Classifications

• • C—CHEMISTRY; METALLURGY
  • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
  • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
  • C08J11/00—Recovery or working-up of waste materials
  • C08J11/04—Recovery or working-up of waste materials of polymers
  • C08J11/10—Recovery or working-up of waste materials of polymers by chemically breaking down the molecular chains of polymers or breaking of crosslinks, e.g. devulcanisation
  • C08J11/12—Recovery or working-up of waste materials of polymers by chemically breaking down the molecular chains of polymers or breaking of crosslinks, e.g. devulcanisation by dry-heat treatment only
• • 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
  • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
  • C10G1/10—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
• • 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
  • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
  • C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
  • C10G45/04—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used
  • C10G45/06—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof
• • 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
  • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
  • C10G45/32—Selective hydrogenation of the diolefin or acetylene compounds
• • 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
  • 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

Definitions

• the present invention relates to a method for manufacturing chemical products using waste materials.
• the present invention also relates to a method for managing chemical products, which is carried out using a management device used when manufacturing chemical products using waste materials.
• Patent Document 1 In recent years, conversion of waste materials such as waste tires, waste rubber, and waste plastics into chemical products through pyrolysis or other methods has been considered as a method of recycling such materials (for example, Patent Document 1).
• the inventors have investigated a series of processes, particularly in a method for producing chemical products using waste materials, including a pyrolysis step in which waste materials are pyrolyzed to obtain pyrolysis oil, a separation step (atmospheric distillation step) in which the pyrolysis oil is distilled to obtain naphtha fraction and other fractions (kerosene fraction, diesel fraction), and a steam cracking step in which at least one of the naphtha fraction and/or other fractions is subjected to steam cracking to obtain chemical products.
• the present invention aims to provide a method for efficiently producing chemical products from waste materials, including waste tires, by improving each step in a series of processes, thereby enabling long-term operation of the process.
• the present invention also aims to provide a method for managing chemical products, which is carried out using a management device used when manufacturing chemical products from waste materials.
• the inventors conducted research to solve the above problems, and discovered that by improving the above-mentioned series of processes in the method of manufacturing chemical products using waste materials and performing a low-temperature hydrogenation process in which low-temperature hydrogenation is performed on the pyrolysis oil to obtain low-temperature hydrogenated oil, and a high-temperature hydrogenation process in which high-temperature hydrogenation is performed on the low-temperature hydrogenated oil to obtain high-temperature hydrogenated oil, between the pyrolysis process and the separation process (atmospheric distillation process), it is possible to suppress the generation of fouling (by-products such as hydrocarbon polymers).
• the inventors completed the present invention based on this knowledge.
• One aspect of the present invention relates, for example, to the following: [1] A pyrolysis step of obtaining a first gas fraction, a pyrolysis oil, and a residue fraction by pyrolysis of crushed waste materials including waste tires; a low-temperature hydrogenation step of subjecting a feedstock oil containing at least a portion of the pyrolysis oil to low-temperature hydrogenation treatment at a temperature of 180° C. or more and 350° C.
• a high-temperature hydrogenation step in which a feedstock oil containing at least a portion of the low-temperature hydrogenated oil is subjected to a hydrotreatment at a temperature higher than that of the low-temperature hydrogenation step to obtain a second gas fraction and a high-temperature hydrogenated oil;
• a steam cracking process for subjecting a steam cracking feedstock oil containing at least a portion of the naphtha fraction and/or the other fraction to a steam cracking process to obtain a chemical product,
• the amount of the pyrolysis oil is 40 mass% or more relative to the total amount of the first gas component, the pyrolysis oil, and the residue component.
• the nitrogen content in the atmospheric distillation feedstock oil is 2000 ppm by mass or more, and the nitrogen content in the naphtha fraction is 25 ppm by mass or less.
• the amount of the high-temperature hydrogenated oil relative to the total amount of the high-temperature hydrogenated oil and the crude oil in the atmospheric distillation feedstock oil is 0.001% by mass or more and 9% by mass or less.
• a method for producing synthetic rubber comprising a polymerization step of obtaining synthetic rubber by a polymerization reaction using the butadiene obtained by the production method according to [19] as at least a part of a raw material of the synthetic rubber.
• a tire comprising a synthetic rubber obtained by the production method according to [21].
• a method for producing a tire comprising: a vulcanization step of obtaining a tire by a vulcanization reaction using the synthetic rubber obtained by the production method according to [21] as at least a part of a raw material for the tire.
• a method for managing chemical products which is carried out using a management device used in manufacturing chemical products using waste materials including waste tires, comprising:
• the management method is a method of allocating a value as a renewable product to the chemical product using the management device according to a content ratio of renewable raw materials contained in the waste material using a mass balance method,
• the management method includes a step (V) of confirming that the chemical product is obtained,
• the step (V) includes the following steps (V-1), (V-2), (V-3), (V-4), (V-5), and (V-6),
• the step (V-1) is a step of confirming that the pyrolysis oil is produced from the waste material input into a pyrolysis unit for obtaining pyrolysis oil by pyrolysis of the waste material;
• the step (V-2) is a step of confirming that the low-temperature hydrogenated oil is produced from the pyrolysis oil input into a low-temperature hydrogenation unit in which a feedstock oil containing at least a part of the
• the step (V-3) is a step of confirming that the high-temperature hydrogenated oil is produced from the low-temperature hydrogenated oil input into a high-temperature hydrogenation unit in which a feedstock oil containing at least a portion of the low-temperature hydrogenated oil is subjected to a hydrogenation treatment at a temperature higher than that of the low-temperature hydrogenation treatment to obtain a second gas fraction and a high-temperature hydrogenated oil
• the step (V-4) is a step of confirming that the naphtha fraction and the other fractions are produced from the high-temperature hydrogenated oil input into an atmospheric distillation unit that separates an atmospheric distillation feedstock containing at least a portion of the high-temperature hydrogenated oil and crude oil into a naphtha fraction and other fractions by atmospheric distillation
• the step (V-5) is a step of confirming that the chemical product is obtained from the steam cracking feedstock oil introduced into a steam cracker that subjects
• the management device includes a computer-readable storage medium storing a management program, A management device that executes the management method described in [24] by executing the management program.
• the management device according to [25] which, after executing the management method, outputs a result of assigning a value as a renewable product to a product selected according to the content ratio of renewable raw materials contained in waste materials including scrap tires, obtained by the management method.
• a computer-readable storage medium storing a computer program comprising: A storage medium storing a management program that causes a computer to execute the management method described in [24].
• the present invention provides a method for efficiently producing chemical products from waste materials, including waste tires, by improving each step in a series of processes, thereby enabling long-term operation of the process.
• the present invention also provides a method for managing chemical products, which is executed using a management device used when manufacturing chemical products from waste materials.
• FIG. 1 is a schematic diagram showing an example of a pyrolysis device.
• FIG. 1 is a schematic diagram showing an example of a system for carrying out a method for producing a chemical product.
• FIG. 2 is a schematic diagram illustrating a functional configuration of a management device.
• FIG. 2 is a block diagram showing an example of a hardware configuration of a management device.
• 10 is a flowchart showing an example of a processing procedure of a management program in a control unit of the management device.
• FIG. 1 is a schematic diagram of a stain evaluation test device (HLPS) used in the examples.
• HLPS stain evaluation test device
• the method for producing chemical products in this embodiment includes a pyrolysis step in which a first gas fraction, pyrolysis oil, and a residue fraction are obtained by pyrolysis of crushed waste materials including waste tires; a low-temperature hydrogenation step in which a feedstock oil containing at least a portion of the pyrolysis oil is subjected to low-temperature hydrogenation treatment at 180°C to 350°C to obtain low-temperature hydrogenated oil; a high-temperature hydrogenation step in which a feedstock oil containing at least a portion of the low-temperature hydrogenated oil is subjected to hydrogenation treatment at a temperature higher than the low-temperature hydrogenation treatment to obtain a second gas fraction and high-temperature hydrogenated oil; a separation step in which a feedstock oil for atmospheric distillation containing at least a portion of the high-temperature hydrogenated oil and crude oil is subjected to atmospheric distillation to separate it into a naphtha fraction and other fractions; and a steam cracking step in which a steam cracking feed
• the amount of pyrolysis oil relative to the total amount of the first gas component, pyrolysis oil, and residue component is 40 mass% or more.
• the pyrolysis step is a step of obtaining a first gas fraction, a pyrolysis oil, and a residue fraction by pyrolysis of crushed waste materials including waste tires.
• the waste materials include at least waste tires, and may further include at least one of waste rubber and waste plastic.
• the waste materials can also be called polymer-based waste materials that contain polymer materials.
• polymer materials include rubber materials such as natural rubber, BR (butadiene rubber), SBR (styrene-butadiene rubber), NBR (nitrile rubber), IIR (butyl rubber), Cl-IIR (chlorinated butyl rubber), and Br-IIR (brominated butyl rubber), as well as resin materials such as polyethylene, polypropylene, styrene-butadiene copolymer, ethylene-vinyl acetate copolymer, and polyvinyl chloride.
• waste materials may further contain metals.
• waste tires may contain metals in the steel cords and wires that are the aggregates of the tires.
• the manufacturing method of this embodiment may further include a removal step of removing the metals from the waste material or its crushed material.
• a removal step of removing the metals from the waste material There are no particular limitations on the method for removing the metals from the waste material, and examples of the method include removal using a magnet, a sieve, etc.
• the pyrolysis step will produce a first gas, pyrolysis oil, and a mixture of residue and metals.
• the manufacturing method of this embodiment may further include a removal step of removing metals from the mixture.
• a removal step of removing metals from the mixture There are no particular limitations on the method for removing metals from the mixture, and examples include methods of removing metals using magnets, sieves, etc.
• the method for crushing the waste material is not particularly limited, and may be, for example, mechanical crushing using a single-shaft or twin-shaft crusher, crushing using a water jet, freeze crushing, laser crushing, or the like.
• the pyrolysis of crushed waste materials can be carried out, for example, by placing the crushed waste materials in a pyrolysis furnace, supplying high-temperature gas to the pyrolysis furnace, and bringing the crushed waste materials into contact with the high-temperature gas.
• the high-temperature gas is preferably an oxygen-free gas that contains substantially no oxygen (for example, a gas with an oxygen content of 1% by volume or less).
• the high-temperature gas may be any gas other than oxygen and oxides, and may be, for example, an inert gas such as nitrogen, argon, or helium, hydrogen, or a hydrocarbon with 1 to 4 carbon atoms.
• the pyrolysis furnace is not particularly limited, and may be, for example, a kettle-type pyrolysis furnace, a fluidized bed-type pyrolysis furnace, or a kiln-type pyrolysis furnace.
• the pyrolysis temperature (temperature of high-temperature gas) in the pyrolysis step may be, for example, 300 ° C or higher, and from the viewpoint of further improving the chemical product yield, it is preferably 350 ° C or higher, more preferably 370 ° C or higher, and even more preferably 390 ° C or higher.
• the pyrolysis temperature (temperature of high-temperature gas) in the pyrolysis step may be, for example, 800 ° C or lower, and from the viewpoint of further improving the chemical product yield, it is preferably 750 ° C or lower, more preferably 730 ° C or lower, and even more preferably 710 ° C or lower.
• the pyrolysis temperature (temperature of the high-temperature gas) in the pyrolysis step may be, for example, 300 to 800°C, 300 to 750°C, 300 to 730°C, 300 to 710°C, 350 to 800°C, 350 to 750°C, 350 to 730°C, 350 to 710°C, 370 to 800°C, 370 to 750°C, 370 to 730°C, 370 to 710°C, 390 to 800°C, 390 to 750°C, 390 to 730°C, or 390 to 710°C.
• the pyrolysis may be carried out in the presence of a pyrolysis catalyst or in the absence of a pyrolysis catalyst.
• a pyrolysis catalyst any catalyst used in ordinary petrochemical pyrolysis may be used without any particular restrictions.
• the pyrolysis catalyst may be an acidic catalyst or a basic catalyst.
• an acidic catalyst for example, a catalyst containing an aluminosilicate may be mentioned.
• a smectite group such as zeolite and montmorillonite may be mentioned.
• a catalyst containing montmorillonite for example, clays or minerals such as activated clay, acid clay, and bentonite may be mentioned.
• a basic catalyst for example, a carbonate such as sodium carbonate may be used.
• the pyrolysis conditions may be adjusted as appropriate, for example, so that the resulting component ratios and the properties of the resulting pyrolysis oil are within the preferred ranges described below.
• a first gas fraction, a pyrolysis oil, and a residue fraction are obtained.
• the residue fraction may be obtained as a mixture with a metal fraction, as described above.
• a pyrolysis gas is generated in a pyrolysis furnace, and the pyrolysis gas can be cooled to recover pyrolysis oil as an oil fraction.
• the first gas fraction can be recovered as the residual gas after cooling the pyrolysis gas to recover the oil fraction.
• the residue fraction can be recovered as the solid fraction remaining in the pyrolysis furnace after pyrolysis.
• the amount of pyrolysis oil relative to the total amount of the first gas, pyrolysis oil, and residue is 40 mass% or more.
• the amount of thermal decomposition oil relative to the total amount of the first gas fraction, the thermal decomposition oil and the residue may be, for example, 45% by mass or more.
• the amount of thermal decomposition oil relative to the total amount of the first gas fraction, the thermal decomposition oil and the residue may be preferably 48% by mass or more, more preferably 50% by mass or more, and may be 51% by mass or more or 52% by mass or more.
• the amount of thermal decomposition oil relative to the total amount of the first gas fraction, the thermal decomposition oil and the residue may be, for example, 80% by mass or less, preferably 75% by mass or less, more preferably 70% by mass or less, even more preferably 65% by mass or less, and may be 60% by mass or less.
• the amount of pyrolysis oil relative to the total amount of the first gas component, the pyrolysis oil, and the residue component is, for example, 40 to 80 mass%, 40 to 75 mass%, 40 to 70 mass%, 40 to 65 mass%, 40 to 60 mass%, 45 to 80 mass%, 45 to 75 mass%, 45 to 70 mass%, 45 to 65 mass%, 45 to 60 mass%, 48 to 80 mass%, 48 to 75 mass% , 48-70% by mass, 48-65% by mass, 48-60% by mass, 50-80% by mass, 50-75% by mass, 50-70% by mass, 50-65% by mass, 50-60% by mass, 51-80 quality mass%, 51-75 mass%, 51-70 mass%, 51-65 mass%, 51-60 mass%, 52-80 mass%, 52-75 mass%, 52-70 mass%, 52-65 mass% or 52-65 mass% It may be 60% by mass.
• the amount of the first gas component relative to the total amount of the first gas component, the thermal decomposition oil, and the residue is, for example, 25% by mass or less.
• the amount of the first gas component relative to the total amount of the first gas component, the thermal decomposition oil, and the residue is preferably 20% by mass or less, more preferably 15% by mass or less, and may be 13% by mass or less or 10% by mass or less.
• the amount of the first gas component is 25% by mass or less under the thermal decomposition conditions, the decrease in the yield of the thermal decomposition oil due to the excessive progress of the thermal decomposition of the crushed material can be suppressed.
• the thermal decomposition oil generated by the thermal decomposition of the crushed material can be suppressed from being further thermally decomposed into a gas component, and the yield of the thermal decomposition oil that can be made into a chemical product through the low-temperature hydrogenation step, the high-temperature hydrogenation step, the atmospheric distillation step, and the steam cracking step can be further improved, and the yield of the chemical product can be further improved.
• the amount of the first gas component relative to the total amount of the first gas component, the pyrolysis oil, and the residue is, for example, 0.1% by mass or more. From the viewpoint of improving the purity of the chemical product obtained through the low-temperature hydrogenation process, the high-temperature hydrogenation process, the atmospheric distillation process, and the steam cracking process, it may be 0.5% by mass or more, 0.7% by mass or more, 1% by mass or more, 1.3% by mass or more, or 1.5% by mass or more.
• the crushed material contains, for example, chlorine
• a part of the chlorine content in the crushed material is gasified as chlorine gas or the like by pyrolysis. That is, a part of the chlorine content contained in the crushed material is removed as a part of the first gas content.
• the chlorine content contained in the pyrolysis oil can be reduced compared to when the first gas content is not generated. Therefore, by setting the pyrolysis conditions so that a predetermined amount of the first gas component is generated, the purity of the chemical product obtained through the low-temperature hydrogenation process for the pyrolysis oil, the high-temperature hydrogenation process for the low-temperature hydrogenation oil, the atmospheric distillation process for the atmospheric distillation feed oil containing the high-temperature hydrogenation oil, and the steam cracking process for the steam cracking feed oil is further improved.
• the amount of the first gas component relative to the total amount of the first gas component, the pyrolysis oil, and the residue component is, for example, 0.1 to 25 mass%, 0.1 to 20 mass%, 0.1 to 15 mass%, 0.1 to 13 mass%, 0.1 to 10 mass% or less, 0.5 to 25 mass%, 0.5 to 20 mass%, 0.5 to 15 mass%, 0.5 to 13 mass%, 0.5 to 10 mass% or less, 0.7 to 25 mass%, 0.7 to 20 mass%, 0.7 to 15 mass% , 0.7 to 13 mass%, 0.7 to 10 mass% or less, 1 to 25 mass%, 1 to 20 mass%, 1 to 15 mass%, 1 to 13 mass%, 1 to 10 mass% or less, 1.3 to 25 mass%, 1.3 to 20 mass%, 1.3 ⁇ 15% by mass, 1.3-13% by mass, 1.3-10% by
• the amount of the residue relative to the total amount of the first gas fraction, the thermal decomposition oil, and the residue is, for example, 10% by mass or more.
• the amount of the residue relative to the total amount of the first gas fraction, the thermal decomposition oil, and the residue is preferably 15% by mass or more, more preferably 20% by mass or more.
• the thermal decomposition conditions are such that the amount of the residue is 10% by mass or more, it is possible to suppress a decrease in the yield of the thermal decomposition oil due to excessive progress of the thermal decomposition of the crushed material.
• the amount of the residue relative to the total amount of the first gas fraction, pyrolysis oil, and residue is, for example, 60% by mass or less. From the viewpoint of improving the yield of the chemical product obtained through the low-temperature hydrogenation process, the high-temperature hydrogenation process, the atmospheric distillation process, and the steam cracking process, it is preferably 55% by mass or less, more preferably 50% by mass or less, and even more preferably 45% by mass or less, and may be 40% by mass or less.
• the amount of the residue relative to the total amount of the first gas fraction, pyrolysis oil, and residue increases, the amount of the first gas fraction and pyrolysis oil relative to the total amount of the first gas fraction, pyrolysis oil, and residue decreases.
• the amount of the residue relative to the total amount of the first gas, pyrolysis oil, and residue may be, for example, 10 to 60 mass%, 10 to 55 mass%, 10 to 50 mass%, 10 to 45 mass%, 10 to 40 mass%, 15 to 60 mass%, 15 to 55 mass%, 15 to 50 mass%, 15 to 45 mass%, 15 to 40 mass%, 20 to 60 mass%, 20 to 55 mass%, 20 to 50 mass%, 20 to 45 mass%, or 20 to 40 mass%.
• the first gas component may be, for example, a component of the product produced by pyrolysis that is gaseous at normal pressure and 20°C.
• the first gas component may contain, for example, hydrogen, a hydrocarbon having 1 to 4 carbon atoms, etc.
• the method for recovering the first gas component is not particularly limited.
• the first gas component can be recovered as the residual gas remaining after cooling the pyrolysis gas produced by pyrolysis and recovering the oil component (pyrolysis oil).
• the first gas portion can be reused, for example, as high-temperature gas (oxygen-free gas) in pyrolysis. That is, the first gas portion can be heated and supplied to the pyrolysis furnace as part (or all) of the high-temperature gas (oxygen-free gas).
• the first gas portion can be used, for example, as combustion gas for heating the pyrolysis section in the pyrolysis process or as combustion gas for a heating furnace in other processes.
• the pyrolysis oil may be, for example, a component of the product produced by pyrolysis that is liquid at normal pressure and 20°C.
• the method for recovering the pyrolysis oil is not particularly limited.
• the pyrolysis oil can be recovered, for example, as an oil fraction distilled from a pyrolysis furnace. That is, the pyrolysis oil can be recovered, for example, as an oil fraction condensed by cooling the pyrolysis gas produced by pyrolysis.
• the distillation properties of the pyrolysis oil are not particularly limited, and it is sufficient if the properties allow it to be used as a feedstock oil in the low-temperature hydrogenation process and the high-temperature hydrogenation process.
• the 10% distillation temperature (T10) of the pyrolysis oil may be, for example, 90° C. or higher, and from the viewpoint of being more suitable as a feed oil in the low-temperature hydrogenation step, is preferably 140° C. or higher, more preferably 150° C. or higher, and even more preferably 155° C. or higher.
• the 10% distillation temperature of the pyrolysis oil may be, for example, 200° C. or lower, 190° C. or lower, or 180° C. or lower.
• the 10% distillation temperature (T10) of the pyrolysis oil may be, for example, 90 to 200°C, 90 to 190°C, 90 to 180°C, 140 to 200°C, 140 to 190°C, 140 to 180°C, 150 to 200°C, 150 to 190°C, 150 to 180°C, 155 to 200°C, 155 to 190°C, or 155 to 180°C.
• the 90% distillation temperature (T90) of the pyrolysis oil may be, for example, 350° C. or higher, preferably 370° C. or higher, more preferably 390° C. or higher, and even more preferably 400° C. or higher, and may be 410° C. or higher, 420° C. or higher, 430° C. or higher, 440° C. or higher, or 450° C. or higher.
• the 90% distillation temperature (T90) of the pyrolysis oil may be, for example, 650° C. or lower, preferably 600° C. or lower, and more preferably 550° C. or lower.
• the 90% distillation temperature (T90) of the pyrolysis oil is, for example, 350 to 650 ° C., 350 to 600 ° C., 350 to 550 ° C., 370 to 650 ° C., 370 to 600 ° C., 370 to 550 ° C., 390 to 650 ° C., 390 to 600 ° C., 390 to 550 ° C., 400 to 650 ° C., 400 to 600 ° C., 400 to 550 ° C., 410 to 650 ° C., 410 to 600 ° C., 410 to 550 ° C., 420 to 650 ° C., °C, 420 to 600 °C, 420 to 550 °C, 430 to 650 °C, 430 to 600 °C, 430 to 550 °C, 440 to 650 °C, 440 to 600 °C, 440 to 550 °C, 450 to 650 °C,
• the pyrolysis oil contains low-boiling oils with a boiling point of 350°C or less, and may also contain high-boiling oils with a boiling point of more than 350°C.
• the content of the high boiling point oil in the pyrolysis oil is not particularly limited, but is preferably 50 mass% or less, more preferably 45 mass% or less, even more preferably 40 mass% or less, and even more preferably 35 mass% or less, based on the total amount of the pyrolysis oil.
• the content of high boiling point oil in the pyrolysis oil may be, for example, 5 mass% or more, 8 mass% or more, or 10 mass% or more, based on the total amount of the pyrolysis oil. That is, the content of high boiling point oil in the pyrolysis oil may be, for example, 5 to 50 mass%, 5 to 45 mass%, 5 to 40 mass%, 5 to 35 mass%, 8 to 50 mass%, 8 to 45 mass%, 8 to 40 mass%, 8 to 35 mass%, 10 to 50 mass%, 10 to 45 mass%, 10 to 40 mass%, or 10 to 35 mass%, based on the total amount of the pyrolysis oil.
• the pyrolysis oil may contain nitrogen, sulfur, chlorine, halogen elements, etc.
• the nitrogen content of the pyrolysis oil may be, for example, 100 ppm by mass or more, 2000 ppm by mass or more, 2500 ppm by mass or more, or 3000 ppm by mass or more.
• the nitrogen content is converted into gas components such as ammonia by hydrogenation in the low-temperature hydrogenation process and the high-temperature hydrogenation process, and can be easily separated from the liquid product. Then, by supplying the liquid product with a significantly reduced nitrogen content to the steam cracking process, a high-purity chemical product (a chemical product with little nitrogen content) can be easily obtained.
• the nitrogen content of the pyrolysis oil may be, for example, 20,000 ppm by mass or less, 15,000 ppm by mass or less, or 10,000 ppm by mass or less. If the nitrogen content is 20,000 ppm by mass or less, the nitrogen content of the liquid product after the low-temperature hydrogenation process and the high-temperature hydrogenation process can be more significantly reduced.
• the nitrogen content of the pyrolysis oil may be, for example, 100 to 20,000 ppm by mass, 100 to 15,000 ppm by mass, 100 to 10,000 ppm by mass, 2000 to 20,000 ppm by mass, 2000 to 15,000 ppm by mass, 2000 to 10,000 ppm by mass, 2500 to 20,000 ppm by mass, 2500 to 15,000 ppm by mass, 2500 to 10,000 ppm by mass, 3000 to 20,000 ppm by mass, 3000 to 15,000 ppm by mass, or 3000 to 10,000 ppm by mass.
• the sulfur content of the pyrolysis oil may be, for example, 10 ppm by mass or more, 100 ppm by mass or more, 500 ppm by mass or more, or 1000 ppm by mass or more.
• the sulfur content is converted into gas components such as hydrogen sulfide by hydrogenation in the low-temperature hydrogenation process and the high-temperature hydrogenation process, and can be easily separated from the liquid product. Then, by supplying the liquid product with a significantly reduced sulfur content to the steam cracking process, a high-purity chemical product (a chemical product with little sulfur content) can be easily obtained.
• the sulfur content of the pyrolysis oil may be, for example, 30,000 ppm by mass or less, 20,000 ppm by mass or less, or 10,000 ppm by mass or less. If the sulfur content is 30,000 ppm by mass or less, the sulfur content of the liquid product after the low-temperature hydrogenation process and the high-temperature hydrogenation process can be more significantly reduced.
• the sulfur content of the pyrolysis oil may be, for example, 10 to 30,000 ppm by mass, 10 to 20,000 ppm by mass, 10 to 10,000 ppm by mass, 100 to 30,000 ppm by mass, 100 to 20,000 ppm by mass, 100 to 10,000 ppm by mass, 500 to 30,000 ppm by mass, 500 to 20,000 ppm by mass, 500 to 10,000 ppm by mass, 1000 to 30,000 ppm by mass, 1000 to 20,000 ppm by mass, or 1000 to 10,000 ppm by mass.
• the chlorine content of the pyrolysis oil may be, for example, 10 ppm by mass or more, 30 ppm by mass or more, 50 ppm by mass or more, or 100 ppm by mass or more.
• the chlorine content is converted into gas components such as hydrogen chloride by hydrogenation in the low-temperature hydrogenation step and the high-temperature hydrogenation step, and can be easily separated from the liquid product. Then, by supplying the liquid product with a significantly reduced chlorine content to the steam cracking step, a high-purity chemical product (a chemical product with little chlorine content) can be easily obtained.
• the chlorine content of the pyrolysis oil may be, for example, 2000 ppm by mass or less, 1500 ppm by mass or less, or 1000 ppm by mass or less. If the chlorine content is 1000 ppm by mass or less, the chlorine content of the liquid product after the low-temperature hydrogenation step and the high-temperature hydrogenation step can be more significantly reduced. In addition, it is preferable that not only the chlorine content but also the other halogen element content is in the same range.
• the chlorine content of the pyrolysis oil may be, for example, 10 to 2000 ppm by mass, 10 to 1500 ppm by mass, 10 to 1000 ppm by mass, 30 to 2000 ppm by mass, 30 to 1500 ppm by mass, 30 to 1000 ppm by mass, 50 to 2000 ppm by mass, 50 to 1500 ppm by mass, 50 to 1000 ppm by mass, 100 to 2000 ppm by mass, 100 to 1500 ppm by mass, or 100 to 1000 ppm by mass.
• the residue may be, for example, solids that are not recovered as pyrolysis gas from the products produced by pyrolysis. There are no particular limitations on the method for recovering the residue.
• the residue can be recovered, for example, as solids remaining in the pyrolysis furnace (solids that are not discharged outside the reaction system as pyrolysis gas).
• the residue may be a charcoal formed by thermal decomposition of the crushed waste material.
• the residue may be recovered as a charcoal.
• Carbide is a component in which carbon is the majority.
• the carbide may be a carbon concentrate whose main component is carbon black.
• the carbide may have clumps that have aggregated during the pyrolysis process.
• the aggregated carbide can be pulverized using a crusher or the like to obtain powdered carbide.
• the manufacturing method of this embodiment may further include a step of pulverizing the residue to obtain a powdered carbide.
• a manufacturing method can be said to be a method capable of producing both chemical products and carbides.
• Powdered carbide can be used effectively as an additive for rubber, an additive for resin, a colorant, etc.
• the residue may contain, for example, rubber components of waste materials that were not completely pyrolyzed.
• the rubber components are sticky, the carbonized material is recovered as a mass of a mixture of carbon black and rubber components.
• Such carbonized material is difficult to pulverize using a grinder or the like because the stickiness of the rubber components inhibits the powderization of the carbonized material.
• the lump-shaped carbonized material leads to poor dispersion in the base material, it is difficult to use it as an additive for rubber, an additive for resin, a colorant, or the like.
• the manufacturing method of this embodiment may further include a step of producing a carbonized material by thermal decomposition of the residue.
• the pyrolysis process may be carried out, for example, by a pyrolysis apparatus equipped with a pyrolysis furnace.
• the pyrolysis furnace used in the pyrolysis process may be any furnace capable of pyrolyzing the crushed material, and may be, for example, a batch pyrolysis furnace or a continuous pyrolysis furnace.
• a continuous pyrolysis furnace for example, a rotary kiln or an auger furnace may be used. Note that, in the following, a pyrolysis apparatus equipped with a batch pyrolysis furnace will be described as an example of a pyrolysis apparatus, but the pyrolysis apparatus is not limited to this.
• FIG. 1 is a schematic diagram showing an example of a pyrolysis device.
• the pyrolysis device in Figure 1 includes a heat exchanger 1 for heating an oxygen-free gas, a pyrolysis furnace 2 that contains waste material 6, a decomposition device 7 having an external heating means 8 for heating the pyrolysis furnace 2 from the outside, an oil recovery device 5 for cooling the pyrolysis gas generated in the decomposition device 7 and recovering the condensed oil (pyrolysis oil), a circulation path 4 for supplying the remaining gas after the oil recovery in the oil recovery device 5 to the heat exchanger 1 as an oxygen-free gas, and an oxygen-free gas supply source 3 for supplying the oxygen-free gas to the heat exchanger 1.
• a heat exchanger 1 for heating an oxygen-free gas
• a pyrolysis furnace 2 that contains waste material 6
• a decomposition device 7 having an external heating means 8 for heating the pyrolysis furnace 2 from the outside
• an oil recovery device 5 for cooling the pyrolysis gas generated in the decomposition
• the pyrolysis apparatus of FIG. 1 also includes a flowmeter 9, a damper 10, and a blower 11 in the piping that connects the oxygen-free gas source 3 to the heat exchanger 1 in order to supply oxygen-free gas from the oxygen-free gas source 3, and a flowmeter 9, a damper 10, a blower 11, and a hot air stove 14 in the circulation path 4 in order to circulate the remaining gas after recovery in the oil recovery device 5 to the heat exchanger 1 as oxygen-free gas.
• the oil recovery device 5 may also include multiple dry distillation towers 12a and 12b to separate the recovered oil according to its boiling point.
• Each dry distillation tower 12 may be connected to a recovery tank 13 through piping at its lower part, and the recovered oil can be stored.
• the thermal cracking device in FIG. 1 includes multiple dry distillation towers 12a and 12b, but in this embodiment, the thermal cracking oil can be used as is as feed oil for the low-temperature hydrogenation process, so there may only be one dry distillation tower.
• each dry distillation tower 12 is connected to a separate recovery tank 13, but each dry distillation tower 12 may be connected to the same recovery tank 13.
• By removing at least a portion of the high boiling point oil from the pyrolysis oil it is possible to suppress the generation of fouling in the heat exchanger or heating furnace in the high-temperature hydrogenation step and the atmospheric distillation step, making it possible to realize long-term operation of the process.
• it is more preferable to remove at least a portion of the high boiling point oil for example, with a boiling point exceeding 450°C.
• the method for removing the high boiling point oils is to cool the pyrolysis gas immediately after it is produced in the pyrolysis process, separate it into a pyrolysis oil containing a large amount of high boiling point oils and a gas fraction containing a large amount of low boiling point oils, and then further cool the gas fraction containing a large amount of low boiling point oils to separate it into a first gas fraction and a pyrolysis oil containing a large amount of low boiling point oils.
• the pyrolysis oil can be heated and separated into low boiling point oils and high boiling point oils in a distillation tower, but this is not limited to the methods described above.
• the content of high boiling point oil in the pyrolysis oil from which some of the high boiling point oil has been removed before the low-temperature hydrogenation step (hereinafter also referred to as "fractionated pyrolysis oil”) is not particularly limited, but is 50 mass% or less, more preferably 40 mass% or less, even more preferably 30 mass% or less, and even more preferably 25 mass% or less, based on the total amount of the pyrolysis oil fractionated before the low-temperature hydrogenation step. If the content of high boiling point oil in the pyrolysis oil fractionated before the low-temperature hydrogenation step is 50 mass% or less, the effects of easily heavy components such as heavy olefins and dienes can be suppressed.
• the content of high boiling point oil in the pyrolysis oil fractionated before the low-temperature hydrogenation step may be, for example, 1 mass% or more, 2 mass% or more, or 3 mass% or more, based on the total amount of the pyrolysis oil fractionated before the low-temperature hydrogenation step.
• the removed high boiling oil may be recycled as a raw material for the pyrolysis process, may be used as a raw material for the production of carbon black, or may be used as a fuel.
• the low-temperature hydrogenation step is a step in which a feedstock oil containing at least a portion of the pyrolysis oil is subjected to low-temperature hydrotreatment at 180° C. or higher and 350° C. or lower to obtain a low-temperature hydrogenated oil.
• the feedstock oil in the low-temperature hydrogenation process may contain pyrolysis oil or may contain fractionated pyrolysis oil.
• the feedstock oil in the low-temperature hydrogenation process may further contain components other than pyrolysis oil, or pyrolysis oil may be used as it is as the feedstock oil.
• recycled oil containing at least a portion of the light and heavy fractions obtained in the high-temperature hydrogenation step described below or any diluting hydrocarbon oil may be used.
• recycled oil or any diluting hydrocarbon oil dienes and olefins that tend to polymerize and generate dirt can be diluted, which has the effect of preventing the generation of dirt.
• the heat generation effect in the reactor in the low-temperature hydrogenation step and the high-temperature hydrogenation step can be reduced, and the stability of the process operation can be improved.
• diluting hydrocarbons include kerosene fraction, diesel fraction, and vacuum diesel fraction obtained from an atmospheric distillation unit derived from crude oil, LCO obtained from an FCC unit, and even product kerosene and product diesel.
• the amount of recycled oil relative to the total amount of recycled oil and pyrolysis oil in the feed oil is preferably 10% by mass or more and 99% by mass or less, more preferably 20% by mass or more and 97% by mass or less, even more preferably 30% by mass or more and 95% by mass or less, particularly preferably 40% by mass or more and 93% by mass or less, and most preferably 50% by mass or more and 90% by mass or less.
• the low-temperature hydrogenation process may be a process of hydrogenating a feedstock in the presence of a hydrogenation catalyst.
• Hydrogenation can be carried out, for example, by supplying the feedstock to a reactor in which a hydrogenation catalyst is disposed and contacting the feedstock with the hydrogenation catalyst in the reactor.
• the hydrogenation catalyst for example, a known hydrogenation catalyst used in the hydrogenation of hydrocarbon oils can be used. From the viewpoint of hydrogenation ability, it is preferable that the hydrogenation catalyst contains, for example, a Ni-based or Co-based catalyst.
• a Ni-based catalyst is a catalyst having Ni as an active metal, and Ni may exist in the form of a sulfide or the like.
• a Co-based catalyst is a catalyst having Co as an active metal.
• the hydrogenation catalyst one type of hydrogenation catalyst may be used, or multiple types of hydrogenation catalysts may be used.
• the reaction temperature in the low-temperature hydrogenation step is from 180°C to 350°C, preferably from 190°C to 340°C, more preferably from 200°C to 330°C, even more preferably from 210°C to 320°C, particularly preferably from 220°C to 310°C, and most preferably from 240°C to 305°C.
• the reaction pressure in the low-temperature hydrogenation step is not particularly limited and may be, for example, 1 MPaG or more, preferably 3 MPaG or more, more preferably 5 MPaG or more.
• the reaction pressure in the low-temperature hydrogenation step is not particularly limited and may be, for example, 20 MPaG or less, preferably 19 MPaG or less, more preferably 18 MPaG or less. That is, the reaction pressure in the low-temperature hydrogenation step may be, for example, 1 to 20 MPaG, 1 to 19 MPaG, 1 to 18 MPaG, 3 to 20 MPaG, 3 to 19 MPaG, 3 to 18 MPaG, 5 to 20 MPaG, 5 to 19 MPaG, or 5 to 18 MPaG.
• the weight hourly space velocity (WHSV) of the feed oil may be, for example, 0.1 h ⁇ 1 or more, preferably 0.15 h ⁇ 1 or more, more preferably 0.2 h ⁇ 1 or more.
• the weight hourly space velocity (WHSV) of the feed oil may be, for example, 5 h ⁇ 1 or less, preferably 4 h ⁇ 1 or less, more preferably 3 h ⁇ 1 or less.
• the weight hourly space velocity (WHSV) of the feed oil may be 0.1 to 5 h ⁇ 1 , 0.1 to 4 h ⁇ 1 , 0.1 to 3 h ⁇ 1 , 0.15 to 5 h ⁇ 1 , 0.15 to 4 h ⁇ 1 , 0.15 to 3 h ⁇ 1 , 0.2 to 5 h ⁇ 1 , 0.2 to 4 h ⁇ 1 or 0.2 to 3 h ⁇ 1 .
• the low-temperature hydrogenation step is carried out in the presence of hydrogen.
• the hydrogen/oil ratio may be, for example, 100 NL/L or more, preferably 150 NL/L or more, more preferably 200 NL/L or more.
• the hydrogen/oil ratio may be, for example, 1500 NL/L or less, preferably 1400 NL/L or less, more preferably 1300 NL/L or less.
• the hydrogen/oil ratio may be, for example, 100 to 1500 NL/L, 100 to 1400 NL/L, 100 to 1300 NL/L, 150 to 1500 NL/L, 150 to 1400 NL/L, 150 to 1300 NL/L, 200 to 1500 NL/L, 200 to 1400 NL/L, or 200 to 1300 NL/L.
• the low-temperature hydrogenated oil obtained in the low-temperature hydrogenation step preferably has the following properties:
• the diene value of the low-temperature hydrogenated oil is preferably less than 14.0 gI 2 /100g, more preferably 13.0 gI 2 /100g or less, further preferably 12.0 gI 2 /100g or less, and particularly preferably 11.0 gI 2 /100g or less.
• the iodine value of the low-temperature hydrogenated oil is preferably less than 160 gI 2 /100 g, more preferably 155 gI 2 /100 g or less, further preferably 150 gI 2 /100 g or less, and particularly preferably 145 gI 2 /100 g or less.
• the total acid value of the low-temperature hydrogenated oil is less than 5.0 mgKOH/g, more preferably 4.8 mgKOH/g or less, further preferably 4.7 mgKOH/g or less, and particularly preferably 4.5 mgKOH/g or less.
• the present invention by reducing in advance the olefins, dienes, higher fatty acids, and other substances that polymerize and cause fouling in the pyrolysis oil treated in the low-temperature hydrogenation process, it is possible to suppress the occurrence of fouling in the heat exchangers of the high-temperature hydrogenation process and the atmospheric distillation unit, making it possible to realize long-term operation of the process.
• the high-temperature hydrogenation step is a step of obtaining a second gas fraction and a high-temperature hydrogenated oil by high-temperature hydrotreating a feedstock oil containing at least a portion of the low-temperature hydrogenated oil.
• the high-temperature hydrogenated oil contains a light fraction having a boiling point of 350° C. or less and a heavy fraction having a boiling point of more than 350° C.
• the feedstock oil in the high-temperature hydrogenation process contains low-temperature hydrogenated oil, but may also contain pyrolysis oil, fractionated pyrolysis oil, or other components.
• the feedstock oil in the high-temperature hydrogenation process contains low-boiling oil with a boiling point of 350°C or less and high-boiling oil with a boiling point of over 350°C, and the content of high-boiling oil is, for example, 50 mass% or less based on the total amount of feedstock oil.
• the content of high boiling point oil in the feed oil in the high temperature hydrogenation step is preferably 50 mass% or less, more preferably 40 mass% or less, even more preferably 30 mass% or less, and still more preferably 25 mass% or less, based on the total amount of the feed oil. Furthermore, the content of high boiling point oil in the feed oil in the high temperature hydrogenation step may be 1.0 mass% or more, 2.0 mass% or more, or 3.0 mass% or more, based on the total amount of the feed oil.
• the 10% distillation temperature of the feedstock oil in the high-temperature hydrogenation step may be, for example, 90° C. or higher, preferably 140° C. or higher, more preferably 150° C. or higher, and even more preferably 155° C. or higher.
• the 10% distillation temperature of the feedstock oil may be, for example, 200° C. or lower, 190° C. or lower, or 180° C. or lower.
• the 10% distillation temperature of the feedstock oil in the high-temperature hydrogenation step may be, for example, 90 to 200°C, 90 to 190°C, 90 to 180°C, 140 to 200°C, 140 to 190°C, 140 to 180°C, 150 to 200°C, 150 to 190°C, 150 to 180°C, 155 to 200°C, 155 to 190°C, or 155 to 180°C.
• the 90% distillation temperature of the feedstock oil in the high-temperature hydrogenation step may be, for example, 350° C. or higher, preferably 370° C. or higher, more preferably 390° C. or higher, and even more preferably 400° C. or higher, and may be 410° C. or higher, 420° C. or higher, 430° C. or higher, 440° C. or higher, or 450° C. or higher.
• the 90% distillation temperature of the feedstock oil may be, for example, 650° C. or lower, preferably 600° C. or lower, and more preferably 550° C. or lower.
• the 90% distillation temperature of the feedstock oil in the high-temperature hydrogenation step is, for example, 350 to 650°C, 350 to 600°C, 350 to 550°C, 370 to 650°C, 370 to 600°C, 370 to 550°C, 390 to 650°C, 390 to 600°C, 390 to 550°C.
• the feedstock oil used in the high-temperature hydrogenation process may contain nitrogen, sulfur, chlorine, other halogen elements, etc.
• the nitrogen content of the feedstock oil in the high-temperature hydrogenation step may be, for example, 100 ppm by mass or more, 2000 ppm by mass or more, 2500 ppm by mass or more, or 3000 ppm by mass or more.
• the nitrogen content of the feedstock oil may be, for example, 20,000 ppm by mass or less, 15,000 ppm by mass or less, or 10,000 ppm by mass or less.
• the nitrogen content of the feedstock oil in the high-temperature hydrogenation step may be, for example, 100 to 20,000 ppm by mass, 100 to 15,000 ppm by mass, 100 to 10,000 ppm by mass, 2000 to 20,000 ppm by mass, 2000 to 15,000 ppm by mass, 2000 to 10,000 ppm by mass, 2500 to 20,000 ppm by mass, 2500 to 15,000 ppm by mass, 2500 to 10,000 ppm by mass, 3000 to 20,000 ppm by mass, 3000 to 15,000 ppm by mass, or 3000 to 10,000 ppm by mass.
• the sulfur content of the feedstock oil in the high-temperature hydrogenation step may be, for example, 10 ppm by mass or more, 100 ppm by mass or more, 500 ppm by mass or more, or 1000 ppm by mass or more.
• a chemical product is produced through the high-temperature hydrogenation step and the cracking step, even if a large amount of sulfur is present in the feedstock oil, a high-purity chemical product (a chemical product with little sulfur content) can be easily obtained.
• the sulfur content of the feedstock oil may be, for example, 30,000 ppm by mass or less, 20,000 ppm by mass or less, or 10,000 ppm by mass or less.
• the sulfur content of the feed oil in the high-temperature hydrogenation step may be, for example, 10 to 30,000 ppm by mass, 10 to 20,000 ppm by mass, 10 to 10,000 ppm by mass, 100 to 30,000 ppm by mass, 100 to 20,000 ppm by mass, 100 to 10,000 ppm by mass, 500 to 30,000 ppm by mass, 500 to 20,000 ppm by mass, 500 to 10,000 ppm by mass, 1000 to 30,000 ppm by mass, 1000 to 20,000 ppm by mass, or 1000 to 10,000 ppm by mass.
• the chlorine content of the feedstock oil in the high-temperature hydrogenation step may be, for example, 10 ppm by mass or more, 30 ppm by mass or more, 50 ppm by mass or more, or 100 ppm by mass or more.
• the chlorine content of the feedstock oil may be, for example, 2000 ppm by mass or less, 1500 ppm by mass or less, or 1000 ppm by mass or less.
• other halogen element contents may be in the same range.
• the chlorine content of the feed oil in the high-temperature hydrogenation step may be, for example, 10 to 2000 ppm by mass, 10 to 1500 ppm by mass, 10 to 1000 ppm by mass, 30 to 2000 ppm by mass, 30 to 1500 ppm by mass, 30 to 1000 ppm by mass, 50 to 2000 ppm by mass, 50 to 1500 ppm by mass, 50 to 1000 ppm by mass, 100 to 2000 ppm by mass, 100 to 1500 ppm by mass, or 100 to 1000 ppm by mass.
• the high-temperature hydrogenation process may be a process for hydrogenating a feedstock in the presence of a hydrogenation catalyst.
• Hydrogenation can be carried out, for example, by supplying the feedstock to a reactor in which a hydrogenation catalyst is disposed and contacting the feedstock with the hydrogenation catalyst in the reactor.
• the hydrogenation catalyst for example, a known hydrogenation catalyst used in the hydrogenation of hydrocarbon oils can be used.
• the hydrogenation catalyst when the feedstock oil in the high-temperature hydrogenation process contains high-boiling-point oil, the hydrogenation catalyst is preferably a catalyst that has excellent hydrogenation ability and can efficiently hydrogenate the high-boiling-point oil.
• the hydrogenation catalyst preferably contains, for example, a Ni-based catalyst.
• a Ni-based catalyst is a catalyst that has Ni as an active metal.
• the high-temperature hydrogenation process may be carried out using one type of hydrogenation catalyst, or may be carried out using multiple types of hydrogenation catalysts.
• the hydrogenation catalyst may be an appropriate combination of the desulfurization/denitrification catalyst, high-resolution catalyst, low-resolution catalyst, etc., described below.
• the desulfurization/denitrification catalyst may be a hydrogenation catalyst that has excellent desulfurization and denitrification performance.
• An example of a desulfurization/denitrification catalyst is a hydrocracking catalyst in which an active metal is supported on a support containing alumina. Such hydrogenation catalysts tend to have excellent desulfurization and denitrification performance.
• the support for the desulfurization/denitrification catalyst may be an alumina-containing support, and preferably has an alumina content of 50% by mass or more.
• the alumina content in the support for the desulfurization/denitrification catalyst may be, for example, 50% by mass or more, preferably 55% by mass or more, and more preferably 60% by mass or more, based on the total amount of the support.
• the carrier of the desulfurization/denitrogenation catalyst may contain a component other than alumina.
• the carrier of the desulfurization/denitrogenation catalyst may contain, for example, an oxide of an element of Group 2, 3, 4, 13, 14, or 15 of the periodic table. More specifically, the carrier of the desulfurization/denitrogenation catalyst may contain, for example, at least one oxide of silica, phosphorus, magnesia, zirconia, boria, titania, calcia, zinc, etc.
• the carrier of the desulfurization/denitrogenation catalyst contains silica, silica-alumina, silica-alumina-phosphorus, silica-magnesia, alumina-silica-magnesia, alumina-silica-zirconia, etc.
• the carrier of the desulfurization/denitrogenation catalyst may be crystalline or amorphous.
• the shape of the support for the desulfurization/denitrification catalyst is not particularly limited, and may be, for example, spherical, cylindrical, trilobe, or quadrilobe.
• Examples of active metals contained in the desulfurization/denitrification catalyst include Ni, Mo, Co, W, and P.
• the desulfurization/denitrification catalyst may contain one type of active metal, or may contain two or more types. From the viewpoint of easily realizing excellent hydrogenation ability and enabling more efficient desulfurization/denitrification, the desulfurization/denitrification catalyst preferably contains at least Ni, and more preferably contains Ni and Mo or W.
• the active metal may be activated by a sulfurization treatment. By containing sulfides of Ni, among the above metals, in particular, the desulfurization/denitrification catalyst is more likely to realize excellent hydrogenation ability.
• a high-resolution catalyst is a hydrogenation catalyst that has an active metal supported on a carrier containing zeolite. Such hydrogenation catalysts have small pores and tend to have excellent hydrogenation resolution.
• the carrier of the high resolution catalyst may be a carrier containing zeolite, and preferably the zeolite content is 1 mass% or more.
• the zeolite content in the carrier of the high resolution catalyst may be, for example, 2 mass% or more, preferably 3 mass% or more, and more preferably 5 mass% or more, based on the total amount of the carrier.
• the carrier of the high-resolution catalyst may contain a component other than zeolite.
• the carrier of the high-resolution catalyst may contain, for example, an oxide of an element of Groups 2, 3, 4, 13, 14, or 15 of the periodic table. More specifically, the carrier of the high-resolution catalyst may contain at least one oxide of, for example, silica, alumina, phosphorus, magnesia, zirconia, boria, titania, calcia, zinc, etc.
• the carrier of the high-resolution catalyst contains alumina, silica, silica-alumina, silica-alumina-phosphorus, silica-magnesia, alumina-silica-magnesia, alumina-silica-zirconia, etc.
• the carrier of the high-resolution catalyst may be crystalline or amorphous.
• the shape of the carrier of the high-resolution catalyst is not particularly limited, and may be, for example, spherical, cylindrical, trilobal, or quadrolobal.
• Examples of active metals contained in the high-resolution catalyst include Ni, Mo, Co, W, and P.
• the high-resolution catalyst may contain one type of active metal, or may contain two or more types. From the viewpoint of easily realizing excellent hydrogenation ability and being able to hydrogenate high-boiling-point oils more efficiently, the high-resolution catalyst preferably contains at least Ni, and more preferably contains Ni and Mo or W.
• the active metal may be activated by a sulfurization treatment. By containing sulfides of Ni, particularly of the above metals, the desulfurization/denitrogenation catalyst is more likely to realize excellent hydrogenation ability.
• a low-resolution catalyst is a hydrogenation catalyst in which an active metal is supported on a support containing alumina.
• Such hydrogenation catalysts have many large pores compared to high-resolution catalysts, and tend to have milder hydrogenation resolution than high-resolution catalysts.
• the support of the low-resolution catalyst may be a support containing alumina.
• the alumina content in the support of the low-resolution catalyst may be, for example, 20 mass% or more, preferably 25 mass% or more, and more preferably 30 mass% or more, based on the total amount of the support.
• the support of the low-resolution catalyst may contain a component other than alumina.
• the support of the low-resolution catalyst may contain, for example, an oxide of an element of Groups 2, 3, 4, 13, 14, or 15 of the periodic table. More specifically, the support of the low-resolution catalyst may contain at least one oxide of, for example, silica, phosphorus, magnesia, zirconia, boria, titania, calcia, zinc, etc.
• the support of the low-resolution catalyst contains silica, silica-alumina, silica-alumina-phosphorus, silica-magnesia, alumina-silica-magnesia, alumina-silica-zirconia, etc.
• the support of the low-resolution catalyst may be crystalline or amorphous.
• the shape of the support of the low-resolution catalyst is not particularly limited, and may be, for example, spherical, cylindrical, trilobal, or quadrolobal.
• Examples of active metals contained in the low-resolution catalyst include Ni, Mo, Co, W, and P.
• the low-resolution catalyst may contain one type of active metal, or may contain two or more types. From the viewpoint of being able to hydrogenate high-boiling-point oils more efficiently, the low-resolution catalyst preferably contains at least Ni, and more preferably contains Ni and Mo or W.
• the active metal may be activated by a sulfurization treatment. By containing sulfides of Ni, particularly of the above metals, the desulfurization/denitrogenation catalyst is more likely to achieve excellent hydrogenation ability.
• a desulfurization/denitrification catalyst may be used in combination with a cracking catalyst.
• the cracking catalyst may be a combination of a high-resolution catalyst and a low-resolution catalyst, or only a high-resolution catalyst or only a low-resolution catalyst.
• the desulfurization/denitrification catalyst may be placed at least in front of the high-resolution catalyst and the low-resolution catalyst, or may be placed both in front of and behind the high-resolution catalyst and the low-resolution catalyst.
• the nitrogen in the feedstock oil may adhere to the active sites of the high-resolution catalyst or low-resolution catalyst, thereby reducing the cracking performance of the high-resolution catalyst or low-resolution catalyst.
• the nitrogen in the feedstock oil is converted to ammonia, etc., and the nitrogen content in the feedstock oil is reduced. Therefore, in the high-temperature hydrogenation process, it is preferable to place the desulfurization/denitrification catalyst in a stage before the high-resolution catalyst or low-resolution catalyst.
• the desulfurization/denitrification catalyst in a stage before the high-temperature hydrogenation unit described below. With this arrangement, even if the feedstock oil contains nitrogen, the cracking performance of the high-resolution catalyst or low-resolution catalyst can be prevented from decreasing.
• the high-temperature hydrogenation step may be carried out, for example, using a flow reactor.
• a flow reactor it is preferable to arrange, in the flow reactor from the inlet side, a first catalyst layer containing a desulfurization/denitrification catalyst and a second catalyst layer containing a decomposition catalyst in this order.
• a third catalyst layer containing a type of decomposition catalyst with a different decomposition ability and a fourth catalyst layer containing a desulfurization/denitrification catalyst may be further arranged downstream of the second catalyst layer.
• the reaction temperature in the high-temperature hydrogenation step is not particularly limited, and may be, for example, 300°C or higher, preferably 320°C or higher, and more preferably 340°C or higher.
• the reaction temperature in the high-temperature hydrogenation step may be, for example, 480°C or lower, preferably 460°C or lower, and more preferably 440°C or lower. That is, the reaction temperature in the high-temperature hydrogenation step may be, for example, 300 to 480°C, 300 to 460°C, 300 to 440°C, 320 to 480°C, 320 to 460°C, 320 to 440°C, 340 to 480°C, 340 to 460°C, or 340 to 440°C.
• the reaction pressure in the high-temperature hydrogenation step is not particularly limited and may be, for example, 1 MPaG or more, preferably 3 MPaG or more, more preferably 5 MPaG or more.
• the reaction pressure in the high-temperature hydrogenation step is not particularly limited and may be, for example, 20 MPaG or less, preferably 19 MPaG or less, more preferably 18 MPaG or less. That is, the reaction pressure in the high-temperature hydrogenation step may be, for example, 1 to 20 MPaG, 1 to 19 MPaG, 1 to 18 MPaG, 3 to 20 MPaG, 3 to 19 MPaG, 3 to 18 MPaG, 5 to 20 MPaG, 5 to 19 MPaG, or 5 to 18 MPaG.
• the weight hourly space velocity (WHSV) of the feed oil may be, for example, 0.1 h ⁇ 1 or more, preferably 0.15 h ⁇ 1 or more, more preferably 0.2 h ⁇ 1 or more.
• the weight hourly space velocity (WHSV) of the feed oil may be, for example, 5 h ⁇ 1 or less, preferably 4 h ⁇ 1 or less, more preferably 3 h ⁇ 1 or less.
• the weight hourly space velocity (WHSV) of the feed oil may be 0.1 to 5 h ⁇ 1 , 0.1 to 4 h ⁇ 1 , 0.1 to 3 h ⁇ 1 , 0.15 to 5 h ⁇ 1 , 0.15 to 4 h ⁇ 1 , 0.15 to 3 h ⁇ 1 , 0.2 to 5 h ⁇ 1 , 0.2 to 4 h ⁇ 1 or 0.2 to 3 h ⁇ 1 .
• the high-temperature hydrogenation step is carried out in the presence of hydrogen.
• the hydrogen/oil ratio may be, for example, 100 NL/L or more, preferably 150 NL/L or more, more preferably 200 NL/L or more.
• the hydrogen/oil ratio may be, for example, 1500 NL/L or less, preferably 1400 NL/L or less, more preferably 1300 NL/L or less.
• the hydrogen/oil ratio may be, for example, 100 to 1500 NL/L, 100 to 1400 NL/L, 100 to 1300 NL/L, 150 to 1500 NL/L, 150 to 1400 NL/L, 150 to 1300 NL/L, 200 to 1500 NL/L, 200 to 1400 NL/L, or 200 to 1300 NL/L.
• the feedstock oil is hydrogenated to produce a second gas fraction and high-temperature hydrogenated oil.
• the second gas component may be, for example, a component of the product produced by hydrogenation that is gaseous at room temperature, 20°C.
• the second gas component may contain, for example, hydrogen, a hydrocarbon having 1 to 4 carbon atoms, etc.
• the second gas may be used, for example, as combustion gas for heating the pyrolysis section in the pyrolysis process or as combustion gas for a heating furnace in other processes.
• the sulfur content in the high-temperature hydrogenated oil is, for example, 1500 ppm by mass or less, and from the viewpoints of reducing the amount of impurities in the chemical products obtained in the cracking process, preventing catalyst poisoning in the later stages of the cracking process, and preventing equipment corrosion, it is preferably 1000 ppm by mass or less, and more preferably 900 ppm by mass or less.
• the nitrogen content in the high-temperature hydrogenated oil is, for example, 100 ppm by mass or less, and from the viewpoint of reducing the amount of impurities in the chemical products obtained in the cracking process, it is preferably 25 ppm by mass or less, and more preferably 20 ppm by mass or less.
• the chlorine content in the high-temperature hydrogenated oil is, for example, 20 ppm by mass or less, and from the viewpoint of reducing the amount of impurities in the chemical products obtained in the cracking process and preventing catalyst poisoning and equipment corrosion in the subsequent stages of the cracking process, it is preferably 15 ppm by mass or less, and more preferably 10 ppm by mass or less. In addition, it is preferable that not only the chlorine content but also the contents of other halogen elements are in the same range.
• the separation step is a step of separating the raw oil for atmospheric distillation, which contains at least a part of the high-temperature hydrogenated oil and crude oil, into a naphtha fraction and other fractions by atmospheric distillation.
• the naphtha fraction may include light naphtha and heavy naphtha, and preferably includes light naphtha.
• the other fractions include conventionally known fractions other than the naphtha fraction, such as a gas fraction with a low boiling point, a kerosene fraction with a high boiling point, a diesel fraction, and a residual oil fraction.
• the amount of high-temperature hydrogenated oil relative to the total amount of high-temperature hydrogenated oil and crude oil in the atmospheric distillation feedstock oil in the separation process is preferably 0.001 mass% or more, more preferably 0.005 mass% or more, even more preferably 0.01 mass% or more, still more preferably 0.05 mass% or more, and is preferably 9 mass% or less, more preferably 7 mass% or less, even more preferably 5 mass% or less, particularly preferably 3 mass% or less, and most preferably 1 mass% or less.
• the amount of high-temperature hydrogenated oil relative to the total amount of high-temperature hydrogenated oil and crude oil in the atmospheric distillation feedstock oil is, for example, preferably 0.001 mass% or more and 9 mass% or less, more preferably 0.005 mass% or more and 7 mass% or less, even more preferably 0.01 mass% or more and 57 mass% or less, even more preferably 0.05 mass% or more and 3 mass% or less, and most preferably 0.05 mass% or more and 1 mass% or less.
• the amount of high-temperature hydrogenated oil is within the above numerical range, when the high-temperature hydrogenated oil is mixed with crude oil low in nitrogen and dienes to obtain atmospheric distillation feedstock oil, the nitrogen and dienes contained in the high-temperature hydrogenated oil are diluted in the atmospheric distillation feedstock oil, which not only suppresses the generation of fouling in the heat exchanger of the atmospheric distillation unit, but also suppresses the impact of impurities such as nitrogen on downstream equipment.
• the crude oil used in the separation process is not particularly limited, and any conventionally known crude oil can be used.
• the atmospheric distillation feedstock oil in the separation step may contain nitrogen, sulfur, chlorine, other halogen elements, etc. Since the atmospheric distillation feedstock oil is usually mostly composed of crude oil, it is preferable that the amount of nitrogen and dienes in the crude oil is less than the amount of nitrogen and dienes in the high-temperature hydrogenated oil. For example, it is preferable that the crude oil has the following properties: The nitrogen content of the crude oil is preferably 2000 ppm by mass or less, more preferably 1500 ppm by mass or less, and further preferably 1000 ppm by mass or less.
• the nitrogen content of the naphtha fraction obtained in the separation process is preferably 500 ppm by mass or less, more preferably 400 ppm by mass or less, and even more preferably 300 ppm by mass or less.
• the steam cracking process is a process for obtaining chemical products by subjecting a steam cracking feedstock oil containing a naphtha fraction and/or a part of other fractions obtained in the atmospheric distillation process to a steam cracking treatment.
• the steam cracking feedstock oil is thermally treated with steam to crack the naphtha fraction (light naphtha, etc.), producing components useful as chemical products.
• the steam cracking feedstock oil in the steam cracking process may further contain ethane, naphtha, kerosene, light oil fractions, etc. derived from petroleum, etc.
• the naphtha fraction may be used as it is as the steam cracking feedstock oil, or the naphtha fraction may be used as the steam cracking feedstock oil after additional treatment such as desulfurization treatment.
• the conditions for the steam cracking process are not particularly limited and may be appropriately selected from known conditions used in the steam cracking processes of ethane, naphtha, kerosene, etc.
• the reaction temperature of the steam cracking treatment may be, for example, 650° C. or higher, preferably 700° C. or higher, and more preferably 750° C. or higher.
• the reaction temperature of the steam cracking treatment may be, for example, 1000° C. or lower, preferably 950° C. or lower, and more preferably 900° C. or lower. That is, the reaction temperature of the steam cracking treatment may be, for example, 650 to 1000°C, 650 to 950°C, 650 to 900°C, 700 to 1000°C, 700 to 950°C, 700 to 900°C, 750 to 1000°C, 750 to 950°C, or 750 to 900°C.
• the reaction time (residence time) of the steam cracking treatment may be, for example, 0.05 seconds or more, preferably 0.06 seconds or more, more preferably 0.08 seconds or more, and may be, for example, 2.0 seconds or less, preferably 1.9 seconds or less, more preferably 1.8 seconds or less. That is, the reaction time of the steam cracking treatment may be, for example, 0.05 to 2.0 seconds, 0.05 to 1.9 seconds, 0.05 to 1.8 seconds, 0.06 to 2.0 seconds, 0.06 to 1.9 seconds, 0.06 to 1.8 seconds, 0.08 to 2.0 seconds, 0.08 to 1.9 seconds, or 0.08 to 1.8 seconds.
• the steam/steam cracking feedstock oil ratio (mass ratio) in the steam cracking treatment may be, for example, 0.2 or more, preferably 0.25 or more, more preferably 0.3 or more, and may be, for example, 1.0 or less, preferably 0.9 or less, more preferably 0.8 or less. That is, the ratio (mass ratio) of steam to steam cracking feed oil may be, for example, 0.2 to 1.0, 0.2 to 0.9, 0.2 to 0.8, 0.25 to 1.0, 0.25 to 0.9, 0.25 to 0.8, 0.3 to 1.0, 0.3 to 0.9, or 0.3 to 0.8.
• the outlet reaction pressure of the steam cracking treatment may be, for example, 0.1 MPaA or more, preferably 0.15 MPaA or more, more preferably 0.2 MPaA or more.
• the reaction pressure of the steam cracking treatment may be, for example, 1.0 MPaA or less, preferably 0.8 MPaA or less, more preferably 0.6 MPaA or less. That is, the outlet reaction pressure of the steam cracking treatment may be, for example, 0.1 to 1.0 MPaA, 0.1 to 0.8 MPaA, 0.1 to 0.6 MPaA, 0.15 to 1.0 MPaA, 0.15 to 0.8 MPaA, 0.15 to 0.6 MPaA, 0.2 to 1.0 MPaA, 0.2 to 0.8 MPaA, or 0.2 to 0.6 MPaA.
• Chemical products obtained from the steam cracking process include, for example, ethylene, propylene, butadiene, butenes, isoprene, benzene, toluene, xylene, ethylbenzene, styrene, cyclopentadiene, dicyclopentadiene, indene, methylstyrene, and other olefin-containing C9 aromatics for resin conversion.
• light fractions may be obtained in addition to chemical products.
• light fractions include methane, ethane, butane, pentane, propane, and hexane.
• a heavy fraction may be obtained in addition to chemical products.
• the heavy fraction may be reused as a raw material for the steam cracking process, or may be used as a raw material for producing charcoal.
• the heavy fraction obtained in the steam cracking process of this embodiment tends to have a high aromatic content, and can be suitably used as a raw material for producing charcoal (particularly carbon black).
• charcoal (particularly carbon black) can be obtained by thermal decomposition or incomplete combustion of the heavy fraction.
• the heavy fraction may be, for example, a fraction having a 10% distillation temperature of 190° C. or higher, or may be a fraction having a 10% distillation temperature of 200° C. or higher.
• the 10% distillation temperature of the heavy fraction may be, for example, 250° C. or lower, or may be 240° C. or lower.
• the 90% distillation temperature of the heavy fraction may be, for example, 450° C. or higher, or may be 500° C. or higher.
• the 90% distillation temperature of the heavy fraction may be, for example, 750° C. or lower, or may be 700° C. or lower.
• the 10% distillation temperature of the heavy fraction may be, for example, 190 to 250° C., 190 to 240° C., 200 to 250° C., or 200 to 240° C.
• the 90% distillation temperature of the heavy fraction may be, for example, 450 to 750° C., 450 to 700° C., 500 to 750° C., or 500 to 700° C.
• the aromatic content of the heavy fraction may be, for example, 30% by mass or more, preferably 35% by mass or more, more preferably 40% by mass or more, and may be, for example, 90% by mass or less. That is, the aromatic content of the heavy fraction may be, for example, 30 to 90 mass %, 35 to 90 mass %, or 40 to 90 mass %.
• FIG. 2 is a schematic diagram showing an example of a system for carrying out the manufacturing method of this embodiment.
• the system 100 shown in FIG. 2 includes a pyrolysis unit 110, a first separation unit 111, a pulverization unit 112, a low-temperature hydrogenation unit 115, a high-temperature hydrogenation unit 120, an atmospheric distillation unit 125, and a steam cracker 130.
• the waste material S1 is first supplied to the pyrolysis unit 110, where it is pyrolyzed.
• a mixture S4 of a first gas component S2, pyrolysis oil S3, a residue component, and a metal component is generated.
• the first gas component S2 may be discharged outside the system, or may be reused as an oxygen-free gas in the pyrolysis unit 110.
• the pyrolysis oil S3 is supplied to the low-temperature hydrogenation unit 115.
• the mixture S4 is supplied to the first separation unit 111, where it is separated into a residue component S5 and a metal component S6.
• the residue component S5 is pulverized in the pulverization unit 112 and collected as powdered charcoal S7.
• low-temperature hydrogenation unit 115 low-temperature hydrogenation of the pyrolysis oil S3 produces low-temperature hydrogenated oil S8.
• the low-temperature hydrogenated oil S8 is supplied to the high-temperature hydrogenation unit 120.
• a second gas fraction S9 and a high-temperature hydrogenated oil S10 are produced by high-temperature hydrogenation treatment of the low-temperature hydrogenated oil S8.
• the second gas fraction S9 may be discharged from the system, or may be used as a combustion gas for heating the thermal cracking section in the thermal cracking process or as a combustion gas for a heating furnace in other processes.
• the high-temperature hydrogenated oil S10 is supplied to the atmospheric distillation unit 125.
• the high-temperature hydrogenated oil S10 may also be reused in the low-temperature hydrogenation unit 115 as recycled oil S15.
• the high-temperature hydrogenated oil S10 is distilled at atmospheric pressure to produce steam cracking feedstock S11, which contains at least a portion of the naphtha fraction and other fractions (kerosene fraction, light oil fraction).
• the steam cracking feedstock S11 may be obtained as a single fraction or as a mixture.
• the steam cracking feedstock S11 is supplied to the steam cracker 130.
• the steam cracking feedstock oil S11 is subjected to steam cracking processing to produce a product gas S12, a product oil S13, and a heavy fraction S14.
• the product gas S12 and the product oil S13 contain ethylene, propylene, butadiene, butenes, isoprene, benzene, toluene, xylene, ethylbenzene, styrene, cyclopentadiene, dicyclopentadiene, olefin-containing C9 aromatics for resin conversion such as indene and methylstyrene, which are useful as chemical products, and the product gas S12 and the product oil S13 are appropriately separated and recovered to obtain chemical products.
• the heavy fraction S14 is preferably used as a raw material for producing charcoal, and may also be used as a fuel.
• the method for producing butadiene according to the present embodiment includes a polymerization step of obtaining synthetic rubber by a polymerization reaction using the butadiene obtained by the above-described production method as at least a part of the raw material of the synthetic rubber.
• a polymerization composition containing at least butadiene as a monomer is polymerized by a conventionally known method to obtain synthetic rubber.
• the polymerization method is not particularly limited, and conventionally known methods such as emulsion polymerization, solution polymerization, suspension polymerization, and bulk polymerization can be used.
• the polymerization conditions are not particularly limited, and can be adjusted as appropriate depending on the polymerization method, the composition of the polymerization composition, etc.
• the monomer may be butadiene alone, or in addition to butadiene, other conventionally known monomers for synthetic rubber may be used depending on the composition and properties of the desired synthetic rubber.
• Other monomers for synthetic rubber include conjugated diene compounds other than butadiene and aromatic vinyl compounds.
• Conjugated diene compounds other than butadiene include, for example, isoprene, 2,3-dimethyl-1,3-butadiene, 1,3-pentadiene, 1,3-hexadiene, 1,3-heptadiene, 2-phenyl-1,3-butadiene, 3-methyl-1,3-pentadiene, 2-chloro-1,3-butadiene, etc.
• Conjugated diene compounds other than butadiene may be used alone or in combination of two or more kinds.
• Aromatic vinyl compounds include, for example, styrene, 2-methylstyrene, 3-methylstyrene, 4-methylstyrene, ⁇ -methylstyrene, 2,4-dimethylstyrene, 2,4-diisopropylstyrene, 4-t-butylstyrene, 5-t-butyl-2-methylstyrene, vinylethylbenzene, divinylbenzene, trivinylbenzene, divinylnaphthalene, t-butoxystyrene, vinylbenzyldimethylamine, (4-vinylbenzyl)dimethylaminoethylether, N,N-dimethylaminoethylstyrene, N,N-dimethylaminomethylstyrene, 2-ethylstyrene, 3-ethylstyrene, 4-ethylstyrene, 2-t-buty
• the polymerization composition may contain, in addition to the monomer, additives and solvents that are conventionally known.
• additives include polymerization initiators, emulsifiers, and surfactants.
• an alkali metal compound is used as the polymerization initiator.
• alkali metal compounds include alkyl lithium such as methyl lithium, ethyl lithium, n-propyl lithium, n-butyl lithium, sec-butyl lithium, and t-butyl lithium; 1,4-dilithiobutane, phenyl lithium, stilbene lithium, naphthyl lithium, 1,3-bis(1-lithio-1,3-dimethylpentyl)benzene, 1,3-phenylenebis(3-methyl-1-phenylpentylidene)dilithium, naphthyl sodium, naphthyl potassium, and ethoxy potassium.
• the tire of the present embodiment contains synthetic rubber obtained by the above-described method for producing synthetic rubber.
• the method for producing a tire according to the present embodiment includes a vulcanization step of obtaining a tire by a vulcanization reaction using the synthetic rubber obtained by the above-described method for producing synthetic rubber as at least a part of the raw materials for the tire.
• a tire in the vulcanization process, can be obtained by vulcanizing a vulcanization composition containing at least synthetic rubber using a conventional method.
• the vulcanization conditions are not particularly limited and can be adjusted as appropriate depending on the composition of the vulcanization composition and the shape and structure of the desired tire.
• the vulcanization composition may contain, in addition to synthetic rubber, additives that are conventionally known.
• additives include vulcanizing agents, vulcanization accelerators, vulcanization accelerator assistants, antioxidants, softeners, antioxidants, and colorants. These additives may be used alone or in combination of two or more.
• vulcanizing agents include sulfur-based vulcanizing agents such as powdered sulfur, precipitated sulfur, highly dispersible sulfur, surface-treated sulfur, insoluble sulfur, dimorpholine disulfide, and alkylphenol disulfide, as well as zinc oxide, magnesium oxide, litharge, p-quinone dioxime, p-dibenzoylquinone dioxime, tetrachloro-p-benzoquinone, poly-p-dinitrobenzene, methylene dianiline, phenolic resin, brominated alkylphenol resin, and chlorinated alkylphenol resin.
• sulfur-based vulcanizing agents such as powdered sulfur, precipitated sulfur, highly dispersible sulfur, surface-treated sulfur, insoluble sulfur, dimorpholine disulfide, and alkylphenol disulfide, as well as zinc oxide, magnesium oxide, litharge, p-quinone dioxime, p-dibenzoylquinone dioxime, te
• vulcanization accelerators include thiuram-based agents such as tetramethylthiuram disulfide (TMTD), tetraethylthiuram disulfide (TETD), and tetramethylthiuram monosulfide (TMTM); aldehyde/ammonia-based agents such as hexamethylenetetramine; guanidine-based agents such as diphenylguanidine (DPG); thiazole-based agents such as 2-mercaptobenzothiazole (MBT) and dibenzothiazyl disulfide (DM); sulfenamide-based agents such as N-cyclohexyl-2-benzothiazylsulfenamide (CBS) and N-t-butyl-2-benzothiazylsulfenamide (BBS); and dithiocarbamate-based agents such as zinc dimethyldithiocarbamate (ZnPDC).
• TMTD tetramethylthiuram disul
• vulcanization accelerators include fatty acids, zinc fatty acids, zinc salts of fatty acids, and zinc oxide.
• fatty acids that can be used include acetic acid, propionic acid, butanoic acid, stearic acid, acrylic acid, and maleic acid.
• zinc fatty acids that can be used include zinc acetate, zinc propionate, zinc butyrate, zinc stearate, zinc acrylate, and zinc maleate.
• antioxidants include aliphatic and aromatic hindered amine and hindered phenol compounds.
• antioxidants examples include butylhydroxytoluene (BHT) and butylhydroxyanisole (BHA).
• Colorants include inorganic pigments such as titanium dioxide, zinc oxide, ultramarine, red iron oxide, lithopone, lead, cadmium, iron, cobalt, aluminum, hydrochloride, and sulfate, azo pigments, and copper phthalocyanine pigments.
• the mass balance method has been attracting attention in various industries, including the chemical, steel, and aluminum industries, in order to sell environmentally friendly products that use plant-based raw materials and recycled materials in a more attractive manner. It is desirable to be able to assign a value as a renewable product using the mass balance method in a simple and reliable manner for each product produced by the manufacturing method of the present invention using waste materials including waste tires. Therefore, the present invention provides a management method that can simply and reliably assign a value as a renewable product to each product in accordance with the content of renewable raw materials in waste materials including waste tires when chemical products are produced using the above-mentioned production method of the present invention.
• renewable raw materials refers to renewable organic resource raw materials.
• Renewable raw materials are not intended to be limited to products derived from biological resources, but are broadly interpreted as anything that falls under the category of renewable organic resources. For example, even if the product is derived from petroleum, it is intended to include those derived from recycled products that use petroleum-derived products as raw materials, such as waste tires.
• the mass balance method refers to a method in which, for example, when raw materials with specific characteristics, such as biomass raw materials, are mixed with raw materials without those characteristics during the distribution and processing process from raw materials to products, the characteristics are assigned as credits to part of the product in accordance with the content ratio of the raw materials with those characteristics. Since the mass balance method is a method in which biomass fractions are used as credits and allocated arbitrarily by the producer, it is common for the legitimacy of the method to be verified by a third-party certification body, such as ISCC (International Sustainable Carbon) or RSB (Roundtable on Sustainable Biofuels).
• ISCC International Sustainable Carbon
• RSB Raundtable on Sustainable Biofuels
• the method for managing chemical products of the present invention can be used when producing chemical products using waste materials including waste tires.
• the management method of the present invention is a method of using a management device to assign a value as a renewable product to a chemical product according to the content ratio of renewable raw materials contained in the waste material using a mass balance method.
• the management method of the present invention includes, for example, a step (V) in which a management device described below confirms that chemical products can be obtained (the management device acquires information indicating that chemical products can be obtained using waste materials including waste tires), and a step (Z) in which the management device confirms the proportion of products to which a value as a renewable product is assigned (the management device acquires information indicating the proportion of products to which a value as a renewable product is assigned).
• the step (V) of confirming that a chemical product is obtained includes the following steps (V-1), (V-2), (V-3), (V-4), (V-5), and (V-6).
• the step (V-1) is a step in which the management device confirms that the pyrolysis oil is produced from the waste material input into a pyrolysis unit that obtains the pyrolysis oil by pyrolysis of the waste material.
• the step (V-2) is a step in which the management device confirms that the low-temperature hydrogenated oil is produced from the pyrolysis oil input into a low-temperature hydrogenation unit in which a feedstock oil containing at least a portion of the pyrolysis oil is subjected to low-temperature hydrogenation treatment at 180°C or higher and 350°C or lower to obtain low-temperature hydrogenated oil.
• Step (V-3) is a step in which the management device confirms that the high temperature hydrogenated oil is produced from the low temperature hydrogenated oil that has been input into a high temperature hydrogenation unit in which a feedstock oil containing at least a portion of the low temperature hydrogenated oil is subjected to a hydrogenation treatment at a temperature higher than that of the low temperature hydrogenation treatment to obtain a second gas fraction and high temperature hydrogenated oil.
• Step (V-4) is a step in which the management device confirms that the naphtha fraction and the other fractions are produced from the high-temperature hydrogenated oil input into an atmospheric distillation unit that separates an atmospheric distillation feedstock oil containing at least a portion of the high-temperature hydrogenated oil and crude oil by atmospheric distillation.
• the step (V-5) is a step in which the management device confirms that the chemical product is obtained from the steam cracking feedstock oil introduced into a steam cracker that subjects the steam cracking feedstock oil containing at least a portion of the naphtha fraction and/or the other fraction to a steam cracking treatment.
• the step (V-6) is a step in which the management device confirms that the chemical products can be obtained from the waste materials by processing the waste materials in the order of the thermal cracking unit, the low-temperature hydrogenation unit, the high-temperature hydrogenation unit, the atmospheric distillation unit, and the steam cracker.
• Step (Z) of identifying the proportion of a product to be assigned a value as a renewable product includes the following steps (Z-1), (Z-2), (Z-3), and (Z-4).
• the step (Z-1) is a step in which the management device selects a product to be allocated as a renewable product from among the products obtained by the steam cracker.
• the step (Z-2) is a step in which the management device determines the value of the proportion (P) to be allocated as a renewable product among the proportion of the product selected in the step (Z-1) to the products obtained by the steam cracker.
• the step (Z-3) is a step in which the management device grasps the content ratio (Q) of renewable raw materials contained in the waste material.
• Step (Z-4) is a step in which the management device compares the value of the ratio (P) with the value of the content ratio (Q) and confirms that the value of the ratio (P) is equal to or less than the value of the content ratio (Q).
• Step (Z-1) If the products obtained by the steam cracker are ethylene, propylene, butadiene, and other products, select butadiene.
• Step (Z-3) When the waste material contains 5% by mass of renewable raw materials and 95% by mass of non-renewable raw materials, the content ratio (Q) of renewable raw materials is determined (obtained) to be 5% by mass.
• the content ratio (Q) of the renewable raw material is 5 mass%
• the ratio (P) allocated to the butadiene as a renewable product is 5 mass% or less.
• the butadiene product from the steam cracker can be assigned a value as a renewable product according to the proportion of renewable raw materials contained in the waste material.
• the butadiene product excluding (P) mass% out of 10 mass% butadiene product (10-(P) mass% butadiene product) actually contains renewable components.
• the (P) mass% butadiene is assigned a credit for 100% renewable butadiene, it is not treated as renewable butadiene.
• the value of 5% by mass of the content ratio (Q) of the renewable raw material and the value of 10% by mass of the butadiene product are set for the sake of convenience in order to facilitate understanding of the present invention, and are not limited to these values.
• the management method of the present invention can be executed by using a management device as described above. Furthermore, the processes in the management method executed by the management device are executed by a computer having a control unit constituting the management device.
• a management device for executing the management method of the present invention and a management program (computer program) executed by a computer of the management device will be described below.
• the management device is a device that assigns a value as a renewable product to the chemical product using a mass balance method in accordance with the content ratio of renewable raw materials contained in the waste material,
• the management device has a confirmation unit (I) for confirming that the chemical product is obtained,
• the confirmation unit (I) includes the following means (V-1), (V-2), (V-3), (V-4), (V-5), and (V-6):
• the means (V-1) is a means for confirming that the pyrolysis oil is produced from the waste material input into a pyrolysis unit for obtaining pyrolysis oil by pyrolysis of the waste material;
• the means (V-2) is a means for confirming that the low-temperature hydrogenated oil is produced from the pyrolysis oil input into a low-temperature hydrogenation unit in which a feedstock oil containing at least a part of the pyro
• the means (V-3) is a means for confirming that the high-temperature hydrogenated oil is produced from the low-temperature hydrogenated oil input into a high-temperature hydrogenation unit in which a feedstock oil containing at least a portion of the low-temperature hydrogenated oil is subjected to a hydrogenation treatment at a temperature higher than that of the low-temperature hydrogenation treatment to obtain a second gas fraction and a high-temperature hydrogenated oil
• the means (V-4) is a means for confirming that the naphtha fraction and the other fractions are produced from the high-temperature hydrogenated oil input into an atmospheric distillation unit that separates an atmospheric distillation feedstock oil containing at least a portion of the high-temperature hydrogenated oil and crude oil into a naphtha fraction and other fractions by atmospheric distillation
• the means (V-5) is a means for confirming that the chemical product is obtained from the steam cracking feedstock oil introduced into a steam cracker that subjects
• the management program executed by a management device used in manufacturing chemical products using waste materials including waste tires
• the management program is a program that uses the management device to assign a value as a renewable product to the chemical product using a mass balance method in accordance with a content ratio of renewable raw materials contained in the waste material
• the management program includes: (V-1): Confirm that the pyrolysis oil is produced from the waste material input into a pyrolysis unit that obtains pyrolysis oil by pyrolysis of the waste material; (V-2): A step of confirming that the low-temperature hydrogenated oil is produced from the pyrolysis oil introduced into a low-temperature hydrogenation unit in which a feedstock oil containing at least a portion of the pyrolysis oil is subjected to low-temperature hydrogenation treatment at 180° C.
• (V-3) is a step of confirming that the high-temperature hydrogenated oil is produced from the low-temperature hydrogenated oil input into a high-temperature hydrogenation unit in which a feedstock oil containing at least a portion of the low-temperature hydrogenated oil is subjected to a hydrogenation treatment at a temperature higher than that of the low-temperature hydrogenation treatment to obtain a second gas fraction and a high-temperature hydrogenated oil;
• (V-5) A step of confirming that the chemical product is obtained from the steam cracking feedstock oil introduced into a steam cracker that subjects the steam cracking feedstock oil containing
• 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 with reference to FIG.
• the management device 100 includes a control unit 110 and a storage unit 120 .
• the control unit 110 has a confirmation unit (I) 130 , a comparison unit 140 , and a notification unit (output unit) 150
• the storage unit 120 has a reaction database 160 .
• the hardware configuration and the functional configuration of the management device 100 will be described.
• FIG. 4 is a block diagram showing an example of the hardware configuration of the management device 100.
• the management device 100 includes the following components, which are 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 realizes various functions by executing an OS and computer programs stored in the main memory device 202, etc. That is, in this embodiment, the CPU 201 executes a management program to function as the control unit 110 of the management device and execute the management method.
• the CPU 201 controls the overall operation of the management device 100.
• the device that controls the overall operation of the management device 100 is the CPU 201, but this is not limited thereto, and may be, for example, an FPGA (Field Programmable Gate Array).
• the management program and various databases do not necessarily have to be stored in the main storage device 202, the auxiliary storage device 203, etc.
• the management program and various databases may be stored in other information processing devices connected to the management device 100 via the Internet, a local area network (LAN), a wide area network (WAN), etc.
• the management device 100 may acquire the management program and various databases from these other information processing devices and execute them.
• the main memory device 202 is a computer-readable storage medium that stores various programs and stores data necessary to execute the various programs.
• the main memory device 202 includes a ROM and a RAM, both of which are not shown.
• the ROM stores various programs such as the BIOS.
• the RAM functions as a working area in which various programs stored in the ROM are deployed when the CPU 201 executes them.
• the RAM there are no limitations on the RAM, and it can be appropriately selected according to 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 information, and can be appropriately selected depending on the purpose, and examples of the auxiliary storage device 203 include a solid state drive, a hard disk drive, etc.
• the auxiliary storage device 203 may also be a portable storage device such as a CD drive, a DVD drive, or a BD drive.
• a display, a speaker, etc. can be used as the output device 204.
• 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 may be used as appropriate, such as a keyboard, a mouse, or a touch panel.
• the communication interface (communication I/F) 206 is not particularly limited and may be any known interface as appropriate, such as a wireless or wired communication device.
• the processing functions of the management device 100 can be realized by the above hardware configuration.
• the management device 100 includes a control unit 110 and a storage unit 120.
• the control unit 110 controls the entire management device 100.
• the control unit 110 has 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-6).
• the confirmation unit (I) of the control unit 110 selects, in the above means (Z-1), a product to be allocated as a renewable product from among the products obtained by the steam cracker, and in the above means (Z-2), determines the value of the proportion (P) to be allocated as a renewable product from the proportion of the product selected in the above means (Z-1) to the product obtained by the steam cracker. In the above means (Z-3), it grasps the value of the content proportion (Q) of the renewable raw material contained in the waste material.
• the comparison unit 140 of the control unit 110 performs a comparison operation to compare the value of the ratio (P) with the value of the content ratio (Q) in order to have the confirmation unit (I) confirm the value in the above-mentioned means (Z-4).
• the notification section 150 of the control section 110 When the value of the proportion (P) is less than or equal to the content proportion (Q), the notification section 150 of the control section 110 notifies (outputs) that the selected product in an amount of (P) mass% can be allocated as a renewable product in the product, and when the value of the proportion (P) exceeds the content proportion (Q), the notification section 150 notifies (outputs) that the value has been exceeded. That is, after executing the management method, the management device 100 outputs the result of assigning a value as a renewable product to the selected product according to the content ratio of renewable raw materials contained in the waste material, including waste tires, obtained by the management method. Information about the apparatus used in the management method of the present invention and information about the reactions carried out in the apparatus are stored in the reaction database 160 in the storage unit 120.
• the storage unit 120 is a computer-readable storage medium that stores a computer program, and includes a storage medium that stores the management program that causes the control unit 110 including a computer to execute the management method.
• the amount and yield of the product produced from each device can be determined by measurement. However, in addition to obtaining yield results by actual measurement, by using the reaction database 160, it is possible to obtain the yield theoretically by calculation or to predict the yield based on accumulated data from the past.
• Figure 5 is a flowchart showing an example of the processing procedure of the management program in the control unit 110 of the management device 100. The following description will be given with reference to Figure 5.
• step S101 the confirmation unit 130 of the control unit 110 of the management device 100 acquires information about the pyrolysis unit, and the process proceeds to step S102.
• step S102 the confirmation unit 130 of the control unit 110 of the management device 100 confirms, for example, based on information output from the pyrolysis unit, that pyrolysis oil (OUT) is being produced from waste materials (IN) including waste tires, and if it is confirmed that pyrolysis oil (OUT) is being produced, the process proceeds to step S103.
• step S103 the confirmation unit 130 of the control unit 110 of the management device 100 acquires information related to the low-temperature hydrogenation unit, and the process proceeds to step S104.
• step S104 the confirmation unit 130 of the control unit 110 of the management device 100 confirms, for example, based on information output from the low-temperature hydrogenation unit, that low-temperature hydrogenated oil (OUT) is produced from the pyrolysis oil (IN) in the low-temperature hydrogenation unit, and confirms that the low-temperature hydrogenated oil (OUT) has been produced.
• the process proceeds to step S105.
• step S105 the confirmation unit 130 of the control unit 110 of the management device 100 confirms that the processing is carried out in the order of the pyrolysis unit, low-temperature hydrogenation unit, high-temperature hydrogenation unit, atmospheric distillation unit, and steam cracker, for example, based on information output from the pyrolysis unit, low-temperature hydrogenation unit, high-temperature hydrogenation unit, atmospheric distillation unit, and steam cracker, and confirms that as a result of these processes, chemical products (OUT) are produced from the waste materials (IN) including waste tires, and if it is confirmed that chemical products (OUT) have been produced, the process proceeds to step S106.
• step S106 the confirmation unit 130 of the control unit 110 of the management device 100 receives information from the input device (input device 205 in FIG. 4) in the management device 100 indicating that the operator has selected which products generated by the steam cracker should be assigned as renewable products, and transitions to step S107.
• step S107 the confirmation unit 130 of the control unit 110 of the management device 100 receives the value of the proportion (P) of the selected product that the operator has set to be allocated as a renewable product from the input device in the management device 100 (input device 205 in Figure 4), and transitions to step S108.
• P proportion
• 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 raw materials in the waste material input into the pyrolysis unit, and the process proceeds 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) with the value of the content ratio (Q), and the process proceeds to S110.
• step S110 the confirmation unit 130 of the control unit 110 of the management device 100 checks whether the value of the proportion (P) is equal to or less than the value of the content proportion (Q) based on the comparison result between the value of the proportion (P) and the value of the content proportion (Q) performed by the comparison unit 140 of the control unit 110 of the management device 100, and if it is confirmed that the value is equal to or less than the value of the content proportion (Q), it terminates this processing.
• a value as a renewable product can be assigned to the selected desired product according to the content ratio of renewable raw materials contained in the waste material including the waste tires. The result of the assignment is notified to the user through the notification unit 150 of the control unit 110 of the chemical product management device 100.
• the chemical product management device 100 outputs the result of the assignment of the value as a renewable product to the selected product according to the content ratio of renewable raw materials contained in the waste material including the waste tires obtained by the chemical product management method. If the conditions are not met during this process, the user is notified of this fact, for example, through the notification unit 150 of the control unit 110 of the chemical product management device 100. In this case, the operator can review the type of product selected, review the value of the allocation ratio (P) of the selected product, review the value of the content ratio (Q) of the renewable raw material, and further review various conditions such as reaction conditions, and try the process again.
• P the value of the allocation ratio
• Q content ratio
• Iodine value JIS K 0070 (Testing methods for acid value, saponification value, ester value, iodine value, hydroxyl value, and unsaponifiable matter of chemical products)
• Total acid number JIS K 2501 (Petroleum products and lubricants - Neutralization test method)
• Heat exchange fouling evaluation for low-temperature hydrogenated oil after the low-temperature hydrogenation process The temperature drop (°C) due to fouling attached to a test piece 61 of a fouling evaluation test device (HLPS) 60 for evaluating heat exchange fouling shown in Figure 6 is measured in the following order. 1. Low-temperature hydrogenated oil at 25° C.
• the difference between the initial measured temperature at the outlet 63 and the measured temperature after a certain time has elapsed is defined as the "temperature decrease caused by the decrease in heat transfer due to fouling.”
• a "heat exchanger fouling evaluation” is performed according to the following criteria. (Evaluation Criteria) ⁇ : The temperature drop during evaluation for a certain period of time (200 minutes) was 5° C. or less, and it was determined that fouling of the heat exchanger was suppressed.
• Example 1 Pyrolysis Step The pyrolysis step is carried out using the pyrolysis apparatus shown in FIG. Specifically, about 100 kg of cut-up truck tires (scrap 6) are put into the pyrolysis furnace 2 (volume 0.5 m 3 ), the atmosphere inside the pyrolysis furnace 2 is replaced with nitrogen gas, and the gas temperature is then raised to 500°C by the heat exchanger 1 while circulating the nitrogen gas in the pyrolysis device, and this temperature is maintained.
• the flow rate of the nitrogen gas introduced into the pyrolysis furnace 2 is set to 0.005 m 3 /s [ntp] and controlled in the range of 0.0045 m 3 /s [ntp] to 0.0055 m 3 /s [ntp].
• the oxygen concentration in the pyrolysis device system is controlled to a range of 1% by volume or less.
• a zirconia oxygen sensor is used to measure the oxygen concentration in the pyrolysis device.
• a pyrolysis oil is obtained from the bottom of the pyrolysis tower 12a, and a first gas fraction is obtained from the top of the pyrolysis tower 12a. The reaction is continued until the distillation of the pyrolysis oil stops, after which the heat exchanger 1 is stopped and the mixture is left to cool for about 12 hours.
• the mixture of the residue and metal is then removed from the pyrolysis furnace. The metal is removed from the mixture using a magnetic separator to obtain the residue.
• the residue is pulverized into fine powder with a particle size of 1 mm or less using a hammer-type pulverizer, and classified using a wind classifier with rotating blades to remove coarse powder with a particle size of 50 ⁇ m or more, thereby obtaining charcoal with a particle size of 10 ⁇ m or less and a most frequent value of 4 ⁇ m.
• the ratio of each component and the properties of the pyrolysis oil are as shown in Table 1.
• the impregnated solution is impregnated into the support by incipient wetness method, and the Ni content in terms of oxide is 4% by mass and the Mo content in terms of oxide is 20% by mass based on the mass of the support.
• the obtained impregnated product (catalyst precursor) is dried at 120°C for 3 hours, and then calcined at 500°C for 1 hour under air flow to obtain hydrogenation catalyst A-1.
• the impregnated solution is impregnated into the support by incipient wetness, and the support is supported so that the Ni content calculated as an oxide is 10% by mass and the W content calculated as an oxide is 20% by mass, based on the mass of the support.
• the obtained impregnated product (catalyst precursor) is dried at 120°C for 3 hours, and then fired at 500°C for 1 hour under air flow to obtain hydrogenation catalyst B-1.
• Atmospheric distillation step Crude oil having the properties shown in Table 2 and the high-temperature hydrogenated oil obtained in the high-temperature hydrogenation step are mixed in a mass ratio of 99:1 to obtain a feedstock oil for atmospheric distillation.
• the feedstock oil for atmospheric distillation is then fed into an atmospheric distillation unit, and distilled in a boiling range of 60 to 160°C while controlling the column top temperature to obtain a naphtha fraction.
• a kerosene fraction having a boiling range of 160 to 350°C is obtained while controlling the column top temperature.
• Example 2 A chemical product is produced in the same manner as in Example 1, except that the low-temperature hydrogenation temperature in the low-temperature hydrogenation step is changed to 190°C.
• Example 3 A chemical product is produced in the same manner as in Example 1, except that the low-temperature hydrogenation temperature in the low-temperature hydrogenation step is changed to 200°C.
• Example 4 A chemical product is produced in the same manner as in Example 1, except that the low-temperature hydrogenation temperature in the low-temperature hydrogenation step is changed to 210°C.
• Example 5 A chemical product was produced in the same manner as in Example 1, except that the low-temperature hydrogenation temperature in the low-temperature hydrogenation step was changed to 250°C.
• Example 6 A chemical product was produced in the same manner as in Example 1, except that the low-temperature hydrogenation temperature in the low-temperature hydrogenation step was changed to 300°C.
• Example 7 Chemical products are produced in the same manner as in Example 1, except that the mixing ratio of crude oil to high-temperature hydrogenated oil in the atmospheric distillation process is changed to 99.5:0.5.
• Example 8 Chemical products are produced in the same manner as in Example 1, except that the mixing ratio of crude oil to high-temperature hydrogenated oil in the atmospheric distillation process is changed to 98:2.
• Example 1 Chemical products are produced in the same manner as in Example 1, except that the pyrolysis oil obtained in the pyrolysis step is used as the raw material for the high-temperature hydrogenation step without going through the low-temperature hydrogenation step.
• Comparative Example 2 A chemical product is produced in the same manner as in Example 1, except that the low-temperature hydrogenation temperature in the low-temperature hydrogenation step is changed to 150°C.
• Example 3 Chemical products are produced in the same manner as in Example 1, except that the low-temperature hydrogenated oil obtained in the low-temperature hydrogenation step is used as part of the atmospheric distillation feedstock oil instead of the high-temperature hydrogenated oil, without going through the high-temperature hydrogenation step.
• Example 4 Chemical products are produced in the same manner as in Example 1, except that the pyrolysis oil obtained in the pyrolysis step is used as part of the feedstock oil for atmospheric distillation instead of the low-temperature hydrogenation step and the high-temperature hydrogenation step, without going through the low-temperature hydrogenation step and the high-temperature hydrogenation step.
• the results of the thermal decomposition step, low-temperature hydrogenation step, high-temperature hydrogenation step, atmospheric distillation step, and steam cracking step in Examples 1 to 8 and Comparative Examples 1 to 4 are shown in Tables 1 to 5.
• the chemical product yield (mass%) relative to the total amount of thermal decomposition products excluding metals indicates the ratio of the total amount of chemical products (ethylene, propylene, butadiene, butenes, isoprene, cyclopentadiene, benzene, toluene, xylene, ethylbenzene, styrene, indene, methylstyrene) to the total amount of the first gas component, thermal decomposition oil, and residue obtained in the thermal decomposition step.
• Example 9 Chemical products are produced in the same manner as in Example 1, except that a feedstock oil containing 50 mass% of pyrolysis oil obtained in the pyrolysis step and 50 mass% of recycled oil consisting of high-temperature hydrogenated oil (light and heavy fractions) obtained in the high-temperature hydrogenation step is used to carry out low-temperature hydrogenation treatment in the low-temperature hydrogenation step.
• Example 10 Chemical products are produced in the same manner as in Example 1, except that a feedstock oil containing 20 mass% of pyrolysis oil obtained in the pyrolysis step and 80 mass% of recycled oil consisting of high-temperature hydrogenated oil (light and heavy fractions) obtained in the high-temperature hydrogenation step is used to perform low-temperature hydrogenation treatment in the low-temperature hydrogenation step.
• the results of the low-temperature hydrogenation step, the high-temperature hydrogenation step, the atmospheric distillation step, and the steam cracking step in Examples 9 and 10 are shown in Tables 6 to 9.
• Tables 6 to 9 even if the mixing ratio of the pyrolysis oil and the recycled oil in the low-temperature hydrogenation process is changed, the feed oil to be subjected to the high-temperature hydrogenation treatment (low-temperature hydrogenated oil after the low-temperature hydrogenation process) suppresses fouling of the heat exchanger, and the feed oil for atmospheric distillation to be subjected to the atmospheric distillation process suppresses fouling of the heat exchanger, and chemical products can be efficiently produced. Therefore, it is suitable for long-term operation and can reduce production costs.
• Example 11 Chemical products are produced in the same manner as in Example 1, except that a low-temperature hydrogenation process is carried out using a feedstock oil (75% by mass of low boiling point oil, 25% by mass of high boiling point oil) obtained by fractionating the pyrolysis oil to remove 18% by mass of high boiling point oil.
• feedstock oil 75% by mass of low boiling point oil, 25% by mass of high boiling point oil
• the properties of the feedstock oil used in the low-temperature hydrogenation step are shown in Table 10.
• Example 12 Chemical products are produced in the same manner as in Example 1, except that a low-temperature hydrogenation process is carried out using a feedstock oil (67% by mass of low boiling point oil, 33% by mass of high boiling point oil) obtained by fractionating the pyrolysis oil to remove 10% by mass of high boiling point oil.
• a feedstock oil (67% by mass of low boiling point oil, 33% by mass of high boiling point oil) obtained by fractionating the pyrolysis oil to remove 10% by mass of high boiling point oil.
• Table 10 The properties of the feedstock oil used in the low-temperature hydrogenation step are shown in Table 10.
• Example 13 Chemical products are produced in the same manner as in Example 1, except that the pyrolysis step is carried out at a pyrolysis oil temperature of 400° C.
• the properties of the feedstock oil used in the low-temperature hydrogenation step are shown in Table 10.
• Example 14 Chemical products are produced in the same manner as in Example 1, except that the pyrolysis step is carried out at a pyrolysis oil temperature of 700° C.
• the properties of the feedstock oil used in the low-temperature hydrogenation step are shown in Table 10.
• the product ratios are the product ratios after pyrolysis at each pyrolysis temperature, and the pyrolysis oil properties of Examples 11 and 12 indicate the pyrolysis oil properties after removal of high boiling oil.
• Example 15 Chemical products are produced in the same manner as in Example 1, except that a low-temperature hydrogenation process is carried out in the low-temperature hydrogenation process using a feedstock oil containing 50 mass% of a feedstock oil obtained by distilling a pyrolysis oil to remove 18 mass% of high-boiling point oil and 50 mass% of a recycled oil composed of high-temperature hydrogenated oil obtained in the high-temperature hydrogenation process.
• Example 16 Chemical products are produced in the same manner as in Example 1, except that a low-temperature hydrogenation process is carried out in the low-temperature hydrogenation process using a feedstock oil containing 20 mass% of a feedstock oil obtained by distilling a pyrolysis oil to remove 10 mass% of high-boiling point oil and 80 mass% of a recycled oil consisting of high-temperature hydrogenated oil obtained in the high-temperature hydrogenation process.
• the product ratios are the product ratios after pyrolysis at 500° C., and the pyrolysis oil properties of Examples 15 and 16 indicate the pyrolysis oil properties after removal of high boiling oil.

Landscapes

• Chemical & Material Sciences (AREA)
• Oil, Petroleum & Natural Gas (AREA)
• Organic Chemistry (AREA)
• Chemical Kinetics & Catalysis (AREA)
• Engineering & Computer Science (AREA)
• General Chemical & Material Sciences (AREA)
• Physics & Mathematics (AREA)
• Thermal Sciences (AREA)
• Life Sciences & Earth Sciences (AREA)
• Sustainable Development (AREA)
• Health & Medical Sciences (AREA)
• Medicinal Chemistry (AREA)
• Polymers & Plastics (AREA)
• Wood Science & Technology (AREA)
• Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Priority Applications (2)

Applications Claiming Priority (2)

Publications (1)

Family

ID=94375427

Family Applications (1)

Country Status (3)

Cited By (3)

Citations (7)

• 2024
  • 2024-07-25 WO PCT/JP2024/026605 patent/WO2025023296A1/ja active Pending
  • 2024-07-25 JP JP2025535869A patent/JPWO2025023296A1/ja active Pending
  • 2024-07-25 CN CN202480046935.5A patent/CN121511289A/zh active Pending

Patent Citations (7)

Also Published As

Similar Documents

Legal Events