Classifications

• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
  • C10G9/34—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts
  • C10G9/36—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C6/00—Preparation of hydrocarbons from hydrocarbons containing a different number of carbon atoms by redistribution reactions
  • C07C6/08—Preparation of hydrocarbons from hydrocarbons containing a different number of carbon atoms by redistribution reactions by conversion at a saturated carbon-to-carbon bond
  • C07C6/12—Preparation of hydrocarbons from hydrocarbons containing a different number of carbon atoms by redistribution reactions by conversion at a saturated carbon-to-carbon bond of exclusively hydrocarbons containing a six-membered aromatic ring
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C15/00—Cyclic hydrocarbons containing only six-membered aromatic rings as cyclic parts
  • C07C15/02—Monocyclic hydrocarbons
  • C07C15/04—Benzene
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C15/00—Cyclic hydrocarbons containing only six-membered aromatic rings as cyclic parts
  • C07C15/02—Monocyclic hydrocarbons
  • C07C15/06—Toluene
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C4/00—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms
  • C07C4/02—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by cracking a single hydrocarbon or a mixture of individually defined hydrocarbons or a normally gaseous hydrocarbon fraction
  • C07C4/04—Thermal processes
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
  • C07C51/16—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation
  • C07C51/21—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen
  • C07C51/255—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of compounds containing six-membered aromatic rings without ring-splitting
  • C07C51/265—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of compounds containing six-membered aromatic rings without ring-splitting having alkyl side chains which are oxidised to carboxyl groups
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C6/00—Preparation of hydrocarbons from hydrocarbons containing a different number of carbon atoms by redistribution reactions
  • C07C6/08—Preparation of hydrocarbons from hydrocarbons containing a different number of carbon atoms by redistribution reactions by conversion at a saturated carbon-to-carbon bond
  • C07C6/12—Preparation of hydrocarbons from hydrocarbons containing a different number of carbon atoms by redistribution reactions by conversion at a saturated carbon-to-carbon bond of exclusively hydrocarbons containing a six-membered aromatic ring
  • C07C6/123—Preparation of hydrocarbons from hydrocarbons containing a different number of carbon atoms by redistribution reactions by conversion at a saturated carbon-to-carbon bond of exclusively hydrocarbons containing a six-membered aromatic ring of only one hydrocarbon
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C63/00—Compounds having carboxyl groups bound to a carbon atoms of six-membered aromatic rings
  • C07C63/14—Monocyclic dicarboxylic acids
  • C07C63/15—Monocyclic dicarboxylic acids all carboxyl groups bound to carbon atoms of the six-membered aromatic ring
  • C07C63/26—1,4 - Benzenedicarboxylic acid
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C7/00—Purification; Separation; Use of additives
  • C07C7/04—Purification; Separation; Use of additives by distillation
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C7/00—Purification; Separation; Use of additives
  • C07C7/10—Purification; Separation; Use of additives by extraction, i.e. purification or separation of liquid hydrocarbons with the aid of liquids
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C7/00—Purification; Separation; Use of additives
  • C07C7/12—Purification; Separation; Use of additives by adsorption, i.e. purification or separation of hydrocarbons with the aid of solids, e.g. with ion-exchangers
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C7/00—Purification; Separation; Use of additives
  • C07C7/14—Purification; Separation; Use of additives by crystallisation; Purification or separation of the crystals
• • C—CHEMISTRY; METALLURGY
  • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
  • C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
  • C08G63/00—Macromolecular compounds obtained by reactions forming a carboxylic ester link in the main chain of the macromolecule
  • C08G63/02—Polyesters derived from hydroxycarboxylic acids or from polycarboxylic acids and polyhydroxy compounds
  • C08G63/12—Polyesters derived from hydroxycarboxylic acids or from polycarboxylic acids and polyhydroxy compounds derived from polycarboxylic acids and polyhydroxy compounds
  • C08G63/16—Dicarboxylic acids and dihydroxy compounds
  • C08G63/18—Dicarboxylic acids and dihydroxy compounds the acids or hydroxy compounds containing carbocyclic rings
  • C08G63/181—Acids containing aromatic rings
  • C08G63/183—Terephthalic acids
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
  • C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
  • C10G69/06—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of thermal cracking in the absence of hydrogen
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
  • C10G2400/30—Aromatics

Definitions

• 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).
• the present invention also relates to a method for producing a monocyclic aromatic hydrocarbon, terephthalic acid, and a method for managing polyethylene terephthalate.
• Benzene is a basic raw material for styrene monomer, phenol, cyclohexane, etc., which are processed into chemical products such as plastics, synthetic rubber, and nylon, and are used in a variety of everyday items such as plastic products and clothing.
• Paraxylene is also a basic raw material for terephthalic acid, is processed into polyester fibers, etc., and is used in a variety of everyday products.
• the demand for these useful basic raw materials, such as benzene and paraxylene continues to increase. Incidentally, in light of the recent trend toward decarbonization, there is a rapid movement toward green raw materials in the petrochemical industry.
• Bio-naphtha has a composition similar to the light fraction of petroleum-derived naphtha and can be thermally decomposed in the presence of steam.
• xylene is produced, but it is not suitable as a raw material for producing para-xylene because it contains a high content of ethylbenzene, a by-product.
• para-xylene is produced by hydrodesulfurizing heavy naphtha obtained by distilling crude oil and then isomerizing ortho-xylene and meta-xylene obtained by a catalytic reforming reaction.
• heavy naphtha is generally used as a raw material for a catalytic reforming reaction
• light naphtha or bionaphtha having a composition similar to light naphtha is not normally used as a raw material for a catalytic reforming reaction.
• the conventionally known existing chemical industrial processes use bio-naphtha as effective basic raw materials such as benzene and para-xylene (hereinafter benzene and para-xylene are also collectively referred to as monocyclic aromatic hydrocarbons).
• monocyclic aromatic hydrocarbons derived from bionaphtha.
• an object of the present invention is to provide a method for producing monocyclic aromatic hydrocarbons such as benzene and paraxylene, which are effective as basic raw materials, using naphtha raw materials including renewable naphtha.
• the present invention also provides a method for managing monocyclic aromatic hydrocarbons that can be used when producing monocyclic aromatic hydrocarbons using naphtha raw materials including the above-mentioned renewable naphtha.
• the purpose of the present invention is to provide a management method that allocates value as a renewable product to monocyclic aromatic hydrocarbon products according to the content ratio of renewable naphtha.
• the inventors of the present invention found that by combining reaction steps that are not normally combined in existing chemical industrial processes, and providing a new chemical industrial process, the new chemical
• an industrial process can solve the above problems, and have completed the present invention having the following gist. That is, the present invention includes the following.
• a method for producing at least one monocyclic aromatic hydrocarbon of benzene and xylene using a naphtha raw material including renewable naphtha comprising: a step (A-1) of generating and separating toluene by thermally decomposing the naphtha raw material in the presence of steam; A step (A-2) of producing and separating at least one monocyclic aromatic hydrocarbon of benzene and xylene by disproportionation reaction or transalkylation reaction of toluene; A method for producing a monocyclic aromatic hydrocarbon, including: [2] In the step (A-1), among the thermal decomposition products obtained by thermally decomposing the naphtha raw material in the presence of steam, for components containing monocyclic aromatic hydrocarbons, The production method according to [1], wherein toluene is produced and separated by performing separation and purification by distillation or extraction.
• [6] Xylene containing 14 C radioactive carbon atoms.
• a method for producing terephthalic acid using naphtha raw material including renewable naphtha comprising: A step (A-3) of obtaining paraxylene by the method described in [3] or [4]; A method for producing terephthalic acid, comprising a step (A-4) of obtaining terephthalic acid by oxidizing paraxylene.
• Terephthalic acid containing 14 C radioactive carbon atoms is derived from bionaphtha.
• a method for producing polyethylene terephthalate using a naphtha raw material including renewable naphtha comprising: Step (A-4) of obtaining terephthalic acid by the method described in [8]; A step (A-5) of obtaining polyethylene terephthalate by a condensation reaction of terephthalic acid and ethylene glycol; A method for producing polyethylene terephthalate, including: [12] Polyethylene terephthalate containing 14 C radioactive carbon atoms derived from bionaphtha.
• a method for managing monocyclic aromatic hydrocarbons used when producing at least one monocyclic aromatic hydrocarbon of benzene and xylene using a naphtha raw material including renewable naphtha comprising:
• the management method is a method of assigning value as a renewable product to the at least one type of monocyclic aromatic hydrocarbon according to the content ratio of the renewable naphtha contained in the naphtha raw material,
• the management method includes at least one or more steps selected from a step (V) of confirming that xylene and/or benzene is produced, and a step (W) of confirming that para-xylene is obtained,
• 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 raw material inputted into an apparatus for thermal decomposition in the presence of water vapor (steam cracker),
• the step (V-2) is
• 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 raw material inputted into an apparatus for thermal decomposition in the presence of water vapor (steam cracker)
• the step (V-2) is a step of confirming that xylene and/or benzene is produced from toluene introduced into a disproportionation device or a transalkylation (TA) device together with a C9-based component
• the step (W-3) is a step of confirming that para-xylene can be obtained from the xylene input into the para-xylene device, By performing the step (W-4) in the order of the device for thermal decomposition in the presence of water vapor (steam cracker), the disproportionation device or the transalkylation
• the management method includes the step (V) and the step (W)
• the management method includes a step (Z) of confirming the proportion of the product that is assigned a value as a renewable product
• 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) selects one or more products to be assigned as renewable products from among the products obtained by the disproportionation device or the transalkylation (TA) device and the paraxylene device.
• the ratio of the product selected in the step (Z-1) to the product obtained by the disproportionation device or the transalkylation (TA) device and the paraxylene device is A step of determining the value of the proportion (P) to be allocated as a renewable product
• the step (Z-3) is a step of grasping the value of the content ratio (Q) of the renewable naphtha contained in the naphtha raw material
• the step (Z-4) compares the value of the ratio (P) and the value of the content ratio (Q), and determines that the value of the ratio (P) is equal to or less than the value of the content ratio (Q). This is the process of confirming that How to manage monocyclic aromatic hydrocarbons.
• the management method includes the step (X) of confirming the proportion of the product to which value is assigned as a renewable product.
• 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 to be assigned as renewable products from among the products produced by the disproportionation device or the transalkylation (TA) device,
• the proportion of the product selected in the step (X-1) to the product produced from the disproportionation device or the transalkylation (TA) device is renewable.
• the step (X-3) is a step of determining the content ratio (Q) of the renewable naphtha contained in the naphtha raw material
• the step (X-4) compares the value of the ratio (P) and the value of the content ratio (Q), and the value of the ratio (P) is equal to or less than the value of the content ratio (Q).
• 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 value is assigned as a renewable product.
• 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 to be assigned as renewable products from among the products obtained by the paraxylene device
• the step (Y-2) determines the value of the percentage (P) to be allocated as a renewable product out of the percentage occupied by the product selected in the step (Y-1) to the product obtained by the paraxylene device.
• the step (Y-3) is a step of determining the content ratio (Q) of the renewable naphtha contained in the naphtha raw material
• the step (Y-4) compares the value of the ratio (P) and the value of the content ratio (Q), and the value of the ratio (P) is less than or equal to the value of the content ratio (Q).
• the step (X-1), the step (Y-1), or the step (Z-1) when selecting two or more types of products to be assigned as the renewable products, the step (X-2) ), the value of the ratio (P) to be allocated as a renewable product determined in the step (Y-2) and the step (Z-2) is the sum of the ratios allocated to each of the two or more selected products.
• the management method according to any one of [13] to [15], which is a value. [17]
• the management method includes the step (V) and the step (W), and in the step (Z-1), two types of products, benzene and paraxylene, are selected as the renewable products.
• the value of the proportion (P) assigned as the renewable product determined in the step (Z-2) is the benzene ratio to the product obtained by the disproportionation device or the transalkylation (TA) device and the paraxylene device.
• the proportion occupied by renewable benzene the proportion allocated to renewable benzene (P1), and the proportion occupied by paraxylene to the proportion obtained by the disproportionation device or the transalkylation (TA) device, and the paraxylene device, the renewable para
• the management method according to [13] wherein the value is the sum of the ratio (P2) allocated as xylene.
• a method for managing terephthalic acid used when producing terephthalic acid using naphtha raw material including renewable naphtha comprising:
• the management method is a method of assigning value to the terephthalic acid as a renewable product according to the content ratio of the renewable naphtha contained in the naphtha raw material,
• the control method includes 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 raw material inputted into an apparatus for thermal decomposition in the presence of water vapor (steam cracker),
• the step (G-2) is a step of confirming that xylene is produced from toluene input into a disproportionation device or a transalkylation (TA) device
• the management method includes a step (H) of identifying a proportion of the product that is assigned value as a renewable product;
• 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 assigned as a renewable product from among the products obtained by the terephthalic acid device,
• the step (H-2) determines the value of the percentage (P) to be allocated as a renewable product out of the percentage occupied by the product selected in the step (H-1) to the product obtained by the terephthalic acid device.
• the step (H-3) is a step of determining the content ratio (Q) of the renewable naphtha contained in the naphtha raw material
• the step (H-4) compares the value of the ratio (P) and the value of the content ratio (Q), and the value of the ratio (P) is less than or equal to the value of the content ratio (Q). This is the process of confirming that How to manage terephthalic acid.
• a method for managing polyethylene terephthalate used when producing polyethylene terephthalate using naphtha raw material including renewable naphtha comprising:
• the management method is a method of assigning value as a renewable product to the polyethylene terephthalate according to the content ratio of the renewable naphtha contained in the naphtha raw material,
• the management method includes 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 Including (F-6),
• the step (V-1) is a step of confirming that toluene is produced from the naphtha raw material inputted into an apparatus for thermal decomposition in the presence of water vapor (steam cracker),
• the step (G-2) is a step of confirming that xylene is produced from toluene input into a disproportion
• the step (J-3) is a step of determining the content ratio (Q) of the renewable naphtha contained in the naphtha raw material
• the step (J-4) compares the value of the ratio (P) and the value of the content ratio (Q), and the value of the ratio (P) is equal to or less than the value of the content ratio (Q). This is the process of confirming that How to manage polyethylene terephthalate.
• a management device comprising a computer-readable storage medium storing a management program, A management device, wherein the management device executes the management method according to any one of [13] to [19] by executing the management program.
• the present invention it is possible to provide a method for producing monocyclic aromatic hydrocarbons such as benzene and paraxylene, which are effective as basic raw materials, using naphtha raw materials including renewable naphtha. Further, according to the present invention, there is provided a method for managing monocyclic aromatic hydrocarbons that can be used when producing monocyclic aromatic hydrocarbons using naphtha raw materials including renewable naphtha. It is possible to provide a management method that assigns value as a renewable product such as renewable benzene, renewable para-xylene, etc. to monocyclic aromatic hydrocarbon products according to the content ratio of renewable naphtha contained therein.
• FIG. 2 is a schematic diagram for explaining the manufacturing method of the present invention.
• FIG. 2 is a schematic diagram for explaining a process when performing step (A-1) using a steam cracker (1).
• FIG. 2 is a schematic diagram for explaining a process when performing step (A-3) using a paraxylene production apparatus (4).
• FIG. 1 is a schematic diagram for explaining the method for producing terephthalic acid of the present invention. BRIEF DESCRIPTION OF THE DRAWINGS
• FIG. 1 is a schematic diagram for explaining the method for producing polyethylene terephthalate of the present invention.
• FIG. 2 is a schematic diagram comparing the compositions of petroleum-derived light naphtha (also referred to as conventional naphtha) and bio naphtha.
• FIG. 2 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) but does not include step (W).
• FIG. 2 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).
• FIG. 3 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).
• FIG. 2 is a schematic diagram for explaining step (X-1) 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).
• FIG. 2 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).
• FIG. 2 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).
• FIG. 2 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).
• FIG. 2 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 (W) but does not include step (V).
• FIG. 3 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).
• FIG. 3 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).
• FIG. 3 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).
• FIG. 2 is a schematic diagram for explaining step (Y-1) 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).
• FIG. 2 is a schematic diagram for explaining step (Y-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).
• FIG. 2 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).
• FIG. 3 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).
• FIG. 2 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).
• FIG. 3 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).
• FIG. 3 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).
• FIG. 3 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).
• FIG. 3 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).
• FIG. 2 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).
• FIG. 2 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).
• FIG. 3 is a schematic diagram for explaining step (Z-3) in the management method of the present invention when the management method of the present invention includes step (V) and step (W).
• FIG. 2 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).
• FIG. 2 is a schematic diagram for explaining the functional configuration of a management device.
• FIG. 2 is a block diagram illustrating an example of the hardware configuration of a management device.
• 3 is a flowchart illustrating an example of a processing procedure of a management program in a control unit of a management device. It is a flowchart which shows the 1st modification of the processing procedure of the management program in the control part of a management apparatus. It is a flowchart which shows the 2nd modification of the processing procedure of the management program in the control part of a management apparatus.
• renewable raw materials refer to raw materials from renewable organic resources. Renewable raw materials are not intended to be limited to products derived from biological resources, but are broadly understood as long as they fall under the category of renewable organic resources. For example, even if it is a product derived from petroleum, it is intended to include products derived from recycled products made from petroleum-derived products as raw materials, such as products derived from waste plastics. “Renewable naphtha” refers to naphtha derived from renewable raw materials. “Renewable products” (renewable toluene, renewable para-xylene, etc.) are those to which credits are assigned using the mass balance method.
• Biomass raw material refers to raw material of biological resources.
• Bio-naphtha refers to naphtha derived from biomass raw materials.
• Naphtha refers to a group of hydrocarbons with 5 to 10 carbon atoms obtained by refining petroleum.
• Xylene is intended to include at least one kind of isomers (mixtures) consisting of para-xylene, ortho-xylene, and meta-xylene.
• the production method of the present invention is a method for producing at least one kind of monocyclic aromatic hydrocarbon of benzene and xylene using a naphtha raw material containing renewable naphtha (hereinafter sometimes simply referred to as "renewable naphtha raw material").
• the renewable naphtha feedstock contains at least renewable naphtha, but may further contain non-renewable naphtha (conventional petroleum-derived naphtha).
• Examples of renewable naphtha include bio-naphtha made from biological raw materials and naphtha obtained by processing waste plastics.
• Bio-naphtha refers to naphtha made from biological raw materials, such as waste cooking oil, animal oils such as beef tallow, palm oil, tall oil (a by-product of pulp and paper), and vegetable oils.
• biological raw materials such as waste cooking oil, animal oils such as beef tallow, palm oil, tall oil (a by-product of pulp and paper), and vegetable oils.
• bio-naphtha derived from plants such as plants, wood, waste vegetable oil, and paper.
• Such bio-naphtha exhibits a composition similar to light fractions of naphtha derived from petroleum.
• At least one kind of monocyclic aromatic hydrocarbon, benzene and xylene, produced by the production method of the present invention is produced using a renewable naphtha raw material, and therefore is derived from renewable naphtha.
• the produced monocyclic aromatic hydrocarbons include: Contains biomass components derived from bio-naphtha.
• a biomass component is contained in a monocyclic aromatic hydrocarbon can be confirmed, for example, by measuring 14 C radioactive carbon atoms. That is, by using, for example, bio-naphtha as a raw material, xylene containing 14 C of radioactive carbon atoms can be obtained.
• there is no difference in physical properties such as molecular weight, mechanical properties, and thermal properties between biologically derived and petroleum-derived compounds and compositions.
• biomass degree is generally used.
• carbon in petroleum-derived compounds and compositions does not contain 14 C (radioactive carbon 14, half-life 5730 years), so the concentration of 14 C can be measured by accelerator mass spectrometry. This makes it possible to confirm whether the generated compound or composition is manufactured only from petroleum-derived naphtha or from bio-naphtha raw materials containing bio-naphtha.
• a sample to be measured is burned to generate carbon dioxide, and the carbon dioxide purified in a vacuum line is reduced with hydrogen using iron as a catalyst to generate graphite.
• this graphite was attached to a 14 C-AMS dedicated device (manufactured by NEC Corporation) based on a tandem accelerator, and the 14 C count, the 13 C concentration ( 13 C/ 12 C), and the 14 C concentration ( 14 It is obtained by measuring C/ 12 C) and calculating the ratio of the 14 C concentration of the sample carbon to the standard modern carbon from this measured value.
• oxalic acid HOxII
• NIST National Institute of Standards
• the manufacturing method of the present invention includes at least A step (A-1) of generating and separating toluene by thermally decomposing naphtha raw material in the presence of steam; a step (A-2) of producing and separating at least one monocyclic aromatic hydrocarbon of benzene and xylene by a disproportionation reaction or a transalkylation reaction from the toluene;
• a step (A-1) of generating and separating toluene by thermally decomposing naphtha raw material in the presence of steam a step (A-2) of producing and separating at least one monocyclic aromatic hydrocarbon of benzene and xylene by a disproportionation reaction or a transalkylation reaction from the toluene;
• the manufacturing method of the present invention includes: The method may further include a step (A-3) of performing adsorption separation or crystallization separation on the xylene obtained in the step (A-2) to separate para-xylene.
• the manufacturing method of the present invention includes: After separating para-xylene in the step (A-3), the residue containing at least one of ortho-xylene and meta-xylene is subjected to isomerization treatment to produce para-xylene, and then adsorption separation or crystallization is performed.
• the method may further include a step of performing analytical separation to separate para-xylene.
• FIG. 1 A preferred embodiment of the manufacturing method of the present invention will be described using FIG. 1.
• an apparatus (1) that performs thermal decomposition in the presence of water vapor is simply referred to as a "steam cracker (1).”
• the device (2) that performs the disproportionation reaction is also referred to as the “disproportionation device (2)”
• the device (3) that performs the transalkylation reaction is also referred to as the "TA device (3).”
• the apparatus (4) that performs crystallization separation to separate para-xylene is also referred to as "para-xylene production apparatus (4)".
• Disproportionation reaction is a reaction that produces benzene C6 and xylene C8 from toluene C7
• transalkylation reaction is a reaction that produces benzene C6 and xylene C8 from toluene C7.
• h) and/or a C10 component monocyclic aromatic hydrocarbon having 10 carbon atoms
• i) to produce benzene C6 and xylene C8 i
• the raw material for the transalkylation reaction may contain a C11 or higher component (a monocyclic aromatic hydrocarbon having 11 or more carbon atoms) in addition to the C7, C9, and C10 components.
• renewable naphtha e.g., more specifically, bio naphtha is used
• petroleum-derived naphtha e.g., more specifically, petroleum-derived light naphtha is used
• -2) is charged into a steam cracker (1) to separate toluene (b), which is a joint product with ethylene, etc.
• the benzene (c) is then charged into the device (2) or TA device (3) to separate it.
• benzene (c) derived from the renewable naphtha raw material (a) can be produced.
• toluene (b) is charged into the TA device (3) together with the disproportionation device (2) or the C9-based component (h) and the xylene (d) is separated, it can be derived from the renewable naphtha raw material (a). of xylene (d) can be produced.
• xylene (d) By charging the xylene (d) into the para-xylene production apparatus (4) and separating para-xylene (e), para-xylene (e) derived from the renewable naphtha raw material (a) can be produced.
• a 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).
• Step (A-1) is a step of generating and separating toluene (b) by introducing renewable naphtha raw material (a) into a steam cracker (1)
• Step (A-2) is to add toluene (b) to the disproportionation device (2) or the TA device (3) together with the C9 component (h) to convert benzene (c) and xylene (d). This is the process of generating and separating.
• the above production method further includes the following step (A-3) of producing paraxylene.
• Step (A-3) is a step of separating para-xylene (e) by charging xylene (d) into the para-xylene production apparatus (4).
• 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 bio-naphtha ( This is a bio-naphtha raw material (a) containing a-1) and petroleum-derived light naphtha (a-2).
• the content ratio of the renewable naphtha (a-1) to be contained in the renewable naphtha raw material (a) is not particularly limited and can be appropriately selected depending on the purpose.
• light oil can be used in addition to the renewable naphtha raw material (a).
• the light oil it is preferable to use light oil derived from biomass raw materials such as biodiesel.
• the biomass raw materials include vegetable oils such as rapeseed oil, palm oil, olive oil, sunflower oil, soybean oil, and rice oil, animal fats and oils such as beef tallow, lard, and fish oil, and waste cooking oil.
• the mixing ratio of the renewable naphtha raw material (a) and the light oil derived from the biomass raw material is not particularly limited and can be appropriately selected depending on the purpose.
• the steam cracker (1) is a device that can generate and separate toluene, which is a co-product of ethylene, by thermally decomposing the renewable naphtha raw material (a) in the presence of steam.
• a more detailed process of performing step (A-1) using the steam cracker (1) will be explained using FIG. 2.
• the components containing aromatic compounds are separated and purified by distillation or extraction, thereby containing renewable components.
• Toluene (b) is obtained.
• the decomposition temperature of the steam cracker is preferably 750°C to 900°C, more preferably 770°C to 850°C.
• the residence time (reaction time) of the raw material is preferably 0.1 to 0.5 seconds, more preferably 0.1 to 0.3 seconds.
• the steam/raw material (mass ratio) is preferably 0.2 to 0.9, more preferably 0.3 to 0.7.
• toluene (b) is converted into benzene and xylene by a reaction in which methyl groups are transferred between toluenes, producing benzene (c) and xylene (d), which are separated (step (A-2)).
• Toluene (b) may be the toluene obtained in the steam cracker (1), or may be other toluene (for example, toluene derived from petroleum), or may be the toluene obtained in the steam cracker (1). Mixtures of other toluenes may also be used.
• the toluene (b) may be the toluene obtained in the steam cracker (1), or may be other toluene (for example, toluene derived from petroleum), or may be the toluene obtained in the steam cracker (1). Mixtures of other toluenes may also be used.
• the raw material for the transalkylation reaction may contain a C11 or higher component in addition to toluene (b), a C9 component (h), and a C10 component (i).
• the C9 components include trimethylbenzene and methylethylbenzene
• examples of the C10 components include tetramethylbenzene and ethylxylene
• examples of the C11 and higher components include trimethylethylbenzene and diethyltoluene.
• ⁇ Paraxylene production equipment (4) In the para-xylene production equipment (4), the xylene (d) obtained in the disproportionation equipment (2) or the TA equipment (3) (more specifically, mixed xylene containing meta-xylene, ortho-xylene, para-xylene, etc.) is Para-xylene is separated by adsorption separation or crystallization separation (step (A-3)).
• step (A-3) the residue containing at least one of ortho-xylene and meta-xylene after separating para-xylene is further subjected to isomerization treatment to produce para-xylene, and then adsorbed again.
• the method may include a step of separating para-xylene by performing separation or crystallization separation.
• xylene production by adsorption separation method A preferred embodiment of the paraxylene production apparatus (4) will be described using FIG. 3.
• xylene (d) (more specifically, mixed xylene in which meta-xylene, ortho-xylene, para-xylene, etc. are mixed) is separated using a para-xylene production apparatus (which adsorbs and separates para-xylene using an adsorbent). 4) into the adsorption tower (4-1).
• Para-xylene (e) is separated in the adsorption tower (4-1).
• the residue (f) containing ortho-xylene and meta-xylene remaining after separating para-xylene is charged into the isomerization device (4-2) in the para-xylene production device (4), and isomerized.
• Mixed xylene (g) after isomerization treatment containing para-xylene obtained by isomerization treatment (more specifically, mixed xylene after isomerization treatment in which meta-xylene, ortho-xylene, para-xylene, etc. are mixed) ) is again subjected to the adsorption tower (4-1).
• Para-xylene (e) is separated in the adsorption tower (4-1).
• This step of separating para-xylene (e) via the isomerization device ⁇ adsorption tower can be repeated. The repeated operation is terminated at the stage when the desired amount of paraxylene (e) can be separated.
• xylene (d) (more specifically, a mixed xylene containing meta-xylene, ortho-xylene, para-xylene, etc.) is separated from para-xylene and meta-xylene/ortho-xylene by utilizing the difference in melting point. Separate. The mixed xylene fed into the paraxylene production equipment is cooled, and paraxylene, which has a higher melting point than other xylene isomers, is crystallized, and paraxylene is separated through the steps of centrifugation, crystal washing, and recrystallization. .
• the production method of the present invention is a method for producing terephthalic acid using light oil derived from renewable naphtha raw materials and/or biomass raw materials, and includes the step (A-3) of obtaining para-xylene, and the step of oxidizing para-xylene. , and step (A-4) of obtaining terephthalic acid.
• the step (A-3) of obtaining the renewable naphtha raw material and paraxylene is as described above.
• the renewable naphtha raw material it is preferable to use bionaphtha, and as the light oil derived from the biomass raw material, it is preferable to use biodiesel.
• renewable naphtha raw material (a) containing bio-naphtha is charged into a steam cracker (1), undergoes the above-mentioned reactions, and then paraxylene is obtained from a paraxylene device (4). Subsequently, the obtained paraxylene is charged into a terephthalic acid production apparatus (5) to obtain terephthalic acid (step (A-4)).
• terephthalic acid containing 14 C of radioactive carbon atoms can be obtained by using light oil derived from bionaphtha and/or biomass raw material as a renewable naphtha raw material.
• terephthalic acid production equipment (5) In the terephthalic acid production device (5), paraxylene obtained in the paraxylene production device (4) is oxidized to produce terephthalic acid (step (A-4)).
• step (A-4) paraxylene is oxidized to produce terephthalic acid by a conventionally known method.
• terephthalic acid is produced by liquid phase oxidation of paraxylene with molecular oxygen in an acetic acid solvent in the presence of a catalyst.
• a catalyst conventionally known for use in the oxidation reaction is used, and specific examples thereof include heavy metal compounds such as cobalt compounds, manganese compounds, iron compounds, and chromium compounds, and bromine compounds. It is preferable that the catalyst be present in the reaction system in a molten or dissolved state because the reaction rate increases if the catalyst is in a molten or dissolved state during the oxidation reaction. Conditions for the oxidation reaction can be set as appropriate.
• the production method of the present invention is a method for producing polyethylene terephthalate using light oil derived from renewable naphtha raw materials and/or biomass raw materials, and includes the step (A-4) of obtaining terephthalic acid, and the condensation of terephthalic acid and ethylene glycol. and a step (A-5) of obtaining polyethylene terephthalate by reaction.
• the step (A-4) of obtaining the renewable naphtha raw material and terephthalic acid is as described above.
• the renewable naphtha raw material it is preferable to use bionaphtha, and as the light oil derived from the biomass raw material, it is preferable to use biodiesel.
• renewable naphtha raw material (a) containing bio-naphtha is charged into a steam cracker (1), and after undergoing the above-mentioned reactions, terephthalic acid is obtained from the terephthalic acid production device (5) (step (A) -4)). Subsequently, the obtained terephthalic acid is put into a polyethylene terephthalate (PET) manufacturing apparatus (6) to obtain polyethylene terephthalate (PET) (step (A-5)).
• PET polyethylene terephthalate
• polyethylene terephthalate containing 14 C of radioactive carbon atoms can be obtained by using light oil derived from bionaphtha and/or biomass raw material as a renewable naphtha raw material.
• the obtained polyethylene terephthalate can be used for conventionally known purposes, such as preforms, PET bottles, shrink films, stretch films, and the like.
• polyethylene terephthalate (PET) manufacturing equipment (6) 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)).
• polyethylene terephthalate is produced by a condensation reaction of terephthalic acid and ethylene glycol using a conventionally known method.
• a condensation reaction dehydration condensation
• the polymerization catalyst for example, metal compounds containing titanium, zirconium, germanium, zinc, aluminum, magnesium, and calcium, and mixtures thereof are preferable, and titanium compounds, zirconium compounds, and germanium compounds are particularly preferable.
• the polymerization catalyst is preferably a compound that is liquid during the condensation reaction or dissolves in the ester low polymer or polyester because the reaction rate increases if it is in a melted or dissolved state during the condensation reaction.
• Conditions for the condensation reaction can be set as appropriate.
• Ethylene glycol which is one of the raw materials for producing polyethylene terephthalate (PET) in step (A-5), may be derived from petroleum, biomass raw material, or biomass using a mass balance method. Ethylene glycol may also be used. By using ethylene glycol derived from biomass raw material in step (A-5), the biomass degree of the obtained polyethylene terephthalate can be improved.
• ⁇ Characteristics of the manufacturing method of the present invention According to the production method of the present invention, by partially or completely replacing petroleum-derived raw materials with renewable raw materials such as biomass raw materials and recycled raw materials, the environmental burden is reduced by conserving petroleum resources and reducing carbon dioxide emissions. While making it possible to obtain monocyclic aromatic hydrocarbon products that are produced, the composition is comparable to that of conventional monocyclic aromatic hydrocarbon products produced using petroleum-derived raw materials. Can be done. To explain in more detail, the typical compositions of petroleum-derived light naphtha (also referred to as conventional naphtha) and bio naphtha are similar as shown in FIG.
• bio-naphtha having a composition similar to that of conventional naphtha is used, and raw material naphtha in which the conventional naphtha is partially or completely replaced with bio-naphtha is used, so the yield of products from bio-naphtha is , there is no difference in yield compared to the product yield from conventional naphtha, and it becomes possible to produce monocyclic aromatic hydrocarbons with a similar composition.
• the quality of the produced monocyclic aromatic hydrocarbons can be the same as that of monocyclic aromatic hydrocarbons produced from conventional naphtha.
• the present invention provides a method for producing a monocyclic aromatic hydrocarbon containing a renewable component of the present invention when producing a monocyclic aromatic hydrocarbon using the method for producing a monocyclic aromatic hydrocarbon containing a renewable component of the present invention.
• a management method that allows a value as a renewable product to be assigned to a monocyclic aromatic hydrocarbon product in a simple and reliable manner according to the ratio.
• the mass balance method refers to, for example, when raw materials with specific characteristics such as biomass raw materials are mixed with raw materials that do not have those characteristics during the distribution and processing process from raw materials to products.
• the mass balance method is used to virtually allocate biomass fractions as credits to some products such as benzene and paraxylene. Note that a detailed explanation of how to allocate will be given later. Since the mass balance method (material balance method) is a method in which manufacturers arbitrarily allocate biomass fractions as credits, its legitimacy is generally verified through certification by a third-party certification body. . Third-party certification bodies include ISCC (International Sustainable Carbon) and RSB (Roundtable for Sustainable Biofuels).
• 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 raw material containing renewable naphtha.
• the management method of the present invention is a method of assigning value as a renewable product to a product of at least one type of monocyclic aromatic hydrocarbon according to the content ratio of renewable naphtha contained in a renewable naphtha raw material. .
• the management method of the present invention includes at least one or more steps selected from a step (V) of confirming that xylene and/or benzene is produced, and a step (W) of confirming that para-xylene is obtained. .
• the management method including step (V) and step (W) will be explained in detail for each case.
• Step (V) of confirming that xylene and/or benzene is produced includes the following step (V-1), the following step (V-2), and the following step (V-3). Furthermore, when the management method of the present invention includes step (V) but does not include step (W), it also includes step (X) of confirming the proportion of the product to which value as a renewable product is assigned. Step (X) includes the following step (X-1), the following step (X-2), the following step (X-3), and the following step (X-4).
• Step (V-1) is a step of confirming that toluene (b) is produced from the renewable naphtha raw material (a) charged into the steam cracker (1), as shown in FIG. 7A. In other words, for the steam cracker, it is confirmed whether the desired output (toluene) is produced for the input (renewable naphtha raw material).
• step (V-2) as shown in FIG. 7B, toluene (b) is added to the TA device (3) together with the disproportionation device (2) or the C9 component (h) and/or the C10 component.
• xylene (d) and/or benzene (c) are produced.
• the desired output xylene and / or benzene.
• the toluene (b) fed into the disproportionation device (2) or the TA device (3) is the toluene (b) obtained in the step (V-1). It may also be other toluene (for example, petroleum-derived toluene), or it may be a mixture of toluene (b) obtained in step (V-1) and other toluenes, preferably other toluenes. It is.
• step (V-3) as shown in FIG.
• xylene is extracted from the renewable naphtha raw material (a) by processing it in the order of a steam cracker (1), a disproportionation device (2), or a TA device (3). This is a step of confirming that (d) and/or benzene (c) is produced.
• the steam cracker (1), the disproportionation device (2), or the TA device (3) are used for reaction in this order, the desired output (xylene and/or benzene ) is done.
• toluene (b) fed into the disproportionation device (2) or TA device (3) in step (V-3) is not shown, it is similar to toluene (b) in step (V-2). The same is true.
• Step (X-1) is a step of selecting one or more products to be assigned as renewable products from among the products produced by the disproportionation device (2) or the TA device (3).
• Step (X-2) allocates the proportion of the product selected in step (X-1) to the product produced from the disproportionation device (2) or TA device (3) as a renewable product.
• This is a step of determining the value of the ratio (P).
• Step (X-3) is a step of determining the value of the content ratio (Q) of renewable naphtha contained in the renewable naphtha raw material.
• Step (X-4) is a step of comparing the value of the ratio (P) and 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). It is.
• Steps (X-1) to (X-4) (these steps are also collectively referred to as step (X)) will be specifically explained using FIG. 8.
• step (X-1) in the reaction step to obtain the desired product, the end-use device (here, the disproportionation device (2) or the TA device (3)) produces the Select one or more desired products to be assigned as renewable products from among the products (e.g., benzene (c), xylene (d), other products (v) and (w)), etc. .
• the end-use device here, the disproportionation device (2) or the TA device (3)
• the end-use device produces the Select one or more desired products to be assigned as renewable products from among the products (e.g., benzene (c), xylene (d), other products (v) and (w)), etc.
• the end-use device here, the disproportionation device (2) or the TA device (3)
• the end-use device produces the Select one or more desired products to be assigned as renewable products from among the products (
• the desired product selected in step (X-1) from among the products produced from the disproportionation device (2) or the TA device (3) determine the value of the proportion (P) to be allocated as a renewable product.
• the products produced from the disproportionation device (2) are benzene (c), xylene (d), and other products ((v) and (w)).
• the proportions occupied by 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. %.
• the product produced from the TA device (3) will be described assuming that it is produced at the same product ratio as the disproportionation device (2).
• the products generated from the TA device (3) are benzene (c), xylene (d), and other products ((v) and (w)), respectively.
• 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.
• step (X-1) when benzene is selected in step (X-1), the proportion (P1) to be allocated as renewable benzene out of 20% by mass of the benzene product is determined.
• step (X-1) when xylene is selected in step (X-1), the proportion (P2) to be allocated as renewable xylene out of 65% by mass of the xylene product is determined.
• step (X-1) when two types of benzene and xylene are selected in step (X-1), the proportion (P1) to be allocated as renewable benzene out of 20% by mass of the benzene product and the proportion (P1) to be allocated as renewable xylene out of 65% by mass of the xylene product.
• the ratio (P2) is determined.
• step (X-3) as shown in FIG.
• the value of the content ratio (Q) of the renewable naphtha (a-1) contained in the renewable naphtha raw material (a) is determined. For example, as shown in FIG. 8C, when the renewable naphtha raw material (a) contains 10% by mass of renewable naphtha (a-1) and 90% by mass of petroleum-derived naphtha (a-2), the renewable naphtha (a) -1) is understood to be 10% by mass.
• step (X-4) the value of the ratio (P) and the value of the content ratio (Q) are compared, and it is confirmed that the value of the ratio (P) is less than or equal to the value of the content ratio (Q). , as shown in FIG.
• the ratio (P) assigned as a renewable product to the product is 10% by mass or less. shall be. If there are two or more types of products to be allocated as renewable products, this allocation ratio (P) is the sum of the allocation ratios for each of the selected products.
• step (X-1) If only benzene is selected in step (X-1), the proportion (P1) allocated as renewable benzene is the proportion (P), and if only xylene is selected in step (X-1), the proportion allocated as renewable xylene ( P2) is the ratio (P), and when two types of benzene and xylene are selected in step (X-1), the sum of the ratio allocated as renewable benzene (P1) and the ratio allocated as renewable xylene (P2) is It is the ratio (P).
• step (X-1) if the content (Q) of renewable naphtha (a-1) is 10% by mass, if benzene is selected as the product to be assigned as a renewable product in step (X-1), the benzene product Of the 20% by weight, 10% by weight can be allocated as renewable benzene.
• step (X-4) it is confirmed whether the proportion allocated as renewable benzene (P1) does not exceed the content proportion (Q) of renewable naphtha (a-1) (10% by mass in the example of FIG. 8D). There is.
• step (X-1) 10% by mass of the 65% by mass of the xylene product can be allocated as renewable xylene.
• step (X-4) it is confirmed whether the proportion allocated as renewable xylene (P2) does not exceed the content proportion (Q) of renewable naphtha (a-1) (10% by mass in the example of FIG. 8D). There is.
• step (X-1) when two types of products, benzene and xylene, are selected as renewable products in step (X-1), (P1) mass% of the benzene product 20 mass% and xylene product 65 mass% % (P2) by mass can be assigned as renewable benzene and renewable xylene, respectively.
• P1 is 5% by mass and P2 is 5% by mass
• the total will be 10% by mass or less, so they can be allocated at such a ratio.
• P1 is 1% by mass and P2 is 9% by mass
• the total will be 10% by mass or less, and thus it is possible to allocate at such a ratio.
• step (X-4) the sum of the proportion allocated as renewable benzene (P1) and the proportion allocated as renewable xylene (P2) is the content proportion (Q) of renewable naphtha (a-1) (in the example of FIG. 8D, 10 (mass%).
• the desired product selected in step (X-1) among the products produced from the disproportionation device (2) or the TA device (3) is contained in the renewable naphtha feedstock.
• the value of the product as a renewable product can be assigned.
• Each product produced by the production method of the present invention contains a renewable component in accordance with the content ratio of renewable naphtha contained in the renewable naphtha raw material, and the renewable component is distributed in all the products. .
• the content of renewable components depends on the yield produced by each device.
• a specific product can be treated as a renewable product with 100% renewable components allocated within the range of the content ratio of renewable naphtha contained in the renewable naphtha raw material.
• the benzene products excluding (P1) mass % of the 20 mass % benzene products (20 - (P1) mass % benzene products) actually have Contains renewable ingredients. However, since 100% renewable benzene credits were assigned to (P1) mass% benzene, it is not treated as renewable benzene.
• the xylene product excluding (P2) mass% of the 65 mass% xylene product actually contains renewable components, but ( P2) Since 100% renewable xylene credits were assigned to xylene in mass%, it is not treated as renewable xylene.
• third-party certification bodies such as ISCC (International Sustainable Carbon) and RSB (Roundtable for Sustainable Biofuels) audit the manufacturer's management system and ensure that it meets the specified standards. We issue certifications and ensure their accuracy.
• the mass balance method is also used for monocyclic aromatic hydrocarbons produced using the method for producing monocyclic aromatic hydrocarbons containing renewable components of the present invention. It is possible to easily and reliably allocate a value as a renewable product, and the accuracy of the above value allocation result can be guaranteed by a third-party certification body.
• the value of 10% by mass of the content (Q) of the renewable naphtha (a-1) described in FIG. This value is set for convenience to facilitate the process, and is not limited to this value.
• the content ratio (Q) of the renewable naphtha (a-1) may be, for example, 1% by mass or 30% by mass, and the desired content ratio (Q) may be set depending on the purpose.
• the reaction conditions etc. may be adjusted as appropriate so that the products are produced at the desired production ratio.
• the management method of the present invention includes: ⁇ In cases where the process includes the step (W) of confirming that paraxylene is obtained but does not include the step (V), ⁇ Even in the case of including both the above step (V) and the above step (W), The same management method as that described in the case where step (V) is included but step (W) is not included can be applied.
• a management method in which the process (W) is included but not the process (V) and a management method in the case where the process (V) and the process (W) are included will also be described.
• Step (W) of confirming that paraxylene is obtained includes the following step (V-1), the following step (V-2), the following step (W-3), and the following step (W-4).
• step (V-1) and step (V-2) are as described in the above section ⁇ Management method including step (V) but not including step (W)>.
• the management method of the present invention includes step (W) but does not include step (V)
• Step (Y) includes the following step (Y-1), the following step (Y-2), the following step (Y-3), and the following step (Y-4).
• step (V-1) toluene (b) is produced from the renewable naphtha raw material (a) that is fed into a device (steam cracker) (1) for thermal decomposition in the presence of steam. This is the process of confirming that. In other words, for a device (steam cracker) that performs thermal decomposition in the presence of steam, it is confirmed whether the desired output (toluene) is produced for the input (renewable naphtha raw material).
• step (V-2) as shown in FIG.
• step (V-2) the toluene (b) fed into the disproportionation device (2) or the TA device (3) is the toluene (b) obtained in the step (V-1). It may also be other toluene (for example, petroleum-derived toluene), or it may be a mixture of toluene (b) obtained in step (V-1) and other toluenes, preferably other toluenes. It is.
• Step (W-3) is a step of confirming that para-xylene (e) can be obtained from xylene (d) charged into the para-xylene production apparatus (4), as shown in FIG. 9C. In other words, it is confirmed whether the para-xylene production apparatus (4) produces the desired output (para-xylene) in response to the input (xylene).
• step (W-4) includes a device for thermal decomposition in the presence of water vapor (steam cracker) (1), the disproportionation device (2) or the TA device (3), and the This is a step of confirming that paraxylene (e) can be obtained from the renewable naphtha raw material (a) by processing in the order of the xylene production apparatus (4).
• a device for thermal decomposition in the presence of water vapor (steam cracker) (1), a disproportionation device (2) or TA device (3), and a paraxylene production device (4) were subjected to the reaction in this order.
• toluene (b) fed into the disproportionation device (2) or TA device (3) in step (W-4) is not shown, it is similar to toluene (b) in step (V-2). The same is true.
• Step (Y-1) is a step of selecting one or more products to be assigned as renewable products from among the products obtained by the paraxylene equipment.
• Step (Y-2) is a step of determining the value of the proportion (P) to be allocated as a renewable product out of the proportion occupied by the product selected in step (Y-1) to the product obtained by the paraxylene equipment.
• Step (Y-3) is a step of determining the content ratio (Q) of renewable naphtha contained in the renewable naphtha raw material.
• Step (Y-4) is a step of comparing the value of the ratio (P) and 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). It is.
• Steps (Y-1) to (Y-4) will be specifically explained using FIG. 10.
• step (Y-1) in the reaction step to obtain a desired product, a product (for example, para- Select one or more desired products to be assigned as renewable products from xylene (e), ortho-xylene (x), meta-xylene (y), and other products (z). For example, select para-xylene. do.
• step (Y-2) as shown in FIG. 10B, a renewable product is added to the desired product selected in the step (Y-1) among the products obtained by the paraxylene production apparatus (4). Determine the value of the proportion (P) to be allocated as . For example, as shown in FIG.
• the products obtained by the para-xylene production apparatus (4) are para-xylene (e), ortho-xylene (x), meta-xylene (y), and other products (z).
• the proportions of each product are paraxylene (e): 80% by mass, orthoxylene (x): 5% by mass, metaxylene (y): 10% by mass, and other products (z): 5% by mass. Assume that it is mass%.
• the proportion (P1) to be allocated as renewable benzene out of 80% by mass of the paraxylene product is determined.
• step (Y-3) as shown in FIG.
• the value of the content ratio (Q) of the renewable naphtha (a-1) contained in the renewable naphtha raw material (a) is determined. For example, as shown in FIG. 10C, if the renewable naphtha raw material (a) contains 10% by mass of renewable naphtha (a-1) and 90% by mass of petroleum-derived naphtha (a-2), then -1) is understood to be 10% by mass.
• step (Y-4) the value of the ratio (P) and the value of the content ratio (Q) are compared, and it is confirmed that the value of the ratio (P) is less than or equal to the value of the content ratio (Q). , as shown in FIG.
• the ratio (P) assigned as a renewable product to the product is 10% by mass or less. shall be. If there are two or more types of products to be allocated as renewable products, this allocation ratio (P) is the sum of the allocation ratios for each of the selected products.
• the ratio (P1) allocated as renewable paraxylene is the ratio (P).
• step (Y-1) if the content (Q) of renewable naphtha (a-1) is 10% by mass, if paraxylene is selected as the product to be assigned as a renewable product in step (Y-1), paraxylene Of the 80% by weight of the product, 10% by weight can be allocated as renewable para-xylene.
• step (Y-4) it is confirmed whether the proportion allocated as renewable para-xylene (P1) does not exceed the content proportion (Q) of renewable naphtha (a-1) (10% by mass in the example of FIG. 10D). ing.
• the content ratio of renewable naphtha contained in the renewable naphtha raw material is adjusted to the desired product selected in step (Y-1) among the products obtained by the paraxylene production equipment (4). Accordingly, it can be assigned a value as a renewable product. That is, using FIG. 10D as an example, it can be determined that (P1) mass % of the para-xylene product out of 80 mass % of the para-xylene product is renewable para-xylene with a renewable component of 100%.
• the mass balance method is based on the para-xylene product (80-( P1) Mass% para-xylene product) actually contains renewable components, but since we assigned the credit of 100% renewable para-xylene to (P1) Mass% para-xylene, what is renewable para-xylene? It will be treated as not.
• steps (V-1) to (V-3) and steps (W-3) to (W-4) are the above-mentioned ⁇ control method including step (V) but not including step (W)>. and the above ⁇ Management method including step (W) but not including step (V)> section.
• Step (V) when the management method of the present invention includes step (V) and step (W), it also includes a step (Z) of confirming the proportion of the product to which value as a renewable product is assigned.
• Step (Z) includes the following step (Z-1), the following step (Z-2), the following step (Z-3), and the following step (Z-4).
• FIG. 11 11A to 11E (collectively referred to as FIG. 11) and FIGS. 12A to 12E (collectively referred to as FIG. 11) and FIGS. 11A to 11E (collectively referred to as FIG. (also referred to as FIG. 12).
• step (V-1) toluene (b) is produced from the renewable naphtha raw material (a) that is fed into a device (steam cracker) (1) for thermal decomposition in the presence of steam.
• a device steam cracker
• step (V-2) xylene (d) and/or Alternatively, this is a step to confirm that benzene (c) is produced.
• the desired output (xylene and/or benzene) is produced for the input (toluene (in some cases, also checking the input of C9 components)).
• the toluene (b) fed into the disproportionation device (2) or the TA device (3) is the toluene (b) obtained in the step (V-1).
• It may also be other toluene (for example, petroleum-derived toluene), or it may be a mixture of toluene (b) obtained in step (V-1) and other toluenes, preferably other toluenes. It is.
• Step (W-3) is a step of confirming that para-xylene (e) can be obtained from xylene (d) charged into the para-xylene production apparatus (4), as shown in FIG. 11C. In other words, it is confirmed whether the para-xylene production apparatus (4) produces the desired output (para-xylene) in response to the input (xylene).
• step (V-3) as shown in FIG. 11D, the process is performed in the following order: a device for thermal decomposition in the presence of water vapor (steam cracker) (1), a disproportionation device (2), or a TA device (3).
• the device for thermal decomposition in the presence of steam (steam cracker) (1), the disproportionation device (2), or the TA device (3) are subjected to the reaction in this order, the input (renewable naphtha raw material)
• the desired output (xylene and/or benzene) is achieved.
• toluene (b) fed into the disproportionation device (2) or TA device (3) in step (V-3) is not shown, it is similar to toluene (b) in step (V-2). The same is true.
• step (W-4) includes a device for thermal decomposition in the presence of water vapor (steam cracker) (1), a disproportionation device (2) or a TA device (3), and a paraxylene production device.
• This is a step of confirming that paraxylene (e) is produced from the renewable naphtha raw material (a) by processing in the order of (4).
• a device for thermal decomposition in the presence of water vapor (steam cracker) (1), a disproportionation device (2) or TA device (3), and a paraxylene production device (4) were subjected to the reaction in this order. In this case, confirm whether the desired output (paraxylene) is produced for the input (renewable naphtha raw material).
• toluene (b) fed into the disproportionation device (2) or TA device (3) in step (W-4) is not shown, it is similar to toluene (b) in step (V-2). The same is true.
• Step (Z-1) is a step of selecting one or more products to be assigned as renewable products from among the products obtained by the disproportionation device or TA device and the paraxylene device.
• Step (Z-2) is a step (Z-2) in which a proportion ( This is a step of determining the value of P).
• Step (Z-3) is a step of determining the content ratio (Q) of renewable naphtha contained in the renewable naphtha raw material.
• Step (Z-4) is a step of comparing the value of the ratio (P) and 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). It is.
• Steps (Z-1) to (Z-4) (these steps are also collectively referred to as step (Z)) will be specifically explained using FIG. 12.
• the end-use equipment here, the disproportionation equipment (2) or the TA equipment (3), and the paraxylene Production equipment (4)
• the paraxylene Production equipment (4) e.g., benzene (c), xylene (d), other products (v) and (w), para-xylene (e), ortho-xylene (x), meth xylene (y), other products (z), etc.
• select one or more desired products to be assigned as renewable products For example, even if benzene and para-xylene are selected, xylene and para- Xylene may be selected, or benzene, xylene, and para-xylene may be selected.
• the steps (Z-2), as shown in FIG. Determine the value of the proportion (P) to be assigned as a renewable product for the desired product selected in ).
• the products obtained by the disproportionation device (2) or the TA device (3) and the paraxylene production device (4) contain 20% by mass of benzene (c) and other products.
• the product produced from the TA device (3) will be described assuming that it is produced at the same product ratio as the disproportionation device (2). That is, as shown in FIG. 12B, the products generated from the TA device (3) are benzene (c): 20% by mass, other products (v): 10% by mass, and other products (w). : 5% by mass, para-xylene (e): 52% by mass, ortho-xylene (x): 3% by mass, meta-xylene (y): 7% by mass, and other products (z): 3% by mass. .
• step (Z-1) when benzene and paraxylene are selected in step (Z-1), the ratio (P1) to be allocated as renewable benzene out of 20% by mass of the benzene product and the proportion (P1) allocated to renewable paraxylene among 52% by mass of the paraxylene product.
• the proportion to be allocated (P2) is determined.
• step (Z-3) as shown in FIG. 12C, the value of the content ratio (Q) of the renewable naphtha (a-1) contained in the renewable naphtha raw material (a) is determined. For example, as shown in FIG.
• step (Z-4) when the renewable naphtha raw material (a) contains 10% by mass of renewable naphtha (a-1) and 90% by mass of petroleum-derived naphtha (a-2), the renewable naphtha (a) -1) is understood to be 10% by mass.
• step (Z-4) the value of the ratio (P) and the value of the content ratio (Q) are compared, and it is confirmed that the value of the ratio (P) is less than or equal to the value of the content ratio (Q).
• the proportion (P) assigned as a renewable product to the product is 10% by mass or less. shall be.
• this allocation ratio (P) is the sum of the allocation ratios for each of the selected products.
• the ratio (P) is the sum of the ratio (P1) allocated as renewable benzene and the ratio (P2) allocated as renewable paraxylene.
• the content (Q) of renewable naphtha (a-1) is 10% by mass, when two types of products, benzene and paraxylene, are selected as renewable products in step (Z-1).
• (P1) mass % of the 20 mass % benzene product and (P2) mass % of the 52 mass % paraxylene product can be allocated as renewable benzene and renewable para-xylene, respectively.
• P1 is 5% by mass and P2 is 5% by mass
• the total will be 10% by mass or less, so they can be allocated at such a ratio.
• P1 is 1% by mass and P2 is 9% by mass
• the total will be 10% by mass or less, and thus it can be allocated at such a ratio.
• step (Z-4) the sum of the proportion allocated as renewable benzene (P1) and the proportion allocated as renewable paraxylene (P2) is the content proportion (Q) of renewable naphtha (a-1) (in the example of FIG. 12D, 10% by mass).
• the desired product selected in step (Z-1) among the products obtained by the disproportionation device (2) or the TA device (3) and the paraxylene production device (4) is Therefore, the value as a renewable product can be assigned according to the content ratio of renewable naphtha contained in the renewable naphtha raw material.
• the paraxylene product is 52 mass %.
• the (P2) mass % of the paraxylene product it can be determined that the product is renewable paraxylene with 100% renewable components.
• FIG. 12D for (P1) mass % of the benzene product out of 20 mass % of the benzene product, if the renewable benzene is 100% renewable component, then the paraxylene product is 52 mass %.
• the (P2) mass % of the paraxylene product it can be determined that the product is renewable paraxylene with 100% renewable components.
• FIG. 12D for (P1) mass % of the benzene product out of 20 mass % of the benzene product, if the renewable
• the mass balance method is based on the benzene product (20-(P1) % by mass of benzene product) actually contains a renewable component, but since a credit of 100% renewable benzene was assigned to (P1) % by mass of benzene, it is not treated as renewable benzene.
• the para-xylene product excluding (P2) mass % of the 52 mass % para-xylene product actually contains a renewable component.
• (P2) Mass % of para-xylene was assigned a credit of 100% renewable para-xylene, so it is not treated as renewable para-xylene. Note that the value of 10% by mass of the content (Q) of the renewable naphtha (a-1) and the values of 20% by mass of the benzene product and 52% by mass of the paraxylene product described in FIG. As described above, this value is set for convenience to facilitate understanding, and is not limited to this value.
• step (Z-1) the case where benzene and paraxylene are selected in the step (Z-1) is explained as an example, but for example, xylene can also be selected in the step (Z-1).
• step (Z-1) if xylene and para-xylene are selected in step (Z-1), the (P1) mass % of xylene to be allocated as renewable xylene and the (P2) mass % of para-xylene to be allocated as renewable para-xylene. It is necessary that the total amount does not exceed 10% by mass.
• FIG. 12A the case where benzene and paraxylene are selected in the step (Z-1) is explained as an example, but for example, xylene can also be selected in the step (Z-1).
• step (Z-1) when benzene, xylene, and para-xylene are selected in step (Z-1), the (P1) mass% of benzene to be allocated as renewable benzene and the xylene to be allocated as renewable xylene are It is necessary to ensure that the sum of (P2) mass % of (P2) and (P3) mass % of para-xylene to be allocated as renewable para-xylene does not exceed 10 mass %.
• Management method of terephthalic acid It is desired that a value be assigned to terephthalic acid produced using the method for producing terephthalic acid of the present invention as a renewable product using a mass balance method in a simple and reliable manner. Therefore, the present invention provides that when producing terephthalic acid using the method for producing terephthalic acid of the present invention, etc., a renewable product is added to terephthalic acid according to the content ratio of renewable naphtha contained in the renewable naphtha raw material. To provide a management method that allows assigning value in a simple and reliable manner. Note that the explanation of the mass balance method is as described above.
• the terephthalic acid management method of the present invention can be used when producing terephthalic acid using naphtha raw materials including renewable naphtha.
• the management method of the present invention is a method of assigning value as a renewable product to the terephthalic acid according to the content ratio of renewable naphtha contained in the renewable naphtha raw material.
• the control method of the present invention includes a step (E) of confirming that terephthalic acid is obtained, and step (E) includes the following step (V-1), the following step (G-2), and the following step (W- 3), the following step (E-4), and the following step (E-5).
• Step (V-1) is a step of confirming that toluene is produced from the naphtha raw material introduced into an apparatus for thermal decomposition in the presence of steam (steam cracker).
• Step (G-2) is a step of confirming that xylene is produced from toluene introduced into a disproportionation device or a transalkylation (TA) device together with a C9-based component.
• Step (W-3) is a step of confirming that para-xylene can be obtained from the xylene charged into the para-xylene apparatus.
• Step (E-4) is a step of confirming that terephthalic acid can be obtained from paraxylene charged into the terephthalic acid apparatus.
• Step (E-5) is the treatment in the order of the device for thermal decomposition in the presence of water vapor (steam cracker), the disproportionation device or the transalkylation (TA) device, the paraxylene device, and the terephthalic acid device.
• This is a step of confirming that terephthalic acid can be obtained from the naphtha raw material.
• each confirmation process can be performed based on the same concept as the above-mentioned (management method of renewable monocyclic aromatic hydrocarbon).
• the method for managing terephthalic acid of the present invention includes a step (H) of confirming the proportion of the product to which value is assigned as a renewable product, 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).
• Step (H-1) is a step of selecting a product to be assigned as a renewable product from among the products obtained by the terephthalic acid device.
• Step (H-2) determines the value of the proportion (P) to be allocated as a renewable product out of the proportion occupied by the product selected in the step (H-1) to the product obtained by the terephthalic acid device. It is a process.
• Step (H-3) is a step of determining the content ratio (Q) of the renewable naphtha contained in the naphtha raw material.
• Step (H-4) compares the value of the ratio (P) and the value of the content ratio (Q), and the value of the ratio (P) is equal to or less than the value of the content ratio (Q). This is the process of confirming that.
• the determination and understanding of the value of the proportion (P) to be allocated as a renewable product, and the comparison of the value of the proportion (P) and the value of the proportion (Q) are carried out in accordance with the above-mentioned (Management method for renewable monocyclic aromatic hydrocarbons). It can be done based on a similar idea.
• the PET produced using the PET production method of the present invention be assigned a value as a renewable product using a mass balance method in a simple and reliable manner. Therefore, the present invention provides that when PET is manufactured using the PET manufacturing method of the present invention, the value of PET as a renewable product is increased depending on the content ratio of renewable naphtha contained in the renewable naphtha raw material. To provide a management method that can allocate information in a simple and reliable manner. Note that the explanation of the mass balance method is as described above.
• the PET management method of the present invention can be used when producing PET using naphtha raw materials including renewable naphtha.
• the management method of the present invention is a method of assigning value as a renewable product to the PET according to the content ratio of the renewable naphtha contained in the naphtha raw material.
• the control method of the present invention includes a step (F) of confirming that PET is obtained, and step (F) includes the following step (V-1), the following step (G-2), and the following step (W-3). ), the following step (E-4), the following step (F-5), and the following step (F-6).
• Step (V-1) is a step of confirming that toluene is produced from the naphtha raw material introduced into an apparatus for thermal decomposition in the presence of steam (steam cracker).
• Step (G-2) is a step of confirming that xylene is produced from toluene introduced into a disproportionation device or a transalkylation (TA) device together with a C9-based component.
• Step (W-3) is a step of confirming that para-xylene can be obtained from the xylene charged into the para-xylene apparatus.
• Step (E-4) is a step of confirming that terephthalic acid can be obtained from paraxylene charged into the terephthalic acid apparatus.
• Step (F-5) is a step of confirming that PET can be obtained from the terephthalic acid charged into the PET apparatus.
• Step (F-6) includes the apparatus for thermal decomposition in the presence of water vapor (steam cracker), the disproportionation apparatus or the transalkylation (TA) apparatus, the paraxylene apparatus, the terephthalic acid apparatus, and the PET apparatus. This is a step of confirming that PET can be obtained from the naphtha raw material by processing in this order.
• each confirmation process can be performed based on the same concept as the above-mentioned (management method of renewable monocyclic aromatic hydrocarbon).
• the PET management method of the present invention includes a step (J) of confirming the proportion of the product to which value as a renewable product is assigned, and step (J) includes the following step (J-1), the following step ( J-2), the following step (J-3), and the following step (J-4).
• Step (J-1) is a step of selecting a product to be assigned as a renewable product from among the products obtained by the PET apparatus.
• Step (J-2) is a step of determining the value of the proportion (P) to be allocated as a renewable product out of the proportion occupied by the product selected in the step (J-1) to the product obtained by the PET apparatus. It is.
• Step (J-3) is a step of determining the content ratio (Q) of the renewable naphtha contained in the naphtha raw material.
• Step (J-4) compares the value of the ratio (P) with the value of the content ratio (Q), and the value of the ratio (P) is equal to or less than the value of the content ratio (Q). This is the process of confirming that.
• the determination and understanding of the value of the proportion (P) to be allocated as a renewable product, and the comparison of the value of the proportion (P) and the value of the proportion (Q) are carried out in accordance with the above-mentioned (Management method for renewable monocyclic aromatic hydrocarbons). It can be done based on a similar idea.
• the management method of the present invention described above can be executed using a management device. Furthermore, processing in each step of the management method performed by the management device is executed by a computer having a control unit that constitutes the management device.
• a management device that executes the management method of the present invention and a management program (computer program) executed by the computer of the management device will be explained below using an example in which the management method includes step (V) but does not include step (W). do.
• the following explanation regarding the management device and management program applies equally to cases where the management method includes step (W) but does not include step (V), and when it includes step (V) and step (W). Can be applied.
• Preferred embodiments of the management device of the present invention include the following management device.
• a renewable monocyclic aromatic hydrocarbon management device used when producing at least one monocyclic aromatic hydrocarbon of benzene and xylene using a naphtha raw material containing renewable naphtha
• the management device is a device that assigns a value as a renewable product to the product of the at least one type of monocyclic aromatic hydrocarbon according to a content ratio of the renewable naphtha contained in the naphtha raw material.
• the management device has a confirmation unit (I) that confirms that xylene and/or benzene is generated
• the confirmation unit (I) has the following means (V-1), the following means (V-2), and the following means (V-3)
• the means (V-1) is a means for confirming that toluene is produced from the naphtha raw material introduced into an apparatus for thermal decomposition in the presence of water vapor (steam cracker)
• the means (V-2) is a means for confirming that xylene and/or benzene is produced from toluene introduced into the disproportionation device or the TA device
• the means (V-3) converts xylene and/or benzene from the naphtha raw material by processing in the order of the thermal decomposition device (steam cracker) in the presence of steam, the disproportionation device, or the TA device.
• the management device has a confirmation unit (I) for confirming the proportion of the product to which value is assigned as a renewable product;
• the confirmation unit (I) has the following means (X-1), the following means (X-2), the following means (X-3), and the following means (X-4),
• the means (X-1) is means for selecting one or more types of products to be assigned as renewable products from among the products produced by the disproportionation device or the TA device,
• the means (X-2) allocates a proportion ( P) is a means for determining the value of
• the means (X-3) is a means for grasping the value of the content ratio (Q) of the renewable naphtha contained in the naphtha raw material,
• the means (X-4) compares the value of the ratio (P) and the value of the content ratio (Q), and determines that the value of the ratio (P) is equal to or less than the value of the content ratio (Q). This is a means of confirming that ⁇ Renewable monocyclic aromatic hydrocarbon management device
• Preferred embodiments of the management program of the present invention include the following management program.
• ⁇ A management program for renewable monocyclic aromatic hydrocarbons used when producing at least one type of monocyclic aromatic hydrocarbons of benzene and xylene using naphtha raw materials including renewable naphtha The management program is a program that assigns value as a renewable product to the product of the at least one type of monocyclic aromatic hydrocarbon according to the content ratio of the renewable naphtha contained in the naphtha raw material.
• the management program includes: (V-1): Confirm that toluene is produced from the naphtha raw material introduced into a device for thermal decomposition in the presence of steam (steam cracker), (V-2): Confirm that xylene and/or benzene is produced from toluene fed into the disproportionation device or TA device, (V-3): Xylene and/or benzene is produced from the naphtha raw material by processing in the order of the device for thermal decomposition in the presence of steam (steam cracker), the disproportionation device, or the TA device.
• the management program includes: (X-1): Selecting one or more products to be assigned as renewable products from among the products produced by the disproportionation device or the TA device, (X-2): Value of the proportion (P) allocated as a renewable product out of the proportion occupied by the product selected in the above (X-1) to the product produced from the disproportionation device or the TA device decide, (X-3): Grasp the value of the content ratio (Q) of the renewable naphtha contained in the naphtha raw material, (X-4): Compare the value of the ratio (P) with the value of the content ratio (Q), and confirm that the value of the ratio (P) is less than or equal to the value of the content ratio (Q). do, This is a renewable monocyclic aromatic hydrocarbon management program that allows a computer to execute the process.
• the method for managing terephthalic acid of the present invention described above can also be executed using a management device. Further, the processing in each step of the management method performed by the management device is also executed by a computer having a control unit that constitutes the management device.
• a management device that executes the terephthalic acid management method of the present invention and a management program (computer program) executed by a computer of the management device will be described below.
• Preferred embodiments of the terephthalic acid management device of the present invention include the following management device.
• a terephthalic acid management device used when producing terephthalic acid using naphtha raw materials including renewable naphtha The management device is a device that assigns a value to the terephthalic acid as a renewable product according to a content ratio of the renewable naphtha contained in the naphtha raw material,
• the management device includes a confirmation unit (I) for confirming that terephthalic acid is obtained,
• the confirmation section (I) includes the following means (V-1), the following means (G-2), the following means (W-3), the following means (E-4), and the following means (E-5).
• the means (V-1) is a means for confirming that toluene is produced from the naphtha raw material introduced into an apparatus for thermal decomposition in the presence of water vapor (steam cracker)
• the means (G-2) is a means for confirming that xylene is produced from toluene input into a disproportionation device or a transalkylation (TA) device together with a C9-based component
• the means (W-3) is a means for confirming that para-xylene can be obtained from the xylene input into the para-xylene apparatus
• the means (E-4) is a means for confirming that terephthalic acid is obtained from paraxylene charged into the terephthalic acid apparatus
• the means (E-5) is, in order, the device for thermal decomposition in the presence of water vapor (steam cracker), the disproportionation device or the transalkylation (TA) device, the paraxylene device, and the terephthalic acid device.
• the management device includes a confirmation unit (I) for confirming the proportion of the product to which value is assigned as a renewable product;
• the confirmation part (I) includes the following means (H-1), the following means (H-2), the following means (H-3), and the following means (H-4),
• the means (H-1) is means for selecting a product to be assigned as a renewable product from among the products obtained by the terephthalic acid device,
• the means (H-2) determines the value of the proportion (P) to be allocated as a renewable product out of the proportion occupied by the product selected in the means (H-1) to the product obtained by the terephthalic acid device.
• the means (H-3) is a means for grasping the value of the content ratio (Q) of the renewable naphtha contained in the naphtha raw material.
• the means (H-4) compares the value of the ratio (P) and the value of the content ratio (Q), and determines that the value of the ratio (P) is equal to or less than the value of the content ratio (Q). This is a means of confirming that "Terephthalic acid management device.”
• terephthalic acid management program of the present invention include the following management program.
• a terephthalic acid management program used when producing terephthalic acid using naphtha raw materials including renewable naphtha The management program is a program that assigns a value to the terephthalic acid as a renewable product according to the content ratio of the renewable naphtha contained in the naphtha raw material
• the management program includes: (V-1): Confirm that toluene is produced from the naphtha raw material introduced into a device for thermal decomposition in the presence of steam (steam cracker), (G-2): Confirm that xylene is produced from toluene fed into a disproportionation device or a transalkylation (TA) device together with a C9 component, (W-3): Confirm that para-xylene can be obtained from the xylene put into the para-xylene equipment, (E-4): Confirmed that terephthalic acid can be obtained from para
• the management program includes: (H-1): Selecting a product to be assigned as a renewable product from among the products obtained by the terephthalic acid device, (H-2): Determining the value of the proportion (P) to be allocated as a renewable product among the proportion of the product selected in the step (H-1) to the product obtained by the terephthalic acid device; (H-3): Grasp the value of the content ratio (Q) of the renewable naphtha contained in the naphtha raw material, (H-4): Compare the value of the ratio (P) with the value of the content ratio (Q), and check that the value of the ratio (P) is less than or equal to the value of the content ratio (Q). do, This is a terephthalic acid management program that allows a computer to carry out the process.
• the polyethylene terephthalate management method of the present invention described above can also be executed using a management device. Further, the processing in each step of the management method performed by the management device is also executed by a computer having a control unit that constitutes the management device.
• a management device that executes 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 below.
• Preferred embodiments of the polyethylene terephthalate management device of the present invention include the following management device.
• the management device is a device that assigns a value to the polyethylene terephthalate as a renewable product according to the content ratio of the renewable naphtha contained in the naphtha raw material
• the management device includes a confirmation unit (I) that confirms that polyethylene terephthalate is obtained,
• the confirmation section (I) includes the following means (V-1), the following means (G-2), the following means (W-3), the following means (E-4), the following means (F-5), and the following means including means (F-6);
• the means (V-1) is a means for confirming that toluene is produced from the naphtha raw material introduced into an apparatus for thermal decomposition in the presence of water vapor (steam cracker),
• the means (G-2) is a means for confirming that xy
• the management device includes a confirmation unit (I) for confirming the proportion of the product to which value is assigned as a renewable product;
• the confirmation unit (I) includes the following means (J-1), the following means (J-2), the following means (J-3), and the following means (J-4),
• the means (J-1) is means for selecting a product to be assigned as a renewable product from among the products obtained by the PET apparatus,
• the means (J-2) determines the value of the proportion (P) to be allocated as a renewable product out of the proportion occupied by the product selected in the means (J-1) to the product obtained by the PET apparatus.
• the means (J-3) is a means for grasping the value of the content ratio (Q) of the renewable naphtha contained in the naphtha raw material
• the means (J-4) compares the value of the ratio (P) and the value of the content ratio (Q), and determines that the value of the ratio (P) is equal to or less than the value of the content ratio (Q). This is a means of confirming that "Polyethylene terephthalate management device.”
• a preferred embodiment of the polyethylene terephthalate management program of the present invention includes the following management program.
• ⁇ A management program for polyethylene terephthalate used when manufacturing polyethylene terephthalate using naphtha raw materials including renewable naphtha The management program is a program that assigns a value to the polyethylene terephthalate as a renewable product according to the content ratio of the renewable naphtha contained in the naphtha raw material
• the management program includes: (V-1): Confirm that toluene is produced from the naphtha raw material introduced into a device for thermal decomposition in the presence of steam (steam cracker), (G-2): Confirm that xylene is produced from toluene fed into a disproportionation device or a transalkylation (TA) device together with a C9 component, (W-3): Confirm that para-xylene can be obtained from the xylene put into the para-xylene equipment, (E-4): Confirmed that tere
• the management program includes: (J-1): Selecting a product to be assigned as a renewable product from among the products obtained by the PET device, (J-2): Determining the value of the proportion (P) to be allocated as a renewable product out of the proportion occupied by the product selected in the step (J-1) to the product obtained by the PET apparatus, (J-3): Grasp the value of the content ratio (Q) of the renewable naphtha contained in the naphtha raw material, (J-4): Compare the value of the ratio (P) with the value of the content ratio (Q), and check that the value of the ratio (P) is less than or equal to the value of the content ratio (Q). do, This is a polyethylene terephthalate management program that allows a computer to execute the process.
• the management device is a device that executes the management method of the present invention. A preferred embodiment of the management device will be described based on FIG. 13.
• the management device 100 includes a control section 110 and a storage section 120.
• the control unit 110 includes a confirmation unit (I) 130, a comparison unit 140, and a notification unit (output unit) 150
• the storage unit 120 includes a reaction database 160.
• the hardware configuration and functional configuration of the management device 100 will be explained.
• FIG. 14 is a block diagram showing an example of the hardware configuration of the management device 100.
• the management device 100 includes the following units. Each part is connected to each other via a bus 207.
• 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 and the like. 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. Further, the CPU 201 controls the operation of the management device 100 as a whole.
• the CPU 201 is used as a device that controls the operation of the entire management device 100, but the device is not limited to this, and may be, for example, an FPGA (Field Programmable Gate Array).
• FPGA Field Programmable Gate Array
• the management program and various databases do not necessarily need to be stored in the main storage device 202, the auxiliary storage device 203, or the like.
• the management program and various databases may be stored in other information processing devices connected to the management device 100 via the Internet, a LAN (Local Area Network), a WAN (Wide Area Network), or the like.
• the management device 100 may acquire management programs and various databases from these other information processing devices and execute them.
• the main storage device 202 is a computer-readable storage medium that stores various programs and data necessary to execute the various programs.
• the main storage device 202 includes a ROM and a RAM (not shown).
• the ROM stores various programs such as BIOS.
• the RAM functions as a work area in which various programs stored in the ROM are expanded when the CPU 201 executes them.
• the RAM is not limited and can be selected as appropriate depending on the purpose. Examples of the RAM include DRAM and SRAM.
• the auxiliary storage device 203 is not particularly limited as long as it can store various types of information, and can be appropriately selected depending on the purpose. Examples include a solid state drive, a hard disk drive, and the like. Further, the auxiliary storage device 203 may be a portable storage device such as a CD drive, a DVD drive, or a BD drive.
• the output device 204 can be a display, a speaker, or the like. There are no particular limitations on the display, and any known display can be used as appropriate, including, for example, a liquid crystal display and an organic EL display.
• the input device 205 is not particularly limited as long as it can accept various requests to the management device 100, and any known device can be used as appropriate, such as a keyboard, mouse, touch panel, etc.
• the communication interface (communication I/F) 206 is not particularly limited, and any known one can be used as appropriate, such as a wireless or wired communication device. With the hardware configuration as described above, the processing functions of the management device 100 can be realized.
• the management device 100 includes a control section 110 and a storage section 120.
• the control unit 110 controls the entire management device 100.
• the control unit 110 includes a confirmation unit (I) 130, a comparison unit 140, and a notification unit (output unit) 150.
• the confirmation unit (I) of the control unit 110 performs the confirmation operations described in the above means (V-1) to (V-3). Further, the confirmation unit (I) of the control unit 110 confirms that the product to be allocated as a renewable product is selected in the above means (X-1), and the confirmation unit (I) in the above means (X-2) confirms that the product to be allocated as a renewable product is selected.
• the notification unit 150 of the control unit 110 converts (P) mass % of the selected product into a renewable product.
• the value of the proportion (P) exceeds the value of the content proportion (Q)
• the results are output.
• the reaction database 160 in the storage unit 120 of the control unit 110 stores information regarding devices used in the management method of the present invention and information regarding reactions performed in the device.
• the storage unit 120 is a computer-readable storage medium that stores a computer program, and includes a storage medium that stores a management program that causes the control unit 110 including a computer to execute the management method.
• the production amount and yield of the product obtained from each device can be determined by measurement, but in addition to obtaining the yield result by actual measurement, it can also be determined by theoretical calculation using the reaction database 160. Alternatively, predictions can be made based on past accumulated data.
• FIG. 15 is a flowchart illustrating an example of the processing procedure of the management program in the control unit 110 of the management device 100. This will be explained below with reference to FIG.
• step S101 the confirmation unit 130 of the control unit 110 of the management device 100 acquires information regarding the steam cracker, and moves the process to step S102.
• step S102 the confirmation unit 130 of the control unit 110 of the management device 100 confirms that toluene (OUT) is generated from the renewable naphtha raw material (IN) in the steam cracker, and if it is confirmed that toluene (OUT) is generated, , the process moves to step S103.
• step S103 the confirmation unit 130 of the control unit 110 of the management device 100 acquires information regarding the disproportionation device or the TA device, and moves the process to step S104.
• step S104 the confirmation unit 130 of the control unit 110 of the management device 100 confirms with the disproportionation device or the TA device that xylene and/or benzene (OUT) is generated from toluene (IN), If it is confirmed that it has been generated, the process moves to step S105.
• step S105 the confirmation unit 130 of the control unit 110 of the management device 100 confirms that the process is performed in the order of the steam cracker, the disproportionation device, or the TA device, and as a result of these processes, the renewable naphtha raw material (IN) If it is confirmed that xylene and/or benzene (OUT) is generated, the process moves to step S106.
• step S106 the confirmation unit 130 of the control unit 110 of the management device 100 stores in the management device 100 information that the operator has selected to allocate as a renewable product from among the products generated by the disproportionation device or the TA device. is received from the input device (input device 205 in FIG. 14), and the process moves to step S107.
• step S107 the confirmation unit 130 of the control unit 110 of the management device 100 sets the value of the percentage (P) set by the operator to be allocated as a renewable product among the percentages occupied by the selected product in the management device 100. It is received from the input device (input device 205 in FIG. 14), and the process moves to step S108.
• P percentage
• step S108 the confirmation unit 130 of the control unit 110 of the management device 100 acquires the value of the content ratio (Q) of renewable naphtha among the renewable naphtha raw materials to be fed into the steam cracker, and moves the process to step S109.
• step S109 the comparison unit 140 of the control unit 110 of the management device 100 compares the value of the ratio (P) and the value of the content ratio (Q), and moves the process to step S110.
• step S110 the confirmation unit 130 of the control unit 110 of the management device 100 checks the comparison result between 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.
• the process is ended.
• a value as a renewable product can be assigned to the selected desired product according to the content ratio of renewable naphtha contained in the renewable naphtha raw material.
• the assigned 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 performs renewable generation on a product selected according to the content ratio of renewable naphtha contained in the naphtha raw material obtained by the management method. It is designed to output the results that have been assigned a value as an object.
• the operator should review the type of product selected in (X-1) above, review the value of the proportion (P) assigned to the selected product, or change the content proportion (Q) of the renewable naphtha. You can review the values, or even review various conditions such as reaction conditions, and try the process again.
• a management method that includes step (V) but does not include step (W) is used as an example, and a management device and a management program using the management method are explained.
• the same management device and management program can be applied to a management method including step (V) but not step (V), and a management method including step (V) and step (W).
• the functional configuration of the management device that executes the above-described terephthalic acid management method also has the same basic configuration as the management device 100 shown in FIGS. 13 and 14 described above. Therefore, the functional configuration of the management device that executes the terephthalic acid management method will be described with reference to FIGS. 13 and 14.
• the management device 100 that executes the terephthalic acid management method also includes a control section 110 and a storage section 120.
• the control unit 110 controls the entire management device 100.
• the control unit 110 includes a confirmation unit (I) 130, a comparison unit 140, and a notification unit (output unit) 150.
• the confirmation unit (I) of the control unit 110 confirms the above-mentioned means (V-1), means (G-2), means (W-3), means (E-4), and means (E-5). Confirm the information.
• the confirmation unit (I) of the control unit 110 confirms that the product to be assigned as a renewable product is selected from among the products obtained by the terephthalic acid device in the above-mentioned means (H-1).
• the value of the proportion (P) to be allocated as a renewable product out of the proportion occupied by the product selected in the means (H-1) to the product obtained by the terephthalic acid device was set.
• the value of the content ratio (Q) of renewable naphtha contained in the naphtha raw material is confirmed, and in the means (H-4), the value of the ratio (P) and the content Confirmation work is performed by comparing the value of the ratio (Q) and confirming that the value of the ratio (P) is less than or equal to the value of the content ratio (Q).
• the comparison unit 140 of the control unit 110 performs a comparison operation of comparing the value of the proportion (P) and the value of the content proportion (Q) in order to have the confirmation unit (I) confirm it. .
• the notification unit 150 of the control unit 110 converts (P) mass % of the selected product into a renewable product.
• the value of the proportion (P) exceeds the value of the content proportion (Q)
• the system outputs the results of assigning value as a renewable product to the selected product.
• the reaction database 160 in the storage unit 120 of the control unit 110 stores information regarding the equipment used in the terephthalic acid management method of the present invention and information regarding the reactions performed in the equipment. That is, this storage unit 120 is a computer-readable storage medium that stores a computer program, and includes a storage medium that stores a management program that causes the control unit 110 including a computer to execute the terephthalic acid management method. ing.
• the production amount and yield of the product obtained from each device can be determined by measurement, but in addition to obtaining the yield result by actual measurement, it can also be determined by theoretical calculation using the reaction database 160. Alternatively, predictions can be made based on past accumulated data.
• FIG. 16 is a flowchart showing an example of the processing procedure of the terephthalic acid management program in the control unit 110 of the terephthalic acid management device 100. This will be explained below with reference to FIG.
• step S201 the confirmation unit 130 of the control unit 110 of the terephthalic acid management device 100 acquires information regarding the steam cracker, and moves the process to step S202.
• step S202 the confirmation unit 130 of the control unit 110 of the terephthalic acid management device 100 confirms that toluene (OUT) is generated from the renewable naphtha raw material (IN) in the steam cracker, and confirms that toluene (OUT) has been generated. If so, the process moves to step S203.
• step S203 the confirmation unit 130 of the control unit 110 of the terephthalic acid management device 100 acquires information regarding the disproportionation device or the TA device, and moves the process to step S204.
• step S204 the confirmation unit 130 of the control unit 110 of the terephthalic acid management device 100 confirms to the disproportionation device or the TA device that xylene and/or benzene (OUT) is generated from toluene (IN). If it is confirmed that it has been generated, the process moves to step S205.
• 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 device or TA device, the paraxylene device, and the terephthalic acid device are processed in this order, and As a result of the process, it is confirmed that terephthalic acid (OUT) is generated from the renewable naphtha raw material (IN), and if it is confirmed that terephthalic acid (OUT) is generated, the process moves to step S206.
• step S206 the confirmation unit 130 of the control unit 110 of the terephthalic acid management device 100 stores the information selected by the operator to be allocated as a renewable product from among the products produced in the terephthalic acid device into the management device 100.
• step S207 the confirmation unit 130 of the control unit 110 of the terephthalic acid management device 100 determines the value of the proportion (P) set by the operator to be allocated as a renewable product among the proportions occupied by the selected product. from the input device (input device 205 in FIG. 14) in the management device 100, and the process moves to step S208.
• step S208 the confirmation unit 130 of the control unit 110 of the terephthalic acid management device 100 acquires the value of the content ratio (Q) of renewable naphtha among the renewable naphtha raw materials to be fed into the steam cracker, and the process proceeds to step S209. Transition.
• Q content ratio
• 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 moves the process to step S210.
• step S210 the confirmation unit 130 of the control unit 110 of the terephthalic acid management device 100 compares the value of the ratio (P) and the content ratio (Q) determined by the comparison unit 140 of the control unit 110 of the terephthalic acid management device 100. Based on the comparison result with the value, it is confirmed whether the value of the proportion (P) is less than or equal to the value of the content proportion (Q). If it is confirmed that it is less than or equal to the value of the content proportion (Q), this process is ended.
• a value as a renewable product can be assigned to the selected desired product according to the content ratio of renewable naphtha contained in the renewable naphtha raw material.
• the assigned 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 adjusts the content ratio of renewable naphtha contained in the naphtha raw material obtained by the terephthalic acid management method.
• the system outputs the result of assigning a value as a renewable product to the selected product accordingly.
• the operator should review the type of product selected in (X-1) above, review the value of the proportion (P) assigned to the selected product, or change the content proportion (Q) of the renewable naphtha. You can review the values, or even review various conditions such as reaction conditions, and try the process again. (Second modification)
• the management device 100 that executes the polyethylene terephthalate management method also includes a control section 110 and a storage section 120.
• the control unit 110 controls the entire management device 100.
• the control unit 110 includes a confirmation unit (I) 130, a comparison unit 140, and a notification unit (output unit) 150.
• the confirmation unit (I) of the control unit 110 includes the above-mentioned means (V-1), means (G-2), means (W-3), means (E-4), means (F-5), and Perform the confirmation work described in Measures (F-6).
• the confirmation unit (I) of the control unit 110 confirms that a product to be assigned as a renewable product is selected from among the products obtained by the PET apparatus in the above-mentioned means (J-1), In the means (J-2), the value of the proportion (P) to be allocated as a renewable product out of the proportion of the product selected in the means (J-1) to the product obtained by the PET device is set.
• the value of the content ratio (Q) of renewable naphtha contained in the naphtha raw material is confirmed, and in the means (J-4), the value of the ratio (P) and the content ratio ( Confirmation work is performed by comparing the value of Q) and confirming that the value of the ratio (P) is less than or equal to the value of the content ratio (Q).
• the comparison unit 140 of the control unit 110 performs a comparison operation of comparing the value of the proportion (P) and the value of the content proportion (Q) in order to have the confirmation unit (I) confirm it. conduct.
• the notification unit 150 of the control unit 110 converts (P) mass % of the selected product into a renewable product.
• the value of the proportion (P) exceeds the value of the content proportion (Q)
• the system outputs the results of assigning value as a renewable product to the selected product.
• the reaction database 160 in the storage unit 120 of the control unit 110 stores information regarding the equipment used in the polyethylene terephthalate management method of the present invention and information regarding the reactions performed in the equipment. That is, this storage unit 120 is a computer-readable storage medium that stores a computer program, and includes a storage medium that stores a management program that causes the control unit 110 including a computer to execute the polyethylene terephthalate management method. ing.
• the production amount and yield of the product obtained from each device can be determined by measurement, but in addition to obtaining the yield result by actual measurement, it can also be determined by theoretical calculation using the reaction database 160. Alternatively, predictions can be made based on past accumulated data.
• FIG. 17 is a flowchart showing an example of the processing procedure of the polyethylene terephthalate management program in the control unit 110 of the polyethylene terephthalate management device 100. This will be explained below with reference to FIG.
• step S301 the confirmation unit 130 of the control unit 110 of the polyethylene terephthalate management device 100 acquires information regarding the steam cracker, and moves the process to step S302.
• step S302 the confirmation unit 130 of the control unit 110 of the polyethylene terephthalate management device 100 confirms that toluene (OUT) is generated from the renewable naphtha raw material (IN) in the steam cracker, and confirms that toluene (OUT) has been generated. If so, the process moves to step S303.
• step S303 the confirmation unit 130 of the control unit 110 of the polyethylene terephthalate management device 100 acquires information regarding the disproportionation device or the TA device, and moves the process to step S304.
• step S304 the confirmation unit 130 of the control unit 110 of the polyethylene terephthalate management device 100 confirms to the disproportionation device or the TA device that xylene and/or benzene (OUT) is generated from toluene (IN). If it is confirmed that it has been generated, the process moves to step S305.
• step S305 the confirmation unit 130 of the control unit 110 of the polyethylene terephthalate management device 100 confirms that the processing will be performed in the order of steam cracker, disproportionation device or TA device, paraxylene device, terephthalic acid device, and PET device.
• step S306 the confirmation unit 130 of the control unit 110 of the polyethylene terephthalate management device 100 inputs into the management device 100 information that the operator has selected to allocate as a renewable product from among the products generated by the PET device. It is received from the device (input device 205 in FIG. 14), and the process moves to step S307.
• step S307 the confirmation unit 130 of the control unit 110 of the polyethylene terephthalate management device 100 sets the value of the proportion (P) set by the operator to be allocated as a renewable product among the proportions occupied by the selected product to polyethylene terephthalate. from the input device (input device 205 in FIG. 14) in the management device 100, and the process moves to step S308.
• step S308 the confirmation unit 130 of the control unit 110 of the polyethylene terephthalate management device 100 acquires the value of the content ratio (Q) of renewable naphtha among the renewable naphtha raw materials to be fed into the steam cracker, and the process proceeds to step S309. Transition.
• 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 moves the process to step S310.
• step S310 the confirmation unit 130 of the control unit 110 of the polyethylene terephthalate management device 100 compares the ratio (P) value and the content rate (Q) determined by the comparison unit 140 of the control unit 110 of the polyethylene terephthalate management device 100. Based on the comparison result with the value, it is confirmed whether the value of the proportion (P) is less than or equal to the value of the content proportion (Q). If it is confirmed that it is less than or equal to the value of the content proportion (Q), this process is ended.
• a value as a renewable product can be assigned to the selected desired product according to the content ratio of renewable naphtha contained in the renewable naphtha raw material.
• the assigned 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 adjusts the content ratio of renewable naphtha contained in the naphtha raw material obtained by the polyethylene terephthalate management method.
• the system outputs the result of assigning a value as a renewable product to the selected product accordingly.
• the operator should review the type of product selected in (X-1) above, review the value of the proportion (P) assigned to the selected product, or change the content proportion (Q) of the renewable naphtha. You can review the values, or even review various conditions such as reaction conditions, and try the process again.

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• 2022
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