities.

[0003] The demand for these useful basic raw materials such as benzene and paraxylene is increasing.

[0004] However, in view of the current trend of decarbonization, the trend of pursuing green raw materials in the petrochemical industry is also spreading rapidly. From the perspective of retaining petroleum resources for sustainable development and reducing carbon dioxide emissions, a method is being actively developed by replacing part or all of the petroleum-derived raw materials used as raw materials for chemical products with biomass raw materials (for example, waste cooking oil, tall oil (a byproduct of pulp and paper) and other biologically derived oils and fats, etc.), and recyclable raw materials to develop basic raw materials derived from renewable raw materials, and processing them to produce chemical products derived from renewable raw materials.

[0005] A method is disclosed in which petroleum-derived naphtha and bio-naphtha are used together and thermally cracked in the presence of steam to produce propane and propylene (for example, see Patent Document 1).

[0006] As a method for producing a base raw material derived from a renewable raw material, there is known a method for producing propane and propylene described in Patent Document 1, but there is no known method for producing benzene and p-xylene derived from a renewable raw material.

[0007] Prior art literature

[0008] Patent Literature

[0009] Patent Document 1: Japanese Patent Application No. 2016-501124 Summary of the invention

[0010] Bio-naphtha has a composition close to that of a light fraction of petroleum-derived naphtha, and can be thermally cracked in the presence of water vapor.

[0011] When the above-mentioned thermal cracking is carried out using bio-naphtha as a raw material, xylene is produced. However, since the content rate of ethylbenzene as a by-product is high, it is not suitable as a raw material for producing paraxylene.

[0012] On the other hand, paraxylene is produced by hydrodesulfurizing heavy naphtha obtained by distilling crude oil, performing a catalytic reforming reaction to obtain ortho-xylene and meta-xylene, and isomerizing them.

[0013] Thus, the material generally used as a raw material for the catalytic reforming reaction is heavy naphtha, and light naphtha and bio-naphtha having a composition close to light naphtha are generally not used as a raw material for the catalytic reforming reaction.

[0014] That is, the conventional chemical industrial processes known in the past are not methods for producing benzene and para-xylene (hereinafter, benzene and para-xylene are also collectively referred to as monocyclic aromatic hydrocarbons) which are effective basic raw materials using bio-naphtha, and are unable to provide monocyclic aromatic hydrocarbons derived from bio-naphtha.

[0015] Therefore, an object of the present invention is to provide a method for producing monocyclic aromatic hydrocarbons such as benzene and p-xylene which are effective as base raw materials using a naphtha raw material including renewable naphtha.

[0016] In addition, an object of the present invention is to provide a method for managing monocyclic aromatic hydrocarbons that can be used when producing monocyclic aromatic hydrocarbons using a naphtha feedstock containing the above-mentioned renewable naphtha, wherein the management method allocates the value of the monocyclic aromatic hydrocarbon products as renewable products based on the content ratio of the renewable naphtha contained in the naphtha feedstock.

[0017] The present inventors have conducted research to solve the above-mentioned problems and have found that by providing a new chemical industrial process by combining reaction steps that are not usually combined in existing chemical industrial processes, the above-mentioned problems can be solved, thereby completing the present invention having the following gist.

[0018] That is, the present invention includes the following contents.

[0019] [1] A method for producing monocyclic aromatic hydrocarbons, comprising producing at least one of benzene and xylene using a naphtha feedstock containing renewable naphtha, comprising:

[0020] Step (A-1), generating toluene by thermally cracking the naphtha raw material in the presence of water vapor and separating the toluene; and

[0021] In step (A-2), toluene is subjected to a disproportionation reaction or a transalkylation reaction to produce at least one monocyclic aromatic hydrocarbon of benzene and xylene, and the resulting mixture is separated.

[0022] [2] The production method according to [1], wherein in the step (A-1), components containing monocyclic aromatic hydrocarbons in the thermal cracking product obtained by thermally cracking the naphtha feedstock in the presence of water vapor are separated and purified by distillation or extraction, thereby generating and separating toluene.

[0023] [3] The production method according to [1] or [2], further comprising: step (A-3) of separating paraxylene by adsorption separation or crystallization separation of the xylene obtained in the above step (A-2).

[0024] [4] The production method according to [3], which includes the following steps: isomerizing the residue containing at least one of o-xylene and m-xylene after separating p-xylene in the above step (A-3) to produce p-xylene, and then separating p-xylene by adsorption separation or crystallization separation.

[0025] [5] The production method according to any one of [1] to [4], wherein the monocyclic aromatic hydrocarbon contains a radioactive carbon atom. 14 C.

[0026] [6] A type of xylene containing radioactive carbon atoms 14 C.

[0027] [7] The xylene according to [6], wherein the radioactive carbon atom 14 C comes from bio-naphtha.

[0028] [8] A method for producing terephthalic acid using a naphtha feedstock containing renewable naphtha, comprising:

[0029] Step (A-3), obtaining p-xylene by the method described in [3] or [4], and

[0030] In step (A-4), terephthalic acid is obtained by oxidizing p-xylene.

[0031] [9] A form of terephthalic acid containing radioactive carbon atoms 14 C.

[0032]

[10] The terephthalic acid according to [9], wherein the radioactive carbon atom 14 C comes from bio-naphtha.

[0033]

[11] A method for producing polyethylene terephthalate using a naphtha feedstock containing renewable naphtha, comprising:

[0034] Step (A-4), obtaining terephthalic acid by the method described in [8], and

[0035] In step (A-5), polyethylene terephthalate is obtained by a condensation reaction of terephthalic acid and ethylene glycol.

[0036]

[12] A polyethylene terephthalate containing radioactive carbon atoms derived from bio-naphtha 14 C.

[0037]

[13] A method for managing monocyclic aromatic hydrocarbons, for use when producing at least one monocyclic aromatic hydrocarbon selected from benzene and xylene using a naphtha feedstock comprising renewable naphtha,

[0038] The management method is a method of allocating the value of the at least one monocyclic aromatic hydrocarbon as a renewable product according to the content ratio of the renewable naphtha contained in the naphtha raw material,

[0039] The management method comprises at least one step selected from the group consisting of a step (V) of confirming the production of xylene and / or benzene, and a step (W) of confirming the production of p-xylene.

[0040] The above step (V) includes the following step (V-1), the following step (V-2) and the following step (V-3),

[0041] The step (V-1) is a step of confirming that toluene is produced from the naphtha feedstock fed into a device (steam cracker) for thermal cracking in the presence of water vapor.

[0042] The step (V-2) is a step of confirming that xylene and / or benzene is produced from toluene fed to the disproportionation unit or fed to the transalkylation (TA) unit together with the C9-based components.

[0043] The step (V-3) is a step of confirming that xylene and / or benzene is produced from the naphtha feedstock by sequentially treating with the device for thermal cracking in the presence of water vapor (steam cracker), the disproportionation device or the transalkylation (TA) device,

[0044] The above step (W) includes the following step (V-1), the following step (V-2), the following step (W-3) and the following step (W-4),

[0045] The step (V-1) is a step of confirming that toluene is produced from the naphtha feedstock fed into a device (steam cracker) for thermal cracking in the presence of water vapor.

[0046] The step (V-2) is a step of confirming that xylene and / or benzene is produced from toluene fed to the disproportionation unit or fed to the transalkylation (TA) unit together with the C9-based components.

[0047] The step (W-3) is a step of confirming that paraxylene is obtained from the xylene fed into the paraxylene device.

[0048] The step (W-4) is a step of confirming that paraxylene is obtained from the naphtha feedstock by sequentially treating with the device for thermal cracking in the presence of water vapor (steam cracker), the disproportionation device or the transalkylation (TA) device, and the paraxylene device.

[0049] When the management method includes the step (V) and the step (W), the management method includes the step (Z) of confirming the ratio of the product to which the value as the renewable product is allocated,

[0050] The above step (Z) includes the following step (Z-1), the following step (Z-2), the following step (Z-3) and the following step (Z-4).

[0051] The step (Z-1) is a step of selecting one or more products from among the products obtained from the disproportionation unit or the transalkylation (TA) unit and the para-xylene unit to be distributed as renewable products.

[0052] The step (Z-2) is a step of determining a value of a ratio (P) of the product selected in the step (Z-1) to be allocated as a renewable product relative to the ratio of the product obtained from the disproportionation unit or the transalkylation (TA) unit and the paraxylene unit,

[0053] The step (Z-3) is a step of obtaining the value of the content ratio (Q) of the renewable naphtha contained in the naphtha raw material.

[0054] The step (Z-4) is a step of comparing the value of the ratio (P) with the value of the content ratio (Q) to confirm that the value of the ratio (P) is equal to or less than the value of the content ratio (Q).

[0055]

[14] The management method according to

[13] , wherein when the management method includes the step (V) but does not include the step (W), the management method includes the step (X) of confirming the proportion of the product to which the value is allocated as a renewable product,

[0056] The above step (X) includes the following step (X-1), the following step (X-2), the following step (X-3) and the following step (X-4).

[0057] The step (X-1) is a step of selecting one or more products from among the products generated by the disproportionation unit or the transalkylation (TA) unit to be distributed as renewable products.

[0058] The step (X-2) is a step of determining a value of a ratio (P) of the product selected in the step (X-1) to be allocated as a renewable product relative to the ratio of the product generated by the disproportionation unit or the transalkylation (TA) unit,

[0059] The step (X-3) is a step of obtaining the value of the content ratio (Q) of the renewable naphtha contained in the naphtha raw material.

[0060] The step (X-4) is a step of comparing the value of the ratio (P) with the value of the content ratio (Q) to confirm that the value of the ratio (P) is equal to or less than the value of the content ratio (Q).

[0061]

[15] The management method according to

[13] , wherein when the management method includes the step (W) but does not include the step (V), the management method includes the step (Y) of confirming the proportion of the product to which the value is allocated as a renewable product,

[0062] The above-mentioned step (Y) includes the following step (Y-1), the following step (Y-2), the following step (Y-3) and the following step (Y-4).

[0063] The step (Y-1) is a step of selecting one or more products to be distributed as renewable products from among the products obtained from the paraxylene unit.

[0064] The step (Y-2) is a step of determining a value of a ratio (P) to be allocated as a renewable product in the ratio of the product selected in the step (Y-1) to the product obtained from the paraxylene unit.

[0065] The step (Y-3) is a step of obtaining the value of the content ratio (Q) of the renewable naphtha contained in the naphtha raw material.

[0066] The step (Y-4) is a step of comparing the value of the ratio (P) with the value of the content ratio (Q) to confirm that the value of the ratio (P) is equal to or less than the value of the content ratio (Q).

[0067]

[16] A management method according to any one of

[13] to

[15] , wherein in the step (X-1), the step (Y-1) or the step (Z-1), when two or more products are selected to be allocated as the renewable products, the value of the proportion (P) allocated as the renewable product determined in the step (X-2), the step (Y-2) or the step (Z-2) is the value obtained by summing up the proportions allocated to the two or more selected products.

[0068]

[17] The management method according to

[13] , wherein the management method comprises the step (V) and the step (W), and in the step (Z-1), when the products to be distributed as the renewable products are benzene and para-xylene,

[0069] The value of the ratio (P) allocated as a renewable product determined in the above step (Z-2) is a value obtained by summing the ratio (P1) and the ratio (P2), wherein the ratio (P1) is the ratio of benzene allocated as renewable benzene relative to the ratio of products obtained from the above disproportionation unit or the above transalkylation (TA) unit and the above para-xylene unit, and the ratio (P2) is the ratio of para-xylene allocated as renewable para-xylene relative to the ratio of products obtained from the above disproportionation unit or the above transalkylation (TA) unit and the above para-xylene unit.

[0070]

[18] A method for managing terephthalic acid when producing terephthalic acid using a naphtha feedstock comprising renewable naphtha,

[0071] The management method is a method of allocating the value of the terephthalic acid as a renewable product according to the content ratio of the renewable naphtha contained in the naphtha raw material.

[0072] The management method comprises the step (E) of confirming that terephthalic acid is obtained,

[0073] The above step (E) includes the following step (V-1), the following step (G-2), the following step (W-3), the following step (E-4) and the following step (E-5).

[0074] The step (V-1) is a step of confirming that toluene is produced from the naphtha feedstock fed into a device (steam cracker) for thermal cracking in the presence of water vapor.

[0075] The above step (G-2) is a step of confirming that xylene is produced from toluene fed into a disproportionation unit or fed into a transalkylation (TA) unit together with C9 components.

[0076] The step (W-3) is a step of confirming that paraxylene is obtained from the xylene fed into the paraxylene device.

[0077] The above step (E-4) is a step for confirming that terephthalic acid is obtained from paraxylene fed into a terephthalic acid plant.

[0078] The step (E-5) is a step of confirming that terephthalic acid is obtained from the naphtha raw material by sequentially treating with the device for thermal cracking in the presence of water vapor (steam cracker), the disproportionation device or the transalkylation (TA) device, the paraxylene device, and the terephthalic acid device.

[0079] The management method includes a step (H) of confirming the ratio of the product to which the value is allocated as a renewable product,

[0080] The above step (H) includes the following step (H-1), the following step (H-2), the following step (H-3) and the following step (H-4).

[0081] The step (H-1) is a step of selecting a product to be distributed as a renewable product from among the products obtained from the terephthalic acid plant.

[0082] The step (H-2) is a step of determining a value of a ratio (P) of the product selected in the step (H-1) to be allocated as a renewable product relative to the product obtained from the terephthalic acid plant.

[0083] The step (H-3) is a step of obtaining the value of the content ratio (Q) of the renewable naphtha contained in the naphtha raw material.

[0084] The step (H-4) is a step of comparing the value of the ratio (P) with the value of the content ratio (Q) to confirm that the value of the ratio (P) is equal to or less than the value of the content ratio (Q).

[0085]

[19] A method for managing polyethylene terephthalate, for use when producing polyethylene terephthalate using a naphtha feedstock comprising renewable naphtha,

[0086] The management method is a method of allocating the value of the polyethylene terephthalate as a renewable product according to the content ratio of the renewable naphtha contained in the naphtha raw material.

[0087] The management method includes the step (F) of confirming that polyethylene terephthalate is obtained,

[0088] The above step (F) includes the following step (V-1), the following step (G-2), the following step (W-3), the following step (E-4), the following step (F-5) and the following step (F-6).

[0089] The step (V-1) is a step of confirming that toluene is produced from the naphtha feedstock fed into a device (steam cracker) for thermal cracking in the presence of water vapor.

[0090] The above step (G-2) is a step of confirming that xylene is produced from toluene fed into a disproportionation unit or fed into a transalkylation (TA) unit together with C9 components.

[0091] The step (W-3) is a step of confirming that paraxylene is obtained from the xylene fed into the paraxylene device.

[0092] The above step (E-4) is a step for confirming that terephthalic acid is obtained from paraxylene fed into a terephthalic acid plant.

[0093] The above step (F-5) is a step for confirming that polyethylene terephthalate is obtained from terephthalic acid fed into the PET device.

[0094] The step (F-6) is a step of confirming that polyethylene terephthalate is obtained from the naphtha raw material by sequentially treating with the device for thermal cracking in the presence of water vapor (steam cracker), the disproportionation device or the transalkylation (TA) device, the paraxylene device, the terephthalic acid device, and the PET device,

[0095] The management method includes a step (J) of confirming the ratio of the product to which the value as a renewable product is allocated,

[0096] The above step (J) includes the following step (J-1), the following step (J-2), the following step (J-3) and the following step (J-4),

[0097] The step (J-1) is a step of selecting a product to be distributed as a renewable product from among the products obtained from the PET device.

[0098] The step (J-2) is a step of determining a value of a ratio (P) to be allocated as a renewable product in the ratio of the product selected in the step (J-1) to the product obtained from the PET device.

[0099] The step (J-3) is a step of obtaining the value of the content ratio (Q) of the renewable naphtha contained in the naphtha raw material.

[0100] The step (J-4) is a step of comparing the value of the ratio (P) with the value of the content ratio (Q) to confirm that the value of the ratio (P) is equal to or less than the value of the content ratio (Q).

[0101]

[20] A management device comprising a computer-readable storage medium storing a management program,

[0102] The management device executes the management method described in any one of

[13] to

[19] by executing the management program.

[0103]

[21] A management device according to

[20] , wherein after executing the management method, the result of allocating the value of the selected product as a renewable product based on the content ratio of renewable naphtha contained in the naphtha raw material obtained by the management method is output.

[0104]

[22] A storage medium is a computer-readable storage medium storing a computer program,

[0105] A management program is stored that causes a computer to execute the management method described in any one of

[13] to

[19] .

[0106]

[23] A management program for causing a computer to execute the management method described in any one of

[13] to

[19] .

[0107] According to the present invention, it is possible to provide a method for producing monocyclic aromatic hydrocarbons such as benzene and paraxylene which are effective as base raw materials using a naphtha raw material including renewable naphtha.

[0108] In addition, according to the present invention, there can be provided a management method for monocyclic aromatic hydrocarbons that can be used when producing monocyclic aromatic hydrocarbons using a naphtha feedstock containing renewable naphtha, in which the value of the monocyclic aromatic hydrocarbon products as renewable products such as renewable benzene and renewable paraxylene is allocated to the monocyclic aromatic hydrocarbon products according to the content ratio of renewable naphtha contained in the naphtha feedstock. BRIEF DESCRIPTION OF THE DRAWINGS

[0109] Figure 1 This is a schematic diagram for explaining the production method of the present invention.

[0110] Figure 2 This is a schematic diagram for explaining the process when the step (A-1) is carried out using the steam cracker (1).

[0111] Figure 3 This is a schematic diagram for explaining the process when the step (A-3) is carried out using the paraxylene production apparatus (4).

[0112] Figure 4 This is a schematic diagram for explaining the method for producing terephthalic acid of the present invention.

[0113] Figure 5 This is a schematic diagram for explaining the method for producing polyethylene terephthalate of the present invention.

[0114] Figure 6 This is a simplified diagram comparing the composition of petroleum-derived light naphtha (also called conventional naphtha) and bio-naphtha.

[0115] Fig. 7A This is a schematic diagram for explaining the step (V-1) in the management method of the present invention when the management method of the present invention includes the step (V) but does not include the step (W).

[0116] Figure 7B This is a schematic diagram for explaining step (V-2) in the management method of the present invention when the management method of the present invention includes step (V) but does not include step (W).

[0117] Figure 7C This is a schematic diagram for explaining step (V-3) in the management method of the present invention when the management method of the present invention includes step (V) but does not include step (W).

[0118] Fig. 8A This is a schematic diagram for explaining the step (X-1) in the management method of the present invention when the management method of the present invention includes the step (V) but does not include the step (W).

[0119] Figure 8B This is a schematic diagram for explaining step (X-2) in the management method of the present invention when the management method of the present invention includes step (V) but does not include step (W).

[0120] Figure 8C This is a schematic diagram for explaining step (X-3) in the management method of the present invention when the management method of the present invention includes step (V) but does not include step (W).

[0121] Fig.8D This is a schematic diagram for explaining step (X-4) in the management method of the present invention when the management method of the present invention includes step (V) but does not include step (W).

[0122] Fig.9A This is a schematic diagram for explaining the step (V-1) in the management method of the present invention when the management method of the present invention includes the step (W) but does not include the step (V).

[0123] Fig. 9BThis is a schematic diagram for explaining step (V-2) in the management method of the present invention when the management method of the present invention includes step (W) but does not include step (V).

[0124] Fig. 9C This is a schematic diagram for explaining step (W-3) in the management method of the present invention when the management method of the present invention includes step (W) but does not include step (V).

[0125] Fig.9D This is a schematic diagram for explaining step (W-4) in the management method of the present invention when the management method of the present invention includes step (W) but does not include step (V).

[0126] Fig. 10A This is a schematic diagram for explaining the step (Y-1) in the management method of the present invention when the management method of the present invention includes the step (W) but does not include the step (V).

[0127] Fig. 10B This is a schematic diagram for explaining the step (Y-2) in the management method of the present invention when the management method of the present invention includes the step (W) but does not include the step (V).

[0128] Fig. 10C This is a schematic diagram for explaining step (Y-3) in the management method of the present invention when the management method of the present invention includes step (W) but does not include step (V).

[0129] Fig. 10D This is a schematic diagram for explaining step (Y-4) in the management method of the present invention when the management method of the present invention includes step (W) but does not include step (V).

[0130] Fig.11A This is a schematic diagram for explaining step (V-1) in the management method of the present invention when the management method of the present invention includes step (V) and step (W).

[0131] Fig. 11B This is a schematic diagram for explaining step (V-2) in the management method of the present invention when the management method of the present invention includes step (V) and step (W).

[0132] Fig. 11C This is a schematic diagram for explaining step (W-3) in the management method of the present invention when the management method of the present invention includes step (V) and step (W).

[0133] Fig.11D This is a schematic diagram for explaining step (V-3) in the management method of the present invention when the management method of the present invention includes step (V) and step (W).

[0134] Fig.11E This is a schematic diagram for explaining step (W-4) in the management method of the present invention when the management method of the present invention includes step (V) and step (W).

[0135] Fig. 12A This is a schematic diagram for explaining step (Z-1) in the management method of the present invention when the management method of the present invention includes step (V) and step (W).

[0136] Fig. 12B This is a schematic diagram for explaining step (Z-2) in the management method of the present invention when the management method of the present invention includes step (V) and step (W).

[0137] Fig. 12C This is a schematic diagram for explaining step (Z-3) used in the management method of the present invention when the management method of the present invention includes step (V) and step (W).

[0138] Fig.12D This is a schematic diagram for explaining step (Z-4) in the management method of the present invention when the management method of the present invention includes step (V) and step (W).

[0139] Fig.12E This is a schematic diagram for explaining another embodiment of the step (Z) in the management method of the present invention when the management method of the present invention includes the step (V) and the step (W).

[0140] Fig.13 This is a simplified diagram for explaining the functional configuration of the management device.

[0141] Fig.14 This is a block diagram showing an example of the hardware configuration of the management device.

[0142] Fig.15 This is a flowchart showing an example of the processing procedure of the management program of the control unit of the management device.

[0143] Fig.16 This is a flowchart showing a first modified example of the processing procedure of the management program of the control unit of the management device.

[0144] Fig.17 This is a flowchart showing a second modified example of the processing procedure of the management program of the control unit of the management device. DETAILED DESCRIPTION

[0145] (definition)

[0146] The present invention will be described in more detail below. It should be noted that the following terms are used in this specification.

[0147] "Renewable raw materials" refer to raw materials from renewable organic resources. Renewable raw materials are not intended to be limited to biological resource derivatives, but should be broadly understood as raw materials from renewable organic resources. For example, even petroleum derivatives include raw materials from recyclable products such as waste plastic derivatives that use petroleum derivatives as raw materials.

[0148] "Renewable naphtha" means naphtha derived from renewable feedstocks.

[0149] "Renewable products" (renewable toluene, renewable para-xylene, etc.) refer to substances for which credits are allocated using the mass balance method.

[0150] "Biomass feedstock" refers to feedstock from biological resources.

[0151] "Bio-naphtha" refers to naphtha derived from biomass feedstock.

[0152] "Naphtha" refers to a hydrocarbon group having 5 to 10 carbon atoms obtained by purifying petroleum.

[0153] The "xylene" is intended to include at least one isomer (mixture) consisting of p-xylene, o-xylene, and m-xylene.

[0154] (Method for producing monocyclic aromatic hydrocarbons)

[0155] The production method of the present invention is a method for producing at least one monocyclic aromatic hydrocarbon among benzene and xylene using a naphtha feedstock containing renewable naphtha (hereinafter, sometimes simply referred to as "renewable naphtha feedstock").

[0156] The renewable naphtha feedstock contains at least renewable naphtha, and may further contain non-renewable naphtha (conventional petroleum-derived naphtha).

[0157] Examples of renewable naphtha include bio-naphtha produced from biological raw materials, naphtha obtained by processing waste plastics, etc. Among them, bio-naphtha is more preferably used from the viewpoint of preserving petroleum resources and reducing carbon dioxide emissions.

[0158] Bio-naphtha refers to naphtha produced based on biologically derived raw materials such as animal oils and vegetable oils such as waste cooking oil, tallow, palm oil, and tall oil (a byproduct of pulp and paper).

[0159] As the renewable naphtha contained in the renewable naphtha raw material of the present invention, bio-naphtha derived from plants, wood, waste vegetable oil, paper, etc. is preferably used. Such bio-naphtha has a composition close to the light fraction of naphtha derived from petroleum.

[0160] In the present invention, specific examples of the monocyclic aromatic hydrocarbons to be produced by the production method include benzene and xylene.

[0161] Since at least one of the monocyclic aromatic hydrocarbons of benzene and xylene produced by the production method of the present invention is produced using a renewable naphtha raw material, it is a substance derived from renewable naphtha.

[0162] For example, when bio-naphtha is used as renewable naphtha and monocyclic aromatic hydrocarbons are produced by the production method of the present invention using a bio-naphtha raw material containing the bio-naphtha, the produced monocyclic aromatic hydrocarbons contain biomass components derived from the bio-naphtha.

[0163] The biomass components contained in monocyclic aromatic hydrocarbons can be determined by, for example, determining the radioactive carbon atoms. 14 That is, it is possible to obtain a substance containing radioactive carbon atoms by using, for example, bio-naphtha as a raw material. 14 C of xylene.

[0164] Here, there is no difference between biological and petroleum-derived compounds and compositions in terms of physical properties such as molecular weight, mechanical properties, and thermal properties. In order to distinguish between them, the biomass degree is generally used. 14 C (radiocarbon 14, half-life 5730 years), so the 14 By measuring the concentration of C, it is possible to confirm whether the generated compound or composition is produced only from petroleum-derived naphtha or from a bio-naphtha raw material containing bio-naphtha.

[0165] The biomass degree is measured by, for example, burning a sample to be measured to generate carbon dioxide, and then reducing the carbon dioxide purified in a vacuum line with hydrogen using iron as a catalyst to generate graphite.

[0166] Then, by mounting the graphene on a tandem accelerator 14 In the C-AMS dedicated device (manufactured by NEC Corporation), 14 The count of C, 13 The concentration of C 13 C / 12 C) 14 The concentration of C 14 C / 12 C) is measured, and the carbon content of the sample relative to the standard modern carbon is calculated based on the measured value. 14 It is to be determined by the ratio of the concentration of C. In the measurement, oxalic acid (HOxII) provided by the National Institute of Standards and Technology (NIST) of the United States can be used as a standard sample.

[0167] The manufacturing method of the present invention at least comprises:

[0168] Step (A-1), thermally cracking the naphtha raw material in the presence of water vapor to generate toluene and separating the toluene; and

[0169] In step (A-2), the toluene is subjected to a disproportionation reaction or a transalkylation reaction to produce at least one monocyclic aromatic hydrocarbon of benzene and xylene, and the resulting mixture is separated.

[0170] The production method of the present invention may further include the step (A-3) of separating paraxylene by adsorption separation or crystallization separation of the xylene obtained in the above step (A-2).

[0171] The production method of the present invention may further include the step of isomerizing a residue containing at least one of o-xylene and m-xylene after separation of p-xylene in the step (A-3) to produce p-xylene, and then isolating p-xylene by adsorption separation or crystallization separation.

[0172] use Figure 1 A preferred embodiment of the production method of the present invention is described. It should be noted that in the accompanying drawings, the device (1) for performing thermal cracking in the presence of water vapor is simply expressed as a "steam cracker (1)". In addition, the device (2) for performing a disproportionation reaction is expressed as a "disproportionation device (2)", the device (3) for performing a transalkylation reaction is also expressed as a "TA device (3)", and the device (4) for separating para-xylene by adsorption separation or crystallization separation is also expressed as a "para-xylene production device (4)". The disproportionation reaction refers to a reaction in which benzene C6 and xylene C8 are produced from toluene C7, and the transalkylation reaction refers to a reaction in which benzene C6 and xylene C8 are produced from toluene C7 and C9-based components (monocyclic aromatic hydrocarbons having 9 carbon atoms) (h) and / or C10-based components (monocyclic aromatic hydrocarbons having 10 carbon atoms) (i). It should be noted that the raw material for the transalkylation reaction may contain components above C11 (monocyclic aromatic hydrocarbons having 11 carbon atoms or more) in addition to C7, C9, and C10-based components.

[0173] exist Figure 1 In the process, a renewable naphtha raw material (a) containing renewable naphtha (for example, more specifically, bio-naphtha) (a-1) and petroleum-derived naphtha (for example, more specifically, petroleum-derived light naphtha) (a-2) is fed into a steam cracker (1), to separate toluene (b) as a co-product with ethylene and the like, and the toluene (b) is fed into a disproportionation unit (2) or a TA unit (3) to separate benzene (c). In this way, benzene (c) derived from the renewable naphtha raw material (a) can be produced.

[0174] On the other hand, if the above-mentioned toluene (b) is fed into a disproportionation device (2) or fed into a TA device (3) together with a C9-based component (h) to separate xylene (d), xylene (d) derived from a renewable naphtha raw material (a) can be produced.

[0175] By feeding the xylene (d) into a p-xylene production device (4) and separating the p-xylene (e), it is possible to produce p-xylene (e) derived from the renewable naphtha raw material (a).

[0176] In the conventional chemical industrial processes, a steam cracker (1) and a disproportionation device (2) or a TA device (3) are not combined to produce monocyclic aromatic hydrocarbons, and a series of processes of naphtha → steam cracker (1) → toluene → disproportionation device (2) → benzene or xylene → p-xylene, or naphtha → steam cracker (1) → toluene → TA device (3) → benzene or xylene → p-xylene is a new process that is not usually performed. By this new process, monocyclic aromatic hydrocarbons derived from a renewable naphtha raw material (a) can be produced.

[0177] The following Figure 1 The manufacturing method of the present invention shown will be described in more detail.

[0178] The method for producing at least one monocyclic aromatic hydrocarbon of benzene and xylene using a renewable naphtha raw material includes the following step (A-1) and the following step (A-2).

[0179] Step (A-1) is a step of feeding a renewable naphtha raw material (a) into a steam cracker (1) to generate and separate toluene (b).

[0180] Step (A-2) is a step of feeding toluene (b) into a disproportionation device (2) or feeding it together with a C9 component (h) into a TA device (3) to generate and separate benzene (c) and xylene (d).

[0181] The above production method further includes the following step (A-3) of producing p-xylene.

[0182] The step (A-3) is a step of separating paraxylene (e) by feeding xylene (d) into a paraxylene production apparatus (4).

[0183] The apparatus used in the production method of the present invention will be described in more detail.

[0184] <Steam Cracker(1)>

[0185] The raw material fed into the steam cracker (1) is a renewable naphtha raw material (a). A preferred embodiment of the renewable naphtha raw material (a) is a renewable naphtha raw material (a) containing renewable naphtha (a-1) and petroleum-derived light naphtha (a-2), and more preferably a bio-naphtha raw material (a) containing bio-naphtha (a-1) and petroleum-derived light naphtha (a-2).

[0186] Here, the content ratio of the renewable naphtha (a-1) contained in the renewable naphtha raw material (a) is not particularly limited and can be appropriately selected depending on the purpose.

[0187] As a raw material fed to the steam cracker (1), light oil may be used in addition to the renewable naphtha raw material (a). As the light oil, light oil derived from a biomass raw material such as biodiesel is preferably used.

[0188] Examples of the biomass raw material include vegetable oils such as rapeseed oil, palm oil, olive oil, sunflower oil, soybean oil, and rice bran oil; animal fats such as beef tallow, lard, and fish oil; and waste cooking oil.

[0189] Here, the mixing ratio of the renewable naphtha raw material (a) and the light oil derived from the biomass raw material in the raw material fed to the steam cracker (1) is not particularly limited and can be appropriately selected depending on the purpose.

[0190] The steam cracker (1) is a device for producing and separating toluene as a co-product such as ethylene by thermally cracking a renewable naphtha raw material (a) in the presence of water vapor.

[0191] use Figure 2 A more detailed process when the step (A-1) is performed using the steam cracker (1) will be described.

[0192] A renewable naphtha raw material (a) is fed into a steam cracker (1) to obtain a product, and components containing aromatic compounds are separated and purified by distillation or extraction, thereby obtaining toluene (b) containing renewable components.

[0193] The decomposition temperature of the steam cracker is preferably 750°C to 900°C, more preferably 770°C to 850°C.

[0194] Furthermore, in order to operate the steam cracker efficiently, the residence time (reaction time) of the feedstock is preferably 0.1 to 0.5 seconds, more preferably 0.1 to 0.3 seconds. In addition, the steam / feedstock (mass ratio) is preferably 0.2 to 0.9, more preferably 0.3 to 0.7.

[0195] <Disproportionation device (2)>

[0196] In the disproportionation device (2), toluene (b) is converted into benzene and xylene by a reaction in which methyl groups are transferred between toluenes, and benzene (c) and xylene (d) are generated and separated (step (A-2)). The toluene (b) may be the toluene obtained in the steam cracker (1), may be other toluene (e.g., toluene derived from petroleum), or may be a mixture of the toluene obtained in the steam cracker (1) and other toluene.

[0197] <TA device (3)>

[0198] In the TA device (3), toluene (b), C9-based components (h) and C10-based components (i) are converted into benzene and xylenes by a reaction in which methyl groups are transferred between toluene (b) and C9-based components and / or C10-based components, thereby generating benzene (c) and xylenes (d), which are then separated (step (A-2)). The toluene (b) may be the toluene obtained in the steam cracker (1), other toluene (e.g., petroleum-derived toluene), or a mixture of the toluene obtained in the steam cracker (1) and other toluene.

[0199] In addition, the raw material for the transalkylation reaction may contain C11 or higher components in addition to toluene (b), C9-based components (h) and C10-based components (i).

[0200] Examples of the C9 component include trimethylbenzene and methylethylbenzene, examples of the C10 component include tetramethylbenzene and ethylxylene, and examples of the C11 and above components include trimethylethylbenzene and diethyltoluene.

[0201] <Para-xylene production equipment (4)>

[0202] In the paraxylene production device (4), the xylene (d) (more specifically, a mixed xylene including meta-xylene, ortho-xylene, para-xylene, etc.) obtained in the disproportionation device (2) or the TA device (3) is subjected to adsorption separation or crystallization separation to separate para-xylene (step (A-3)).

[0203] The step (A-3) may further include isomerizing a residue containing at least one of o-xylene and m-xylene after separation of p-xylene to produce p-xylene, and then isolating p-xylene by adsorption separation or crystallization separation again.

[0204] (Production of paraxylene based on adsorption separation)

[0205] use Figure 3 A preferred embodiment of the paraxylene production apparatus (4) will be described.

[0206] In the adsorption separation method, xylene (d) (more specifically, a mixed xylene containing meta-xylene, ortho-xylene, para-xylene, etc.) is introduced into an adsorption tower (4-1) in a para-xylene production device (4) that uses an adsorbent to adsorb and separate para-xylene. In the adsorption tower (4-1), para-xylene (e) is separated.

[0207] The residue (f) containing ortho-xylene and meta-xylene remaining after the separation of para-xylene is fed into the isomerization device (4-2) in the para-xylene production device (4) for isomerization treatment, and the isomerized mixed xylene (g) containing para-xylene obtained by the isomerization treatment (more specifically, the isomerized mixed xylene mixed with meta-xylene, ortho-xylene, para-xylene, etc.) is supplied to the adsorption tower (4-1) again. In the adsorption tower (4-1), para-xylene (e) is separated.

[0208] The step of separating the paraxylene (e) via the isomerization unit → the adsorption tower can be repeated. The repeated operation is terminated when the target amount of paraxylene (e) can be separated.

[0209] (Production of paraxylene by crystallization separation)

[0210] In the crystallization separation method, paraxylene is separated from metaxylene and orthoxylene by using the difference in melting points from xylene (d) (more specifically, a mixed xylene in which metaxylene, orthoxylene, paraxylene, etc. are mixed). The mixed xylene introduced into the paraxylene production device is cooled to crystallize paraxylene having a higher melting point than other xylene isomers, and the paraxylene is separated through the steps of centrifugal separation, crystal washing, and recrystallization.

[0211] (Method for producing terephthalic acid)

[0212] The production method of the present invention is a method for producing terephthalic acid using a renewable naphtha raw material and / or a light oil derived from a biomass raw material, comprising a step (A-3) of obtaining p-xylene, and a step (A-4) of obtaining terephthalic acid by oxidizing p-xylene. The renewable naphtha raw material and the step (A-3) of obtaining p-xylene are as described above. As a renewable naphtha raw material, bionaphtha is preferably used, and as a light oil derived from a biomass raw material, biodiesel is preferably used.

[0213] Reference Figure 4 The preferred embodiment of the present invention is described below. Figure 4As shown, a renewable naphtha raw material (a) containing bio-naphtha is fed into a steam cracker (1), and after the above-mentioned reactions, paraxylene is obtained from a paraxylene unit (4). Next, the obtained paraxylene is fed into a terephthalic acid production unit (5) to obtain terephthalic acid (step (A-4)).

[0214] According to the production method of the present invention, by using bio-naphtha and / or light oil derived from biomass raw materials as renewable naphtha raw materials, it is possible to obtain 14 C of terephthalic acid.

[0215] <Terephthalic acid production equipment (5)>

[0216] In the terephthalic acid production apparatus (5), the p-xylene obtained in the p-xylene production apparatus (4) is oxidized to produce terephthalic acid (step (A-4)).

[0217] In step (A-4), p-xylene is oxidized by a conventionally known method to generate terephthalic acid. For example, p-xylene is subjected to liquid-phase oxidation in an acetic acid solvent using molecular oxygen in the presence of a catalyst to generate terephthalic acid. As a catalyst, a catalyst known to be used in the oxidation reaction in the past is used, specifically, heavy metal compounds such as cobalt compounds, manganese compounds, iron compounds, chromium compounds, and bromine compounds, etc. can be cited. The catalyst is preferably present in the reaction system in a molten or dissolved state because the reaction rate is accelerated when the catalyst is in a molten or dissolved state during the oxidation reaction. The conditions of the oxidation reaction can be appropriately set.

[0218] (Method for producing polyethylene terephthalate)

[0219] The production method of the present invention is a method for producing polyethylene terephthalate using a renewable naphtha raw material and / or a light oil derived from a biomass raw material, comprising a step (A-4) of obtaining terephthalic acid, and a step (A-5) of obtaining polyethylene terephthalate by a condensation reaction of terephthalic acid and ethylene glycol. The renewable naphtha raw material and the step (A-4) of obtaining terephthalic acid are as described above. As a renewable naphtha raw material, bio-naphtha is preferably used, and as a light oil derived from a biomass raw material, biomass diesel is preferably used.

[0220] Reference Figure 5 The preferred embodiment of the present invention is described below. Figure 5As shown, a renewable naphtha raw material (a) containing bio-naphtha is fed into a steam cracker (1), and after the above-mentioned reactions, terephthalic acid is obtained from a terephthalic acid production device (5) (step (A-4)). Next, the obtained terephthalic acid is fed into a polyethylene terephthalate (PET) production device (6) to obtain polyethylene terephthalate (PET) (step (A-5)).

[0221] According to the production method of the present invention, by using bio-naphtha and / or light oil derived from biomass raw materials as renewable naphtha raw materials, it is possible to obtain 14 C of polyethylene terephthalate.

[0222] The obtained polyethylene terephthalate can be used for conventionally known applications, for example, it can be used for preforms, plastic bottles, shrink films, stretch films, and the like.

[0223] <Polyethylene terephthalate (PET) production equipment (6)>

[0224] In the polyethylene terephthalate production apparatus (6), polyethylene terephthalate is produced by a condensation reaction between the terephthalic acid obtained in the terephthalic acid production apparatus (5) and ethylene glycol (step (A-5)).

[0225] In step (A-5), polyethylene terephthalate is generated by a condensation reaction of terephthalic acid and ethylene glycol using a conventionally known method. For example, it can be produced by a condensation reaction (dehydration condensation) of terephthalic acid and ethylene glycol in the presence of a polymerization catalyst. As a polymerization catalyst, for example, metal compounds containing titanium, zirconium, germanium, zinc, aluminum, magnesium and calcium, and mixtures thereof are preferred, and titanium compounds, zirconium compounds and germanium compounds are particularly preferred. The polymerization catalyst is preferably liquid during the condensation reaction, or preferably a compound dissolved in an ester oligomer or polyester, for reasons such as the reaction rate becomes faster if it is in a molten or dissolved state during the condensation reaction. The conditions of the condensation reaction can be appropriately set.

[0226] The ethylene glycol, which is one of the raw materials for producing polyethylene terephthalate (PET) in the crop step (A-5), may be derived from petroleum, may be derived from a biomass raw material, or may be biomass ethylene glycol obtained by applying a mass balance method. By using ethylene glycol derived from a biomass raw material in the step (A-5), the biomass content of the obtained polyethylene terephthalate can be increased.

[0227] <Features of the production method of the present invention>

[0228] According to the production method of the present invention, by partially or completely replacing the raw materials derived from petroleum with renewable raw materials such as biomass raw materials and recyclable raw materials, it is possible to conserve petroleum resources, reduce carbon dioxide emissions and reduce environmental load, and the monocyclic aromatic hydrocarbon products generated can also have the same composition as the monocyclic aromatic hydrocarbon products previously generated using raw materials derived from petroleum.

[0229] When more detailed description is given, such as Figure 6 As shown in FIG. 1 , petroleum-derived light naphtha (also referred to as conventional naphtha) is similar to the representative composition of bio-naphtha. In the production method of the present invention, since bio-naphtha having a composition similar to that of conventional naphtha is used and raw material naphtha obtained by partially or completely replacing the conventional naphtha with bio-naphtha is used, the yield of the product from the bio-naphtha is not different from the yield of the product from the conventional naphtha, and monocyclic aromatic hydrocarbons of the same composition can be generated. In addition, the quality of the generated monocyclic aromatic hydrocarbons can also be obtained to the same degree as the quality of the monocyclic aromatic hydrocarbons generated from conventional naphtha.

[0230] In addition, in the production method of the present invention, not only the composition of the final product of monocyclic aromatic hydrocarbons but also the composition of each co-product including toluene obtained from the steam cracker is confirmed, and there is no difference in the composition of each co-product when conventional naphtha contains bio-naphtha and when conventional naphtha alone is used.

[0231] (Management Methods for Renewable Monocyclic Aromatic Hydrocarbons)

[0232] In recent years, the mass balance method (hereinafter also referred to as the material balance method) has attracted attention in the chemical industry in order to sell environmentally friendly products using plant-derived raw materials, recyclable materials, etc. in a more attractive form.

[0233] It is desired to allocate the value of monocyclic aromatic hydrocarbons produced by the method for producing monocyclic aromatic hydrocarbons containing renewable components of the present invention as renewable products using a simple and reliable method using a mass balance method.

[0234] Therefore, the present invention provides a management method that can allocate the value of monocyclic aromatic hydrocarbon products as renewable products using a simple and reliable method based on the content ratio of renewable naphtha contained in the renewable naphtha raw material when monocyclic aromatic hydrocarbons are produced using the above-mentioned method for producing monocyclic aromatic hydrocarbons containing renewable components of the present invention.

[0235] Here, the mass balance method refers to the following method: for example, when raw materials such as biomass raw materials with specific characteristics are mixed with raw materials without such characteristics in the distribution and processing steps from raw materials to products, the characteristics are allocated as credit to a part of the product according to the content ratio of the raw materials with the characteristics.

[0236] For example, when renewable naphtha (bio-naphtha) raw materials are fed into a steam cracker to produce benzene, benzene contains renewable components (biomass components), but the biomass fraction in the renewable naphtha raw materials fed into the steam cracker is simultaneously distributed to each joint product (since it is a joint product, the renewable components cannot be distributed to a specific product). Therefore, in order to virtually distribute the biomass fraction as credit to some products such as benzene and paraxylene, there is a mass balance method. It should be noted that how to distribute or its specific method will be described later.

[0237] Since the mass balance method (material balance method) is a method in which the manufacturer arbitrarily distributes biomass fractions as credits, its legitimacy is usually proved by certification by a third-party certification agency. Third-party certification agencies include ISCC (International Sustainability and Carbon Certification) and RSB (Roundtable on Sustainable Biomaterials Certification).

[0238] The method for managing renewable monocyclic aromatic hydrocarbons of the present invention can be used when producing at least one monocyclic aromatic hydrocarbon of benzene and xylene using a renewable naphtha feedstock containing renewable naphtha.

[0239] The management method of the present invention is a method of allocating the value of at least one monocyclic aromatic hydrocarbon product as a renewable product according to the content ratio of renewable naphtha contained in the renewable naphtha raw material.

[0240] The management method of the present invention includes at least one step selected from the group consisting of a step (V) of confirming the production of xylene and / or benzene, and a step (W) of confirming the production of p-xylene.

[0241] Hereinafter, the management method including the step (V) and the step (W) will be described in detail for each case.

[0242] <Management method including process (V) but not including process (W)>

[0243] The step (V) of confirming the production of xylene and / or benzene includes the following step (V-1), the following step (V-2), and the following step (V-3).

[0244] When the management method of the present invention includes the step (V) but does not include the step (W), the management method includes the step (X) of confirming the ratio of the product to which the value as the renewable product is allocated.

[0245] The step (X) includes the following step (X-1), the following step (X-2), the following step (X-3), and the following step (X-4).

[0246] use Figure 7A to Figure 7C (they are collectively referred to as Figure 7) and Figures 8A to 8D (These are also collectively referred to as FIG. 8 ) A preferred embodiment of the management method of the present invention when the step (V) is included but the step (W) is not included will be described.

[0247] like Fig. 7A As shown, step (V-1) is a step of confirming the production of toluene (b) from the renewable naphtha feedstock (a) fed into the steam cracker (1). That is, it is confirmed whether the desired output (toluene) occurs with respect to the input (renewable naphtha feedstock) of the steam cracker.

[0248] like Figure 7B As shown, step (V-2) is a step of confirming the generation of xylene (d) and / or benzene (c) from toluene (b) fed into the disproportionation device (2) or fed into the TA device (3) together with the C9 component (h) and / or the C10 component. That is, for the disproportionation device (2) or the TA device (3), it is confirmed whether the desired output (xylene and / or benzene) occurs relative to the input (toluene (depending on the situation, it also includes confirming the input of the C9 component and / or the C10 component)). It should be noted that in step (V-2), the toluene (b) fed into the disproportionation device (2) or the TA device (3) may be the toluene (b) obtained in step (V-1), or may be other toluene (for example, petroleum-derived toluene), or may be a mixture of the toluene (b) obtained in step (V-1) and other toluene, preferably other toluene.

[0249] like Figure 7C As shown, step (V-3) is a step for confirming that xylene (d) and / or benzene (c) are produced from a renewable naphtha feedstock (a) by treating it sequentially with a steam cracker (1), a disproportionation device (2) or a TA device (3). That is, when the steam cracker (1) and the disproportionation device (2) or the TA device (3) are sequentially provided for the reaction, it is confirmed whether the desired output (xylene and / or benzene) occurs relative to the input (renewable naphtha feedstock). It should be noted that in step (V-3), although the toluene (b) fed into the disproportionation device (2) or the TA device (3) is not shown in the figure, it is the same as the toluene (b) in step (V-2).

[0250] The step (X-1) is a step of selecting one or more products to be distributed as renewable products from among the products generated by the disproportionation device (2) or the TA device (3).

[0251] Step (X-2) is a step of determining a value of a ratio (P) of the product selected in step (X-1) to be allocated as a renewable product relative to the product generated by the disproportionation device (2) or the TA device (3).

[0252] The step (X-3) is a step of finding the value of the content ratio (Q) of renewable naphtha contained in the renewable naphtha raw material.

[0253] Step (X-4) is a step of comparing the value of the ratio (P) with the value of the content ratio (Q) to confirm that the value of the ratio (P) is equal to or less than the value of the content ratio (Q).

[0254] Steps (X-1) to (X-4) (these steps are also collectively referred to as step (X)) will be specifically described using FIG. 8 .

[0255] In process (X-1), if Fig. 8A As shown, in the reaction step for obtaining the desired product, one or more desired products are selected as renewable products from the products (for example, benzene (c), xylene (d), other products ((v), (w)), etc.) generated by the final use device (here, the disproportionation device (2) or the TA device (3)) and distributed. For example, benzene may be selected, xylene may be selected, or both benzene and xylene may be selected.

[0256] like Figure 8B As shown, in step (X-2), among the products generated by the disproportionation device (2) or the TA device (3), the value of the ratio (P) allocated as a renewable product to the desired product selected in step (X-1) is determined. Figure 8B As shown, the products generated by the disproportionation device (2) are benzene (c), xylene (d), and other products ((v), (w)), and the proportions of the products are benzene (c): 20% by mass, xylene (d): 65% by mass, other products (v): 10% by mass, and other products (w): 5% by mass. In addition, for the sake of convenience, the products generated by the TA device (3) are also described in the same proportions as those of the disproportionation device (2). That is, Figure 8B As shown, the products generated by the TA device (3) are benzene (c), xylene (d), and other products ((v), (w)), and the proportions of each product are benzene (c): 20% by mass, xylene (d): 65% by mass, other products (v): 10% by mass, and other products (w): 5% by mass.

[0257] Here, when benzene is selected in step (X-1), the proportion (P1) allocated as renewable benzene in 20 mass% of the benzene product is determined. Alternatively, when xylene is selected in step (X-1), the proportion (P2) allocated as renewable xylene in 65 mass% of the xylene product is determined. Alternatively, when both benzene and xylene are selected in step (X-1), the proportion (P1) allocated as renewable benzene in 20 mass% of the benzene product and the proportion (P2) allocated as renewable xylene in 65 mass% of the xylene product are determined.

[0258] In process (X-3), if Figure 8C As shown in FIG. 1 , the value of the content ratio (Q) of the renewable naphtha (a-1) contained in the renewable naphtha raw material (a) is known. For example, Figure 8C As shown, in the case where the renewable naphtha raw material (a) contains 10 mass % of renewable naphtha (a-1) and 90 mass % of petroleum-derived naphtha (a-2), it is understood that the content ratio of the renewable naphtha (a-1) is 10 mass %.

[0259] In step (X-4), the value of the ratio (P) is compared with the value of the content ratio (Q), and it is confirmed that the value of the ratio (P) is less than the value of the content ratio (Q). Fig.8D As shown, when the content ratio (Q) of the renewable naphtha (a-1) is 10 mass %, the ratio (P) of the product allocated as a renewable product is 10 mass % or less.

[0260] When there are two or more products allocated as renewable products, the allocation ratio (P) is a value obtained by summing up the ratios allocated to the selected products.

[0261] When only benzene is selected in step (X-1), the ratio (P1) allocated as renewable benzene is the ratio (P), when only xylene is selected in step (X-1), the ratio (P2) allocated as renewable xylene is the ratio (P), and when both benzene and xylene are selected in step (X-1), the total of the ratio (P1) allocated as renewable benzene and the ratio (P2) allocated as renewable xylene is the ratio (P).

[0262] That is, if the content ratio (Q) of renewable naphtha (a-1) is 10 mass %, when benzene is selected as the product to be distributed as the renewable product in step (X-1), 10 mass % of the 20 mass % of the benzene product can be distributed as renewable benzene. In step (X-4), it is confirmed whether the proportion (P1) distributed as renewable benzene does not exceed the content ratio (Q) of renewable naphtha (a-1) (in Fig.8DIn the example of 10 mass %).

[0263] In addition, when xylene is selected as the product to be distributed as the renewable product in step (X-1), 10% by mass of the 65% by mass of the xylene product can be distributed as renewable xylene. In step (X-4), it is confirmed whether the proportion (P2) distributed as renewable xylene does not exceed the content proportion (Q) of the renewable naphtha (a-1) (in Fig.8D In the example of 10 mass %).

[0264] In addition, when the two products of benzene and xylene are selected as the products to be distributed as renewable products in step (X-1), (P1) mass % of the 20 mass % of the benzene product and (P2) mass % of the 65 mass % of the xylene product can be distributed as renewable benzene and renewable xylene, respectively. For example, when P1 is 5 mass % and P2 is 5 mass %, since the total is 10 mass % or less, they can be distributed according to the above ratio. Or, for example, when P1 is 1 mass % and P2 is 9 mass %, since the total is 10 mass % or less, they can be distributed according to the above ratio. On the other hand, for example, when P1 is 6 mass % and P2 is 7 mass %, since the total is 13 mass %, which exceeds 10 mass %, they cannot be distributed according to the above ratio. In step (X-4), confirm whether the total of the ratio (P1) distributed as renewable benzene and the ratio (P2) distributed as renewable xylene does not exceed the content ratio (Q) of renewable naphtha (a-1) (in Fig.8D In the example of 10 mass %).

[0265] In this way, the value as a renewable product can be allocated to the desired product selected in step (X-1) among the products produced by the disproportionation unit (2) or the TA unit (3) according to the content ratio of renewable naphtha contained in the renewable naphtha raw material.

[0266] The products generated by the production method of the present invention contain renewable components according to the content ratio of renewable naphtha contained in the renewable naphtha raw material, and the renewable components are distributed to all products. That is, the content of renewable components is obtained according to the yield produced by each device. If the mass balance method is used, it is possible to treat a specific product as a renewable product to which 100% of renewable components are distributed within the range of the content ratio of renewable naphtha contained in the renewable naphtha raw material.

[0267] That is, Fig.8DFor example, the benzene product (P1) mass % in the 20 mass % benzene product can be determined as renewable benzene with 100% renewable components, and the xylene product (P2) mass % in the 65 mass % xylene product can be determined as renewable xylene with 100% renewable components. Fig.8D The total of (P1) mass % and (P2) mass % needs to be no more than 10 mass %.

[0268] It should be noted that according to the mass balance method, Fig.8D In the 20 mass% of benzene products, the benzene products other than (P1) mass% (20-(P1) mass% of benzene products) actually contain renewable components. However, since 100% of renewable benzene credit is allocated to (P1) mass% of benzene, it is not considered as renewable benzene. Similarly, the xylene products other than (P2) mass% of xylene products (65-(P2) mass% of xylene products) actually contain renewable components, but since 100% of renewable xylene credit is allocated to (P2) mass% of xylene, it is not considered as renewable xylene. The above allocation is ensured by third-party certification organizations such as ISCC (International Sustainability and Carbon Certification) and RSB (Roundtable on Sustainable Biomaterials Certification) that audit the management and operation system of the manufacturer and issue certification if it meets the specified standards.

[0269] According to the management method of the present invention, the value of monocyclic aromatic hydrocarbons generated by the method for producing monocyclic aromatic hydrocarbons containing renewable components using the above-mentioned method of the present invention can be easily and reliably allocated as renewable products using a mass balance method, and the accuracy of the above-mentioned value allocation results can be guaranteed by a third-party certification agency.

[0270] It should be noted that the values ​​of 10% by mass of the content ratio (Q) of renewable naphtha (a-1), 20% by mass of the benzene product, and 65% by mass of the xylene product recorded in FIG. 8 are values ​​set for convenience in order to make the present invention easy to understand, and are not limited to these values. The content ratio (Q) of renewable naphtha (a-1) can be, for example, 1% by mass or 30% by mass, and the desired content ratio (Q) can be set according to the purpose. In addition, the production ratio of each product also varies according to the reaction conditions, etc., so the reaction conditions can be appropriately adjusted to produce the product at the desired production ratio.

[0271] The management method of the present invention can also be applied to the following cases in which the same management method as described above when step (V) is included but step (W) is not included. That is,

[0272] In the case where the step (W) in which p-xylene is confirmed to be obtained is included but the step (V) is not included,

[0273] A case where two steps of the above step (V) and the above step (W) are included.

[0274] Hereinafter, the management method when the step (W) is included but the step (V) is not included and the management method when the step (V) and the step (W) are included will also be described.

[0275] <Management method including process (W) but not including process (V)>

[0276] The step (W) for confirming the production of paraxylene includes the following step (V-1), the following step (V-2), the following step (W-3), and the following step (W-4). Here, step (V-1) and step (V-2) are as described in the above-mentioned "Management method including step (V) but not including step (W)".

[0277] When the management method of the present invention includes the step (W) but does not include the step (V), the management method includes the step (Y) of confirming the ratio of the product to which the value as the renewable product is allocated.

[0278] The step (Y) includes the following step (Y-1), the following step (Y-2), the following step (Y-3), and the following step (Y-4).

[0279] use Figures 9A to 9C (also collectively referred to as Figure 9) and FIG. 10A to FIG. 10D (These are also collectively referred to as FIG. 10 ) A preferred embodiment of the management method of the present invention when the step (W) is included but the step (V) is not included will be described.

[0280] like Fig.9A As shown, step (V-1) is a step of confirming the production of toluene (b) from a renewable naphtha feedstock (a) fed into a device (steam cracker) (1) for thermal cracking in the presence of water vapor. That is, for a device (steam cracker) for thermal cracking in the presence of water vapor, it is confirmed whether the desired output (toluene) is generated relative to the input (renewable naphtha feedstock).

[0281] like Fig. 9BAs shown, step (V-2) is a step of confirming the generation of xylene (d) and / or benzene (c) from toluene (b) fed into the disproportionation device (2) or fed into the TA device (3) together with the C9-based component (h). That is, for the disproportionation device (2) or the TA device (3), it is confirmed whether the desired output (xylene and / or benzene) occurs relative to the input (toluene (including confirming the input of the C9-based component and / or the C10-based component as the case may be)). It should be noted that in step (V-2), the toluene (b) fed into the disproportionation device (2) or the TA device (3) may be the toluene (b) obtained in step (V-1), or may be other toluene (for example, petroleum-derived toluene), or may be a mixture of the toluene (b) obtained in step (V-1) and other toluene, preferably other toluene.

[0282] like Fig. 9C As shown, step (W-3) is a step of confirming that paraxylene (e) is obtained from xylene (d) fed into the paraxylene production device (4). That is, for the paraxylene production device (4), it is confirmed whether the expected output (paraxylene) occurs relative to the input (xylene).

[0283] like Fig.9D As shown, step (W-4) is a step for confirming that paraxylene (e) is obtained from a renewable naphtha raw material (a) by treating it in sequence with a device for thermal cracking in the presence of water vapor (steam cracker) (1), the above-mentioned disproportionation device (2) or the above-mentioned TA device (3), and the above-mentioned paraxylene production device (4). That is, when the device for thermal cracking in the presence of water vapor (steam cracker) (1), the disproportionation device (2) or the TA device (3), and the paraxylene production device (4) are sequentially provided for the reaction, it is confirmed whether the desired output (paraxylene) is generated relative to the input (renewable naphtha raw material). It should be noted that in step (W-4), although the toluene (b) fed into the disproportionation device (2) or the TA device (3) is not shown in the figure, it is the same as the toluene (b) in step (V-2).

[0284] The step (Y-1) is a step of selecting one or more products to be distributed as renewable products from among the products obtained from the paraxylene unit.

[0285] The step (Y-2) is a step of determining the value of the ratio (P) of the product selected in the step (Y-1) to be allocated as a renewable product relative to the product obtained from the paraxylene unit.

[0286] The step (Y-3) is a step of finding the value of the content ratio (Q) of renewable naphtha contained in the renewable naphtha raw material.

[0287] The step (Y-4) is a step of comparing the value of the ratio (P) with the value of the content ratio (Q) to confirm that the value of the ratio (P) is equal to or less than the value of the content ratio (Q).

[0288] Steps (Y-1) to (Y-4) will be specifically described using FIG. 10 .

[0289] In process (Y-1), if Fig. 10A As shown, in the reaction step for obtaining the desired product, one or more desired products are selected from the products (for example, p-xylene (e), o-xylene (x), m-xylene (y), and other products (z)) obtained from the final use device (here, the p-xylene production device (4)) and distributed as renewable products. For example, p-xylene is selected.

[0290] In process (Y-2), if Fig. 10B As shown, among the products obtained from the paraxylene production device (4), the value of the proportion (P) allocated as a renewable product is determined for the desired product selected in step (Y-1). Fig. 10B As shown, the products obtained from the paraxylene manufacturing device (4) are paraxylene (e), o-xylene (x), m-xylene (y), and other products (z), and the proportion of each product is paraxylene (e): 80% by mass, o-xylene (x): 5% by mass, m-xylene (y): 10% by mass, and other products (z): 5% by mass.

[0291] Here, when paraxylene is selected in step (Y-1), the proportion (P1) allocated as renewable benzene among 80 mass % of the paraxylene product is determined.

[0292] In process (Y-3), if Fig. 10C As shown in FIG. 1 , the value of the content ratio (Q) of the renewable naphtha (a-1) contained in the renewable naphtha raw material (a) is known. For example, Fig. 10C As shown, in the case where the renewable naphtha raw material (a) contains 10 mass % of renewable naphtha (a-1) and 90 mass % of petroleum-derived naphtha (a-2), it is understood that the content ratio of the renewable naphtha (a-1) is 10 mass %.

[0293] In step (Y-4), the value of the ratio (P) is compared with the value of the content ratio (Q), and it is confirmed that the value of the ratio (P) is less than the value of the content ratio (Q). Fig. 10D As shown, when the content ratio (Q) of the renewable naphtha (a-1) is 10 mass %, the ratio (P) of the product allocated as a renewable product is 10 mass % or less.

[0294] When there are two or more products allocated as renewable products, the allocation ratio (P) is a value obtained by summing up the ratios allocated to the respective selected products.

[0295] When paraxylene is selected in the step (Y-1), the proportion (P1) allocated as renewable paraxylene is the proportion (P).

[0296] That is, if the content ratio (Q) of renewable naphtha (a-1) is 10 mass %, when paraxylene is selected as the product to be distributed as the renewable product in step (Y-1), 10 mass % of 80 mass % of the paraxylene product can be distributed as renewable paraxylene. In step (Y-4), it is confirmed whether the proportion (P1) distributed as renewable paraxylene does not exceed the content ratio (Q) of renewable naphtha (a-1) ( Fig. 10D In the example of 10 mass %).

[0297] In this way, among the products obtained from the paraxylene production apparatus (4), the value as a renewable product can be allocated to the desired product selected in step (Y-1) according to the content ratio of renewable naphtha contained in the renewable naphtha raw material.

[0298] That is, Fig. 10D For example, for the (P1) mass % of the para-xylene product in the 80 mass % of the para-xylene product, it can be determined as renewable para-xylene with 100% renewable components.

[0299] It should be noted that according to the third-party certification agency, for the mass balance method (material balance method), Fig. 10D In the above, the paraxylene products other than (P1) mass % in the 80 mass % of the paraxylene product (80 - (P1) mass % of the paraxylene product) actually contain renewable components, but since the (P1) mass % of paraxylene is allocated 100% of the credit of renewable paraxylene, it is not regarded as renewable paraxylene.

[0300] It should be noted that, as described above, the value of 10 mass % of the content ratio (Q) of the renewable naphtha (a-1) and the value of 80 mass % of the paraxylene product recorded in the above FIG. 10 are values ​​set for convenience in order to facilitate understanding of the present invention, but are not limited to these values.

[0301] <Management methods including process (V) and process (W)>

[0302] When the step (V) of confirming the production of xylene and / or benzene and the step (W) of confirming the production of paraxylene are included, the following step (V-1), the following step (V-2), the following step (V-3), the following step (W-3), and the following step (W-4) are included. Here, the steps (V-1) to (V-3) and the steps (W-3) to (W-4) are as described in the above-mentioned <Management method including step (V) but not including step (W)> and the above-mentioned <Management method including step (W) but not including step (V)>.

[0303] Furthermore, when the management method of the present invention includes the step (V) and the step (W), the method further includes the step (Z) of confirming the ratio of the product to which the value as the renewable product is allocated.

[0304] The step (Z) includes the following step (Z-1), the following step (Z-2), the following step (Z-3), and the following step (Z-4).

[0305] use Figures 11A to 11E (also collectively referred to as Figure 11) and Figures 12A to 12E (These are also collectively referred to as FIG. 12 ) A preferred embodiment of the management method of the present invention when including step (V) and step (W) will be described.

[0306] like Fig.11A As shown, step (V-1) is a step of confirming the production of toluene (b) from a renewable naphtha feedstock (a) fed into a device (steam cracker) (1) for thermal cracking in the presence of water vapor. That is, for a device (steam cracker) for thermal cracking in the presence of water vapor, it is confirmed whether the desired output (toluene) is generated relative to the input (renewable naphtha feedstock).

[0307] like Fig. 11B As shown, step (V-2) is a step of confirming the generation of xylene (d) and / or benzene (c) from toluene (b) fed into the disproportionation device (2) or fed into the TA device (3) together with the C9-based component (h). That is, for the disproportionation device (2) or the TA device (3), it is confirmed whether the desired output (xylene and / or benzene) occurs relative to the input (toluene (including confirmation of the input of the C9-based component as the case may be)). It should be noted that in step (V-2), the toluene (b) fed into the disproportionation device (2) or the TA device (3) may be the toluene (b) obtained in step (V-1), or may be other toluene (e.g., petroleum-derived toluene), or may be a mixture of the toluene (b) obtained in step (V-1) and other toluene, preferably other toluene.

[0308] like Fig. 11CAs shown, step (W-3) is a step of confirming that paraxylene (e) is obtained from xylene (d) fed into the paraxylene production device (4). That is, for the paraxylene production device (4), it is confirmed whether the expected output (paraxylene) occurs relative to the input (xylene).

[0309] like Fig.11D As shown, step (V-3) is a step for confirming that xylene (d) and / or benzene (c) are produced from a renewable naphtha feedstock (a) by treating it in sequence with a device for thermal cracking in the presence of water vapor (steam cracker) (1), a disproportionation device (2) or a TA device (3). That is, when a device for thermal cracking in the presence of water vapor (steam cracker) (1), a disproportionation device (2) or a TA device (3) is sequentially provided for the reaction, it is confirmed whether the desired output (xylene and / or benzene) is generated relative to the input (renewable naphtha feedstock). It should be noted that in step (V-3), although toluene (b) fed into the disproportionation device (2) or the TA device (3) is not shown, it is the same as the toluene (b) in step (V-2).

[0310] like Fig.11E As shown, step (W-4) is a step for confirming that paraxylene (e) is produced from a renewable naphtha feedstock (a) by treating it in sequence with a device for thermal cracking in the presence of water vapor (steam cracker) (1), a disproportionation device (2) or a TA device (3), and a paraxylene production device (4). That is, when the device for thermal cracking in the presence of water vapor (steam cracker) (1), a disproportionation device (2) or a TA device (3), and a paraxylene production device (4) are sequentially provided for the reaction, it is confirmed whether the desired output (paraxylene) is generated relative to the input (renewable naphtha feedstock). It should be noted that in step (W-4), although the toluene (b) fed into the disproportionation device (2) or the TA device (3) is not shown in the figure, it is the same as the toluene (b) in step (V-2).

[0311] The step (Z-1) is a step of selecting one or more products to be distributed as renewable products from among the products obtained from the disproportionation unit or the TA unit and the para-xylene unit.

[0312] Step (Z-2) is a step of determining the value of the ratio (P) of the product selected in step (Z-1) to be allocated as a renewable product relative to the ratio of the products obtained from the disproportionation unit or the TA unit and the paraxylene unit.

[0313] The step (Z-3) is a step of finding the value of the content ratio (Q) of renewable naphtha contained in the renewable naphtha raw material.

[0314] The step (Z-4) is a step of comparing the value of the ratio (P) with the value of the content ratio (Q) to confirm that the value of the ratio (P) is equal to or less than the value of the content ratio (Q).

[0315] Steps (Z-1) to (Z-4) (these steps are also collectively referred to as step (Z)) will be specifically described using FIG. 12 .

[0316] In process (Z-1), if Fig. 12A As shown, in the reaction step for obtaining the desired product, one or more desired products are selected as renewable products from the products (for example, benzene (c), xylene (d), other products ((v), (w)), p-xylene (e), o-xylene (x), m-xylene (y), other products (z), etc.) obtained from the final use device (here, the disproportionation device (2) or the TA device (3) and the p-xylene production device (4)) and distributed. For example, benzene and p-xylene may be selected, xylene and p-xylene may be selected, or benzene, xylene, and p-xylene may be selected.

[0317] In process (Z-2), if Fig. 12B As shown, among the products obtained from the disproportionation device (2) or the TA device (3) and the paraxylene production device (4), the value of the proportion (P) allocated as a renewable product for the desired product selected in the step (Z-1) is determined. For example, Fig. 12B As shown, the products obtained from the disproportionation device (2) or TA device (3) and the paraxylene production device (4) are benzene (c): 20 mass%, other products (v): 10 mass%, other products (w): 5 mass%, paraxylene (e): 52 mass%, o-xylene (x): 3 mass%, m-xylene (y): 7 mass%, and other products (z): 3 mass. In addition, for the sake of convenience, the products produced by the TA device (3) are also described in the same product ratio as the disproportionation device (2). That is, Fig. 12B As shown, the products generated by the TA device (3) are benzene (c): 20 mass%, other products (v): 10 mass%, other products (w): 5 mass%, p-xylene (e): 52 mass%, o-xylene (x): 3 mass%, m-xylene (y): 7 mass%, and other products (z): 3 mass%.

[0318] Here, when benzene and paraxylene are selected in step (Z-1), the proportion (P1) of 20 mass % of the benzene product allocated as renewable benzene and the proportion (P2) of 52 mass % of the paraxylene product allocated as renewable paraxylene are determined.

[0319] In process (Z-3), if Fig. 12CAs shown in FIG. 1 , the value of the content ratio (Q) of the renewable naphtha (a-1) contained in the renewable naphtha raw material (a) is known. For example, Fig. 12C As shown, in the case where the renewable naphtha raw material (a) contains 10 mass % of renewable naphtha (a-1) and 90 mass % of petroleum-derived naphtha (a-2), it is understood that the content ratio of the renewable naphtha (a-1) is 10 mass %.

[0320] In step (Z-4), the value of the ratio (P) is compared with the value of the content ratio (Q), and it is confirmed that the value of the ratio (P) is less than the value of the content ratio (Q). Fig.12D As shown, when the content ratio (Q) of the renewable naphtha (a-1) is 10 mass %, the ratio (P) of the product allocated as the renewable product is 10 mass % or less.

[0321] When there are two or more products allocated as renewable products, the allocation ratio (P) is a value obtained by summing up the ratios allocated to the respective selected products.

[0322] When two kinds of benzene and paraxylene are selected in step (Z-1), the total of the ratio (P1) allocated as renewable benzene and the ratio (P2) allocated as renewable paraxylene is the ratio (P).

[0323] That is, if the content ratio (Q) of renewable naphtha (a-1) is 10 mass%, when the two products of benzene and para-xylene are selected as the products to be distributed as renewable products in step (Z-1), (P1) mass% of the 20 mass% of benzene products and (P2) mass% of the 52 mass% of para-xylene products can be distributed as renewable benzene and renewable para-xylene, respectively. For example, when P1 is 5 mass% and P2 is 5 mass%, the total is 10 mass% or less, so it can be distributed according to this ratio. Or, for example, when P1 is 1 mass% and P2 is 9 mass%, the total is 10 mass% or less, so it can be distributed according to this ratio. On the other hand, for example, when P1 is 6 mass% and P2 is 7 mass%, the total is 13 mass%, which exceeds 10 mass%, so it cannot be distributed according to this ratio. In step (Z-4), it is confirmed whether the sum of the proportion (P1) allocated as renewable benzene and the proportion (P2) allocated as renewable paraxylene does not exceed the content ratio (Q) of the renewable naphtha (a-1) (in Fig.12D In the example of 10 mass %).

[0324] In this way, among the products obtained from the disproportionation unit (2) or the TA unit (3) and the paraxylene production unit (4), the value as a renewable product can be allocated according to the content ratio of renewable naphtha contained in the renewable naphtha raw material, with respect to the desired product selected in the step (Z-1).

[0325] That is, Fig.12D For example, the benzene product (P1) mass % in the 20 mass % of the benzene product can be determined as renewable benzene with 100% renewable components, and the para-xylene product (P2) mass % in the 52 mass % of the para-xylene product can be determined as renewable para-xylene with 100% renewable components. Fig.12D The total of (P1) mass % and (P2) mass % needs to be no more than 10 mass %.

[0326] It should be noted that according to the third-party certification agency, for the mass balance method (material balance method), Fig.12D In the above, the benzene products other than (P1) mass% in the benzene product 20 mass% (benzene products 20-(P1) mass%) actually contain renewable components, but since 100% of the credit for renewable benzene is allocated to (P1) mass% of benzene, it is not considered as renewable benzene. Similarly, the para-xylene products other than (P2) mass% in the para-xylene product 52 mass% (xylene products 52-(P2) mass%) actually contain renewable components, but since 100% of the credit for renewable para-xylene is allocated to (P2) mass% of para-xylene, it is not considered as renewable para-xylene.

[0327] It should be noted that, as described above, the value of 10 mass % of the content ratio (Q) of the renewable naphtha (a-1), 20 mass % of the benzene product, and 52 mass % of the paraxylene product recorded in the above Figure 12 are values ​​set for convenience in order to make the present invention easy to understand, but are not limited to these values.

[0328] Fig. 12A In the above description, benzene and p-xylene are selected in step (Z-1). However, for example, xylene may be selected in step (Z-1).

[0329] For example, in step (Z-1), when xylene and paraxylene are selected, the total mass % of xylene (P1) desired to be allocated as renewable xylene and the mass % of paraxylene (P2) desired to be allocated as renewable paraxylene need not exceed 10 mass %. Fig.12EAs shown, in step (Z-1), when benzene, xylene and para-xylene are selected, the total of the mass % of benzene (P1) desired to be allocated as renewable benzene, the mass % of xylene (P2) desired to be allocated as renewable xylene, and the mass % of para-xylene (P3) desired to be allocated as renewable para-xylene needs to be no more than 10 mass %.

[0330] (Management Methods for Terephthalic Acid)

[0331] It is also desired to allocate the value of terephthalic acid produced by the above-mentioned method for producing terephthalic acid of the present invention as a renewable product using a mass balance method by a simple and reliable method.

[0332] Therefore, the present invention provides a management method that can allocate the value of terephthalic acid as a renewable product to terephthalic acid by a simple and reliable method according to the content ratio of renewable naphtha contained in the renewable naphtha raw material when terephthalic acid is produced using the above-mentioned terephthalic acid production method of the present invention.

[0333] It should be noted that the explanation of the mass balance method is as described above.

[0334] The terephthalic acid management method of the present invention can be used when terephthalic acid is produced using a naphtha feedstock containing renewable naphtha.

[0335] The management method of the present invention is a method for allocating the value of the above-mentioned terephthalic acid as a renewable product according to the content ratio of renewable naphtha contained in the renewable naphtha raw material.

[0336] The management method of the present invention includes step (E) of confirming the production of terephthalic acid, and step (E) includes the following step (V-1), the following step (G-2), the following step (W-3), the following step (E-4), and the following step (E-5).

[0337] The step (V-1) is a step of confirming the production of toluene from the naphtha raw material fed into a device (steam cracker) that performs thermal cracking in the presence of water vapor.

[0338] The step (G-2) is a step of confirming the production of xylene from toluene fed to the disproportionation device or fed to the transalkylation (TA) device together with the C9-based components.

[0339] The step (W-3) is a step of confirming that paraxylene is obtained from the xylene fed into the paraxylene unit.

[0340] The step (E-4) is a step of confirming that terephthalic acid is obtained from the paraxylene fed into the terephthalic acid plant.

[0341] Step (E-5) is a step of confirming that terephthalic acid is obtained from the naphtha raw material by sequentially treating with the apparatus for thermal cracking in the presence of water vapor (steam cracker), the disproportionation apparatus or the transalkylation (TA) apparatus, the paraxylene apparatus, and the terephthalic acid apparatus.

[0342] In addition, each confirmation step can be performed based on the same considerations as those in the above-mentioned (management method of renewable monocyclic aromatic hydrocarbons).

[0343] Furthermore, the terephthalic acid management method of the present invention includes a step (H) of confirming the ratio of products to which value is allocated as renewable products, and the step (H) includes the following step (H-1), the following step (H-2), the following step (H-3), and the following step (H-4).

[0344] The step (H-1) is a step of selecting a product to be distributed as a renewable product from among the products obtained from the above-mentioned terephthalic acid plant.

[0345] The step (H-2) is a step of determining a value of a ratio (P) of the product selected in the step (H-1) to be allocated as a renewable product relative to the product obtained from the terephthalic acid plant.

[0346] The step (H-3) is a step of finding the value of the content ratio (Q) of the renewable naphtha contained in the naphtha raw material.

[0347] The step (H-4) is a step of comparing the value of the ratio (P) with the value of the content ratio (Q) to confirm that the value of the ratio (P) is equal to or less than the value of the content ratio (Q).

[0348] It should be noted that the determination and grasp of the value of the ratio (P) allocated as a renewable product and the comparison of the value of the ratio (P) and the value of the ratio (Q) can be carried out based on the same considerations as the above-mentioned (management method of renewable monocyclic aromatic hydrocarbons).

[0349] (Management Methods for Polyethylene Terephthalate (PET))

[0350] It is also desired to allocate the value of PET produced by the above-mentioned PET production method of the present invention as a renewable product using a simple and reliable method using a mass balance method.

[0351] Therefore, the present invention provides a management method for allocating the value of PET as a renewable product to PET using a simple and reliable method based on the content ratio of renewable naphtha contained in the renewable naphtha raw material when PET is produced using the PET production method of the present invention.

[0352] It should be noted that the explanation of the mass balance method is as described above.

[0353] The PET management method of the present invention can be used when PET is produced using a naphtha feedstock containing renewable naphtha.

[0354] The management method of the present invention is a method of allocating the value of the PET as a renewable product according to the content ratio of the renewable naphtha contained in the naphtha raw material.

[0355] The management method of the present invention includes a step (F) of confirming that PET is obtained, and the step (F) includes the following step (V-1), the following step (G-2), the following step (W-3), the following step (E-4), the following step (F-5), and the following step (F-6).

[0356] The step (V-1) is a step of confirming the production of toluene from the naphtha raw material fed into a device (steam cracker) that performs thermal cracking in the presence of water vapor.

[0357] The step (G-2) is a step of confirming the production of xylene from toluene fed to the disproportionation device or fed to the transalkylation (TA) device together with the C9-based components.

[0358] The step (W-3) is a step of confirming that paraxylene is obtained from the xylene fed into the paraxylene unit.

[0359] The step (E-4) is a step of confirming that terephthalic acid is obtained from the paraxylene fed into the terephthalic acid plant.

[0360] The step (F-5) is a step of confirming that PET is obtained from the terephthalic acid fed into the PET device.

[0361] Step (F-6) is a step of confirming that PET is obtained from the naphtha raw material by treating it with the above-mentioned device for thermal cracking in the presence of water vapor (steam cracker), the above-mentioned disproportionation device or the above-mentioned transalkylation (TA) device, the above-mentioned paraxylene device, the terephthalic acid device, and the PET device.

[0362] In addition, each confirmation step can be performed based on the same considerations as those in the above-mentioned (management method of renewable monocyclic aromatic hydrocarbons).

[0363] Furthermore, the PET management method of the present invention includes a step (J) of confirming the ratio of products to which value is allocated as renewable products, and the step (J) includes the following step (J-1), the following step (J-2), the following step (J-3), and the following step (J-4).

[0364] The step (J-1) is a step of selecting products to be distributed as renewable products from among the products obtained from the above-mentioned PET device.

[0365] The step (J-2) is a step of determining a value of a ratio (P) to be allocated as a renewable product in the ratio of the product selected in the step (J-1) to the product obtained from the PET device.

[0366] The step (J-3) is a step of finding the value of the content ratio (Q) of the renewable naphtha contained in the naphtha raw material.

[0367] The step (J-4) is a step of comparing the value of the ratio (P) with the value of the content ratio (Q) to confirm that the value of the ratio (P) is equal to or less than the value of the content ratio (Q).

[0368] It should be noted that the determination and grasp of the value of the ratio (P) allocated as a renewable product and the comparison of the value of the ratio (P) and the value of the ratio (Q) can be carried out based on the same considerations as the above-mentioned (management method of renewable monocyclic aromatic hydrocarbons).

[0369] <Management device, management program>

[0370] The management method of the present invention described above can be executed using a management device. In addition, the processing of each step of the management method performed by the management device can be executed by a computer having a control unit constituting the management device.

[0371] Hereinafter, a management device for implementing the management method of the present invention and a management program (computer program) executed by a computer of the management device will be described by taking the case where the management method includes step (V) but does not include step (W) as an example. It should be noted that the following description related to the management device and the management program can also be applied in the same manner when the management method includes step (W) but does not include step (V) and when the management method includes step (V) and step (W).

[0372] As a preferred embodiment of the management device of the present invention, the following management devices can be mentioned.

[0373] "A management device for renewable monocyclic aromatic hydrocarbons, used when producing at least one monocyclic aromatic hydrocarbon of benzene and xylene using a naphtha feedstock containing renewable naphtha,

[0374] The management device is a device for allocating the value of the at least one monocyclic aromatic hydrocarbon product as a renewable product according to the content ratio of the renewable naphtha contained in the naphtha raw material.

[0375] The management device comprises a confirmation unit (I) for confirming the generation of xylene and / or benzene.

[0376] The confirmation unit (I) comprises the following mechanism (V-1), the following mechanism (V-2) and the following mechanism (V-3),

[0377] The above-mentioned means (V-1) is a means for confirming that toluene is produced from the above-mentioned naphtha raw material fed into a device (steam cracker) for thermal cracking in the presence of water vapor,

[0378] The above-mentioned means (V-2) is a means for confirming that xylene and / or benzene are produced from toluene fed to the disproportionation device or the TA device.

[0379] The above-mentioned means (V-3) is a means for confirming that xylene and / or benzene are produced from the above-mentioned naphtha raw material by treating it in the above-mentioned device for thermal cracking in the presence of water vapor (steam cracker), the above-mentioned disproportionation device or the above-mentioned TA device in sequence,

[0380] The management device comprises a confirmation unit (I) for confirming the ratio of the product to be allocated as a value of the renewable product,

[0381] The confirmation unit (I) comprises the following mechanism (X-1), the following mechanism (X-2), the following mechanism (X-3) and the following mechanism (X-4),

[0382] The means (X-1) is a means for selecting one or more products to be distributed as renewable products from among the products generated by the disproportionation device or the TA device.

[0383] The means (X-2) is a means for determining a value of a ratio (P) of the product selected in the means (X-1) to be allocated as a renewable product relative to the ratio of the product generated by the disproportionation device or the TA device.

[0384] The means (X-3) is a means for obtaining a value of a content ratio (Q) of the renewable naphtha contained in the naphtha raw material.

[0385] The above-mentioned mechanism (X-4) is a mechanism for comparing the value of the above-mentioned ratio (P) with the value of the above-mentioned content ratio (Q) and confirming that the value of the above-mentioned ratio (P) is less than the value of the above-mentioned content ratio (Q). "

[0386] As a preferred embodiment of the management program of the present invention, the following management program can be mentioned.

[0387] "A renewable monocyclic aromatic hydrocarbon management process for use in producing at least one monocyclic aromatic hydrocarbon selected from the group consisting of benzene and xylene using a naphtha feedstock comprising renewable naphtha,

[0388] The management program is a program for allocating the value of the at least one monocyclic aromatic hydrocarbon product as a renewable product according to the content ratio of the renewable naphtha contained in the naphtha raw material.

[0389] The above management program causes the computer to execute the following processing:

[0390] (V-1): Toluene is confirmed to be produced from the naphtha feedstock fed into a device (steam cracker) for thermal cracking in the presence of water vapor,

[0391] (V-2): Confirmation of the production of xylene and / or benzene from the toluene fed to the disproportionation unit or the TA unit,

[0392] (V-3): confirming that xylene and / or benzene are produced from the naphtha feedstock by sequentially treating the naphtha feedstock with the device for thermal cracking in the presence of water vapor (steam cracker), the disproportionation device or the TA device,

[0393] The above management program causes the computer to execute the following processing:

[0394] (X-1): selecting one or more products from among the products generated by the disproportionation device or the TA device to be distributed as renewable products,

[0395] (X-2): the value of the ratio (P) of the product selected in (X-1) to be allocated as a renewable product relative to the ratio of the product generated by the disproportionation device or the TA device,

[0396] (X-3): the value of the content ratio (Q) of the above-mentioned renewable naphtha contained in the above-mentioned naphtha raw material is known,

[0397] (X-4): Compare the value of the above ratio (P) with the value of the above content ratio (Q), and confirm that the value of the above ratio (P) is less than the value of the above content ratio (Q).

[0398] The above-described terephthalic acid management method of the present invention can also be executed using a management device. The processing of each step of the management method performed by the management device is also executed by a computer having a control unit constituting the management device.

[0399] Hereinafter, a management device for executing the management method of terephthalic acid of the present invention and a management program (computer program) executed by a computer of the management device will be described.

[0400] As a preferred embodiment of the terephthalic acid management device of the present invention, the following management devices can be mentioned.

[0401] "A terephthalic acid management device for use in producing terephthalic acid using a naphtha feedstock containing renewable naphtha,

[0402] The management device is a device for allocating the value of the terephthalic acid as a renewable product according to the content ratio of the renewable naphtha contained in the naphtha raw material.

[0403] The management device comprises a confirmation unit (I) for confirming that terephthalic acid has been obtained,

[0404] The above-mentioned confirmation section (I) includes the following mechanism (V-1), the following mechanism (G-2), the following mechanism (W-3), the following mechanism (E-4) and the following mechanism (E-5),

[0405] The above-mentioned means (V-1) is a means for confirming that toluene is produced from the above-mentioned naphtha raw material fed into a device (steam cracker) for thermal cracking in the presence of water vapor,

[0406] The above-mentioned mechanism (G-2) is a mechanism for confirming that xylene is produced from toluene fed to a disproportionation unit or fed to a transalkylation (TA) unit together with C9 components.

[0407] The above-mentioned mechanism (W-3) is a mechanism for confirming that paraxylene is obtained from the xylene fed into the paraxylene device.

[0408] The above-mentioned mechanism (E-4) is a mechanism for confirming that terephthalic acid is obtained from paraxylene fed into a terephthalic acid plant.

[0409] The above-mentioned mechanism (E-5) is a mechanism for confirming that terephthalic acid is obtained from the above-mentioned naphtha raw material by treating it in the above-mentioned device for thermal cracking in the presence of water vapor (steam cracker), the above-mentioned disproportionation device or the above-mentioned transalkylation (TA) device, the above-mentioned paraxylene device, and the terephthalic acid device in this order,

[0410] The management device includes a confirmation unit (I) for confirming the ratio of the product to be allocated as a value of the renewable product,

[0411] The confirmation section (I) includes the following mechanism (H-1), the following mechanism (H-2), the following mechanism (H-3) and the following mechanism (H-4),

[0412] The above-mentioned means (H-1) is a means for selecting products to be distributed as renewable products from among the products obtained from the above-mentioned terephthalic acid plant,

[0413] The means (H-2) is a means for determining a value of a ratio (P) to be allocated as a renewable product in the ratio of the product selected in the means (H-1) to the product obtained from the terephthalic acid plant,

[0414] The means (H-3) is a means for obtaining a value of a content ratio (Q) of the renewable naphtha contained in the naphtha raw material.

[0415] The above-mentioned mechanism (H-4) is a mechanism for comparing the value of the above-mentioned ratio (P) with the value of the above-mentioned content ratio (Q) and confirming that the value of the above-mentioned ratio (P) is less than the value of the above-mentioned content ratio (Q). "

[0416] As a preferred embodiment of the management procedure of terephthalic acid of the present invention, the following management procedure can be mentioned.

[0417] “A terephthalic acid management process for use when producing terephthalic acid using a naphtha feedstock comprising renewable naphtha,

[0418] The management program is a program for allocating the value of the terephthalic acid as a renewable product according to the content ratio of the renewable naphtha contained in the naphtha raw material.

[0419] The above management program causes the computer to execute the following processing:

[0420] (V-1): Toluene is confirmed to be produced from the naphtha feedstock fed into a device (steam cracker) for thermal cracking in the presence of water vapor,

[0421] (G-2): Confirmation of the production of xylene from toluene fed to the disproportionation unit or fed to the transalkylation (TA) unit together with the C9-based components,

[0422] (W-3): Confirm that paraxylene is obtained from the xylene fed into the paraxylene unit,

[0423] (E-4): Confirmation of obtaining terephthalic acid from paraxylene fed into a terephthalic acid plant,

[0424] (E-5): confirming that terephthalic acid is obtained from the naphtha raw material by sequentially treating with the device for thermal cracking in the presence of water vapor (steam cracker), the disproportionation device or the transalkylation (TA) device, the paraxylene device, and the terephthalic acid device,

[0425] The above management program causes the computer to execute the following processing:

[0426] (H-1): Products selected from the products obtained from the above-mentioned terephthalic acid plant and distributed as renewable products,

[0427] (H-2): a value of a ratio (P) of the product selected in the step (H-1) to be allocated as a renewable product relative to the ratio of the product obtained from the terephthalic acid plant,

[0428] (H-3): understanding the value of the content ratio (Q) of the above-mentioned renewable naphtha contained in the above-mentioned naphtha raw material,

[0429] (H-4): Compare the value of the above ratio (P) with the value of the above content ratio (Q), and confirm that the value of the above ratio (P) is less than the value of the above content ratio (Q).

[0430] Furthermore, the polyethylene terephthalate management method of the present invention described above can also be executed using a management device. In addition, the processing of each step of the management method performed by the management device is also executed by a computer having a control unit constituting the management device.

[0431] Hereinafter, a management device for executing the polyethylene terephthalate management method of the present invention and a management program (computer program) executed by a computer of the management device will be described.

[0432] As a preferred embodiment of the polyethylene terephthalate management device of the present invention, the following management devices can be mentioned.

[0433] "A polyethylene terephthalate management device for use when polyethylene terephthalate is produced using a naphtha feedstock containing renewable naphtha,

[0434] The management device is a device for allocating the value of the polyethylene terephthalate as a renewable product according to the content ratio of the renewable naphtha contained in the naphtha raw material.

[0435] The management device includes a confirmation unit (I) for confirming that polyethylene terephthalate is obtained,

[0436] The above-mentioned confirmation section (I) includes the following mechanism (V-1), the following mechanism (G-2), the following mechanism (W-3), the following mechanism (E-4), the following mechanism (F-5) and the following mechanism (F-6),

[0437] The above-mentioned means (V-1) is a means for confirming that toluene is produced from the above-mentioned naphtha raw material fed into a device (steam cracker) for thermal cracking in the presence of water vapor,

[0438] The above-mentioned mechanism (G-2) is a mechanism for confirming that xylene is produced from toluene fed to a disproportionation unit or fed to a transalkylation (TA) unit together with C9 components.

[0439] The above-mentioned mechanism (W-3) is a mechanism for confirming that paraxylene is obtained from the xylene fed into the paraxylene device.

[0440] The above-mentioned mechanism (E-4) is a mechanism for confirming that terephthalic acid is obtained from paraxylene fed into a terephthalic acid plant.

[0441] The above-mentioned mechanism (F-5) is a mechanism for confirming that polyethylene terephthalate is obtained from terephthalic acid fed into the PET device.

[0442] The above-mentioned mechanism (F-6) is a mechanism for confirming that polyethylene terephthalate is obtained from the above-mentioned naphtha raw material by treating it in the above-mentioned device for thermal cracking in the presence of water vapor (steam cracker), the above-mentioned disproportionation device or the above-mentioned transalkylation (TA) device, the above-mentioned paraxylene device, the terephthalic acid device, and the PET device in this order,

[0443] The management device includes a confirmation unit (I) for confirming the ratio of the product to be allocated as a value of the renewable product,

[0444] The above-mentioned confirmation section (I) includes the following mechanism (J-1), the following mechanism (J-2), the following mechanism (J-3) and the following mechanism (J-4),

[0445] The above-mentioned means (J-1) is a means for selecting products to be distributed as renewable products from among the products obtained from the above-mentioned PET device,

[0446] The means (J-2) is a means for determining a value of a ratio (P) to be allocated as a renewable product in the ratio of the product selected in the means (J-1) to the product obtained by the PET device.

[0447] The means (J-3) is a means for obtaining a value of a content ratio (Q) of the renewable naphtha contained in the naphtha raw material.

[0448] The above-mentioned means (J-4) is a means for comparing the value of the above-mentioned ratio (P) with the value of the above-mentioned content ratio (Q) and confirming that the value of the above-mentioned ratio (P) is less than the value of the above-mentioned content ratio (Q). "

[0449] Moreover, as a preferable embodiment of the management procedure of polyethylene terephthalate of the present invention, the following management procedure can be mentioned.

[0450] “A polyethylene terephthalate management program for use when polyethylene terephthalate is manufactured using a naphtha feedstock comprising renewable naphtha,

[0451] The management program is a program for allocating the value of the polyethylene terephthalate as a renewable product according to the content ratio of the renewable naphtha contained in the naphtha raw material.

[0452] The above management program causes the computer to execute the following processing:

[0453] (V-1): Toluene is confirmed to be produced from the naphtha feedstock fed into a device (steam cracker) for thermal cracking in the presence of water vapor,

[0454] (G-2): Confirmation of the production of xylene from toluene fed to the disproportionation unit or fed to the transalkylation (TA) unit together with the C9-based components,

[0455] (W-3): Confirm that paraxylene is obtained from the xylene fed into the paraxylene unit,

[0456] (E-4): Confirmation of obtaining terephthalic acid from paraxylene fed into a terephthalic acid plant,

[0457] (F-5): Confirming that polyethylene terephthalate is obtained from terephthalic acid fed into the PET device,

[0458] (F-6): Confirming that polyethylene terephthalate is obtained from the naphtha raw material by sequentially treating with the device for thermal cracking in the presence of water vapor (steam cracker), the disproportionation device or the transalkylation (TA) device, the paraxylene device, the terephthalic acid device, and the PET device,

[0459] The above management program causes the computer to execute the following processing:

[0460] (J-1): selecting products to be distributed as renewable products from among the products obtained from the above-mentioned PET device,

[0461] (J-2): Determining a value of a ratio (P) of the product selected in the step (J-1) to be allocated as a renewable product relative to the product obtained from the PET device,

[0462] (J-3): understanding the value of the content ratio (Q) of the above-mentioned renewable naphtha contained in the above-mentioned naphtha raw material,

[0463] (J-4): Compare the value of the above ratio (P) with the value of the above content ratio (Q), and determine that the value of the above ratio (P) is less than the value of the above content ratio (Q).

[0464] <<Management device>>

[0465] The management device is a device that executes the management method of the present invention.

[0466] according to Fig.13 A preferred embodiment of the management device will be described.

[0467] The management device 100 includes a control unit 110 and a storage unit 120 .

[0468] The control unit 110 includes a confirmation unit (I) 130 , a comparison unit 140 , and a notification unit (output unit) 150 , and the storage unit 120 includes a reaction database 160 .

[0469] The hardware configuration and functional configuration of the management device 100 will be described.

[0470] <<Hardware configuration of management device>>

[0471] Fig.14 This is a block diagram showing an example of the hardware configuration of the management device 100 .

[0472] like Fig.14 As shown, the management device 100 includes the following components. The components are connected via a bus 207 .

[0473] The CPU 201 is a processing device (computer) that performs various controls and calculations. The CPU 201 implements various functions by executing the OS and computer programs stored in the main storage device 202. That is, in this embodiment, the CPU 201 functions as the control unit 110 of the management device by executing the management program and executes the management method.

[0474] The CPU 201 controls the operation of the entire management device 100. In this embodiment, the device that controls the operation of the entire management device 100 is the CPU 201, but the present invention is not limited thereto and may be, for example, an FPGA (Field Programmable Gate Array).

[0475] The management program and various databases are not necessarily stored in the main storage device 202, the auxiliary storage device 203, etc. The management program and various databases may be stored in other information processing devices connected to the management device 100 via a network, a LAN (Local Area Network), a WAN (Wide Area Network), etc. The management device 100 can obtain the management program and various databases from these other information processing devices and execute them.

[0476] The main storage device 202 is a computer-readable storage medium that stores various programs and stores data necessary for executing the various programs.

[0477] The main storage device 202 includes a ROM and a RAM (not shown).

[0478] The ROM stores various programs such as BIOS.

[0479] The RAM functions as a work range that is carried out when various programs stored in the ROM are executed by the CPU 201. There is no limitation on the RAM, and it can be appropriately selected according to the purpose. For example, DRAM, SRAM, etc. can be cited as the RAM.

[0480] The auxiliary storage device 203 is not particularly limited as long as it can store various information, and can be appropriately selected as needed, for example, a solid state drive, a hard disk drive, etc. In addition, the auxiliary storage device 203 can also be a removable storage device such as a CD drive, a DVD drive, or a BD drive.

[0481] A display, a speaker, etc. can be used as the output device 204. The display is not particularly limited, and a known display can be used appropriately, and examples thereof include a liquid crystal display and an organic EL display.

[0482] The input device 205 is not particularly limited as long as it can accept various requests to the management device 100 , and a known input device can be used appropriately, for example, a keyboard, a mouse, a touch panel, etc.

[0483] The communication interface (communication I / F) 206 is not particularly limited, and a known communication interface can be used appropriately, and examples thereof include a communication device using wireless or wired communication.

[0484] The processing functions of the management device 100 can be realized by the above-mentioned hardware configuration.

[0485] <<Functional structure of management device>>

[0486] Return to Fig.13 The management device 100 includes a control unit 110 and a storage unit 120. The control unit 110 controls the entire management device 100.

[0487] The control unit 110 includes a confirmation unit (I) 130 , a comparison unit 140 , and a notification unit (output unit) 150 .

[0488] The confirmation unit (I) of the control unit 110 performs the confirmation operations described in the above-mentioned means (V-1) to (V-3).

[0489] In addition, the confirmation unit (I) of the control unit 110 performs the following confirmation operations: in the above-mentioned mechanism (X-1), the product selected to be distributed as a renewable product is confirmed; in the above-mentioned mechanism (X-2), the value of the ratio (P) of the selected product to be distributed as a renewable product is confirmed; in the above-mentioned mechanism (X-3), the value of the content ratio (Q) of renewable naphtha is confirmed; in the above-mentioned mechanism (X-4), the value of the ratio (P) and the value of the content ratio (Q) are compared to confirm that the value of the ratio (P) is less than the value of the content ratio (Q).

[0490] The comparison unit 140 of the control unit 110 performs the following comparison operation: in the above-mentioned mechanism (X-4), the value of the ratio (P) and the value of the inclusion ratio (Q) are compared so that the confirmation unit (I) can confirm.

[0491] The notification unit 150 of the control unit 110 notifies (outputs) that (P) mass % of the selected product can be allocated to the product as a renewable product when the value of the ratio (P) is less than the value of the content ratio (Q). On the other hand, when the value of the ratio (P) exceeds the value of the content ratio (Q), it notifies (outputs) that it has been exceeded.

[0492] That is, after executing the management method, the management device 100 outputs the result obtained by the management method of allocating the value as the renewable product to the selected product according to the content ratio of the renewable naphtha contained in the naphtha raw material.

[0493] The reaction database 160 in the storage unit 120 of the control unit 110 stores information related to the device used in the management method of the present invention and information related to the reaction performed in the device. That is, the storage unit 120 includes a computer-readable storage medium storing a computer program, and stores a management program for causing the control unit 110 including a computer to execute the management method.

[0494] The amount and yield of the product obtained by each device can be obtained by measurement. However, the yield result can be obtained not only by actual measurement but also by theoretical calculation using the reaction database 160 or by prediction based on past accumulated data.

[0495] Next, the processing sequence of the hypervisor will be described. Fig.15 1 is a flowchart showing an example of the processing sequence of the management program of the control unit 110 of the management device 100. Fig.15 Provide explanation.

[0496] In step S101 , the confirmation unit 130 of the control unit 110 of the management device 100 acquires information related to the steam cracker, and the process proceeds to step S102 .

[0497] In step S102, the confirmation unit 130 of the control unit 110 of the management device 100 confirms that toluene (OUT) is produced from the renewable naphtha feedstock (IN) in the steam cracker, and if it is confirmed that toluene is produced, the process proceeds to step S103.

[0498] In step S103, the confirmation unit 130 of the control unit 110 of the management device 100 acquires information related to the disproportionation device or the TA device, and the process proceeds to step S104.

[0499] In step S104, the confirmation unit 130 of the control unit 110 of the management device 100 confirms the generation of xylene and / or benzene (OUT) from toluene (IN) in the disproportionation device or the TA device, and if the generation is confirmed, the process proceeds to step S105.

[0500] In step S105, the confirmation unit 130 of the control unit 110 of the management device 100 confirms that the processing is carried out in sequence by the steam cracker, the disproportionation unit or the TA unit. As a result of these processing, it is confirmed that xylene and / or benzene (OUT) are generated from the renewable naphtha raw material (IN). When it is confirmed that they have been generated, the processing is moved to step S106.

[0501] In step S106, the confirmation unit 130 of the control unit 110 of the management device 100 receives an input from the input device ( Fig.14 The input device 205 in receives the information selected by the operator when distributing the products generated by the disproportionation device or the TA device as renewable products, and the processing is moved to step S107.

[0502] In step S107, the confirmation unit 130 of the control unit 110 of the management device 100 receives an input from the input device ( Fig.14 The input device 205 in receives the value of the ratio (P) set by the operator when allocating the selected product as a renewable product, and the processing moves to step S108.

[0503] In step S108, the confirmation unit 130 of the control unit 110 of the management device 100 obtains the value of the content ratio (Q) of renewable naphtha in the renewable naphtha raw material fed to the steam cracker, and the process proceeds to step S109.

[0504] In step S109 , the comparison unit 140 of the control unit 110 of the management device 100 compares the value of the ratio (P) with the value of the content ratio (Q), and the process proceeds to step S110 .

[0505] In step S110, the confirmation unit 130 of the control unit 110 of the management device 100 confirms whether the value of the ratio (P) is less than the value of the content ratio (Q) based on the comparison result of the value of the ratio (P) and the value of the content ratio (Q) performed by the comparison unit 140 of the control unit 110 of the management device 100, and when it is confirmed to be less than the value, the present processing is terminated.

[0506] By completing this process, the value as a renewable product can be allocated to the selected desired product according to the content ratio of renewable naphtha contained in the renewable naphtha raw material. The allocation result is notified to the user through the notification unit 150 of the control unit 110 of the management device 100. That is, as described above, after executing the management method, the management device 100 outputs the result of allocating the value as a renewable product to the selected product according to the content ratio of renewable naphtha contained in the naphtha raw material obtained by the management method.

[0507] It should be noted that, when the conditions are not met in this process, the user is notified of this fact, for example, by the notification unit 150 of the control unit 110 of the management device 100. In this case, the operator can reconsider the type of product selected in the above (X-1), reconsider the value of the distribution ratio (P) of the selected product, reconsider the value of the content ratio (Q) of renewable naphtha, and further reconsider various conditions such as reaction conditions, and try to perform the process again.

[0508] exist Figures 13-15 In the present invention, a management method including process (V) but not process (W) is taken as an example to explain the management device and management procedure using the management method. However, as mentioned above, the same management device and management procedure can be applied to a management method including process (W) but not process (V) or a management method including process (V) and process (W).

[0509] (First Modification)

[0510] (Functional Structure of Management Device for Executing Terephthalic Acid Management Method)

[0511] Here, the basic functional components of the management device for executing the above-described management method for terephthalic acid also have the same functions as those of the above-described management method. Fig.13 and Fig.14 The management device 100 shown in FIG. Fig.13 and Fig.14 The functional configuration of a management device for executing the terephthalic acid management method will be described.

[0512] like Fig.13As shown, the management device 100 for executing the management method of terephthalic acid also includes a control unit 110 and a storage unit 120. The control unit 110 controls the entire management device 100.

[0513] The control unit 110 includes a confirmation unit (I) 130 , a comparison unit 140 , and a notification unit (output unit) 150 .

[0514] The confirmation unit (I) of the control unit 110 performs the confirmation operations described in the above-described mechanism (V-1), mechanism (G-2), mechanism (W-3), mechanism (E-4), and mechanism (E-5).

[0515] In addition, the confirmation unit (I) of the control unit 110 performs the following confirmation operations: in the described mechanism (H-1), the product selected from the products obtained from the terephthalic acid unit to be allocated as a renewable product is confirmed; in the mechanism (H-2), the value of the ratio (P) set to be allocated as a renewable product in the ratio of the product selected in the mechanism (H-1) to the product obtained from the terephthalic acid unit is confirmed; in the mechanism (H-3), the value of the content ratio (Q) of renewable naphtha contained in the naphtha raw material is confirmed; in the mechanism (H-4), the value of the ratio (P) is compared with the value of the content ratio (Q) to confirm that the value of the ratio (P) is less than the value of the content ratio (Q).

[0516] The comparison unit 140 of the control unit 110 performs a comparison operation by comparing the value of the ratio (P) and the value of the content ratio (Q) in the mechanism (H-4) to allow the confirmation unit (I) to confirm.

[0517] The notification unit 150 of the control unit 110 notifies (outputs) that (P) mass % of the selected product can be allocated to the product as a renewable product when the value of the ratio (P) is less than the value of the content ratio (Q). On the other hand, when the value of the ratio (P) exceeds the value of the content ratio (Q), it notifies (outputs) that it has been exceeded.

[0518] That is, after executing the terephthalic acid management method, the management device 100 that executes the terephthalic acid management method outputs the result of allocating the value as the renewable product to the selected product according to the content ratio of the renewable naphtha contained in the naphtha raw material obtained by the terephthalic acid management method.

[0519] The reaction database 160 in the storage unit 120 of the control unit 110 stores information on the apparatus used in the management method of terephthalic acid of the present invention and information on the reactions performed in the apparatus. That is, the storage unit 120 includes a computer-readable storage medium storing a computer program, and stores the management program for causing the control unit 110 including a computer to execute the management method of terephthalic acid.

[0520] The amount and yield of the product obtained by each device can be obtained by measurement. However, the yield result can be obtained not only by actual measurement but also by theoretical calculation using the reaction database 160 or by prediction based on past accumulated data.

[0521] Next, the processing procedure of the terephthalic acid management program will be described. Fig.16 FIG. 1 is a flowchart showing an example of the processing sequence of the terephthalic acid management program of the control unit 110 of the terephthalic acid management device 100. Fig.16 For explanation.

[0522] In step S201, the confirmation unit 130 of the control unit 110 of the terephthalic acid management device 100 acquires information related to the steam cracker, and the process moves to step S202.

[0523] In step S202, the confirmation unit 130 of the control unit 110 of the terephthalic acid management device 100 confirms that toluene (OUT) is produced from the renewable naphtha feedstock (IN) in the steam cracker, and if it is confirmed that toluene is produced, the process moves to step S203.

[0524] In step S203, the confirmation unit 130 of the control unit 110 of the terephthalic acid management device 100 acquires information on the disproportionation device or the TA device, and the process proceeds to step S204.

[0525] In step S204, the confirmation unit 130 of the control unit 110 of the terephthalic acid management device 100 confirms the generation of xylene and / or benzene (OUT) from toluene (IN) in the disproportionation device or TA device, and if the generation is confirmed, the process proceeds to step S205.

[0526] In step S205, the confirmation unit 130 of the control unit 110 of the terephthalic acid management device 100 confirms that the steam cracker, the disproportionation unit or the TA unit, the paraxylene unit, and the terephthalic acid unit are sequentially processed. As a result of these processes, it is confirmed that terephthalic acid (OUT) is generated from the renewable naphtha raw material (IN). When it is confirmed that terephthalic acid (OUT) is generated, the process is transferred to step S206.

[0527] In step S206, the confirmation unit 130 of the control unit 110 of the terephthalic acid management device 100 receives an input from the input device ( Fig.14 The input device 205 in receives the information selected by the operator when allocating the products generated by the terephthalic acid plant as renewable products, and the processing is moved to step S207.

[0528] In step S207, the confirmation unit 130 of the control unit 110 of the terephthalic acid management device 100 receives the input device ( Fig.14 The input device 205 in receives the value of the ratio (P) set by the operator when allocating the selected product as a renewable product, and the processing moves to step S208.

[0529] In step S208, the confirmation unit 130 of the control unit 110 of the terephthalic acid management device 100 obtains the value of the content ratio (Q) of renewable naphtha in the renewable naphtha raw material fed to the steam cracker, and the process proceeds to step S209.

[0530] In step S209, the comparison unit 140 of the control unit 110 of the terephthalic acid management device 100 compares the value of the ratio (P) and the value of the content ratio (Q), and the process proceeds to step S210.

[0531] In step S210, the confirmation unit 130 of the control unit 110 of the terephthalic acid management device 100 confirms whether the value of the ratio (P) is less than the value of the content ratio (Q) based on the comparison result of the value of the ratio (P) and the value of the content ratio (Q) performed by the comparison unit 140 of the control unit 110 of the terephthalic acid management device 100, and when it is confirmed that it is less than the value, the present processing is terminated.

[0532] By completing this process, the value as a renewable product can be allocated to the selected desired product according to the content ratio of renewable naphtha contained in the renewable naphtha raw material. The allocation result is notified to the user through the notification unit 150 of the control unit 110 of the terephthalic acid management device 100. That is, as described above, after executing the terephthalic acid management method, the terephthalic acid management device 100 outputs the result of allocating the value as a renewable product to the selected product according to the content ratio of renewable naphtha contained in the naphtha raw material obtained by the terephthalic acid management method.

[0533] It should be noted that, when the conditions are not met in the present process, the user is notified of this fact, for example, by the notification unit 150 of the control unit 110 of the terephthalic acid management device 100. In this case, the operator can reconsider the type of product selected in the above (X-1), reconsider the value of the distribution ratio (P) of the selected product, reconsider the value of the content ratio (Q) of renewable naphtha, and further reconsider various conditions such as reaction conditions, and try the process again.

[0534] (Second Modification)

[0535] (Functional Structure of Management Device for Executing Polyethylene Terephthalate Management Method)

[0536] Here, the basic functional components of the management device for executing the management method of polyethylene terephthalate described above also have the same functions as those described above. Fig.13 and Fig.14 The management device 100 shown in FIG. Fig.13 and Fig.14 , the functional structure of a management device for executing a management method for polyethylene terephthalate is described.

[0537] like Fig.13 As shown, the management device 100 for executing the management method of polyethylene terephthalate also includes a control unit 110 and a storage unit 120. The control unit 110 controls the entire management device 100.

[0538] The control unit 110 includes a confirmation unit (I) 130 , a comparison unit 140 , and a notification unit (output unit) 150 .

[0539] The confirmation unit (I) of the control unit 110 performs the confirmation operations described in the above-described mechanism (V-1), mechanism (G-2), mechanism (W-3), mechanism (E-4), mechanism (F-5), and mechanism (F-6).

[0540] In addition, the confirmation unit (I) of the control unit 110 performs the following confirmation operations: in the described mechanism (J-1), the product selected as the renewable product to be allocated from the products obtained from the PET device is confirmed; in the mechanism (J-2), the value of the proportion (P) set as the renewable product to be allocated in the proportion of the product selected in the mechanism (J-1) relative to the product obtained from the PET device is confirmed; in the mechanism (J-3), the value of the content ratio (Q) of the renewable naphtha contained in the naphtha raw material is confirmed; in the mechanism (J-4), the value of the proportion (P) is compared with the value of the content ratio (Q) to confirm that the value of the proportion (P) is less than the value of the content ratio (Q).

[0541] The comparison unit 140 of the control unit 110 performs the following comparison operation: in the above-mentioned mechanism (J-4), the value of the ratio (P) and the value of the content ratio (Q) are compared to make the confirmation unit (I) confirm.

[0542] The notification unit 150 of the control unit 110 notifies (outputs) that the selected product with (P) mass % is distributed in the product as a renewable product when the value of the ratio (P) is less than the value of the content ratio (Q). On the other hand, when the value of the ratio (P) exceeds the value of the content ratio (Q), it notifies (outputs) that it has been exceeded.

[0543] That is, after executing the polyethylene terephthalate management method, the management device 100 that executes the polyethylene terephthalate management method outputs the result of allocating the value of the renewable product to the selected product according to the content ratio of the renewable naphtha contained in the naphtha raw material obtained by the polyethylene terephthalate management method.

[0544] The reaction database 160 in the storage unit 120 of the control unit 110 stores information about the device used in the polyethylene terephthalate management method of the present invention and information about the reaction performed in the device. That is, the storage unit 120 includes a computer-readable storage medium storing a computer program, and stores the management program for causing the control unit 110 including a computer to execute the polyethylene terephthalate management method.

[0545] The amount and yield of the product obtained by each device can be obtained by measurement. However, the yield result can be obtained not only by actual measurement but also by theoretical calculation using the reaction database 160 or by prediction based on past accumulated data.

[0546] Next, the processing procedure of the polyethylene terephthalate management program will be described. Fig.17 FIG. 1 is a flowchart showing an example of the processing sequence of the polyethylene terephthalate management program in the control unit 110 of the polyethylene terephthalate management device 100. Fig.17 Provide explanation.

[0547] In step S301, the confirmation unit 130 of the control unit 110 of the polyethylene terephthalate management device 100 acquires information related to the steam cracker, and the process proceeds to step S302.

[0548] In step S302, the confirmation unit 130 of the control unit 110 of the polyethylene terephthalate management device 100 confirms that toluene (OUT) is produced from the renewable naphtha feedstock (IN) in the steam cracker, and if it is confirmed that toluene is produced, the process proceeds to step S303.

[0549] In step S303, the confirmation unit 130 of the control unit 110 of the polyethylene terephthalate management device 100 acquires information on the disproportionation device or the TA device, and the process proceeds to step S304.

[0550] In step S304, the confirmation unit 130 of the control unit 110 of the polyethylene terephthalate management device 100 confirms that xylene and / or benzene (OUT) are produced from toluene (IN) in the disproportionation device or TA device, and if production is confirmed, the process proceeds to step S305.

[0551] In step S305, the confirmation unit 130 of the control unit 110 of the polyethylene terephthalate management device 100 confirms that the processing is carried out in sequence using the steam cracker, the disproportionation unit or the TA unit, the paraxylene unit, the terephthalic acid unit, and the PET unit. As a result of these processing, it is confirmed that terephthalic acid (OUT) is generated from the renewable naphtha raw material (IN). When it is confirmed that terephthalic acid has been generated, the processing is moved to step S306.

[0552] In step S306, the confirmation unit 130 of the control unit 110 of the polyethylene terephthalate management device 100 receives the input device ( Fig.14 The input device 205 in receives the information selected by the operator when allocating the products generated by the PET device as renewable products, and the processing is moved to step S307.

[0553] In step S307, the confirmation unit 130 of the control unit 110 of the polyethylene terephthalate management device 100 receives the input device ( Fig.14 The input device 205 in receives the value of the ratio (P) set by the operator when allocating the selected product as a renewable product, and the processing moves to step S308.

[0554] In step S308, the confirmation unit 130 of the control unit 110 of the polyethylene terephthalate management device 100 obtains the value of the content ratio (Q) of renewable naphtha in the renewable naphtha raw material fed to the steam cracker, and the process proceeds to step S309.

[0555] In step S309 , the comparison unit 140 of the control unit 110 of the polyethylene terephthalate management device 100 compares the value of the ratio (P) and the value of the content ratio (Q), and the process proceeds to step S310 .

[0556] In step S310, the confirmation unit 130 of the control unit 110 of the polyethylene terephthalate management device 100 confirms whether the value of the ratio (P) is less than the value of the content ratio (Q) based on the comparison result of the value of the ratio (P) and the value of the content ratio (Q) performed in the comparison unit 140 of the control unit 110 of the polyethylene terephthalate management device 100, and when it is confirmed to be less than the value, the present processing is terminated.

[0557] By completing this process, the value as a renewable product can be allocated to the selected desired product according to the content ratio of renewable naphtha contained in the renewable naphtha raw material. The allocation result is notified to the user through the notification unit 150 of the control unit 110 of the polyethylene terephthalate management device 100. That is, as described above, after executing the polyethylene terephthalate management method, the polyethylene terephthalate management device 100 outputs the result of allocating the value as a renewable product to the selected product according to the content ratio of renewable naphtha contained in the naphtha raw material obtained by the polyethylene terephthalate management method.

[0558] It should be noted that, when the conditions are not met in this process, the user is notified of this fact, for example, by the notification unit 150 of the control unit 110 of the polyethylene terephthalate management device 100. In this case, the operator can reconsider the type of product selected in the above (X-1), reconsider the value of the distribution ratio (P) of the selected product, reconsider the value of the content ratio (Q) of renewable naphtha, and further reconsider various conditions such as reaction conditions, and try the process again.

[0559] Although some embodiments of the present invention have been described, these embodiments are provided as examples and are not intended to limit the scope of the invention. These embodiments may be implemented in various other ways, and various omissions, substitutions, and changes may be made without departing from the scope of the invention. These embodiments and their variations are included in the scope and purpose of the invention, and are also included in the invention described in the scope of the patent claim and its equivalent scope.

Claims

1. A method for producing monocyclic aromatic hydrocarbons, comprising producing at least one monocyclic aromatic hydrocarbon selected from benzene and xylene using a naphtha feedstock comprising renewable naphtha, comprising: Step (A-1), generating toluene by thermally cracking the naphtha raw material in the presence of water vapor and separating the toluene, and In step (A-2), toluene is subjected to a disproportionation reaction or a transalkylation reaction to produce at least one monocyclic aromatic hydrocarbon of benzene and xylene, and the resulting mixture is separated.

2. The manufacturing method according to claim 1, wherein: In the step (A-1), components including monocyclic aromatic hydrocarbons in a thermal cracking product obtained by thermally cracking the naphtha feedstock in the presence of water vapor are separated and purified by distillation or extraction, thereby generating and separating toluene.

3. The manufacturing method according to claim 1, wherein: Further including: In step (A-3), the xylene obtained in step (A-2) is subjected to adsorption separation or crystallization separation to separate paraxylene.

4. The manufacturing method according to claim 3, wherein: The method comprises the steps of isomerizing a residue containing at least one of o-xylene and m-xylene after separating p-xylene in the step (A-3) to produce p-xylene, and then isolating the p-xylene by adsorption separation or crystallization separation.

5. The production method according to any one of claims 1 to 4, wherein The monocyclic aromatic hydrocarbons contain radioactive carbon atoms 14 C.

6. A type of xylene containing radioactive carbon atoms 14 C.

7. Xylene according to claim 6, wherein The radioactive carbon atom 14 C comes from bio-naphtha.

8. A method for producing terephthalic acid using a naphtha feedstock containing renewable naphtha, comprising: Step (A-3), obtaining p-xylene by the method according to claim 3, and In step (A-4), p-xylene is oxidized to obtain terephthalic acid.

9. A type of terephthalic acid containing radioactive carbon atoms 14 C.

10. The terephthalic acid according to claim 9, wherein The radioactive carbon atom 14 C comes from bio-naphtha.

11. A method for producing polyethylene terephthalate using a naphtha feedstock containing renewable naphtha to produce polyethylene terephthalate, comprising: Step (A-4), obtaining terephthalic acid by the method according to claim 8, and In step (A-5), polyethylene terephthalate is obtained by a condensation reaction of terephthalic acid and ethylene glycol.

12. A polyethylene terephthalate containing radioactive carbon atoms derived from bio-naphtha 14 C.

13. A method for managing monocyclic aromatic hydrocarbons, the method being used when producing at least one monocyclic aromatic hydrocarbon of benzene and xylene using a naphtha feedstock containing renewable naphtha, The management method is a method of allocating the value of the at least one monocyclic aromatic hydrocarbon as a renewable product according to the content ratio of the renewable naphtha contained in the naphtha raw material. The management method comprises at least one step selected from step (V) and step (W), wherein step (V) is a step for confirming the generation of xylene and / or benzene, and step (W) is a step for confirming the generation of p-xylene. The step (V) includes the following step (V-1), the following step (V-2) and the following step (V-3), The step (V-1) is a step of confirming that toluene is produced from the naphtha feedstock fed into a steam cracker which is a device for thermal cracking in the presence of water vapor. The step (V-2) is a step of confirming that xylene and / or benzene is produced from toluene fed into the disproportionation unit or fed into the transalkylation unit, i.e., the TA unit, together with the C9-based components. The step (V-3) is a step of confirming that xylene and / or benzene are produced from the naphtha feedstock by sequentially treating the naphtha feedstock with the steam cracker, the disproportionation device or the transalkylation device, the TA device. The step (W) includes the following step (V-1), the following step (V-2), the following step (W-3) and the following step (W-4), The step (V-1) is a step of confirming that toluene is produced from the naphtha feedstock fed into a steam cracker which is a device for thermal cracking in the presence of water vapor. The step (V-2) is a step of confirming that xylene and / or benzene is produced from toluene fed into the disproportionation unit or fed into the transalkylation unit, i.e., the TA unit, together with the C9-based components. The step (W-3) is a step of confirming that paraxylene is obtained from the xylene fed into the paraxylene device. The step (W-4) is a step of confirming that paraxylene is obtained from the naphtha raw material by sequentially treating the naphtha raw material with the steam cracker, the disproportionation device or the transalkylation device, the TA device, and the paraxylene device. When the management method includes the step (V) and the step (W), the management method includes a step (Z) of confirming the ratio of products to which the value as renewable products is allocated, The step (Z) includes the following step (Z-1), the following step (Z-2), the following step (Z-3) and the following step (Z-4), The step (Z-1) is a step of selecting one or more products to be distributed as renewable products from among the products obtained from the disproportionation unit or the transalkylation unit (TA unit) and the paraxylene unit. The step (Z-2) is a step of determining a value of a ratio P of the product selected in the step (Z-1) to be allocated as a renewable product relative to the ratio of the product obtained from the disproportionation unit or the transalkylation unit (TA unit) and the paraxylene unit. The step (Z-3) is a step of obtaining a value of a content ratio Q of the renewable naphtha contained in the naphtha raw material. The step (Z-4) is a step of comparing the value of the ratio P with the value of the content ratio Q, and confirming that the value of the ratio P is equal to or less than the value of the content ratio Q.

14. The management method according to claim 13, wherein: When the management method includes the step (V) but does not include the step (W), the management method includes the step (X) of confirming the ratio of the product to which the value as the renewable product is allocated, The step (X) includes the following step (X-1), the following step (X-2), the following step (X-3) and the following step (X-4), The step (X-1) is a step of selecting one or more products from among the products generated by the disproportionation unit or the transalkylation unit (TA unit) as renewable products to be distributed. The step (X-2) is a step of determining a value of a ratio P of the product selected in the step (X-1) to be allocated as a renewable product relative to the ratio of the product generated by the disproportionation unit or the transalkylation unit (TA unit), The step (X-3) is a step of obtaining a value of a content ratio Q of the renewable naphtha contained in the naphtha raw material. The step (X-4) is a step of comparing the value of the ratio P with the value of the content ratio Q, and confirming that the value of the ratio P is equal to or less than the value of the content ratio Q.

15. The management method according to claim 13, wherein: When the management method includes the step (W) but does not include the step (V), the management method includes a step (Y) of confirming the ratio of products to which the value as renewable products is allocated, The step (Y) includes the following step (Y-1), the following step (Y-2), the following step (Y-3) and the following step (Y-4), The step (Y-1) is a step of selecting one or more products from among the products obtained from the paraxylene unit to be distributed as renewable products. The step (Y-2) is a step of determining a value of a ratio P of the product selected in the step (Y-1) to be allocated as a renewable product relative to the ratio of the product obtained from the paraxylene unit. The step (Y-3) is a step of obtaining a value of a content ratio Q of the renewable naphtha contained in the naphtha raw material. The step (Y-4) is a step of comparing the value of the ratio P with the value of the content ratio Q, and confirming that the value of the ratio P is equal to or less than the value of the content ratio Q.

16. The management method according to claim 15, wherein: In the step (X-1), the step (Y-1) or the step (Z-1), when two or more products are selected to be allocated as the renewable products, the value of the proportion P allocated as the renewable product determined in the step (X-2), the step (Y-2) or the step (Z-2) is the value obtained by summing up the proportions allocated to the two or more selected products.

17. The management method according to claim 13, wherein: The management method includes the step (V) and the step (W), and in the step (Z-1), when the products to be distributed as the renewable products are selected from two types: benzene and paraxylene, The value of the ratio P allocated as a renewable product determined in the step (Z-2) is a value obtained by summing the ratio P1 and the ratio P2, wherein the ratio P1 is the ratio of benzene allocated as renewable benzene relative to the ratio of products obtained from the disproportionation unit or the alkyl transfer unit, i.e., the TA unit, and the para-xylene unit, and the ratio P2 is the ratio of para-xylene allocated as renewable para-xylene relative to the ratio of products obtained from the disproportionation unit or the alkyl transfer unit, i.e., the TA unit, and the para-xylene unit.

18. A method for managing terephthalic acid, the method being a method for managing terephthalic acid used when producing terephthalic acid using a naphtha feedstock containing renewable naphtha, The management method is a method of allocating the value of the terephthalic acid as a renewable product according to the content ratio of the renewable naphtha contained in the naphtha raw material. The management method comprises a step (E) of confirming that terephthalic acid is obtained, The step (E) includes the following step (V-1), the following step (G-2), the following step (W-3), the following step (E-4), and the following step (E-5). The step (V-1) is a step of confirming that toluene is produced from the naphtha feedstock fed into a steam cracker which is a device for thermal cracking in the presence of water vapor. The step (G-2) is a step of confirming that xylene is produced from toluene fed into a disproportionation unit or fed into a transalkylation unit, i.e., a TA unit, together with C9 components. The step (W-3) is a step of confirming that paraxylene is obtained from the xylene fed into the paraxylene device. The step (E-4) is a step of confirming that terephthalic acid is obtained from paraxylene fed into a terephthalic acid device. The step (E-5) is a step of confirming that terephthalic acid is obtained from the naphtha raw material by sequentially treating with the steam cracker, the disproportionation device or the transalkylation device, the TA device, the paraxylene device, and the terephthalic acid device. The management method includes a step (H) of confirming the proportion of products that are allocated value as renewable products, The step (H) includes the following step (H-1), the following step (H-2), the following step (H-3) and the following step (H-4), The step (H-1) is a step of selecting a product to be distributed as a renewable product from among the products obtained from the terephthalic acid plant. The step (H-2) is a step of determining a value of a ratio P of the product selected in the step (H-1) to be allocated as a renewable product relative to the product obtained from the terephthalic acid plant. The step (H-3) is a step of obtaining a value of a content ratio Q of the renewable naphtha contained in the naphtha raw material. The step (H-4) is a step of comparing the value of the ratio P with the value of the content ratio Q, and confirming that the value of the ratio P is equal to or less than the value of the content ratio Q.

19. A method for managing polyethylene terephthalate, the method being used when polyethylene terephthalate is produced using a naphtha raw material containing renewable naphtha. The management method is a method of allocating the value of the polyethylene terephthalate as a renewable product according to the content ratio of the renewable naphtha contained in the naphtha raw material. The management method comprises a step (F) of confirming that polyethylene terephthalate is obtained, The step (F) includes the following step (V-1), the following step (G-2), the following step (W-3), the following step (E-4), the following step (F-5), and the following step (F-6), The step (V-1) is a step of confirming that toluene is produced from the naphtha feedstock fed into a steam cracker which is a device for thermal cracking in the presence of water vapor. The step (G-2) is a step of confirming that xylene is produced from toluene fed into a disproportionation unit or fed into a transalkylation unit, i.e., a TA unit, together with C9 components. The step (W-3) is a step of confirming that paraxylene is obtained from the xylene fed into the paraxylene device. The step (E-4) is a step of confirming that terephthalic acid is obtained from paraxylene fed into a terephthalic acid device. The step (F-5) is a step of confirming that polyethylene terephthalate is obtained from the terephthalic acid fed into the PET device. The step (F-6) is a step of confirming that polyethylene terephthalate is obtained from the naphtha raw material by sequentially treating with the steam cracker, the disproportionation device or the transalkylation device, the TA device, the paraxylene device, the terephthalic acid device, and the PET device. The management method comprises a step (J) of confirming the proportion of products to which the value is allocated as renewable products, The step (J) includes the following step (J-1), the following step (J-2), the following step (J-3) and the following step (J-4), The step (J-1) is a step of selecting products to be distributed as renewable products from among the products obtained from the PET device. The step (J-2) is a step of determining a value of a ratio P of the product selected in the step (J-1) to be allocated as a renewable product relative to the product obtained from the PET device. The step (J-3) is a step of obtaining a value of a content ratio Q of the renewable naphtha contained in the naphtha raw material. The step (J-4) is a step of comparing the value of the ratio P with the value of the content ratio Q, and confirming that the value of the ratio P is equal to or less than the value of the content ratio Q.

20. A management device comprising a computer-readable storage medium storing a management program, The management device executes the management method according to any one of claims 13 to 19 by executing the management program.

21. The management device according to claim 20, wherein: After the management method is executed, a result of allocating the value as a renewable product to the selected product according to the content ratio of the renewable naphtha contained in the naphtha raw material obtained by the management method is output.

22. A storage medium is a computer-readable storage medium storing a computer program. A management program for causing a computer to execute the management method according to any one of claims 13 to 19 is stored.

23. A management program for causing a computer to execute the management method according to any one of claims 13 to 19.

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